СПОСОБ СЖИЖЕНИЯ ВОДОРОДА И УСТАНОВКА ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Группа изобретений относится к криогенной технике, а именно к способу и устройству для сжижения газа, и может быть использована в местах получения водорода для создания мобильных модульных комплексов для сжижения водорода. Способ сжижения водорода включает предварительное охлаждение потока водорода, осуществление орто-пара конверсии водорода, дальнейшее охлаждение и сжижение водорода обратным потоком хладагента низкотемпературного контура сжижения, расширение и направление жидкого водорода в хранилище водорода. Предварительное охлаждение потока водорода осуществляют обратным потоком смесевого хладагента в первом, втором, третьем, четвертом и пятом ттеплообменных аппаратах (ТОА). Обратный поток смесевого хладагента (СХА) после выхода из первого ТОА сжимают и охлаждают, после чего поток СХА разделяется в фазовых сепараторах на разных температурных уровнях и дросселируется в обратный поток СХА для охлаждения прямых потоков. Техническим результатом является снижение энергозатрат, вероятности ...

КОМПЛЕКСНОЕ ХРАНЕНИЕ ЖИДКОСТИ

Группа изобретений относится к системе и способу сжижения газа. Способ сжижения газа содержит следующие этапы. Подаваемый поток вводят в ожижитель, содержащий, по меньшей мере, теплый расширитель и холодный расширитель. Подаваемый поток сжимают в ожижителе до давления выше критического давления и охлаждают сжатый подаваемый поток до температуры ниже критической температуры для образования плотнофазного потока высокого давления. Плотнофазный поток высокого давления отводят из ожижителя и снижают давление плотнофазного потока высокого давления в устройстве расширения для образования результирующего двухфазного потока. Затем непосредственно подают результирующий двухфазный поток в резервуар для хранения. Выделенную часть результирующего двухфазного потока объединяют мгновенно с выкипающим паром жидкости в резервуаре для хранения для образования объединенного потока пара. Причем температура плотнофазного потока высокого давления ниже, чем температура выпускного потока холодного расширителя.

НОВОЕ ПРОИЗВОДСТВЕННОЕ ОБОРУДОВАНИЕ И СПОСОБ ПОЛУЧЕНИЯ СЖИЖЕННОГО ВОДОРОДА И СЖИЖЕННОГО ПРИРОДНОГО ГАЗА

Производственное оборудование для получения сжиженного водорода и сжиженного природного газа из природного газа содержит установку по производству сжиженного водорода, установку по получению сжиженного природного газа, первый теплообменник и второй теплообменник. Первый теплообменник выполнен с возможностью охлаждения газообразного водорода посредством теплообмена между газообразным водородом и смешанным хладагентом для сжижения природного газа, содержащим множество видов хладагентов, выбранных из группы, состоящей из метана, этана, пропана и азота. Второй теплообменник выполнен с возможностью охлаждения смешанного хладагента посредством теплообмена между смешанным хладагентом и пропаном; причем первый теплообменник также выполнен с возможностью охлаждения газообразного водорода посредством теплообмена между газообразным водородом и хладагентом, содержащим водород или гелий. Техническим результатом является снижение расхода энергии. 2 н. и 8 з.п. ф-лы, 7 ил., 5 табл.

Крупномасштабное сжижение водорода посредством водородного холодильного цикла высокого давления, объединенного с новым предварительным охлаждением однократно смешанным хладагентом

Настоящее изобретение относится к способу сжижения водорода. Способ включает стадии охлаждения потока подаваемого газа, содержащего водород, с давлением по меньшей мере 1,5 МПа абс. (15 бар абс.) до температуры ниже критической температуры водорода на стадии первого охлаждения с получением потока жидкого продукта. Согласно изобретению поток подаваемого газа охлаждают с помощью замкнутого цикла первого охлаждения с потоком первого хладагента высокого давления, содержащим водород, где поток первого хладагента высокого давления разделяют на два частичных потока. Первый частичный поток расширяют до низкого давления, получая таким образом холод для охлаждения предварительно охлажденного подаваемого газа ниже критического давления водорода, и сжимают до среднего давления. Второй частичный поток расширяют до близкого к среднему давления и направляют в первый частичный поток среднего давления. Техническим результатом является повышение производительности и снижение капитальных затрат. 14 з.п. ф-лы ...

КРИОГЕННОЕ ХОЛОДИЛЬНОЕ УСТРОЙСТВО

НИЗКОТЕМПЕРАТУРНЫЙ СМЕШАННЫЙ ХЛАДАГЕНТ ДЛЯ КРУПНОМАСШТАБНОГО ПРЕДВАРИТЕЛЬНОГО ОХЛАЖДЕНИЯ ВОДОРОДА

High temp. superconductor-based hydrogen magnetic - carnot cycle to cool hydrogen@ vapour in hollow cylinder arrangement contg. different magnetic materials

The linear magnetic H2 liquefier features regenerator stages using high temp. ceramic supercondcutors (HTCS) with successively reducing transition temp.. The regenerators are shaped as hollow cylinders inside which concentric heat exchangers and a H2 conduit are fitted. The liquefier is built inside the LH2 tank and contains pref. type-I or type-II permanent magnetic high field-strength HTCS material which is cooled by LH2. The liquefier pref. is a rotating electrical machine in which between the pole-shoes heat exchangers are built. The machine can be used simultaneously as engine starter motor, 3-phase AC generator and driving engine. Pref. the liquefier is surrounded by thermal insulation (1), a magnetic screen of HTCS (2), the HTCS-spool (3) and the type-II high field-strength HTCS hollow cylinder (4) of Bi-Pb-Sr-Ca-Cu-O based material. The liquefier contains material with successively reducing transition temps., e.g. Bi-Pb-Sr-Ca-Cu-O (107 deg.K.), Y-Ba-Cu-O (93 deg.K.) and Bi-Pb-Ba-O ...

VERFAHREN ZUM HERSTELLEN VON MATSCH TIEFSIEDENDER GASE

Verfahren und Vorrichtung zur Herstellung von Matsch aus verflüssigtem Gas

Low boiling gases purification - by condensation, reheating and adsorption

Low-boiling gases (helium, hydrogen, neon) are purified by removal of higher boiling impurities. The greater part of the latter is separated by condensation. The gas is reheated after the condensation cycle and the remaining impurities are removed at room temp. by adsorption.

Liquefaction of gases

... 974,542. Liquefaction of gases.. PETROCARBON DEVELOPMENTS Ltd. Dec. 4, 1962, No. 45789/62. Addition to 912,478. Heading F4P. The method of cooling a compressed gas stream to below 70‹ K. in a plurality of inclined heat exchangers in series traversed by a separate stream of the gas after expansion in a turbine as claimed in the parent Specification, is modified in that helium is used as the coolant gas. Hydrogen is liquefied by passing it at 10 atmospheres pressure through an ammoniacooled exchanger 53, a nitrogen-cooled exchanger 53, a nitrogen-cooled exchanger 54 where its. temperature is reduced to 70‹ K. and further cooling is effected in exchangers 55, 56, 57 in series and wet hydrogen at 22‹ K. is expanded at a valve 58 into a container 59; each of the exchangers 55, 56, 57 being cooled by a countercurrent flow of helium cooled by expansion at an associated turbine 55b, 56b, 57b at a pressure of 7 atmospheres. The helium circuits are fed in parallel from a common discharge line of ...

METHOD AND APPARATUS FOR LIQUEFYING HELIUM BY ISENTROPIC EXPANSION

... 1358169 Gas liquefaction CRYOGENIC TECHNOLOGY Inc 18 Oct 1971 [19 Oct 1970] 48279/71 Heading F4P A helium liquefaction plant, comprises an indirect heat exchanger 16 in which a high pressure stream 14 of the gas to be liquefied is cooled by a low pressure stream 17 of the same gas, the cooled gas then being fed, via a further heat exchanger 40 and a surge chamber 41 to an engine 42 in which the gas is expanded isentropically to effect at least partial liquefaction any unliquefied gas returning via the low pressure stream. The high pressure stream is produced by a compressor 10 with an after-cooler 11 and is branched, one branch entering the first stage 15 of the heat exchanger, the other passing through a liquid nitrogen pre-cooler 18, the two branches joining up to enter the second stage 22 of the exchanger. The low pressure stream is obtained by drawing off some of the h.p. stream and passing it through charcoal traps 24, 32 before isentropically expanding it in engines 25, 33 and supplying ...

GAS LIQUEFIER

... 1421120 Liquefying gases BOC INTERNATIONAL Ltd 27 Feb 1973 [1 Dec 1971] 55809/71 Heading F4P [Also in Division G1] In an apparatus for liquefying gases, e.g. helium, having a reservoir 4 for collecting the liquefied gas, unliquefied gas is fed via line 32 to the liquid in reservoir 4 through a valve 30 controlled by a level sensor 14, 16, 18, so that some liquid may be evaporated and the level of liquefied gas regulated. Gas is compressed at 2 fed through heat exchangers 6, 8, 10, expanded at 12 to effect partial liquefaction the remaining gas returning via h.e.s 10, 8, 6 to the compressor. A branch line 24 including expansion turbine 28 provides further cooling. The line 32 may terminate in a coil 34 to reduce the risk of explosion. The gas may also be methane, hydrogen or natural gas.

Improvements in or relating to methods of, and apparatus for, producing cold at low tem peratures and/or liquefying a gaseous medium

... 1,056,964. Refrigerating. PHILIPS GLOEILAMPENFABRIEKEN N.V. March 2, 1965 [March 4, 1964], No. 8847/65. Heading F4H. A method of refrigerating comprises compressing a gaseous medium at 10 to above its critical pressure, cooling and liquifying it in heat exchanger 13, expanding the liquid medium to a pressure below its critical pressure at least in part in an expansion machine 14 without phase-transition occurring in the machine, using the expanded liquid to cool a load 18 and returning the vapour to the compressor via heat exchanger 13. The returning vapour cools the compressed medium to substantially the boiling-point of the expanded medium to ensure that phase transition does not occur in the machine 14. As shown, the medium from the machine 14 is further expanded in a throttle 16. For starting the system a valve 23 is used to direct the cooled medium to a throttle 21 until sufficient cooling is achieved in heat exchanger 13 to enable expansion machine 14 to be used. In a modification ...

Production of solidified cooled bodies

Apparatus for producing hydrogen pellets for introduction into a plasma-physical equipment, fusion reactor or the like, comprises an extrusion cryostat T1 and a supply cryostat T2, the temperatures of which can be adjusted independently of each other. The solidified material is extruded from the extrusion cryostat T1 into the supply cryostat T2 at a relatively high temperature appropriate for extrusion, and the material is cooled in the supply cryostat to a lower temperature which is suitable for the ejection operation and which ensures high strength. The apparatus advantageously comprises a double ram 14 which is used as a whole for the extrusion and which incorporates a coaxially guided ejection ram of smaller diameter, by means of which the extruded material can be ejected from the supply cryostat at the required speed. The extruded material is prevented from freezing solid in the supply duct 76 of the supply cryostat T2 by a heating means which has a short time constant and by means ...

Improvements in refrigeration

... 1,096,781. Refrigerating; gas liquefaction processes. AIR PRODUCTS & CHEMICALS Inc. Jan. 5, 1965 [Jan. 16, 1964], No. 409/65. Addition to 1,089,192. Headings F4H and F4P In a refrigeration process gas is passed through two heat-exchange zones in parallel, a portion of the gas is withdrawn from an intermediate point in one zone and merged with the gas leaving the other zone, the merged gases are expanded with the production of work and all of the expanded gas is passed through said one heat exchange zone. As shown, fluid, e.g. air, from a compressor discharge line 7 is divided into two streams 9 and 11 of which the former is cooled in a heat exchanger 13 then adiabatically expanded through valve 15 while the latter stream is cooled by an external refrigerating circuit 21 in heat exchanger 19, merged with a portion of stream 9 drawn from between the ends of exchanger 13 through line 29 and then expanded in a reciprocating engine 31. The stream from valve 15 is forwarded to a separator 17 ...

Process for producing liquefied hydrogen

A process for liquefying hydrogen gas comprising: initial cooling, usually called precooling, of H2 by means of indirect heat exchange with external nitrogen refrigerant in a first heat exchanger A, followed by further cooling and liquefaction of the said cooled hydrogen by means of heat exchange in a second heat exchanger B with hydrogen or helium and enclosing the heat exchangers necessary for the said precooling in a first thermally insulated container C, usually called a cold box enclosing the heat exchangers necessary for the further cooling and liquefaction in a second thermally insulated container D or cold box enclosing the said second thermally insulated container or cold box within the volume of the said first thermally insulated container.

Method for cooling a product, for liquefying a gas, and device for implementing this method.

INTEGRATION OF HYDROGEN LIQUEFACTION WITH GAS PROCESSING UNITS

Abstract A method including, compressing a first hydrogen stream, and expanding a portion to produce a hydrogen refrigeration stream, cooling a second hydrogen stream thereby producing a cool hydrogen stream, wherein at least a portion of the refrigeration is provided by a nitrogen refrigeration stream, further cooling at least a portion of the cool hydrogen stream thereby producing a cold hydrogen stream, and a warm hydrogen refrigeration stream wherein at least a portion of the refrigeration is provided by the hydrogen refrigeration stream, compressing the warm hydrogen refrigeration stream, mixing the balance of the compressed first hydrogen stream with a high-pressure gaseous nitrogen stream to form an ammonia synthesis gas stream, and wherein the first hydrogen stream and the warm hydrogen refrigeration stream are compressed in the same compressor. r- I LO - I * * I0 (N t.0 o (N: I n * * 212 * . I I * * -0 00* LrL. m ...

INTEGRATION OF HYDROGEN LIQUEFACTION WITH GAS PROCESSING UNITS

Abstract A method of liquefying hydrogen, including dividing a hydrogen stream into at least a first fraction and a second fraction, introducing the first fraction into a refrigeration cycle of a hydrogen liquefaction unit, thereby liquefying a product hydrogen stream, withdrawing one or more warm hydrogen stream(s) from the hydrogen liquefaction unit, and returning the one or more warm hydrogen stream to the hydrogen stream, wherein the second fraction is combined with a high-pressure nitrogen stream to form an ammonia synthesis gas stream.

INTEGRATION OF HYDROGEN LIQUEFACTION WITH GAS PROCESSING UNITS

Abstract A method including, compressing a first hydrogen stream, and expanding a portion to produce a hydrogen refrigeration stream, cooling a second hydrogen stream thereby producing a cool hydrogen stream, wherein at least a portion of the refrigeration is provided by a nitrogen refrigeration stream, further cooling at least a portion of the cool hydrogen stream thereby producing a cold hydrogen stream, and a warm hydrogen refrigeration stream wherein at least a portion of the refrigeration is provided by the hydrogen refrigeration stream, compressing the warm hydrogen refrigeration stream, mixing the balance of the compressed first hydrogen stream with a high-pressure gaseous nitrogen stream to form an ammonia synthesis gas stream, and wherein the first hydrogen stream and the warm hydrogen refrigeration stream are compressed in the same compressor. r- I LO - I * * I0 (N t.0 o (N: I n * * 212 * . I I * * -0 00* LrL. m ...

Slush hydrogen production apparatus

CONTINUOUS PROCESS FOR PRODUCING SLUSH HYDROGEN

INDUSTRIAL GAS LIQUEFACTION WITH AZEOTROPIC FLUID FORECOOLING

An industrial gas liquefaction cycle employing a main refrigeration circuit to supply low level refrigeration to the industrial gas (1, 2, 3, 4), and a forecooling circuit employing an azeotropic mixture (15, 50) to provide high level refrigeration to the refrigerant fluid (7) recirculating within the main refrigeration circuit. The azeotropic mixture may be subcooled (35) in the forecooling circuit.

LOW TEMPERATURE REFRIGERATION PROCESS USING MIXED REFRIGERANT

METHOD AND INSTALLATION FOR STORING AND DISPENSING LIQUEFIED HYDROGEN

Installation and method for storing and dispensing liquefied hydrogen, comprising a source (2) of gaseous hydrogen, a liquefier (3), two storage reservoirs (4, 5) for liquid hydrogen at determined respective storage pressures, the liquefier (3) comprising an inlet connected to the source (2) and an outlet connected in parallel, via a set of valves (7, 6, 16), to a respective inlet of each storage reservoir (5, 4), the outlet of the liquefier (3) also being connected to a connection end (15) intended to be connected removably to a tank (10) that is to be filled, each storage reservoir (5, 4) comprising a respective liquid withdrawing pipe (9, 8) comprising an end connected to the storage reservoir (4, 5) and at least one other end intended to be connected to at least one tank (10) that is to be filled, each storage reservoir (4, 5) further comprising a respective gas withdrawing pipe (12, 11) comprising an end connected to the storage reservoir (4, 5) and another end connected to an inlet ...

MAGNETIC REFRIGERATION SYSTEM WITH MULTICOMPONENT REFRIGERANT FLUID FORECOOLING

... ▓▓ A system for generating refrigeration and▓providing refrigeration to a heat load at a very cold▓temperature which includes a forecooling circuit using▓a multicomponent refrigerant fluid and a magnetic▓refrigeration circuit which provides refrigeration to▓the heat load and which rejects heat into the▓forecooling circuit.▓ ...

Kühlanlage

Verfahren zum Tiefkühlen eines schwer verflüssigbaren Gases und Anlage zur Durchführung des Verfahrens

Tieftemperaturanlage

Verfahren zur Herstellung von flüssigem Wasserstoff

Verfahren zum Verflüssigen eines Gases und Anlage zur Durchführung dieses Verfahrens

PROCEDURE FOR THE PRODUCTION OF KAELTE WITHIN THE RANGE OF CRYOGENIC TEMPERATURES.

LIQUEFACTION OF INDUSTRIAL AND HYDROCARBON GAS

Process of separation of the hydrogen and hydrocarbons of a gas of tail of refinery

Sophisticated apparatus of liquefaction

Process of natural gas liquefaction

PROCESS OF PRODUCTION OF COLD ON THE LEVEL OF THE CRYOGENIC TEMPERATURES

GAS LIQUEFACTION SYSTEM HAS ABSORPTION MACHINE AND HEAT PUMP STIRLING

L'invention concerne un système de liquéfaction de gaz comprenant une machine à absorption (1, 2, 3, 4, 5) à au moins un étage, destinée à produire du froid cryogénique par mise en œuvre d'un cycle à absorption, dont la sortie (24) de l'évaporateur (5) est reliée d'amont en aval d'une part à au moins un échangeur (6) pour refroidir le gaz à liquéfier de sorte à abaisser sa température depuis celle ambiante jusqu'à une température donnée, et d'autre part à une pompe à chaleur à compression ou Stirling (15), destinée à mettre en œuvre un cycle de Stirling, pour compléter le refroidissement du gaz à liquéfier de sorte à amener sa température depuis celle donnée jusqu'à au moins la température de condensation du gaz..

SYSTEMS AND METHODS FOR OBTAINING THERMALLY STABLE HIGH-DENSITY CRYOGENIC HYDROGEN AND OXYGEN FROM AN OCEAN SOURCE

An apparatus for obtaining liquid cryogenic hydrogen and oxygen from an ocean source is provided. The apparatus includes a hydrogen and oxygen producing assembly for producing gaseous hydrogen and gaseous oxygen. First and second bottom reservoirs are positioned proximal the ocean floor for stocking the gaseous hydrogen and oxygen produced. A thermal transferring circuit is in fluid communication with the first and second bottom reservoirs. First and second top reservoirs proximal the ocean surface are in fluid communication with the thermal transferring circuit. When gaseous hydrogen and oxygen flow through the thermal transferring circuit, the thermal energy thereof is so dissipated as to provide liquid cryogenic hydrogen and oxygen. The first and second top reservoirs stock the liquid cryogenic hydrogen and oxygen. A method for obtaining liquid cryogenic hydrogen and oxygen from an ocean source is also disclosed. An apparatus for thermally stabilizing liquid cryogenic hydrogen and oxygen ...

CLOSED REFRIGERANT CYCLE FOR THE LIQUEFACTION OF LOW-BOILING GASES

Process and apparatus for the liquefaction of hydrogen

A process and apparatus for the liquefaction of hydrogen, of the type using a refrigeration cycle whose cycle fluid comprises mostly hydrogen, and a closed liquid nitrogen refrigeration cycle. The cycle fluid is hydrogen and a mixture of C2 + hydrocarbons. The hydrocarbons are liquefied and expanded to form fluids which vaporize in a substantially continuous manner between a temperature of the order of -120° C. and a temperature adjacent ambient temperature. More particularly, the mixture of hydrocarbons is saturated C2, C3, and C5 hydrocarbons, and if desired C4, and separated liquefied fractions of these hydrocarbons are expanded at respective temperatures before expansion of the order of 0° C. to -10° C., -40° C. to -50° C. and -110° C. to -120° C., to form refrigerant liquids adapted to be vaporized.

Cryogenic ultra cold hybrid liquefier

A system for effectively generating refrigeration for use in putting a product fluid into an ultra cold condition wherein an active magnetic regenerator or a multicomponent refrigerant fluid cycle is integrated with a pulse tube system for receiving heat generated by the pulse tube system.

Multiple circuit cryogenic liquefaction of industrial gas with multicomponent refrigerant

A method for more efficiently cooling and liquefying industrial gas wherein refrigeration for the cooling and liquefaction is generated using first and second defined multicomponent refrigerant fluids in separate refrigeration circuits to cover a wide temperature range from ambient to cryogenic temperature.

СПОСОБ ПОВТОРНОГО СЖИЖЕНИЯ ОТПАРНОГО ГАЗА, ОБРАЗУЮЩЕГОСЯ В РЕЗЕРВУАРАХ ДЛЯ ХРАНЕНИЯ ЖИДКОГО ВОДОРОДА

Изобретение относится к способу повторного сжижения отпарного газа, образовавшегося в первичном резервуаре жидкого водорода. Способ включает: примешивание отпарного газа к жидкому водороду, хранящемуся во вторичном резервуаре жидкого водорода таким образом, что часть отпарного газа сжижается за счет криогенной тепловой энергии жидкого водорода; подачуоставшейся несжиженной части отпарного газа и парообразного водорода, образовавшегося в указанном вторичном резервуаре жидкого водорода, в блок получения жидкого водорода аппарата для получения жидкого водорода из газообразного водорода; при этом указанный аппарат, наряду с указанным блоком получения жидкого водорода, включает секцию цикла охлаждения, в которой циркулирующий водород выполняет функцию хладагента; сжижение оставшейся несжиженной части отпарного газа и парообразного водорода с помощью аппарата получения жидкого водорода. Изобретение позволяет производить повторное сжижение отпарного газа с целью его дальнейшего использования в ...

СПОСОБ ПОВТОРНОГО ОЖИЖЕНИЯ ОТПАРНОГО ГАЗА, ОБРАЗУЮЩЕГОСЯ В РЕЗЕРВУАРАХ ДЛЯ ХРАНЕНИЯ ЖИДКОГО ВОДОРОДА

... 1. Способ повторного сжижения отпарного газа, образовавшегося в первичном резервуаре жидкого водорода, включающий:примешивание отпарного газа к жидкому водороду, хранящемуся во вторичном резервуаре жидкого водорода таким образом, что по меньшей мере часть отпарного газа сжижается за счет криогенной тепловой энергии жидкого водорода;подачу оставшейся несжиженной части отпарного газа и парообразного водорода, образовавшегося в указанном вторичном резервуаре жидкого водорода, в блок получения жидкого водорода аппарата для получения жидкого водорода из газообразного водорода, при этом указанный аппарат, наряду с указанным блоком получения жидкого водорода, включает секцию цикла охлаждения, в которой циркулирующий водород выполняет функцию хладагента, и сжижение оставшейся несжиженной части отпарного газа и парообразного водорода с помощью аппарата получения жидкого водорода.2. Способ по п. 1, отличающийся тем, что температура жидкого водорода, хранящегося в указанном вторичном резервуаре, ниже ...

СПОСОБ ОХЛАЖДЕНИЯ ПРОДУКТА, В ЧАСТНОСТИ, ДЛЯ СЖИЖЕНИЯ ГАЗА И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

... 1. Способ охлаждения продукта (P), включающий в себя N упорядоченных циклов адсорбции/десорбции (100, 200, 300, 400, 500, 600) в воздушном вакууме, причем N является целым числом, превышающим 1, причем каждый цикл включает в себя этапы, согласно которым извлекают тепло из хладагента в паровой фазе в конденсаторе (101, 201, 301, 401, 501, 601) при первом давлении (P2), которое ниже критического давления указанного хладагента для конденсации указанного хладагента, вводят указанный хладагент в жидкой фазе в испаритель (103, 203, 303, 403, 503, 603) при втором давлении (P1), которое ниже первого давления, для испарения части указанного хладагента и охлаждения другой части хладагента до температуры испарения (T1) указанного хладагента при втором давлении, причем температура испарения снижается от одного цикла к следующему циклу, а первое и второе давления выбирают на каждом цикле таким образом, чтобы температура испарения (T1) в цикле была всегда ниже температуры конденсации (T2) хладагента ...

Kryogenischer ultrakalter hybrider Verflüssiger

Liquiefying a gaseous medium

Water combustion technology-methods,processes,systems and apparatus for the combustion of hydrogen and oxygen

Preparation of liquid hydrogen

... In the thermal decomposition of methane to produce hydrogen with subsequent liquefaction of the hydrogen, at least part of the cold required for the liquefaction is obtained by the vaporization of liquid methane and the vaporized methane is used to form at least part of the feed to the thermal decomposition step. The methane may be decomposed (a) by pyrolysis in the absence of a catalyst, (b) with steam at 700 DEG -800 DEG C. in the presence of a catalyst, or (c) by partial combustion at 800 DEG -900 DEG C. in the presence of nickel as catalyst. The carbon monoxide produced in method (b) or (c) may be converted to carbon dioxide which may be absorbed in a scrubbing liquid, e.g. water or an aqueous amine or caustic alkali solution. Oxygen for method (c) may be supplied from an air separation plant utilizing the vaporization of liquid methane according to Specification 804,944. Residual impurities in the gaseous hydrogen may be removed by fractional liquefaction also ...

Process for the production of liquid hydrogen

... 1,001,938. Liquefaction of hydrogen. SULZER BROS. Ltd. Aug. 4, 1964 [Sept. 6, 1963], No. 31387/64. Heading F4P. An hydrogen liquefaction process comprises circulating hydrogen gas through a refrigeration circuit comprising a compressor 23 and at least two series connected expansion turbines 24 ... 27, withdrawing as a component flow a minor portion of hydrogen through a line 29 upstream of the last turbine 27, further cooling said flow in exchangers 13, 14, 16, 17 cooled by the remainder of the hydrogen having been expanded in turbines 27, 28, converting the component flow at least partly into the paraform by passage through catalysts 30 ... 33, condensing the partly converted component flow in the coil 35 of a liquefier 20 by heat exchange with " crude " hydrogen having been withdrawn from a holder 3 by a compressor 2, cooled in exchangers 8, 9, 11 to 14, 16, 17, purified in absorbers 6, 7, 10, 15, 18 and in part liquefied at 20 by expansion at a valve 19 into a pressure below that of ...

Improvements in or relating to gas-expansion refrigerators

... 1,114,659. Refrigerating; gas liquefaction apparatus. PHILIPS GLOEILAMPENFABRIEKEN N.V. 29 Nov., 1966 [2 Dec., 1965], No. 53327/66. Headings F4H and F4P. Refrigeration apparatus comprises two parallel fed expansion orifices, the input to one orifice being pre-cooled by gas from that orifice and the input to the other orifice being pre-cooled by gas from both orifices. As shown, a first tube 6 has a ribbed section wound around a cylinder 50 and is connected to an expansion orifice 8 inside a coupling piece 50 while a second tube has an unribbed section 5 wound around tube 6 and a ribbed section 51 wound around a further cylinder 51, the second tube being connected to an expansion orifice 14. Apertures, not shown, are provided in coupling 50 so that tube 6 and section 5 are both cooled by gas from orifice 8 while section 51 is cooled by gas from orifice 14. The above apparatus is housed in a vacuuminsulated tube (Fig. 3, not shown) which has an outlet for liquefied gas ( ...

RELIQUEFYING CRYOGENIC GAS BOILOFF FROM HEAT LOSS

PROCEDURE AND DEVICE FOR COOLING STOPS FROM CONTAINERS TO THE STORAGE AND FOR THE TRANSPORT OF LIQUEFACTIONS GASES

INTEGRATION OF HYDROGEN LIQUEFACTION WITH GAS PROCESSING UNITS

Abstract A method including, compressing a first hydrogen stream, and expanding a portion to produce a hydrogen refrigeration stream, cooling a second hydrogen stream thereby producing a cool hydrogen stream, wherein at least a portion of the refrigeration is provided by a nitrogen refrigeration stream, further cooling at least a portion of the cool hydrogen stream thereby producing a cold hydrogen stream, and a warm hydrogen refrigeration stream wherein at least a portion of the refrigeration is provided by the hydrogen refrigeration stream, compressing the warm hydrogen refrigeration stream, mixing the balance of the compressed first hydrogen stream with a high-pressure gaseous nitrogen stream to form an ammonia synthesis gas stream, and wherein the first hydrogen stream and the warm hydrogen refrigeration stream are compressed in the same compressor. r- I LO - I * * I0 (N t.0 o (N: I n * * 212 * . I I * * -0 00* LrL. m ...

Industrial and hydrocarbon gas liquefaction

A method for liquefaction of industrial gases or gas mixtures (hydrocarbon and/or non-hydrocarbon) uses a modified aqua-ammonia absorption refrigeration system (ARP) that is used to chill the gas or gas mixture during the liquefaction process. The gas may be compressed to above its critical point, and the heat of compression energy may be recovered to provide some or all of the thermal energy required to drive the ARP. The method utilizes a Joule Thomson (JT) adiabatic expansion process which results in no requirement for specialty cryogenic rotating equipment. The aqua-ammonia absorption refrigeration system includes a vapour absorber tower (VAT) which permits the recovery of some or all of the heat of solution and heat of condensation energy in the system when anhydrous ammonia vapour is absorbed into a subcooled lean aqua-ammonia solution. The modified ARP with VAT may achieve operating pressures as low as 10 kPa which results in ammonia gas chiller operating temperatures as low as - ...

CRYOGENIC ULTRA COLD HYBRID LIQUEFIER

A system for effectively generating refrigeration for use in putting a product fluid into an ultra cold condition wherein an active magnetic regenerator or a multicomponent refrigerant fluid cycle is integrated with a pulse tube system for receiving heat generated by the pulse tube system.

DEVICE FOR LIQUEFYING GASES CONDENSING AT VERY LOW TEMPERATURE

Process for liquefying hydrogen

The invention relates to a process for liquefying hydrogen. To reduce the specific energy consumption, the following process steps are used: a) the precooling of the hydrogen stream by indirect heat exchange against a pressurized LNG stream to a temperature of between 140 and 130 K, b) the precooling of the hydrogen stream by indirect heat exchange against a coolant to a temperature of between 85 and 75 K, c) where the precooling of the coolant takes place against a pressurized LNG stream, and d) the cooling and at least partial liquefaction of the precooled hydrogen stream takes place by indirect heat exchange against another hydrogen stream channeled through a closed cooling circuit, e) where the precooling of the condensed hydrogen stream, which is channeled through a closed cooling circuit, takes place against a pressurized LNG stream.

PROCESS OF PRODUCTION OF COLD ON THE LEVEL OF THE CRYOGENIC TEMPERATURES

PROCESS FOR LIQUEFYING HYDROGEN

The invention relates to a process for liquefying hydrogen. To reduce the specific energy consumption, the following process steps are used: a) the precooling of the hydrogen stream by indirect heat exchange against a pressurized LNG stream to a temperature of between 140 and 130 K, b) the precooling of the hydrogen stream by indirect heat exchange against a coolant to a temperature of between 85 and 75 K, c) where the precooling of the coolant takes place against a pressurized LNG stream, and d) the cooling and at least partial liquefaction of the precooled hydrogen stream takes place by indirect heat exchange against another hydrogen stream channeled through a closed cooling circuit, e) where the precooling of the condensed hydrogen stream, which is channeled through a closed cooling circuit, takes place against a pressurized LNG stream. © KIPO & WIPO 2009 ...

HYDROGEN GAS LIQUEFACTION METHOD AND HYDROGEN GAS LIQUEFACTION PLANT

A hydrogen gas liquefaction method and a hydrogen gas liquefaction plant are provided in which the cold energy possessed by liquefied hydrogen can be recovered and effectively utilized as energy required for liquefaction of hydrogen gas. The hydrogen gas liquefaction method is characterized by comprising: a hydrogen liquefaction step in which in a hydrogen production place, hydrogen gas is heat-exchanged with liquefied nitrogen to thereby cool the hydrogen gas and produce liquefied hydrogen; a first transportation step in which the liquefied hydrogen is transported to a hydrogen consumption region; a hydrogen vaporization step in which in the hydrogen consumption region, the liquefied hydrogen is heat-exchanged with nitrogen gas to thereby generate hydrogen gas from the liquefied hydrogen; and a second transportation step in which the liquefied nitrogen obtained in the hydrogen vaporization step is transported to the hydrogen production place. The method hence is characterized in that cold ...

WORK RECOVERY FROM PROCESS INVOLVING STEAM GENERATION

A method of conducting a process involving the generation of steam (24; 58; 104; 170; 198; 222; 259) in which a hot process stream (16; "A"; 92; 152; 184; 204; 246) is generated. The hot process stream (16; "A"; 92; 152; 184; 204; 246) can be generated in any manner and can include a burner section of a steam methane reformer (2), a gas turbine of an integrated combined cycle (3), a combustion chamber used to pre-heat incoming air and oxygen for a blast furnace (140), an oxygen transport membrane system (180), and a gas turbine (202) or natural gas engine that is provided to compress air in a cryogenic air separation unit (228; 240).

ACTIVE MAGNETIC REGENERATIVE LIQUEFIER USING PROCESS GAS PRE-COOLING FROM BYPASS FLOW OF HEAT TRANSFER FLUID

A process for liquefying a process gas comprising: 1. A process for liquefying a process gas comprising:introducing a heat transfer fluid into an active magnetic regenerative refrigerator apparatus that comprises (i) a high magnetic field section in which the heat transfer fluid flows from a cold side to a hot side through at least one magnetized bed of at least one magnetic refrigerant, (ii) a first no heat transfer fluid flow section in which the bed is demagnetized, (iii) a low magnetic or demagnetized field section in which the heat transfer fluid flows from a hot side to a cold side through the demagnetized bed, and (iv) a second no heat transfer fluid flow section in which the bed is magnetized;continuously diverting a bypass portion of the heat transfer fluid from the cold side of the low magnetic or demagnetized field section into a bypass flow heat exchanger at a first cold inlet temperature; andcontinuously introducing the process gas into the bypass flow heat exchanger at a first hot inlet temperature and discharging the process gas or liquid from the bypass flow heat exchanger at a first cold exit temperature;wherein the temperature difference between the bypass heat transfer first cold inlet temperature and the process gas first cold exit temperature is 1 to 5 K.2. The process of claim 1 , wherein the temperature difference is 1 to 2 K.3. The process of claim 1 , further comprising introducing the non-bypassed portion of the heat transfer fluid into the cold side of the magnetized bed in the high magnetic field section.4. The process of claim 1 , wherein the bypass portion constitutes 3 to 12% of the total heat transfer fluid exiting the cold side of the low magnetic or demagnetized field section.5. The process of claim 1 , wherein the magnetic refrigerant operates at or below its Curie temperature throughout an entire active magnetic regeneration cycle.6. The process of claim 5 , wherein the magnetic refrigerant operates in a range from less than its ...

COOLING SYSTEM

Cooling system, preferably adapted for use in or including a refrigeration plant and/or liquefier plant, having a refrigeration circuit (1) configured to use a refrigerant including a mixture of helium and neon; wherein the refrigerant is based on a raw mixture, preferably is the raw mixture, including helium and neon, extracted from air by an air separation plant (2). Method for producing a refrigerant usable in a refrigeration circuit (1), comprising: extracting a raw mixture including helium and neon from air, wherein the raw mixture preferably further includes nitrogen and hydrogen; and using the raw mixture as the refrigerant or obtaining the refrigerant from the raw mixture.

Apparatus for producing low temperatures

METHOD FOR THE PRODUCTION OF LIQUEFIED NATURAL GAS

A method for the production of liquefied natural gas is provided. The method may include providing a high pressure natural gas stream, splitting the high pressure natural gas stream into a first portion and a second portion, and liquefying the first portion of the high pressure natural gas stream to produce an LNG stream. The refrigeration needed for cooling and liquefaction of the natural gas can be provided by a closed nitrogen refrigeration cycle and letdown of the second portion of the high pressure natural gas stream. 1. A method for the production of liquefied natural gas (“LNG”) , the method comprising the steps of:a) providing a nitrogen refrigeration cycle, wherein the nitrogen refrigeration cycle is configured to provide refrigeration within a heat exchanger;b) purifying a first natural gas stream in a first purification unit to remove a first set of impurities to produce a purified first natural gas stream;{'sub': 'H', 'c) cooling and liquefying the first natural gas stream in the heat exchanger using the refrigeration from the nitrogen refrigeration cycle to produce an LNG stream, wherein the first natural gas stream has an LNG refrigeration requirement, wherein the LNG stream is liquefied at a first pressure P;'}d) purifying a second natural gas stream in a second purification unit to remove a second set of impurities to produce a purified second natural gas stream;e) partially cooling the second natural gas stream in the heat exchanger;f) withdrawing the partially cooled second natural gas stream from an intermediate section of the heat exchanger;{'sub': M', 'M', 'H, 'g) expanding the partially cooled second natural gas stream to a medium pressure Pin a natural gas expansion turbine to form a cold natural gas stream, wherein the medium pressure Pis at a pressure lower than the first pressure P; and'}h) warming the cold natural gas stream in the heat exchanger by heat exchange against the first natural gas stream to produce a warm natural gas stream at ...

METHOD AND DEVICE FOR PRODUCING SLUSH FROM LIQUEFIED GAS

СПОСОБ ПРОИЗВОДСТВА ЖИДКОГО ВОДОРОДА И ЭЛЕКТРОЭНЕРГИИ

Настоящее изобретение относится к способу производства жидкого водорода и электроэнергии. Способ производства водорода и/или электроэнергии включает создание системы, подходящей для производства водорода и/или электроэнергии, содержащей, по меньшей мере, устройство реформинга, приспособленное для приема сырьевого природного газа и реформинга природного газа с получением водородсодержащего газа; устройство для производства электроэнергии, приспособленное для приема, по меньшей мере, части водорода, содержащегося в водородсодержащем газе, и осуществления реформинга водорода для производства электроэнергии; и устройство для сжижения водорода, приспособленное для приема части водорода, содержащегося в водородсодержащем газе, и для сжижения водорода с получением жидкого водорода, при этом во время работы в устройство для сжижения водорода подают по меньшей мере часть электроэнергии, произведенной в устройстве для выработки электроэнергии, и во время работы из системы отводят жидкий водород и ...

НИЗКОТЕМПЕРАТУРНЫЙ СМЕШАННЫЙ ХЛАДАГЕНТ ДЛЯ КРУПНОМАСШТАБНОГО ПРЕДВАРИТЕЛЬНОГО ОХЛАЖДЕНИЯ ВОДОРОДА

Изобретение может быть использовано при сжижении газовых потоков, в частности газовых потоков, содержащих водород или гелий. Составы хладагентов включают первый компонент азот, второй компонент, выбранный из метана или аргона, третий компонент, выбранный из этана или этилена, и четвертый компонент, выбранный из н-бутана, изобутана, 1-бутена, пропана, пропилена, н-пентана и изопентана. Составы хладагентов могут дополнительно включать пятый и шестой компоненты, выбранные из н-бутана, изобутана, 1-бутена, пропана, пропилена, н-пентана и изопентана. При этом пятый компонент отличен от указанного четвертого компонента, а шестой компонент отличен от пятого компонента. Предложены также применение составов хладагентов для предварительного охлаждения в процессе сжижения газообразного вещества и способ сжижения потока подаваемого газа. Изобретение позволяет повысить эффективность составов хладагентов. 8 н. и 4 з.п. ф-лы, 3 ил.

Криогенная система ожижения водорода, получаемого преимущественно на АЭС

Изобретение относится к криогенной технике, может быть использовано для получения и хранения многотоннажного жидкого водорода. Криогенная система ожижения водорода состоит из установки ожижения водорода, выполненной в виде дожимающего продукционный поток водорода компрессора, блока азотного охлаждения, блока ожижения водорода в виде пяти рекуперативных теплообменников, трех адиабатных конверторов пароводорода и двух дроссельных вентилей, один из которых установлен на линии выдачи жидкого водорода в хранилище жидкого водорода, и гелиевой холодильной установки в составе компрессора, блока предварительного азотного охлаждения, гелиевого блока охлаждения. В установке ожижения водорода перед дожимающим компрессором установлен многоступенчатый пароэжекторный агрегат. Все эжекторные ступени параллельно подключены к коллектору подачи пара, первая эжекторная ступень - к водородному газгольдеру, соединенному с источником получения газообразного водорода, а концевая эжекторная ступень - к дожимающему ...

Verfahren zur Verflüssigung von Gasströmen

Es wird ein Verfahren sowie eine Vorrichtung zur Verflüssigung von Teilgasströmen aus großskaligen Produktionseinheiten beschrieben. Insbesondere wird auf eine effektive Verflüssigung von Wasserstoff aus Dampfreformern hingewiesen, indem die Kompressionsleistung zur Verdichtung des Arbeitsgases vermieden wird.

Verfahren und Vorrichtung zum isothermen Waermeaustausch

Einrichtung zum Verfluessigen eines unter Druck zugefuehrten Gases in einem Raum, der kuehlbar und mit einer Zu- und Ableitung versehen ist

Separation of a refinery tail gas

... 1,068,982. Cold separation of gas mixtures. CONCH INTERNATIONAL METHANE Ltd. Feb. 23, 1966 [March 19, 1965], No. 7852/66. Heading F4P. Separation of hydrogen from admixture with nitrogen, carbon monoxide, methane and C 2 to C 4 hydrocarbons is effected by first condensing and separating the C 2 to C 4 hydrocarbons, then condensing the bulk of the methane by indirect heat exchange with a stream of evaporating liquid nitrogen and with a stream of cold regasified liquefied natural gas and finally by scrubbing effluent hydrogen with L.N.G. to remove nitrogen and carbon monoxide followed by further scrubbing with sub-cooled separated propane to remove residual methane. Compressed feed gas having been cooled in boiling coils (12, 18, 20, 24), Fig. 2 (not shown), of columns (10, 22, 26) hereinafter referred to is condensed at (30, 36) by L.N.G. in a coil (32). Crude ethylene is separated at (40) and is expanded at a valve (42) into a de-methanizer column (26) whilst crude vapour withdrawn from ...

LIQUID HYDROGEN PRODUCTION

Procedure for the liquefaction of gas, in particular of natural gas

KRYOGENI ULTRA COLD ONES HYBRID CONDENSOR

TIEFTEMPERATURKUHLVERFAHREN

Method for cooling a product, particularly, for liquefying a gas, and device for implementing this method

Method for producing liquid hydrogen and electricity

The present invention provides a method for producing hydrogen and electricity, comprising providing a system suitable for producing liquid hydrogen and / or electricity, comprising at least: a)a gas reforming unit arranged to receive a natural gas feed and to reform a natural gas to produce a hydrogen-comprising gas; b) a electricity generation unit arranged to receive at least part of the hydrogen in the hydrogen-comprising gas and to convert the hydrogen to generate electricity; and c) a hydrogen liquefaction unit arranged to receive part of the hydrogen in the hydrogen-comprising gas and to liquefy the hydrogen to produce liquid hydrogen, which hydrogen liquefaction unit during operation is powered by at least part of the electricity produced by the electricity generation unit,during operation which system is arranged to export liquid hydrogen and / or electricity, wherein: i) during a first period, natural gas is provided to the gas reforming unit and the system is operated to export ...

Method for re-liquefying boil-off gas generated at liquid hydrogen storage tank

The boil-off gas discharged from a liquid hydrogen storage tank on a liquid hydrogen transport vessel (16) is introduced into the liquid hydrogen stored within liquid hydrogen storage tanks (19, 20) disposed on the ground by passing through a boil-off gas introduction path (17). At least a portion of the boil-off gas is re-liquefied by means of the cold temperature of the liquid hydrogen. The boil-off gas that was not re-liquefied and the gasified hydrogen generated as a consequence of the liquid hydrogen within the liquid hydrogen storage tanks (19, 20) gasifying are mixed with raw material hydrogen by being supplied to the raw material hydrogen path (11) of a liquid hydrogen production device (HS) by passing through a gasified hydrogen discharge path (21). The boil-off gas and the gasified hydrogen are re-liquefied by means of the liquid hydrogen production device (HS).

Low-temperature mixed--refrigerant for hydrogen precooling in large scale

The present invention relates to a refrigerant composition. According to the invention it is envisioned that the composition comprises comprising an inert gas selected from nitrogen, argon, neon and a mixture thereof, and a mixture of at least two C ...

LOW TEMPERATURE REFRIGERATION PROCESS USING

Process for producing liquid hydrogen

The invention relates to an integrated process for continuous production of liquid hydrogen, comprising (a) producing gaseous hydrogen by electrolysis; and (b) liquefying said gaseous hydrogen in a hydrogen liquefaction unit, which liquefaction unit is powered by energy essentially from renewable sources; and, (c) when additional power is needed, using electrical energy generated in a process in which electrical energy and hydrogen are co-generated by an integrated electrolysis process comprising: (d) electrolysing a metal salt or mixture of metal salts and water into the corresponding metal or metals, acid or acids, and oxygen (electricity storage phase), and (e) producing gaseous hydrogen and recovering electricity in a regeneration reaction of the metal (s) and acid(s) of step (d) (regeneration phase); wherein at least part of the gaseous hydrogen generated in step (e) is used in step (b) of the process.

METHOD AND INSTALLATION FOR STORING AND DISPENSING LIQUEFIED HYDROGEN

Installation and method for storing and dispensing liquefied hydrogen, comprising a source (2) of gaseous hydrogen, a liquefier (3), two storage reservoirs (4, 5) for liquid hydrogen at determined respective storage pressures, the liquefier (3) 5 comprising an inlet connected to the source (2) and an outlet connected in parallel, via a set of valves (7, 6, 16), to a respective inlet of each storage reservoir (5, 4), the outlet of the liquefier (3) also being connected to a connection end (15) intended to be connected removably to a tank (10) that is to be filled, each storage reservoir (5, 4) comprising a respective liquid withdrawing pipe (9, 8) comprising an end 10 connected to the storage reservoir (4, 5) and at least one other end intended to be connected to at least one tank (10) that is to be filled, each storage reservoir (4, 5) further comprising a respective gas withdrawing pipe (12, 11) comprising an end connected to the storage reservoir (4, 5) and another end connected to an ...

Method and filling device for filling a transport tank

The present invention pertains to a method for filling a transport tank with a product medium in a liquid state in a gas liquefaction plant, comprising a step of supplying the product medium in the liquid state from a storage tank (18) of the gas liquefaction plant to the transport tank. The method is characterized in that it further comprises a step of discharging the product medium in a gaseous state from the transport tank into the storage tank (18).

PROCESS AND PLANT FOR THE PRODUCTION OF LIQUID HYDROGEN

Process and plant for the production of liquid hydrogen by means of a liquefier (2) of the electric type and having a variable cooling power dependent on the electrical power consumed, the liquefier (2) being supplied with electricity by a first source (4) of electricity and being connected to at least one additional source (5, 6) of electricity providing an amount of electricity which is intermittent or variable over time, characterized in that liquid hydrogen is produced by the liquefier (2) at first thermodynamic conditions when the liquefier is supplied with electricity at a predetermined nominal electrical energy level and in that, when the liquefier (2) is supplied with electricity at an energy level exceeding the said nominal level, the hydrogen produced by the liquefier (2) is subcooled with respect to the first thermodynamic conditions.

PROCESS FOR THE CO-PRODUCTION OF GASEOUS CARBON DIOXIDE AND HYDROGEN

PROCESS FOR THE CO-PRODUCTION OF CARBON DIOXIDE AND HYDROGEN A process for the co-production of hydrogen and carbon dioxide comprises first treating the effluent of a methane steam reformer in a pressure swing adsorption (PSA) unit. The PSA unit adsorbs carbon dioxide and other impurities and yields an enriched hydrogen gas stream. During regeneration of the PSA unit, a purge gas is produced, which is combusted with oxygen and recycled exhaust gas to form carbon dioxide gas and water. The combustion step produces electricity which can be used to liquify the carbon dioxide and hydrogen products, and to run process compressors. Overall, the process efficiently and economically produces both hydrogen and carbon dioxide for industrial use.

METHOD AND DEVICE FOR PRODUCING SLUSH FROM LIQUEFIED GAS

The invention relates to a method for producing slush from liquefied gas. According to said method, solid crystals are formed and mix or are mixed with the liquefied gas to produce slush. These solid crystals are produced from liquid particles which are released into or enter a gas atmosphere under pressure, the temperature of the gas atmosphere being below the freezing point of the liquid particles. The invention also relates to a device for producing slush from liquefied gas in a cryostat container (1) which is partly filled with the liquefied gas which mixes with the solid crystals to produce slush. The device has an atomising device (2, 12) for producing liquid particles from the liquefied gas supplied to it. Said liquid particles enter a gas atmosphere which exists above the liquefied gas in the container (1). The temperature of said gas atmosphere is below the freezing point of the liquid particles.

INDUSTRIAL AND HYDROCARBON GAS LIQUEFACTION

A method for liquefaction of industrial gases or gas mixtures (hydrocarbon and/or non-hydrocarbon) uses a modified aqua-ammonia absorption refrigeration system (ARP) that is used to chill the gas or gas mixture during the liquefaction process. The gas may be compressed to above its critical point, and the heat of compression energy may be recovered to provide some or all of the thermal energy required to drive the ARP. The method utilizes a Joule Thomson (JT) adiabatic expansion process which results in no requirement for specialty cryogenic rotating equipment. The aqua-ammonia absorption refrigeration system includes a vapour absorber tower (VAT) which permits the recovery of some or all of the heat of solution and heat of condensation energy in the system when anhydrous ammonia vapour is absorbed into a subcooled lean aqua-ammonia solution. The modified ARP with VAT may achieve operating pressures as low as 10 kPa which results in ammonia gas chiller operating temperatures as low as - ...

Active Magnetic Regenerator Method and Apparatus

MULTIPLE CIRCUIT CRYOGENIC LIQUEFACTION OF INDUSTRIAL GAS

A method for more efficiently cooling and liquefying industrial gas wherein refrigeration for the cooling and liquefaction is generated using first and second defined multicomponent refrigerant fluids in separate refrigeration circuits to cover a wide temperature range from ambient to cryogenic temperature.

Method for cooling a product, particularly, for liquefying a gas, and device for implementing this method

PROCESS AND INSTALLATION OF HYDROGEN LIQUEFACTION

Moving thermal bed to time shift liquifaction and vaporization

A method to store and utilize thermal energy is provided. During a first phase, transferring heat from the heat relocation media to the lower temperature reservoir, transferring heat from the higher temperature stream to the heat relocation media, and transferring heat from the heat relocation media to the high temperature reservoir, thereby at least partially liquefying the higher temperature stream. During a second phase, transferring heat from the higher temperature reserve to the heat relocation media, transferring heat from the heat relocation media to the lower temperature stream, and transferring heat from the heat relocation media to the lower temperature reservoir, thereby at least partially vaporizing the lower temperature stream.

Refrigeration process

The present invention relates to a single cycle mixed refrigerant process for industrial cooling applications, for example, the liquefaction of natural gas. The present invention also relates to a refrigeration assembly configured to implement the processes defined herein and a mixed refrigerant composition usable in such processes.

INTEGRATED LIQUID STORAGE

A system and process for liquefying a gas, comprising introducing a feed stream into a liquefier comprising at least a warm expander and a cold expander; compressing the feed stream in the liquefier to a pressure greater than its critical pressure and cooling the compressed feed stream to a temperature below its critical temperature to form a high pressure dense-phase stream; removing the high pressure dense-phase stream from the liquefier, reducing the pressure of the high pressure dense-phase stream in an expansion device to form a resultant two-phase stream and then directly introducing the resultant two-phase stream into a storage tank; and combining a flash portion of the resultant two-phase stream with a boil-off vapor from a liquid in the storage tank to form a combined vapor stream, wherein the temperature of the high pressure dense-phase stream is lower than the temperature of a discharge stream of the cold expander. 1. A process for liquefying a gas , comprising:introducing a feed stream into a liquefier comprising at least a warm expander and a cold expander;compressing the feed stream in the liquefier to a pressure greater than its critical pressure and cooling the compressed feed stream to a temperature below its critical temperature to form a high pressure dense-phase stream;removing the high pressure dense-phase stream from the liquefier and reducing the pressure of the high pressure dense-phase stream in an expansion device to form a resultant two-phase stream and then directly introducing the resultant two-phase stream into a storage tank; andcombining a flash portion of the resultant two-phase stream with a boil-off vapor from a liquid in the storage tank to form a combined vapor stream, wherein the temperature of the high pressure dense-phase stream is lower than the temperature of a discharge stream of the cold expander.2. The process of claim 1 , further comprising heating at least part of the combined vapor stream to ambient temperature.3. The ...

PIPING MODULE FOR AIR FRACTIONATION PLANT

A piping module is described which comprises at least two fluid connections or ports for connection to at least one main heat exchanger of an air fractionation plant, whereby the main heat exchanger becomes linked to at least two fluid lines in a warm part of the air fractionation plant. The piping module comprises at least two ports on the main compressor side, couplable to at least two fluid lines in the warm part of the air fractionation plant, and at least two ports on the main heat exchanger side, couplable to at least two fluid ports of the at least one main heat exchanger, and at least two fluid lines connecting the ports on the main compressor side to the ports on the main heat exchanger side. A corresponding air fractionation plant and a method for erecting such an air fractionation plant () are likewise described. 11010101110010010abab. A piping module () for linking at least two fluid ports (′ , ′) of at least one main heat exchanger ( , ) , constructed for use in an air fractionation plant () , to at least two fluid lines in a warm part of the air fractionation plant () , said piping module () comprising:{'b': '100', 'at least two ports on a main compressor side of the piping module, which are couplable with the at least two fluid lines in a warm part of an air fractionation plant (),'}{'b': 10', '10', '10', '10', '1', '1', '100, 'i': a', 'b', 'a', 'b', 'a', 'b, 'at least two ports (, ) on the main heat exchanger side of the piping module, which are couplable with the at least two fluid ports (′, ′) of the at least one main heat exchanger (, ) in a cold part of an air fractionation plant (), and'}{'b': 10', '10, 'i': a', 'b, 'at least two fluid lines connecting said at least two ports on the main compressor side to said at least two ports (, ) on the main heat exchanger side.'}21011100101010abab. The piping module () according to claim 1 , wherein said piping module is constructed for vertical arrangement beside at least one main heat exchanger ( claim 1 ...

Apparatus for storing hydrogen and magnetic energy and a method for the operation of said apparatus

An apparatus for storing hydrogen and magnetic energy includes a storage tank for liquefied hydrogen with an inlet line for compressed hydrogen and an outlet line for hydrogen at a relatively low pressure. The apparatus includes a superconducting magnetic energy store, which comprises a magnetic coil relative to which electrical energy can be supplied or withdrawn via power supply lines to the magnet coil, the energy being located in a cryogenic tank provided with a cooling device and being held at operating temperature. The storage tank for liquefied hydrogen includes cooling device, at least one regenerator, with a heat-absorbing and heat-emitting storage medium, a warm side and a cold side. From the warm side, the compressed hydrogen and, from the cold side, liquefied hydrogen can be supplied from the storage tank for liquefied hydrogen. A relief valve is located in the field region of the at least one magnet coil. The relief valve is connected to the cold side of the regenerator so the compressed hydrogen, having passed through the regenerator, can be fed into the relief valve and, owing to the pressure relief, can be supplied, at least partially as liquefied hydrogen to the storage tank for liquefied hydrogen.

METHOD AND APPARATUS FOR SEPARATING AIR BY CRYOGENIC DISTILLATION

An apparatus for separating air by cryogenic distillation comprises N air compressors (C C C) connected so as to receive air at ambient pressure and designed to produce air at a first pressure above 12 bar absolute, N being at least 3, each of the compressors being driven by a single asynchronous motor (M M M), the total power of the compressors being at least 10 MW. 111-. (canceled)12. A method for separating air by cryogenic distillation , in which:i) sending N flows of air at approximately ambient pressure each to one of the N air compressors;ii) compressing the air using each of the N compressors at a first pressure above 12 bar absolute and below 35 bar absolute, N being equal to or greater than 3 and the total power of the N compressors being greater than 10 MW;iii) sending the air at the first pressure of the N compressors to a single purification unit in order to remove water and carbon dioxide and cooling the air in the purification unit before sending the air to a single system of columns in a single cold box where the air is separated by cryogenic distillation;iv) extracting an enriched flow from the system of columns, wherein the enriched flow is selected from the group consisting of an oxygen-enriched flow, a nitrogen-enriched flow, and combinations thereof;v) sending air from each of the N compressors to the system of columns through the purification unit, without sending air at the first pressure to an air booster driven by a motor or a steam turbine; andvi) driving each of the N compressors by a single motor, these N motors being asynchronous and having a maximum power below 25 MW.13. The method according to claim 12 , in which all the air sent to the system of columns comes from the N compressors.14. The method according to claim 12 , in which N is equal to 4 claim 12 , 5 claim 12 , 6 claim 12 , 7 claim 12 , 8 claim 12 , 9 or 10.15. The method according to claim 12 , in which N air compressors each send no more than 100%/N of the air that they ...

N2O LIQUEFACTION SYSTEM WITH SUBCOOLING HEAT EXCHANGER FOR MEDICAL DEVICE

A system and kit for using a source of low-pressure refrigerant for a cryotherapy procedure and for subcooling a cryotherapy refrigerant. The system may generally include a fluid reservoir and a fluid flow path in thermal exchange with the fluid reservoir, the fluid flow path including a first thermal exchange device in thermal exchange with the fluid reservoir, a compressor in fluid communication with the first thermal exchange device, a condenser, a reversing valve located between the compressor and the condenser, a second thermal exchange device located between the reversing valve and the compressor, and an expansion valve located between the condenser and the thermal exchange device. The third thermal exchange device may be configured to be in fluid communication with the cryotherapy console and configured to place a secondary refrigerant within the first fluid flow path in thermal communication with a secondary refrigerant of the cryotherapy system. 1. A kit for use with a source of low-pressure refrigerant , the kit comprising:a fluid reservoir; and a first thermal exchange device in thermal exchange with and fluidly isolated from the fluid reservoir;', 'a compressor in fluid communication with the first thermal exchange device;', 'a condenser;', 'a reversing valve located between the compressor and the condenser; and', 'a second thermal exchange device located between the reversing valve and the compressor., 'a closed-loop fluid flow path in thermal exchange with the fluid reservoir, the closed-loop fluid flow path including2. The kit of claim 1 , wherein the second thermal exchange device is configured to be in fluid communication with a cryotherapy console.3. The kit of claim 1 , wherein the fluid flow path is a first fluid flow path claim 1 , the kit further including a second fluid flow path that is fluidly isolated from the first fluid flow path claim 1 , the fluid reservoir being included in the second fluid flow path.4. The kit of claim 3 , wherein the ...

PURIFYING CRYOGENIC FLUIDS

A cryogenic fluid purification device comprising: a first container defining an interior region; a second container defining an interior region in fluid communication with the interior region of the first container; and a cryogenic fluid in contact with an exterior of the second container. 1. A cryogenic fluid purification device comprising:a first container defining an interior region;a second container defining an interior region in fluid communication with the interior region of the first container; anda cryogenic fluid in contact with an exterior of the second container.2. The device of claim 1 , wherein the second container is sized and configured to be received at least partially in the interior region of the first container.3. The device of claim 2 , comprising a manifold extending from an outlet of the first container to an inlet of the second container.4. The device of claim 3 , the manifold comprising an oxygen rejecting filter.5. The device of claim 3 , the manifold comprising pressure relief6. The device of claim 2 , comprising a pump operable to reduce pressure in the interior region of the first container.7. The device of claim 1 , comprising a filter disposed in a path providing fluid communication between the interior region of the second container and the interior region of the first container.8. The device of claim 1 , wherein the first container comprises a spout configured to engage a port of the second container.9. The device of claim 8 , comprising a third container defining an interior region claim 8 , wherein the second container is sized and configured to be received at least partially in the interior region of the third container. This application claims priority to U.S. Provisional Patent Application No. 62/187,936, filed on Jul. 2, 2015, the entire contents of which is incorporated herein by reference.This disclosure relates to devices and methods for purifying cryogenic fluids.Nitrogen, as an element of great technical importance, can be ...

SYSTEM AND METHOD FOR STORAGE AND DELIVERY OF CRYOGENIC LIQUID AIR

One aspect of the disclosure provides a system for storing a cryogenic mixture of liquid air and providing a source of breathable air. In an embodiment, the system comprises an insulated storage vessel, a cryocooler, and a vaporizing unit. The insulated storage vessel contains a cryogenic mixture of liquid air comprising liquid nitrogen (LN) and liquid oxygen (LO) The cryocooler is mounted to an exterior of the storage vessel to condense liquid air that vaporizes within the storage vessel, thereby returning the vaporized liquid air to a liquid phase such that concentrations of the LNand LOin the cryogenic mixture remain approximately constant. The vaporizing unit is external of the storage vessel and is in fluid communication with an interior of the storage vessel. Liquid air from the interior of the storage vessel passes through, vaporizes, and exits the vaporizing unit as the breathable air. 1. A system for storing a cryogenic mixture of liquid air and providing a source of breathable air , comprising:{'sub': 2', '2, 'an insulted storage vessel containing a cryogenic mixture of liquid air comprising liquid nitrogen (LN) and liquid oxygen (LO);'}{'sub': 2', '2, 'a cryocooler mounted to an exterior of said storage vessel to condense liquid air that vaporizes within said storage vessel thereby returning said vaporized liquid air to a liquid phase such that concentrations of said LNand LOin the cryogenic mixture remain approximately constant, said returning said vaporized liquid air to said liquid phase also reducing pressure in said storage vessel within a predetermined pressure range; and'}a vaporizing unit, external of said storage vessel in fluid communication with an interior of said storage vessel, and in which said liquid air from said interior of said storage vessel passes through, vaporizes, and exits said vaporizing unit as said breathable air.2. The system of claim 1 , wherein said cryogenic mixture of said liquid air may comprise about 79% of said LNand ...

SYSTEM AND METHOD FOR LIQUEFYING A FLUID AND STORING THE LIQUEFIED FLUID

A Dewar system is configured to liquefy a flow of fluid, and to store the liquefied fluid. The Dewar system is disposed within a single, portable housing. Disposing the components of the Dewar system within the single housing enables liquefied fluid to be transferred between a heat exchange assembly configured to liquefy fluid and a storage assembly configured to store liquefied fluid in an enhanced manner. In one embodiment, the flow of fluid liquefied and stored by the Dewar system is oxygen (e.g., purified oxygen), nitrogen, and/or some other fluid. 1. A system configured to liquefy a fluid , and to store the liquefied fluid , the system comprising:a housing configured to substantially seal the interior of the housing from atmosphere comprising a first piece and a second piece, wherein the first piece and the second piece are configured to be selectably coupled together to substantially seal the interior of the housing from atmosphere, wherein the second piece of the housing forms a cavity having an opening formed by a rim of the second piece of the housing, and wherein the first piece of the housing is a lid that is selectably coupled to the rim of the second piece of the housing to substantially seal the cavity formed by the first piece of the housing from atmosphere;a heat exchange assembly disposed within the housing, the heat exchange assembly comprising a fluid conduit that passes from inside the housing to outside the housing, the fluid conduit being configured to receive a flow of fluid in its gaseous state from a fluid flow generator located outside the housing, the heat exchange assembly being configured to liquefy the flow of fluid received into the heat exchange assembly via the fluid conduit, and wherein the heat exchange assembly is formed integrally or securely with the first piece of the housing; anda fluid storage assembly disposed within the housing, the fluid storage assembly being in fluid communication with the heat exchange assembly, the ...

RAW MATERIAL GAS LIQUEFYING DEVICE AND METHOD OF CONTROLLING THIS RAW MATERIAL GAS LIQUEFYING DEVICE

A raw material gas liquefying device includes a feed line which feeds a raw material gas, a refrigerant circulation line which circulates a refrigerant, the refrigerant circulation line including an expansion unit of a turbine type which expands the refrigerant to generate cryogenic energy, and an expansion unit entrance valve provided at an entrance side of the expansion unit, a heat exchanger which exchanges heat between the raw material gas and the refrigerant, a cooler which performs initial cooling of the raw material gas and the refrigerant by heat exchange with liquid nitrogen, and a controller which manipulates the opening rate of the expansion unit entrance value and performs a feedback control so that the rotation speed of the expansion unit reaches a predetermined target value, and outputs the opening rate command to the expansion unit entrance valve, at start-up and stop of the expansion unit. 1. raw material gas liquefying device comprising:a feed line which feeds a raw material gas whose boiling temperature is lower than a boiling temperature of nitrogen;a refrigerant circulation line which circulates a refrigerant for cooling the raw material gas, the refrigerant circulation line including an expansion unit of a turbine type which expands the refrigerant to generate cryogenic energy, and an expansion unit entrance valve provided at an entrance side of the expansion unit;a heat exchanger which exchanges heat between the raw material gas and the refrigerant;a cooler which performs initial cooling of the raw material gas and the refrigerant by heat exchange with liquid nitrogen;an expansion unit rotation speed sensor which detects a rotation speed of the expansion unit; anda controller which generates an opening rate command for the expansion unit entrance valve by performing a feedback control so that the rotation speed of the expansion unit reaches a predetermined target value, and outputs the opening rate command to the expansion unit entrance valve, ...

AIR SEPARATION METHOD AND APPARATUS WITH IMPROVED ARGON RECOVERY

A method and apparatus for separating air in which an argon refining column of a distillation column system is reboiled with a liquid air stream. The argon refining column further refines crude argon produced by a crude argon column connected to a lower pressure column of the distillation column system. At least one intermediate reflux stream is formed, at least indirectly, from at least part of the liquid air stream, and is introduced into the lower pressure column at a level thereof above where a crude liquid oxygen column bottoms of a higher pressure column of such system is further refined to increase a liquid to vapor ratio below said level and therefore, argon recovery from the argon refining column. 1. A method of separating air comprising:compressing and purifying the air such that a first compressed air stream and a second compressed air stream are produced, the second compressed air stream having a higher pressure than the first compressed air stream;cooling at least part of the first compressed air stream and condensing the second compressed air stream through indirect heat exchange with return streams produced by a distillation column system to form a liquid air stream;producing a refrigerant stream and imparting refrigeration with the use of the refrigeration stream into the distillation column system;introducing the at least part of the first compressed air stream into a higher pressure column of the distillation column system, the distillation column system also having a lower pressure column operatively associated with the higher pressure column in a heat transfer relationship, a crude argon column connected to the lower pressure column to rectify an argon-oxygen containing vapor stream withdrawn from the lower pressure column to thereby, at least in part, produce a crude argon stream and an argon refining column to rectify the crude argon stream and thereby form an argon product stream from an argon-rich liquid column bottoms produced in the argon ...

AIR SEPARATION METHOD AND APPARATUS WITH IMPROVED ARGON RECOVERY

A method and apparatus for separating air in which an argon refining column of a distillation column system is reboiled with a liquid air stream. The argon refining column further refines crude argon produced by a crude argon column connected to a lower pressure column of the distillation column system. At least one intermediate reflux stream is formed, at least indirectly, from at least part of the liquid air stream, and is introduced into the lower pressure column at a level thereof above where a crude liquid oxygen column bottoms of a higher pressure column of such system is further refined to increase a liquid to vapor ratio below said level and therefore, argon recovery from the argon refining column. 1. An apparatus for separating air comprising:a main air compressor for compressing the air;a purification system connected to the main air compressor for purifying the air and thereby producing a compressed and purified air stream;a booster compressor in flow communication with the purification unit such that a first compressed air stream is produced from at least part of the compressed and purified air stream and a second compressed air stream is produced by compressing another part of the compressed and purified air stream in the booster compressor to a higher pressure than the first compressed air stream;a main heat exchanger configured to cool at least part of the first compressed air stream and to condense the second compressed air stream and form a liquid air stream through indirect heat exchange with return streams produced by a distillation column system;the distillation column system having a higher pressure column in flow communication with the main heat exchanger so as to receive the at least part of the first compressed air stream, a lower pressure column operatively associated with the higher pressure column in a heat transfer relationship, a crude argon column connected to the lower pressure column to rectify an argon-oxygen containing vapor stream ...

Systems and Methods for the Production of Liquefied Natural Gas Using Liquefied Natural Gas

Described herein are systems and processes to produce liquefied nitrogen (LIN) using liquefied natural gas (LNG) as the refrigerant. The LIN may be produced by indirect heat exchange of at least one nitrogen gas stream with at least two LNG streams within at least one heat exchanger where the LNG streams are at different pressures. 1. A method for producing a liquefied first gas stream at a gas processing facility comprising:(a) providing a first gas stream;(b) providing a liquefied second gas stream, where the second gas is different than the first gas and where the liquefied second gas stream is produced from the liquefaction of a second gas stream at a location that is different from the gas processing facility;(c) splitting the liquefied second gas stream into at least a first liquefied second gas stream and a second liquefied second gas stream;(d) reducing the pressure of the first liquefied second gas stream such that the pressure of the first liquefied second gas stream is less than that of the second liquefied second gas stream;(e) liquefying the first gas stream to form a liquefied first gas stream by indirect heat exchange of the first gas stream with the first liquefied second gas stream and the second liquefied second gas stream;(f) vaporizing at least a portion of the first liquefied second gas stream to form a first second gas stream;(g) vaporizing at least a portion of the second liquefied second gas stream to form a second second gas stream;(h) compressing at least one of the first second gas stream and the second second gas stream to form a compressed second gas stream.2. A method for producing a liquefied nitrogen gas (LIN) stream at a liquid natural gas (LNG) regasification facility comprising:(a) providing a nitrogen gas stream;(b) providing at least two LNG streams where the pressures of each LNG stream are independent and different from each other;(c) liquefying the nitrogen gas stream by indirect heat exchange of the nitrogen gas stream with ...

System and Method for the Production of Liquefied Natural Gas

A method for producing liquefied natural gas (LNG) is provided. The method may include feeding natural gas from a high-pressure natural gas source to a separator and removing a non-hydrocarbon from the natural gas. A portion of the natural gas from the separator may be precooled, and the precooled natural gas may be cooled in a first heat exchanger with a first refrigeration stream. A first portion of the cooled natural gas may be expanded in a turbo-expander to generate the first refrigeration stream. A second portion of the cooled natural gas may be cooled in a second heat exchanger with the first refrigeration stream and expanded in an expansion valve to produce a two-phase fluid containing the LNG and a vapor phase. The LNG may be separated from the vapor phase in a liquid separator and stored in a storage tank. 1. A method for producing liquefied natural gas from a high-pressure natural gas source , comprising:feeding natural gas from the high-pressure natural gas source to a separator;removing a non-hydrocarbon from the natural gas in the separator;precooling a portion of the natural gas from the separator in a cooling assembly;cooling the precooled natural gas from the cooling assembly in a first heat exchanger with a first refrigeration stream;expanding a first portion of the cooled natural gas from the first heat exchanger in a turbo-expander to generate the first refrigeration stream;cooling a second portion of the cooled natural gas from the first heat exchanger in a second heat exchanger with the first refrigeration stream;expanding the second portion of the cooled natural gas from the second heat exchanger in an expansion valve to produce a two-phase fluid containing the liquefied natural gas and a vapor phase;separating the liquefied natural gas from the vapor phase in a liquid separator; andstoring the liquefied natural gas in a storage tank.2. The method of claim 1 , further comprising at least partially separating natural gas liquids from the first ...

PROCESS AND PLANT FOR THE PRODUCTION OF LIQUID HYDROGEN

Process and plant for the production of liquid hydrogen with a liquefier that has a variable cooling power dependent on the electrical power consumed. The liquefier is supplied with electricity by a first source of electricity at least one additional source of electricity that provides an intermittent or variable amount of electricity over time. Liquid hydrogen is produced at first thermodynamic conditions when the liquefier is supplied with a predetermined nominal electrical energy level and produced at subcooled conditions, with respect to the first thermodynamic conditions, when electricity supplied to the liquefier exceeds the nominal level. 1. A process for production of liquid hydrogen though use of a liquefier fed by a source of gaseous hydrogen , the liquefier being of the electric type and having a variable cooling power dependent on the electrical power consumed , the liquefier being supplied with electricity by a first source of electricity and being connected to at least one additional source of electricity that provides an amount of electricity which is intermittent or variable over time , wherein liquid hydrogen is produced by the liquefier at first thermodynamic conditions when the liquefier is supplied with electricity at a predetermined nominal electrical energy level and , when the liquefier is supplied with electricity at an energy level exceeding the said nominal level , the hydrogen produced by the liquefier is subcooled with respect to the first thermodynamic conditions.2. The process of claim 1 , wherein claim 1 , when the liquefier is supplied with electricity at the nominal electrical energy level claim 1 , the liquid hydrogen produced by the liquefier is in a saturated state.3. The process of claim 1 , wherein claim 1 , when the liquefier is supplied with electricity at an energy level exceeding the nominal level claim 1 , the liquid hydrogen produced by the liquefier is subcooled with respect to its saturated state.4. The process of claim ...

METHOD AND DEVICE FOR GENERATING ELECTRICAL ENERGY

A method and device for generating electrical energy in a combined system of power plant, cold storage system and air compression system. The air compression system has a primary air compressor for generating a primary compressed air flow at a first pressure level. The power plant has a combustion unit which operates at a second pressure level and generates a combustion gas from which electrical energy is generated. The cold storage system has means for generating cold from compressed air, means for storing cold thus produced and means for generating a compressed air flow at the second pressure level using the stored cold. In a first operating mode (charging mode), a first compressed air flow is introduced from the air compression system into the cold storage system to charge the cold reservoir. In a second operating mode (discharging mode), the first compressed air flow generated in the primary air compressor, is introduced into the cold storage system to discharge the cold reservoir and to generate a third compressed air flow at the second pressure level, which is introduced into the combustion unit. The air compression system has a first booster for boosting compressed air compressed in the primary air compressor to the second pressure level. In a third operating mode (normal mode), the entire primary compressed air flow generated in the primary air compressor is boosted in the first booster to the second compressed air level and introduced into the combustion unit. 2. The method as claimed in claim 1 , characterized in that claim 1 , in the second operating mode (discharging operation) claim 1 , the first compressed air flow is formed only by a first part of the primary compressed air flow generated in the primary air compressor.3. The method as claimed in claim 2 , characterized in that claim 2 , in the second operating mode (discharging operation) claim 2 , a second part of the primary compressed air flow generated in the primary air compressor is led past the ...

LARGE LIQUID OXYGEN AND LIQUEFIED NATURAL GAS PRODUCTION PROCESS

A process for co-producing a liquid oxygen and a liquefied hydrocarbon stream, including introducing a gaseous hydrocarbon stream and a gaseous nitrogen stream into a liquefier, thereby producing a liquefied hydrocarbon stream and a liquid nitrogen stream, liquefying a gaseous oxygen stream, wherein at least a portion of the required refrigeration is obtained from the liquid nitrogen stream. Wherein the liquefied hydrocarbon stream and the liquefied gaseous oxygen stream have mass flow rates. The liquid oxygen stream may be produced in an aft separation unit, wherein at least a portion of the required refrigeration is obtained from the liquid nitrogen stream. 1. A process for co-producing a liquid oxygen and a liquefied hydrocarbon stream , comprising:introducing a gaseous hydrocarbon stream and a gaseous nitrogen stream into a liquefier, thereby producing a liquefied hydrocarbon stream and a liquid nitrogen stream,liquefying a gaseous oxygen stream, wherein at least a portion of he required refrigeration is obtained from the liquid nitrogen stream, wherein the liquefied hydrocarbon stream and the liquefied gaseous oxygen stream have mass flow rates.2. The process of claim 1 , wherein the ratio of mass flow rates of the liquefied gaseous oxygen stream and the liquefied hydrocarbon stream is between 2 to 5.3. The process of claim 1 , wherein the ratio of mass flow rates of the liquefied gaseous oxygen stream and the liquefied hydrocarbon stream is between 3 to 4.4. The process of claim 1 , wherein the liquefier uses a dual refrigerant liquefaction process claim 1 , comprising a first refrigerant and a secondary refrigerant.5. The process of claim 4 , wherein the first refrigerant is nitrogen or neon or a mixture of neon and nitrogen.6. The process of claim 4 , wherein the secondary refrigerant is a hydrocarbon mixed refrigerant.7. A process for co-producing a liquid oxygen and a liquefied hydrocarbon stream claim 4 , comprising:introducing a gaseous hydrocarbon ...

Liquid Air Energy Storage Systems, Devices, and Methods

Liquid air energy storage (LAES) systems with increased efficiency and operating profit obtained through rational selection and configuration of the equipment used and optimization of the configuration/parameters of such equipment. In various embodiments, the LAES system is intended for operation preferably in an environmentally-friendly stand-alone regime with recovery of hot thermal energy extracted from compressed charging air and cold thermal energy extracted from discharged air.

METHODS FOR RECOVERING NATURAL GAS USING NITROGEN REJECTION UNITS

A method and system for enhanced oil recovery by performing the steps of feeding a mixture of nitrogen from a primary nitrogen supply and an optional supplemental nitrogen supply into an oil field; separating recovered oil from a gas mixture comprising nitrogen, natural gas and C2+ hydrocarbons; feeding the gas mixture to a nitrogen rejection unit operating at elevated pressures; and recovering the nitrogen, natural gas and C2+ hydrocarbons. A method for the recovery of natural gas is also described herein. 1. A method for enhanced oil recovery comprising the steps of (a) feeding nitrogen from a primary nitrogen supply into an oil field; (b) recovering oil and a gas mixture comprising nitrogen , natural gas and C2+ hydrocarbons from the oil field; (c) separating the oil from the gas mixture (d) feeding the gas mixture to a nitrogen rejection unit; and (d) recovering nitrogen , natural gas and C2+ hydrocarbons.2. The method as claimed in further comprising feeding a supplemental nitrogen supply into the oil field.3. The method as claimed in wherein the primary nitrogen supply is from an air separation unit.4. The method as claimed in wherein the supplemental nitrogen supply is from a supplemental air separation unit.5. The method as claimed in wherein the primary nitrogen supply is fed to a high pressure compressor.6. The method as claimed in wherein the high pressure compressor operates at a pressure up to 6700 pounds per square inch.7. The method as claimed in wherein the oil and the gas mixture are fed to an oil separation and sour gas removal unit claim 1 , thereby separating the recovered oil from the gas mixture.8. The method as claimed in wherein the recovered oil is fed to a storage system.9. The method as claimed in wherein the nitrogen rejection unit will separate the nitrogen from the natural gas and C2+ hydrocarbons.10. The method as claimed in wherein the nitrogen rejection unit is operating at high pressures.11. The method as claimed in wherein the high ...

METHOD AND INSTALLATION FOR STORING AND RECOVERING ENERGY

A method and installation for storing and recovering energy, according to which a condensed air product is formed in an energy storage period, and in an energy recovery period, a pressure flow is formed and is expanded to produce energy using at least part of the condensed air product. For the formation of the condensed air product: the compression of air in an air conditioning unit, at least by means of at least one isothermally operated compressor device and the adsorptive cleaning of the air by means of at least one adsorptive cleaning device at a hyperbaric pressure level. 1. A method for storing and recovering energy in which , in an energy storage period , an air liquefaction product is formed and , in an energy recovery period , a pressurized stream is formed and expanded to perform work by using at least part of the air liquefaction product , the method comprising , compressing air in an air conditioning unit, at least by means of at least one isothermally operated compressor device, and adsorptively purifying the air by means of at least one adsorptive purification device at a superatmospheric pressure level,', 'liquefying the compressed and adsorptively purified air, starting from a temperature level in a range of 0 to 50° C., in a first fraction in a fixed-bed cold storage unit and in a second fraction in a counterflow heat exchanger unit at a liquefaction pressure level in a range of 40 to 100 bara, and', 'subsequently expanding the liquefied air in at least one cold production unit,, 'for the formation of the air liquefaction product,'} producing a vaporization product from at least part of the liquefaction product at a vaporization pressure level, which deviates by no more than 5 bar from the liquefaction pressure level, in the fixed-bed cold storage unit, and', 'forming a fluid stream from at least part of the vaporization product and conducting it through at least one combustion device, in which a fuel is burned., 'and, for the formation of the ...

LIQUID HYDROGEN PRODUCTION FACILITY AND HYDROGEN GAS PRODUCTION FACILITY

A reformer configured to generate hydrogen gas by reforming a hydrocarbon; a hydrogen liquefier configured to generate liquid hydrogen by liquefying the hydrogen gas; a reservoir for storing the liquid hydrogen; and a heat exchanger configured to cause heat exchange between boil-off gas that occurs in the reservoir and carbon dioxide that occurs during a process of generating the hydrogen gas to liquefy the carbon dioxide. 1. A liquid hydrogen production facility comprising:a reformer configured to generate hydrogen gas by reforming a hydrocarbon;a hydrogen liquefier configured to generate liquid hydrogen by liquefying the hydrogen gas;a reservoir for storing the liquid hydrogen; anda heat exchanger configured to cause heat exchange between boil-off gas that occurs in the reservoir and carbon dioxide that occurs during a process of generating the hydrogen gas to liquefy the carbon dioxide.2. A liquid hydrogen production facility comprising:a reformer configured to generate hydrogen gas by reforming a hydrocarbon;a hydrogen liquefier configured to generate liquid hydrogen by liquefying the hydrogen gas by cooling the hydrogen gas with use of heat of vaporization of liquid nitrogen; anda heat exchanger configured to cause heat exchange between nitrogen gas that is discharged from the hydrogen liquefier and carbon dioxide that occurs during a process of generating the hydrogen gas to liquefy the carbon dioxide.3. The liquid hydrogen production facility according to claim 1 , whereinthe hydrocarbon is methane contained in liquefied natural gas as a major component.4. The liquid hydrogen production facility according to claim 1 , whereinthe reformer reforms the hydrocarbon by steam reforming.5. A hydrogen gas production facility comprising:a reformer configured to generate hydrogen gas by reforming a hydrocarbon;a reservoir for storing liquid hydrogen supplied from outside; anda heat exchanger configured to cause heat exchange between boil-off gas that occurs in the ...

COLD STORAGE METHODS

In a liquid air energy system, cold storage is accomplished using heat pipes as the heat transfer device. The cold energy storage unit is charged by feeding high pressure air to a liquid cold storage unit wherein the high pressure air becomes liquid air; feeding the liquid air to a liquid air storage unit; feeding cold liquid to the liquid cold storage unit wherein the cold liquid becomes warm liquid; and feeding warm liquid to a warm liquid storage unit. 1. A method for charging a cold energy storage unit comprising the steps:Feeding high pressure air to a liquid cold storage unit wherein the high pressure air becomes liquid air;Feeding the liquid air to a liquid air storage unit;Feeding cold liquid to the liquid cold storage unit wherein the cold liquid becomes warm liquid; andFeeding warm liquid to a warm liquid storage unit.2. The method as claimed in wherein the liquid cold storage unit contains heat pipes.3. The method as claimed in wherein the heat pipes are in bundles of heat pipes.4. The method as claimed in wherein the heat pipes contain a refrigerant selected from the group consisting of carbon dioxide claim 2 , carbon tetrafluoride claim 2 , freons and nitrogen.5. The method as claimed in claim I wherein the liquid cold storage unit contains a refrigerant.6. The method as claimed in wherein the liquid cold storage unit will receive heat from the warm liquid tank and dispense cold to the liquid air during discharge.7. The method as claimed in wherein two or more liquid cold storage units are connected in series.8. The method as claimed in wherein the liquid cold storage unit comprises two chambers containing a working fluid.9. The method as claimed in wherein the heat pipes connect the two chambers and are in contact with the working fluid.10. The method as claimed in wherein the heating of pressurized liquid aft to high pressure air provides a source of energy for electricity generation.11. The method as claimed in wherein the electricity generation is ...

Methods and systems for integration of industrial site efficiency losses to produce lng and/or lin

A method includes receiving input corresponding to a proposed configuration of a liquefaction facility and identifying a plurality of components utilized to produce LNG and/or LIN at the facility. The method includes determining an alternative configuration that is different from the proposed configuration. Determining the alternative configuration may include identifying resources accessible to a proposed location for the liquefaction facility and whether at least one of the resources accessible to the proposed location corresponds to a resource generated by a component identified by the proposed configuration, and determining whether to omit at least one component of the plurality of components identified by the proposed configuration. The method includes omitting the at least one component from the alternative configuration, and generating a report based on the proposed configuration and the alternative configuration. The report includes information indicating a difference between the proposed configuration and the alternative configuration.

METHOD FOR THE INTEGRATION OF A NITROGEN LIQUEFIER AND LETDOWN OF NATURAL GAS FOR THE PRODUCTION OF LIQUID NITROGEN AND LOWER PRESSURE NATURAL GAS

A method describing the integration of a nitrogen liquefier and letdown of natural gas for the production of liquid nitrogen and lower pressure natural gas is provided. The method may include: providing a nitrogen liquefier having a nitrogen refrigeration cycle, wherein the nitrogen liquefier comprises a nitrogen compressor, a nitrogen recycle compressor, a heat exchanger, and at least a first turbine booster and introducing a nitrogen gas stream to the nitrogen liquefier under conditions effective for liquefying the nitrogen to produce a liquid nitrogen product. The refrigeration needed to liquefy the nitrogen is provided for by the nitrogen refrigeration cycle and letdown of a high pressure natural gas stream. 1. A method for the integration of a nitrogen liquefier and letdown of natural gas for the production liquid nitrogen (“LIN”) , the method comprising the steps of:a) providing a nitrogen liquefier having a nitrogen refrigeration cycle, wherein the nitrogen liquefier comprises a nitrogen recycle compressor, a heat exchanger, and a first turbine booster;b) introducing a nitrogen gas stream to the nitrogen liquefier under conditions effective for liquefying the nitrogen to produce a liquid nitrogen product;{'sub': 'H', 'c) withdrawing a natural gas stream from a source operating at a first pressure P;'}d) purifying the natural gas stream in a purification unit to produce a purified natural gas;e) partially cooling the purified natural gas in the heat exchanger;withdrawing the partially cooled natural gas from an intermediate section of the heat exchanger;{'sub': M', 'M', 'H, 'g) expanding the partially cooled natural gas to a medium pressure Pin a natural gas expansion turbine to form a cold natural gas stream, wherein the medium pressure Pis at a pressure lower than the first pressure P; and'}h) warming the cold natural gas stream in the heat exchanger by heat exchange against nitrogen from the nitrogen refrigeration cycle to produce a warm natural gas stream ...

METHOD FOR THE PRODUCTION OF LIQUEFIED NATURAL GAS AND LIQUID NITROGEN

A method for the production of liquefied natural gas and liquid nitrogen is provided. The method may include providing a high pressure natural gas stream, splitting the high pressure natural gas stream into a first portion and a second portion, and liquefying the first portion of the high pressure natural gas stream to produce an LNG stream. The refrigeration needed for cooling and liquefaction of the natural gas and liquefaction of the nitrogen can be provided by a nitrogen refrigeration cycle and letdown of the second portion of the high pressure natural gas stream. 1. A method for the production of liquefied natural gas (“LNG”) and liquid nitrogen (“LIN”) , the method comprising the steps of:a) providing a nitrogen refrigeration cycle, wherein the nitrogen refrigeration cycle is configured to provide refrigeration within a heat exchanger, wherein a portion of the nitrogen within the nitrogen refrigeration cycle is withdrawn and liquefied yielding a liquid nitrogen product, wherein at least an equal portion of gaseous nitrogen is introduced to the nitrogen refrigeration cycle as is withdrawn;b) purifying a first natural gas stream in a first purification unit to remove a first set of impurities to produce a purified first natural gas stream;{'sub': 'H', 'c) cooling and liquefying the first natural gas stream in the heat exchanger using the refrigeration from the nitrogen refrigeration cycle to produce an LNG stream, wherein the first natural gas stream has an LNG refrigeration requirement, wherein the LNG stream is liquefied at a first pressure P;'}d) purifying a second natural gas stream in a second purification unit to remove a second set of impurities to produce a purified second natural gas stream;e) partially cooling the second natural gas stream in the heat exchanger;f) withdrawing the partially cooled second natural gas stream from an intermediate section of the heat exchanger;{'sub': M', 'M', 'H, 'g) expanding the partially cooled second natural gas stream ...

METHOD FOR THE INTEGRATION OF A NITROGEN LIQUEFIER AND LIQUEFACTION OF NATURAL GAS FOR THE PRODUCTION OF LIQUEFIED NATURAL GAS AND LIQUID NITROGEN

A method for the integration of a nitrogen liquefier and liquefaction of natural gas for the production of liquefied natural gas and liquid nitrogen is provided. The method may include providing a nitrogen liquefaction unit and providing a natural gas liquefaction unit. Liquefaction of the nitrogen can be achieved via a nitrogen refrigeration cycle within the nitrogen liquefaction unit. Liquefaction of the natural gas can be achieved through the use of natural gas letdown and a second nitrogen refrigeration cycle. The two liquefaction units can be integrated via a common nitrogen recycle compressor, thereby providing significant capital savings. 1. A method for the integration of a nitrogen liquefier and natural gas liquefier for the production of liquefied natural gas (“LNG”) and liquid nitrogen (“LIN”) , the method comprising the steps of:a) providing a nitrogen liquefier having a first nitrogen refrigeration cycle, wherein the nitrogen liquefier comprises a turbine, a booster and a plurality of coolers, wherein the first nitrogen refrigeration cycle is configured to provide refrigeration within a first heat exchanger;b) providing a second nitrogen refrigeration cycle, wherein the second nitrogen refrigeration cycle comprises a second turbine, a second booster and a plurality of second coolers, wherein the second nitrogen refrigeration cycle is configured to provide refrigeration within a second heat exchanger;c) purifying a first natural gas stream in a first purification unit to remove a first set of impurities to produce a purified first natural gas stream;{'sub': 'H', 'd) cooling and liquefying the first natural gas stream in the second heat exchanger using the refrigeration from the nitrogen refrigeration cycle to produce an LNG stream, wherein the first natural gas stream has an LNG refrigeration requirement, wherein the LNG stream is liquefied at a first pressure P;'}e) purifying a second natural gas stream in a second purification unit to remove a second ...

METHOD FOR THE PRODUCTION OF LIQUEFIED NATURAL GAS AND NITROGEN

A method for the production of liquefied natural gas (“LNG”) and nitrogen is provided. The method may include the steps of: a) providing a nitrogen production facility, wherein nitrogen production facility comprises: a main heat exchanger, an air separation unit, a nitrogen recycle compressor, a first nitrogen refrigeration supply configured to provide refrigeration to the main heat exchanger for cooling a main air feed, b) providing a secondary refrigeration supply; c) liquefying a natural gas stream using refrigeration from the secondary refrigeration supply to form an LNG product stream; wherein the secondary refrigeration supply is configured to compress and expand a refrigerant to produce refrigeration, wherein the refrigerant of the secondary refrigeration supply is shared with refrigerant of the first nitrogen refrigeration supply 1. A method for the production of liquefied natural gas (“LNG”) and nitrogen , the method comprising the steps of:a) providing a nitrogen production facility, wherein nitrogen production facility comprises: a main heat exchanger, an air separation unit, a nitrogen recycle compressor, a first nitrogen refrigeration supply configured to provide refrigeration to the main heat exchanger for cooling a main air feed;b) providing a secondary refrigeration supply;c) liquefying a natural gas stream using refrigeration from the secondary refrigeration supply to form an LNG product stream;wherein the secondary refrigeration supply is configured to compress and expand a refrigerant to produce refrigeration, wherein the refrigerant of the secondary refrigeration supply is shared with refrigerant of the first nitrogen refrigeration supply.2. The method as claimed in claim 1 , wherein the secondary refrigeration supply comprises a third turbine-booster claim 1 , wherein the third turbine-booster has a third booster and a third turbine.3. The method as claimed in claim 2 , wherein the natural gas stream is liquefied in a secondary heat exchanger.4. ...

INTEGRATION OF INDUSTRIAL GAS SITE WITH LIQUID HYDROGEN PRODUCTION

The method for producing liquid hydrogen can include the steps of: introducing pressurized natural gas from a high pressure natural gas pipeline to a gas processing unit under conditions effective for producing a purified hydrogen stream; and introducing the purified hydrogen stream to a hydrogen liquefaction unit under conditions effective to produce a liquid hydrogen stream, wherein the hydrogen liquefaction unit provides a warm temperature cooling and a cold temperature cooling to the purified hydrogen stream, wherein the warm temperature cooling is provided by utilizing letdown energy of a pressurized stream selected from the group consisting of a nitrogen stream sourced from a nitrogen pipeline, a natural gas stream sourced from the high pressure natural gas pipeline, an air gas sourced from an air separation unit, and combinations thereof, wherein the cold temperature is provided by utilizing letdown energy of the purified hydrogen stream. 1. A method for liquefying a pressurized hydrogen gas originating from a pressure swing adsorber unit , the method comprising the steps of:withdrawing a hydrogen containing gas from a methanol production unit;introducing the hydrogen containing gas to a pressure swing adsorber (PSA) unit under conditions effective for purifying the hydrogen containing gas to produce a purified hydrogen stream;sending the purified hydrogen gas to a hydrogen liquefaction unit under conditions effective for the liquefaction of hydrogen thereby producing a liquefied hydrogen stream,wherein the hydrogen liquefaction unit is configured to provide a first refrigeration source and a second refrigeration source, wherein the first refrigeration source provides refrigeration using expansion of a high pressure nitrogen stream, wherein the second refrigeration source provides refrigeration using expansion of a high pressure hydrogen gas stream to produce a warm hydrogen gas stream,wherein the high pressure hydrogen gas stream is derived from a hydrogen ...

PLANT FOR THE LIQUEFACTION OF NITROGEN USING THE RECOVERY OF COLD ENERGY DERIVING FROM THE EVAPORATION OF LIQUEFIED NATURAL GAS

Method for the liquefaction of nitrogen using the recovery of cold energy deriving from the evaporation of liquefied natural gas comprising the steps of: sending a flow of nitrogen () to be liquefied to a precooler (); sending a flow () of nitrogen gas exiting said precooler () to a heat exchanger () of the high pressure recirculation compressor; sending a flow () of nitrogen exiting said heat exchanger () to a high pressure recirculation compressor (); sending a flow () of nitrogen exiting said compressor () to a liquefaction heat exchanger (); sending to said liquefaction heat exchanger () a flow () of natural gas, countercurrent to the flow () exiting said compressor (); sending a flow () of nitrogen exiting said liquefaction heat exchanger () to said heat exchanger () countercurrent to said flow () of nitrogen gas and to said flow () of nitrogen; sending a flow () of nitrogen exiting said heat exchanger () to said precooler () countercurrent to said flow of nitrogen () to be liquefied; sending the flow () of nitrogen exiting said liquefaction heat exchanger () to an expander (); sending the flow of nitrogen exiting said expander () to a medium pressure separator () that delivers an exiting flow () of nitrogen. 1100101107101108114108115117120115117121121123120115117126150121108107114151152108101100126130121131131112132. Method for the liquefaction of nitrogen using the recovery of cold energy deriving from the evaporation of liquefied natural gas comprising the steps of: sending a flow of nitrogen () to be liquefied to a precooler (); sending a flow () of nitrogen gas exiting said precooler () to a heat exchanger () of the high pressure recirculation compressor; sending a flow () of nitrogen exiting said heat exchanger () to a high pressure recirculation compressor ( , ); sending a flow () of nitrogen exiting said compressor ( , ) to a liquefaction heat exchanger (); sending to said liquefaction heat exchanger () a flow () of natural gas , countercurrent to the ...

PROCESS INTEGRATION OF A GAS PROCESSING UNIT WITH LIQUEFACTION UNIT

It is proposed to integrate a gas processing unit with a liquefaction unit. The industrial gas stream may be but is not limited to air gases of oxygen, nitrogen argon, hydrocarbon, LNG, syngas or its components, CO, or any other molecule or combination of molecules. It is proposed to integrate the underutilized process inefficiencies of a gas processing unit into the liquefaction unit to produce a liquid at a reduced operating cost. The gas processing unit may be any system or apparatus which alters the composition of a feed gas. Examples could be, but are not limited to, a methanol plant, steam methane reformer, cogeneration plant, and partial oxidation unit. 1. A process for the production of a liquid by integration of a gas processing unit and a liquefaction unit , the process comprising the steps of:a) providing a gas processing unit;b) providing a liquefaction unit, wherein the liquefaction unit is in fluid communication with the gas processing unit, such that the liquefaction unit and the gas processing unit are configured to send and receive fluids from each other;c) extracting a letdown energy from a high pressure gas to produce refrigeration to be used within the liquefaction unit, thereby producing a low pressure gas, wherein the low pressure gas is then used by the gas processing unit as a low pressure feedstream;d) liquefying an industrial gas within the liquefaction unit using refrigeration produced in step c).2. The process as claimed in claim 1 , wherein the gas processing unit is selected from the group consisting of a methanol plant claim 1 , a steam methane reformer claim 1 , a cogeneration plant claim 1 , a partial oxidation unit claim 1 , an autothermal reforming unit claim 1 , and combinations thereof.3. The process as claimed in claim 1 , wherein the industrial gas is selected from the group consisting of an air gas claim 1 , a hydrocarbon claim 1 , syngas claim 1 , carbon dioxide claim 1 , hydrogen claim 1 , carbon monoxide claim 1 , and ...

ADVANCED MULTI-LAYER ACTIVE MAGNETIC REGENERATOR SYSTEMS AND PROCESSES FOR MAGNETOCALORIC LIQUEFACTION

A process for liquefying a process gas that includes introducing a heat transfer fluid into an active magnetic regenerative refrigerator apparatus that comprises a single stage comprising dual multilayer regenerators located axially opposite to each other. 1. A system comprising:a first active magnetic regenerative regenerator comprising 2 to 16 successive layers, wherein each layer comprises an independently compositionally distinct magnetic refrigerant material having an independent Curie temperature and wherein the first layer of the first active magnetic regenerative regenerator has the highest Curie temperature and the last layer of the first active magnetic regenerative regenerator has the lowest Curie temperature;a second active magnetic regenerative regenerator comprising 2 to 16 successive layers, wherein each layer comprises an independently compositionally distinct magnetic refrigerant material having an independent Curie temperature and wherein the first layer of the second active magnetic regenerative regenerator has the lowest Curie temperature and the last layer of the second active magnetic regenerative regenerator has the highest Curie temperature;at least one conduit fluidly coupled between the lowest Curie temperature layer of the first active magnetic regenerative regenerator and the highest Curie temperature layer of the second active magnetic regenerative regenerator;a single bypass flow heat exchanger (a) fluidly coupled to the lowest Curie temperature layer of the first active magnetic regenerative regenerator and (b) fluidly coupled to a process gas source; andfor each layer of the first active magnetic regenerative regenerator and each layer of the second active magnetic regenerative regenerator, an independent fluid conduit between an outlet of each layer of the first active magnetic regenerative regenerator to an inlet of the corresponding Curie temperature layer of the second active magnetic regenerative regenerator, except for lowest ...

Method and apparatus in a cryogenic liquefaction process

Methods and apparatus for the efficient cooling within air liquefaction processes with integrated use of cold recovery from an adjacent LNG gasification process are disclosed.

PROCESS AND APPARATUS FOR SUPPLYING A BACKUP GAS UNDER PRESSURE

The present invention relates to a process and a system for supplying a backup gas at a higher pressure from a source gas at a lower pressure. The backup gas at the lower pressure is at least partially condensed against a backup liquid at a higher pressure in a reprocessing heat exchanger and as a result, the backup liquid is at least partially vaporized. The backup liquid at the higher pressure is formed from boosting liquefied backup gas at the lower pressure. A backup vaporizer is disposed downstream of the reprocessing heat exchanger to completely vaporize the backup liquid at a higher pressure before it was delivered to the customer. The present invention eliminates the use of costly gas compressor and mitigates associated safety risks, in particular when the backup gas is oxygen. 114-. (canceled)15. A process for supplying a backup gas at an elevated pressure , comprising:a) providing a source of backup gas at a first pressure;b) providing at least a reprocessing heat exchanger, a backup vaporizer and a liquid pump;c) heat-exchange between the backup gas at the first pressure and a backup liquid at a second pressure in the reprocessing heat exchanger to produce the at least partially liquefied backup gas at the first pressure and the at least partially vaporized backup liquid at the second pressure;d) warming up the at least partially vaporized backup liquid at the second pressure in the backup vaporizer to produce the backup gas at an elevated pressure; and whereinthe second pressure is higher than the first pressure, and the backup liquid at the second pressure is obtained from elevating the pressure of the liquefied backup gas to the second pressure with the liquid pump.16. The process as claimed in claim 15 , further comprising an expansion valve and a liquid storage tank claim 15 , wherein the at least partially liquefied back-up gas at the first pressure is expanded through the expansion valve before entering the liquid storage tank.17. The process as ...

TRANSPORTABLE PACKAGE WITH A COLD BOX, AND METHOD FOR PRODUCING A LOW-TEMPERATURE AIR SEPARATION SYSTEM

The invention relates to a transportable package with a cold box, in the interior of which at least one double column of a low-temperature air separation system is arranged, i.e., a double column having a high-pressure column and a low-pressure column. The high-pressure and low-pressure columns contain mass transferring elements. The mass transferring elements in at least one sub-region of the low-pressure columns are formed by an ordered packing made of folded metal sheets having a thickness of 0.2 mm or less. The ordered packing has a specified surface area of at least 1000 m2/m3. At least in a sub-region of the high-pressure column, the mass transferring elements are formed by rectifying plates arranged one over the other and which have a clearance of less than 195 mm. The invention further relates to a method for producing a low-temperature air separation system using such a transportable package. 15135355. A transportable package with a cold box () , in the interior of which a double column of a low-temperature air separation system is arranged which has a high-pressure column () and a low-pressure column () which are arranged one above the other , wherein the high-pressure column () and the low-pressure column () contain mass transfer elements , and the mass transfer elements are formed in at least one subregion (A , B , C , D , E) of the low-pressure column () by an ordered packing which is made of folded metal sheets , characterized in thatthe metal sheets have a sheet thickness of 0.2 mm or less, in that{'sup': 2', '3, 'the ordered packing has a specific surface area of at least 1000 m/mand in that'}{'b': '3', 'at least in a subregion of the high-pressure column (), the mass transfer elements are formed by rectification plates arranged one above the other which have a plate spacing of less than 195 mm, in particular less than 180 mm.'}23. The package as claimed in claim 1 , characterized in that the plate spacing of the distillation plates in the high- ...

Integrated Pre-Cooled Mixed Refrigerant System and Method

A system and method for cooling and liquefying a gas in a heat exchanger that includes compressing and cooling a mixed refrigerant using first and last compression and cooling cycles so that high pressure liquid and vapor streams are formed. The high pressure liquid and vapor streams are cooled in the heat exchanger and then expanded so that a primary refrigeration stream is provided in the heat exchanger. The mixed refrigerant is cooled and equilibrated between the first and last compression and cooling cycles so that a pre-cool liquid stream is formed and subcooled in the heat exchanger. The stream is then expanded and passed through the heat exchanger as a pre-cool refrigeration stream. A stream of gas is passed through the heat exchanger in countercurrent heat exchange with the primary refrigeration stream and the pre-cool refrigeration stream so that the gas is cooled. A resulting vapor stream from the primary refrigeration stream passage and a two-phase stream from the pre-cool refrigeration stream passage exit the warm end of the exchanger and are combined and undergo a simultaneous heat and mass transfer operation prior to the first compression and cooling cycle so that a reduced temperature vapor stream is provided to the first stage compressor so as to lower power consumption by the system. Additionally, the warm end of the cooling curve is nearly closed further reducing power consumption. Heavy components of the refrigerant are also kept out of the cold end of the process, reducing the possibility of refrigerant freezing, as well as facilitating a refrigerant management scheme.

Method And Device For Storing And Recovering Energy

The invention relates to a method for storing and recovering energy, wherein an air liquefaction product (LAIR) is formed during an energy storage period, and a fluid pressure flow () is formed during an energy recovery period using at least one part of the air liquefaction product (LAIR) and is expanded for operation in at least one energy recovery device (). The air liquefaction product (LAIR) is obtained as a liquid medium during the energy storage period by compressing air in an air conditioning device (), said compression being operated while supplying energy, in particular while supplying a current (), optionally stored in a cold state, and fed to an evaporator unit (). The air liquefaction product (LAIR) is expanded for operation as a fluid pressure flow () in the at least one energy recovery device () during the energy recovery period after a pressure increase. The aim of the invention is to provide a solution with which even existing gas and steam power plants or open gas turbines are to be equipped with an energy storage capability. This is achieved in that the fluid pressure flow (), in particular an air flow, is expanded in a first energy recovery device () and conducted through a recuperator device (), in particular a heat boiler, upstream of said first energy recovery device (), and thermal energy which has been decoupled from a flue gas flow () fed to the recuperator device () is coupled into the fluid pressure flow () in said heating tank. The flue gas flow () is fed to the recuperator device () from a fuel-fired second energy recovery device (), in particular a gas turbine. 1. A method of storing and recovering energy , in which an air liquefaction product (LAIR) is formed in an energy storage period and a fluid pressure stream is formed using at least a portion of the air liquefaction product (LAIR) in an energy recovery period and is expanded to perform work in at least one energy generation device ,in which the air liquefaction product (LAIR) is ...

Cryogenic combined cycle power plant

In a cryogenic combined cycle power plant electric power drives a cryogenic refrigerator to store energy by cooling air to a liquid state for storage within tanks, followed by subsequent release of the stored energy by first pressurizing the liquid air, then regasifying the liquid air and raising the temperature of the regasified air at least in part with heat exhausted from a combustion turbine, and then expanding the heated regasified air through a hot gas expander to generate power. The expanded regasified air exhausted from the expander may be used to cool and make denser the inlet air to the combustion turbine. The combustion turbine exhaust gases may be used to drive an organic Rankine bottoming cycle. An alternative source of heat such as thermal storage, for example, may be used in place of or in addition to the combustion turbine.

NATURAL GAS LIQUEFACTION WITH INTEGRATED NITROGEN REMOVAL

A natural gas liquefaction method and system having integrated nitrogen removal. Recycled LNG gas is cooled in a separate and parallel circuit from the natural gas stream in the main heat exchanger. Cooled recycled gas and natural gas streams are directed to a nitrogen rectifier column after the warm bundle. The recycle stream is introduced to the rectifier column above the natural gas stream and at least one separation stage is located in the rectifier column between the recycle stream inlet and the natural gas inlet. The bottom stream from the rectifier column is directed to a cold bundle of the main heat exchanger where it is subcooled. 1. A method for producing a nitrogen-depleted LNG product , the method comprising:(a) passing a natural gas feed stream through a first circuit of a main heat exchanger to cool the natural gas feed stream and liquefy at least a portion of the natural gas stream against a first refrigerant, thereby producing a first cooled LNG stream;(b) withdrawing the first cooled LNG stream from the main heat exchanger;(c) expanding the first cooled LNG stream to form a first reduced pressure LNG stream;(d) introducing the first reduced pressure LNG stream into a nitrogen rectifier column at a first location, the first location being located at a bottom end of the nitrogen rectifier column;(e) withdrawing a first LNG bottoms stream from the bottom end of the nitrogen rectifier column;(f) withdrawing an overhead stream from the nitrogen rectifier column;(g) cooling the first LNG bottoms stream to create a subcooled LNG stream;(h) directing at least a portion of the subcooled LNG stream to a flash drum or an LNG storage tank;(i) collecting at least one selected from the group of: a flash gas stream from the flash drum and a boil-off gas stream from the LNG storage tank to form a recycle stream;(j) passing the recycle stream through a second circuit of the main heat exchanger to cool the recycle stream and liquefy at least a portion of the recycle ...

LIQUID HYDROGEN PRODUCTION DEVICE

A device (HS) is provided with a refrigeration cycle unit (R) and a liquid hydrogen generation unit (P) for generating liquid hydrogen by cooling high-pressure raw material hydrogen by means of the refrigeration cycle unit (R) and by adiabatically expanding said raw material hydrogen by means of a Joule-Thomson valve (). A first and second heat exchanger (E, E) are disposed along the refrigeration cycle unit (R) and the liquid hydrogen generation unit (P). The device (HS) is provided with a mechanism for generating liquid hydrogen by re-liquefying the boil-off gas generated in a liquid hydrogen storage tank. The boil-off gas is introduced into a hydrogen circulation path () at a section at which circulating hydrogen having an extremely low temperature flows, and the excessive circulating hydrogen generated therefrom is discharged to a raw material hydrogen path () from a section at which the circulating hydrogen is at room temperature. 1. An apparatus for producing liquid hydrogen comprising:a refrigeration cycle unit in which circulating hydrogen flows as a refrigerant;a liquid hydrogen producing unit for producing the liquid hydrogen from gaseous hydrogen;a boil-off gas supplying unit for supplying boil-off gas generated in a liquid hydrogen reservoir to said refrigeration cycle unit through a predetermined inlet portion in said refrigeration cycle unit; anda circulating hydrogen discharge unit for discharging excessive circulating hydrogen resulting from the boil-off gas supplied to said refrigeration cycle unit by means of said boil-off gas supplying unit, to said liquid hydrogen producing unit through a predetermined outlet portion in said refrigeration cycle unit.2. The apparatus according to claim 1 , wherein said refrigeration cycle unit comprises:a compressor for compressing the circulating hydrogen;an expander for expanding the circulating hydrogen; andat least one heat exchanger interposed between said compressor and said expander, said heat exchanger ...

Methanol production process from syngas produced by catalytic partial oxidation integrated with cracking

A process for producing syngas and olefins including the steps of feeding a catalytic partial oxidation (CPO) reactant mixture (oxygen, first hydrocarbons, steam) to a CPO reactor (CPO catalyst); wherein the CPO reactant mixture reacts, via CPO reaction, in CPO reactor to produce a CPO reactor effluent (H2, CO, CO2, water, unreacted first hydrocarbons). The process further includes feeding a cracking unit feed (second hydrocarbons) to a cracking unit to produce a cracking unit product (olefins), a hydrogen-rich stream (hydrogen, CH4), and a hydrocarbon recovery stream (C4+ hydrocarbons); wherein the first and the second hydrocarbons are the same or different; recovering a hydrogen-enriched stream (hydrogen) and a hydrocarbon-enriched stream (CH4) from the hydrogen-rich stream; and contacting the CPO reactor effluent with the hydrogen-enriched stream to yield hydrogen-enriched syngas, and wherein the M ratio ((H2—CO2)/(CO+CO2)) of the hydrogen-enriched syngas is greater than the M ratio of the CPO reactor effluent.

Method for Operating a Liquid Air Energy Storage

A method for operating the liquid air energy storage (LAES) includes production of the storable liquid air through consumption of a low-demand power and recovery the liquid air for co-production of an on-demand power and a high-grade saleable cold thermal energy which may be used, say, for liquefaction of the delivered natural gas; in so doing zero carbon footprint is provided both for fueled augmentation of the LAES power output and for LNG co-production at the LAES facility. 1. A method for operating a liquid air energy storage (LAES) , comprising in combination:charging the LAES through consuming a low-demand power from a co-located renewable energy source or a grid for after-cooled compressing a process air, as a mixture of a pressurized pre-treated feed air and a recirculating air, further boost after-cooled compressing said process air, work expanding and accompanied refrigerating a recirculating part of the process air, recovering said work of expanding for powering the boost compressing and using a refrigerated recirculating air for in-direct cryogenic cooling a rest of the process air, and further depressurizing, partial liquefying and separating said cryogenically cooled rest of the process air into a liquid air and a cold vapor with combining the refrigerated recirculating air and said cold vapor;storing a liquid air in a storage tank;delivering a natural gas (NG) into the LAES;discharging the LAES through producing and delivering an on-demand power into the grid by means of pumping the liquid air from the storage tank, sequential re-gasifying said liquid air and heating a re-gasified air by a LAES exhaust with further work partial expanding the re-gasified air in a power block and recovering the expanded air as an oxidant for a burning of a minor part of said delivered NG in a fueled prime mover being used in said power block for augmentation of the LAES on-demand power and selected from a group consisting of, but not limited to an industrial rotating ...

METHOD AND FILLING DEVICE FOR FILLING A TRANSPORT TANK

The present invention pertains to a method for filling a transport tank with a product medium in a liquid state in a gas liquefaction plant, comprising a step of supplying the product medium in the liquid state from a storage tank () of the gas liquefaction plant to the transport tank. The method is characterized in that it further comprises a step of discharging the product medium in a gaseous state from the transport tank into the storage tank (). 1. Method for filling a transport tank with a product medium in a liquid state in a gas liquefaction plant , comprising a step of supplying the product medium in the liquid state from a storage tank of the gas liquefaction plant to the transport tank , whereinthe method further comprises a step of discharging the product medium in a gaseous state from the transport tank to the storage tank.2. Method according to claim 1 , wherein the product medium in the gaseous state stored in the transport tank is fed into the storage tank downstream of a cooling and liquefying unit of the gas liquefaction plant which generates a liquid product medium stream to be supplied to the storage tank.3. Method according to claim 1 , wherein the product medium in the gaseous state stored in the transport tank is fed into the storage tank in its gaseous state.4. Method according to claim 1 , wherein the storage tank stores the product medium in both a liquid and a gaseous phase claim 1 , and the product medium in the gaseous state is discharged from the transport tank into the storage tank such that the product medium in the gaseous state is fed into the liquid phase.5. Method according to claim 1 , wherein the product medium in the gaseous state supplied to the storage tank from the transport tank is fed into a static mixer provided in or upstream of the storage tank.6. Method according to claim 1 , wherein the product medium in its gaseous state discharged from the transport tank is fed into a feed gas stream which claim 1 , upon flowing ...

Method for Liquid Air and Gas Energy Storage

A method for liquid air and gas energy storage (LAGES) which integrates the processes of liquid air energy storage (LAES) and regasification of liquefied natural gas (LNG) at the import terminal through the exchange of thermal energy between the streams of air and natural gas (NG) in their gaseous and liquid states and includes harnessing the LNG as an intermediate heat carrier between the air streams being regasified and liquefied, recovering a compression heat from air liquefier for LNG regasification and utilizing a cold thermal energy of liquid air being regasified for reliquefaction of a part of send-out NG stream with its return to LNG terminal. 1. A method for liquid air and gas energy storage (LAGES) comprising in combination:pumping the liquefied natural gas (LNG) from the tanks of LNG Storage and Regasification (LNGSR) terminal into a co-located Liquid Air Energy Storage (LAES) system for continuous regasifying the LNG in the said system and final injecting the regasified LNG into a transmission pipeline;interchanging a waste thermal energy between the LNG being regasified and the process air being continuously liquefied in the LAES system;consuming a required power from the grid and/or other energy source for production of the liquid air with its storing only in the periods of low demand for energy in the grid;on-demand discharging the said LAES system with generation of the on-peak power delivered into grid through consuming both a stored and directly produced liquid air at a rate exceeding a rate of its direct production; andwherein the improvement comprises in combination:pumping the whole amount of LNG destined for regasification and its delivering into LAES system at the first low pressure and first low temperature during the LAES system discharging;using a minor part of cold thermal energy of discharged liquid air for deep cooling the said delivered LNG down to the second low temperature, which is below the first one;controlled dividing the deeply ...

Method for Liquid Air and Gas Energy Storage

A method for liquid air and gas energy storage (LAGES) which integrates the processes of liquid air energy storage (LAES) and regasification of liquefied natural gas (LNG) at the Floating Storage, Regasification and Power (FSRP) facilities through the exchange of thermal energy between the streams of air and natural gas (NG) in their gaseous and liquid states and includes recovering a compression heat from air liquefier and low-grade waste heat of power train for LNG regasification with use of an intermediate heat carrier between the air and LNG streams and utilizing a cold thermal energy of liquid air being regasified for increase in LAGES operation efficiency through using a semi-closed CO2 bottoming cycle.

NOVEL PRODUCTION EQUIPMENT AND PRODUCTION METHOD OF LIQUEFIED HYDROGEN AND LIQUEFIED NATURAL GAS

Provided is a production facility for liquefied hydrogen and a liquefied natural gas from a natural gas, including: a first heat exchanger configured to cool a hydrogen gas through heat exchange between the hydrogen gas and a mixed refrigerant for liquefying a natural gas containing a plurality of kinds of refrigerants selected from the group consisting of methane, ethane, propane, and nitrogen; a second heat exchanger configured to cool the mixed refrigerant through heat exchange between the mixed refrigerant and propane; and a third heat exchanger configured to cool the hydrogen gas through heat exchange between the hydrogen gas and a refrigerant containing hydrogen or helium, wherein the first heat exchanger has a precooling temperature of from −100° C. to −160° C. 1. A production facility for liquefied hydrogen and a liquefied natural gas from a natural gas , comprising:a first heat exchanger configured to cool a hydrogen gas through heat exchange between the hydrogen gas and a mixed refrigerant for liquefying a natural gas containing a plurality of kinds of refrigerants selected from the group consisting of methane, ethane, propane, and nitrogen;a second heat exchanger configured to cool the mixed refrigerant through heat exchange between the mixed refrigerant and propane; anda third heat exchanger configured to cool the hydrogen gas through heat exchange between the hydrogen gas and a refrigerant containing hydrogen or helium,wherein the first heat exchanger has a precooling temperature of from −100° C. to −160° C.2. The production facility for liquefied hydrogen and a liquefied natural gas according to claim 1 ,wherein the production facility further comprises at least one natural gas pretreatment unit selected from the group consisting of a condensate separation unit, an acid gas removal unit, and a mercury removal unit, andwherein the production facility has a configuration in which a natural gas having been subjected to the pretreatment unit is divided ...

Method for Liquid Air Energy Storage with Semi-Closed CO2 Bottoming Cycle

A proposed method provides a highly efficient fueled power output augmentation of the liquid air energy storage (LAES) through its integration with the semi-closed CObottoming cycle. It combines the production of liquid air in air liquefier during LAES charge using excessive power from the grid and an effective recovery of stored air for production of on-demand power in the fueled supercharged reciprocating internal combustion engine (ICE) and associated expanders of the power block during LAES discharge. A cold thermal energy of liquid air being re-gasified is recovered for cryogenic capturing most of COemissions from the facility exhaust with following use of the captured COin the semi-closed bottoming cycle, resulting in enhancement of total LAES facility discharge power output and suppressing the thermal NOx formation in the ICE. 1. A method for liquid air energy storage (LAES) with semi-closed CObottoming cycle comprising in combination:charging the energy storage with liquid air produced through consumption of an excessive power from the co-located renewable energy sources or from the grid;discharging the energy storage with on-demand producing and delivering a power to the grid through pumping and re-gasifying the stored air and its recovering in the multi-stage expander train and as combustion air for the fueled supercharged internal combustion engine (ICE);{'sub': '2', 'recovering the cold thermal energy of discharged liquid air being regasified for cryogenic cooling the LAES facility exhaust with capturing and liquefying at least a part of COemissions formed by combustion of fuel in the said LAES facility; and'}wherein the improvement comprises in combination:{'sub': '2', 'pumping the said liquid COup to pressure somewhat exceeding a pressure of the pumped liquid air,'}{'sub': 2', '2', '2, 'injection of the pumped liquid COinto a stream of re-gasified air, resulting in regasification of injected COand forming a mixed air-COstream;'}{'sub': '2', ' ...

Method for Energy Storage with Co-production of Peaking Power and Liquefied Natural Gas

A method for energy storage with co-production of peaking power and liquefied natural gas (LNG) which integrates the processes of liquid air energy storage and reduction in pressure of natural gas through expander at the co-located city gate station and includes consumption of excessive power from the grid, mechanical power of the natural gas expander and cold thermal energy of expanded natural gas for charging the storage with a liquid air during off-peak hours and production of peaking (on-demand) power by the expanders of natural gas and highly-pressurized re-gasified air with recovering the cold thermal energy of expanded natural gas and regasified liquid air for liquefying a part of delivered natural gas at the city gate station and energy storage facility.

HIGH-PURITY OXYGEN PRODUCTION SYSTEM

Certain embodiments of the present invention lies in providing a high-purity oxygen production system which is capable of supplying liquid nitrogen in order to supply the cold required by a high-purity oxygen production apparatus, without the use of a costly conventional liquefaction apparatus. 1. A high-purity oxygen production system comprising:an air separation apparatus including a main heat exchanger, a medium-pressure column and a low-pressure column; anda high-purity oxygen production apparatus including a nitrogen compressor, a nitrogen heat exchanger and at least one high-purity oxygen rectification column,wherein the low-pressure column is in fluid communication with the high-purity oxygen production apparatus such that the system is configured to supply an oxygen-containing stream serving as a starting material for high-purity oxygen from the low-pressure column to the high-purity oxygen production apparatus, andwherein the medium-pressure column is in fluid communication with the high-purity oxygen production apparatus such that the system is configured to supply liquid nitrogen obtained from the medium-pressure column to the high-purity oxygen production apparatus in order to replenish cold heat required for operation of the high-purity oxygen production apparatus.2. The high-purity oxygen production system according to claim 1 ,wherein the main heat exchanger is configured to subject a starting material air to heat exchange;wherein the medium-pressure column is in fluid communication with a cold end of the main heat exchanger and is configured to receive the starting material air from the main heat exchanger, the medium-pressure column having a medium-pressure column bottom in which a first rectification liquid is collected, a medium-pressure column rectification portion for rectifying the starting material air, and a medium-pressure column top arranged above the medium-pressure column rectification portion,wherein the low-pressure column is arranged ...

Systems and methods of semi-centralized power storage and power production for multi-directional smart grid and other applications

Systems and methods of semi-centralized energy storage and mobile power outflow for vehicle propulsion comprise at least one energy storage facility receiving energy via an electric grid and at least one mobile vehicle. The energy is generated at a first location, and the energy storage facility is at a second location different from the first location. The second location is closer to end users of the energy than the first location. The energy storage facility produces an energy storage medium at the second location and stores the energy from the first location at the second location in the energy storage medium. The energy storage medium comprises liquid air, liquid oxygen, liquid nitrogen, or a combination thereof. The mobile vehicle includes a prime mover and a cryogenic storage vessel and is configured to carry at least a portion of the energy storage medium in the cryogenic storage vessel and use power from the energy storage medium for mobile vehicle propulsion.

LIQUID AIR POWER AND STORAGE WITH CARBON CAPTURE

Apparatus, systems, and methods store energy by liquefying a gas such as air, for example, and then recover the energy by regasifying the cryogenic liquid and combusting or otherwise reacting the gas with a fuel to drive a heat engine. Carbon may be captured from the heat engine exhaust by using the cryogenic liquid to freeze carbon dioxide out of the exhaust. The process of liquefying the gas may be powered with electric power from the grid, for example, and the heat engine may be used to generate electricity. Hence, in effect these apparatus, systems, and methods may provide for storing electric power from the grid and then subsequently delivering it back to the grid. 1. A method of storing and recovering energy , the method comprising:regasifying liquid air or liquid air components to produce gaseous air or gaseous air components;combusting at least a portion of the gaseous air or gaseous air components with a gaseous fuel to form a gaseous primary working fluid at an elevated temperature;expanding the primary working fluid through a first turbine;producing electricity with a generator driven by the first turbine;freezing carbon dioxide out of an exhaust gas stream from the first turbine to form frozen carbon dioxide by transferring heat from the first turbine exhaust gas stream to liquid air or liquid air components to cool the first turbine exhaust gas stream; andsublimating the frozen carbon dioxide to form carbon dioxide vapor.2. The method of claim 1 , wherein regasifying the liquid air or liquid air components to produce gaseous air or gaseous air components comprises regasifying the liquid air or liquid air components using heat from the exhaust gas stream from the first turbine.3. The method of claim 1 , wherein sublimating the frozen carbon dioxide to form carbon dioxide vapor comprises sublimating the frozen carbon dioxide using heat from the first turbine exhaust gas stream.4. The method of claim 1 , comprising sublimating the frozen carbon dioxide to ...

SYSTEM AND METHOD FOR CRYOGENIC PURIFICATION OF A FEED STREAM COMPRISING HYDROGEN, METHANE, NITROGEN AND ARGON

A system and method for cryogenic purification of a hydrogen, nitrogen, methane and argon containing feed stream to produce a methane free, hydrogen and nitrogen containing synthesis gas and a methane rich fuel gas, as well as to recover an argon product stream, excess hydrogen, and excess nitrogen is provided. The disclosed system and method are particularly useful as an integrated cryogenic purifier in an ammonia synthesis process in an ammonia plant. The excess nitrogen is a nitrogen stream substantially free of methane and hydrogen that can be used in other parts of the plant, recovered as a gaseous nitrogen product and/or liquefied to produce a liquid nitrogen product. 1. A method for purifying a hydrogen , nitrogen , methane and argon containing feed stream to produce a hydrogen and nitrogen containing synthesis gas and a methane fuel gas , the method comprising the steps of:conditioning the feed stream to a temperature near saturation at a pressure greater than about 300 psia;directing the conditioned feed stream to a synthesis gas rectification column configured to produce an hydrogen and nitrogen enriched overhead vapor stream and a methane-rich condensed phase stream proximate the bottom of the synthesis gas rectification column;directing the methane-rich condensed phase stream to a hydrogen stripping column configured to strip hydrogen from the methane-rich condensed phase stream and produce a hydrogen free methane bottom stream and a hydrogen enriched gaseous overhead;vaporizing the hydrogen free methane bottom stream to produce a vaporized or partially vaporized hydrogen free methane-rich stream;warming the hydrogen and nitrogen enriched overhead vapor stream via indirect heat exchange with the feed stream to produce the hydrogen and nitrogen containing synthesis gas; andwarming the vaporized or partially vaporized hydrogen free methane-rich stream via indirect heat exchange with the feed stream to produce the methane fuel gas.2. The method of claim 1 , ...

Offshore liquefaction process without compression

A process for producing liquid oxygen, including an offshore platform the system including cooling a high-pressure nitrogen gas stream in a main heat exchanger, thereby producing a cooled high-pressure nitrogen gas stream, expanding the cooled high-pressure nitrogen gas stream in a turbo-expander, thereby producing a cold low-pressure nitrogen gas stream, warming the cold low-pressure nitrogen gas stream by indirect heat exchange with a high-pressure gaseous oxygen stream, thereby producing a liquefied oxygen stream and a warm low-pressure nitrogen gas stream, wherein, at least a portion of the warm low-pressure nitrogen gas stream is vented to the atmosphere.

ACTIVE MAGNETIC REGENERATIVE PROCESSES AND SYSTEMS EMPLOYING HYDROGEN AS HEAT TRANSFER FLUID AND PROCESS

A system including: 1. A process for liquefying a hydrogen gas comprising:introducing a hydrogen heat transfer fluid into an active magnetic regenerative refrigerator apparatus that comprises (i) a high magnetic field section in which the hydrogen heat transfer fluid flows from a cold side to a hot side through at least one magnetized bed of at least one magnetic refrigerant, (ii) a first no heat transfer fluid flow section in which the bed is demagnetized, (iii) a low magnetic or demagnetized field section in which the hydrogen heat transfer fluid flows from a hot side to a cold side through the demagnetized bed, and (iv) a second no heat transfer fluid flow section in which the bed is magnetized;continuously introducing the hydrogen heat transfer fluid from the cold side of the low magnetic or demagnetized field section into the cold side of the high magnetic field section;continuously separating a bypass portion of the cold hydrogen heat transfer fluid flowing from the cold side of the low magnetic field or demagnetized section into an expander; andisenthalpically expanding the separated portion of the hydrogen heat transfer fluid to produce liquefied hydrogen.2. The process of claim 1 , wherein the bypass portion constitutes 3 to 12% of the total hydrogen heat transfer fluid exiting the cold side of the low magnetic or demagnetized field section.3. The process of claim 1 , wherein the magnetic refrigerant operates at or below its Curie temperature throughout an entire active magnetic regeneration cycle.4. The process of claim 1 , wherein the process provides a figure of merit (FOM) of at least 0.5.5. The process of claim 1 , wherein the active magnetic regenerative refrigerator apparatus includes a plurality of magnetic refrigerant layers.6. The process of claim 1 , wherein the active magnetic regenerative refrigerator apparatus includes 1 to 16 layers of compositionally distinct magnetic refrigerant materials.7. The process of claim 5 , wherein the active ...

Method of nitrogen gas recovery from gas vents

A method of vapor recovery is provided. One embodiment of the method of vapor recovery includes providing a combined gas phase and liquid phase fluid, by way of a pipe, wherein the pipe comprises a gas vent. Then removing at least a portion of the gas phase fluid with the gas vent. Then compressing the removed portion of gas phase fluid, thereby forming compressed gas stream. And finally accumulating the compressed gas stream in a storage tank downstream of the compressor.

LIQUID AIR POWER AND STORAGE

Apparatus, systems, and methods store energy by liquefying a gas such as air, for example, and then recover the energy by regasifying the liquid and combusting or otherwise reacting the gas with a fuel to drive a heat engine. The process of liquefying the gas may be powered with electric power from the grid, for example, and the heat engine may be used to generate electricity. Hence, in effect these apparatus, systems, and methods may provide for storing electric power from the grid and then subsequently delivering it back to the grid. 1. A method of storing and recovering energy , the method comprising:regasifying liquid air or liquid air components to produce gaseous air or gaseous air components using heat from an exhaust gas stream from a turbine;mixing a gaseous fuel and at least a portion of the gaseous air or gaseous air components to form a mixture and combusting the mixture to form a gaseous primary working fluid at an elevated temperature;expanding the gaseous primary working fluid through the turbine; andproducing electricity with a generator driven by the turbine; freezing carbon dioxide out of the exhaust gas stream by transferring heat from the exhaust gas stream to the liquid air or liquid air components to cool the turbine exhaust gas stream;', 'cooling a storage medium by transferring heat from the storage medium to the exhaust gas stream after freezing the carbon dioxide out of the exhaust gas stream; and', 'using the cooled storage medium as a heat sink during liquefaction of the liquid air or liquid air components., 'wherein regasifying the liquid air or liquid air components to produce the gaseous air or gaseous air components using heat from the exhaust gas stream from the turbine comprises2. The method of claim 1 , comprising producing the liquid air or liquid air components in an electrically powered liquefaction process and storing the liquid air or liquid air components for later regasification and use in combusting the gaseous fuel.3. The ...

SYSTEMS, METHODS, AND DEVICES FOR LIQUID AIR ENERGY STORAGE IN CONJUNCTION WITH POWER GENERATING CYCLES

Systems, methods, and devices are provided for liquid air energy storage in conjunction with power generating cycles. A system can comprise a power generation apparatus and an energy storage apparatus. The energy storage apparatus can comprise a thermal energy storage unit, and the power generation apparatus and energy storage apparatus can be interconnected via the thermal energy storage unit enabling energy transfer from a first cycle of one of the power generation apparatus and energy storage apparatus to a second cycle of the other apparatus. 1. A system comprising:a power generation apparatus; andan energy storage apparatus comprising a thermal energy storage unit,the power generation apparatus and energy storage apparatus being interconnected via the thermal energy storage unit enabling energy transfer from a first cycle of one of the power generation apparatus and energy storage apparatus to a second cycle of the other apparatus.2. The system of claim 1 , wherein the energy storage apparatus is a Liquid Air Energy Storage (LAES) unit claim 1 , the LAES unit having a plurality of modes of operation claim 1 , the modes of operation comprising:a first mode of operation being a charge mode in which the LAES unit generates liquid air;a second mode of operation being a discharge mode in which the LAES unit generates electricity by heating and evaporating the liquid air and expanding the liquid air through an expander; anda third mode of operation being an idle mode in which the LAES unit does not generate liquid air and does not generate electricity.3. The system of claim 1 ,wherein the power generation apparatus is a power plant where the power generation is achieved by the generation of steam; andwherein the generated steam is expanded through a steam turbine.4. The system of claim 3 ,wherein the power plant is interconnected to the energy storage unit with one or more conduits allowing the transfer of the generated steam to the thermal energy storage unit; ...

AIR SEPARATION COLUMN LOW-DENSITY SOLID-STATE INSULATION PATENT

A cryogenic insulation system is proposed comprising enclosing at least a portion of a cryogenic device with low density high conductivity insulation material. The cryogenic device may be an air separation unit. The cryogenic device does not include an outer containment structure for granulated cryogenic insulation. The low density high conductivity insulation material may consists of at least one layer of abutting or overlapping low density high conductivity insulation material composite with fibrous batting. The portion of the cryogenic device is selected from the group consisting of: a distillation column, a heat exchanger, a condenser, a reboiler, an expansion turbine, valves, piping, or any combination thereof. 1. A method for insulating a cryogenic air separation unit , the method comprising the steps of:providing a distillation system having an outer surface, the distillation system configured to separate a compressed air stream into a nitrogen enriched stream and an oxygen enriched stream;obtaining an insulation material comprising aerogel, wherein the insulation material is configured to be flexible; andcovering the outer surface of the distillation system with the insulation material such that the outer surface of the distillation system is not in direct contact with the atmosphere.2. The method as claimed in claim 1 , further comprising an absence of the step of surrounding the distillation system with an outer containment structure.3. The method as claimed in claim 1 , further comprising an absence of the step of surrounding the distillation system with perlite insulation.4. The method as claimed in claim 1 , wherein the insulation material further comprises a composite material with fibrous batting.5. The method as claimed in claim 1 , wherein the insulation material further comprises a first layer and a second layer claim 1 , wherein the first layer comprises the aerogel and the second layer comprises fibrous batting.6. The method as claimed in claim 1 ...

METHOD AND APPARATUS FOR SEPARATING AIR BY CRYOGENIC DISTILLATION

In a method for separating air by cryogenic distillation, cooled air purified to remove water is sent to a first column operating at a first pressure, where it is separated into a nitrogen-enriched gas as an oxygen-enriched liquid; a gas enriched in argon relative to the air is withdrawn from the second column; at least a portion of the oxygen-enriched liquid is vaporized by heat exchange with the argon-enriched gas; and the vaporized, oxygen-enriched liquid is sent to an intermediate level of the second column. 1. A method for separating air by cryogenic distillation , the method comprising the steps of:(a) sending a cooled air that has previous been purified to remove water to a first column operating at a first pressure, where the cooled air is separated into a nitrogen-enriched gas and an oxygen-enriched liquid;(b) withdrawing a liquid enriched in nitrogen relative to the air from the first column and sending said liquid enriched in nitrogen to the top of a second column that is connected thermally to the first column and operates at a second pressure, wherein the second pressure is lower than the first pressure;(c) withdrawing a liquid enriched in oxygen relative to the air from the first column;(d) withdrawing a gas enriched in argon relative to the air from the second column;(e) at least partially vaporizing at least a portion of the oxygen-enriched liquid by heat exchange with the argon-enriched gas to form a vaporized oxygen-enriched fluid, and then sending the vaporized oxygen-enriched fluid to an intermediate level of the second column;(f) returning at least one condensed portion of the argon-enriched gas to a third column, wherein the third column is also fed with an argon-enriched gas flow originating from the second column, wherein an argon-enriched top gas is withdrawn at a top portion of the third column, and an argon-depleted liquid is returned from the third column to the second column;(g) sending a portion of the oxygen-enriched liquid to an ...

Method and apparatus for the low-temperature fractionation of a fluid mixture

The method and the apparatus are used for the low-temperature fractionation of a fluid mixture. The fluid mixture is introduced into a separation column. At least a portion of the sump liquid from the separation column is introduced into a sump evaporator and at least partly evaporated there. At least a portion of the vapor produced in the sump evaporator is led back into a lower section of the separation column. A top product is removed at the top of the separation column, and a sump product is removed from the sump of the separation column or from the sump evaporator. The sump evaporator is operated by means of inductive heating.

METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION

The invention relates to a method for air separation by cryogenic distillation in a column system that includes at least a first column operating at a first pressure, and a second column operating at a second pressure that is lower than the first pressure, the head of the first column being thermally connected to the tank of the second column via a vaporizer-condenser, a first portion of a nitrogen-enriched gas is drawn from the head of the first column, compressed in a compressor having an inlet temperature no higher than −150° C. and condensed in the vaporizer-condenser, an oxygen-rich fluid is drawn from the lower portion of the second column and heated in the exchange line, a nitrogen-rich gas is drawn from the upper portion of the second column and heated in the exchange line, and a second portion of the nitrogen-enriched gas is expanded in a turbine without being compressed. 113-. (canceled)14. A process for separating air by cryogenic distillation in a system of columns comprising at least a first column operating at a first pressure and a second column operating at a second pressure below the first pressure , the top of the first column being thermally coupled to the bottom of the second column by a vaporizer-condenser wherein:i) cooling purified air in an exchange line and sending the purified air to the first column under conditions effective for separation;ii) withdrawing a nitrogen-enriched gas from the top of the first column and divided into two portions, a first portion is compressed in a compressor having an inlet temperature of at most −150° C. and is condensed in the vaporizer-condenser;iii) reheating a second portion of the nitrogen-enriched gas in the exchange line and expanded in an expansion turbine;iv) sending an oxygen-enriched liquid or a liquid derived from this liquid from the bottom of the first column to the second column in order to be separated therein, without having been reheated against a nitrogen-enriched gas from the first column; ...

GAS LIQUEFACTION USING HYBRID PROCESSING

Disclosed techniques include gas liquefaction using hybrid processing. A gas is compressed adiabatically to produce a compressed gas at a first pressure. The compressing a gas adiabatically is accomplished using one or more compressing stages. Heat is extracted from the compressed gas at a first pressure. The heat that is extracted is collected in a thermal store. The compressed gas at a first pressure is further compressed. The further compressing is accomplished using a first liquid piston compressor. The further compressing produces a compressed gas at a second pressure. The first liquid piston compressor is cooled using a liquid spray. The compressed gas at a second pressure is cooled using a heat exchanger. The cooling accomplishes liquefaction of the compressed gas at a second pressure. The gas that was liquefied is stored for future use. The gas that was liquefied is used to perform work. 1. A method for gas processing comprising:compressing a gas adiabatically to produce a compressed gas at a first pressure;extracting heat from the compressed gas at a first pressure; andfurther compressing the compressed gas at a first pressure, wherein the further compressing is accomplished using a first liquid piston compressor, and wherein the further compressing produces a compressed gas at a second pressure.2. The method of further comprising cooling the compressed gas at a second pressure using a heat exchanger wherein the cooling accomplishes liquefaction of the compressed gas at a second pressure.3. The method of wherein the heat exchanger is cooled using a refrigeration system.4. The method of further comprising additionally compressing a portion of the compressed gas at a second pressure claim 1 , using a second liquid piston compressor claim 1 , to produce a compressed gas at a third pressure.5. The method of further comprising cooling the second liquid piston compressor using a liquid spray.6. The method of wherein cooling the second liquid piston compressor ...

METHOD AND APPARATUS FOR POWER STORAGE

Cryogenic energy storage systems, and particularly methods for capturing cold energy and re-using that captured cold energy, are disclosed. The systems allow cold thermal energy from the power recovery process of a cryogenic energy storage system to be captured effectively, to be stored, and to be effectively utilised. The captured cold energy could be reused in any co-located process, for example to enhance the efficiency of production of the cryogen, to enhance the efficiency of production of liquid natural gas, and/or to provide refrigeration. The systems are such that the cold energy can be stored at very low pressures, cold energy can be recovered from various components of the system, and/or cold energy can be stored in more than one thermal store. 1. A cryogenic energy storage system comprising:a cryogenic storage tank for storing a cryogen;a pump in fluid communication with the cryogenic storage tank, wherein the pump is for compressing the cryogen from the storage tank;a first thermal store having a first pathway therethrough for conveying a first heat transfer fluid at a gauge pressure of less than 4 bar; a second pathway therethrough for conveying the first heat transfer fluid to the first pathway at a gauge pressure of less than 4 bar, and', 'a third pathway therethrough for conveying the compressed cryogen,, 'a first heat exchanger havingwherein the first heat transfer fluid is for capturing cold thermal energy from the cryogen to heat the cryogen, and for conveying said captured cold thermal energy to the first thermal store at a gauge pressure of less than 4 bar;a power recovery system including one or more expansion turbines for expanding the heated cryogen to generate power; and [ a fourth pathway therethrough for conveying the first heat transfer fluid from the first pathway at a gauge pressure of less than 4 bar, and', 'a fifth pathway therethrough for conveying a first working fluid to capture cold thermal energy from the first heat transfer ...

Apparatus and Process for Liquefying Gases

A liquefier device which may be a retrofit to an air separation plant or utilized as part of a new design. The flow needed for the liquefier comes from an air separation plant running in a maxim oxygen state, in a stable mode. The three gas flows are low pressure oxygen, low pressure nitrogen, and higher pressure nitrogen. All of the flows are found on the side of the main heat exchanger with a temperature of about 37 degrees Fahrenheit. All of the gasses put into the liquefier come out as a subcooled liquid, for storage or return to the air separation plant. This new liquefier does not include a front end electrical compressor, and will take a self produced liquid nitrogen, pump it up to a runnable 420 psig pressure, and with the use of turbines, condensers, flash pots, and multi pass heat exchangers. The liquefier will make liquid from a planned amount of any pure gas oxygen or nitrogen an air separation plant can produce. 1. A liquefier device for producing liquid oxygen and liquid nitrogen comprising:a plurality of multi-pass counter current flow heat exchangers including an oxygen cooler, a nitrogen bath boiler, a preheater for heating a vaporized nitrogen flow produced by the boiler, a condenser, an added cooling heat exchanger,the oxygen cooler, boiler, and condenser configured for cooling the oxygen gas flow prior to entering an oxygen production flash pot for converting the oxygen gas flow to subcooled liquid oxygen,a turbine assembly having a plurality of turbine expanders connected in parallel and exiting to a common header, and a plurality of turbine boosters connected in series each having an associated aftercooler,the turbine boosters connected in series configured to produce a major flow of compressed nitrogen gas which major flow provides a warming nitrogen flow to the oxygen cooler, the preheater, and a bypass valve, said warming nitrogen flows rejoining prior to entering the boiler, and then cooling to a two-phase liquid gas nitrogen stream in the ...

Devices and methods for producing liquid air

Methods and devices for continuously producing liquid air. One embodiment includes bringing a first container confining an unpressurised first volume coupled to outer air in contact with a first cryogenic medium, and maintaining a temperature of the first cryogenic medium substantially higher than the boiling temperature of the first cryogenic medium for affecting continuous production of liquid air. 1. A device for continuously producing liquid air from outer air in atmospheric pressure , the device comprising:a first container comprising: a first boundary having high thermal conductivity and a first opening;the first boundary confines a first volume and is configured to conduct heat from an inner side of the first boundary to an outer side thereof, thereby to cool inner air confineable in the first volume;the first opening is configured to couple the first volume with the outer air external to the first volume; the first opening is further configured to allow flow of outer air into the first volume;a filter, coupled to the first opening, configured to clean the outer air flowing into the first volume via the first opening from contaminants;the first container is configured to keep internal pressure of the inner air substantially not higher than the atmospheric pressure, without actively compressing the inner air; anda second container comprising a second volume configured to contain liquid nitrogen and to have the first container immersed in the liquid nitrogen for bringing the first container in thermal contact with the liquid nitrogen, thereby passively cooling the first container;wherein the device is configured to continuously produce the liquid air by passively cooling the inner air thereby passively condensing a portion of the inner air to yield the liquid air, and allowing flow of outer air into the first volume while maintaining a pressure of the inner air substantially equal to the atmospheric pressure.2. The device of claim 1 , wherein the device is ...

METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION

A method for separating air by cryogenic distillation in a system of columns comprising a first column and a second column operating at a lower pressure than the first column, comprising the steps of compressing all of the feed air in a first compressor to a first output pressure of at least 1 bar greater than the pressure of the first column, sending a first portion of the air under the first output pressure to the second compressor, and compressing the air to a second output pressure, cooling and condensing at least a portion of the air under the second output pressure in a heat exchanger, withdrawal of a liquid from a column of the system of columns, pressurising the liquid and evaporating the liquid by heat exchange in the heat exchanger, and pressure reduction of a portion of the compressed air to a second output pressure, at least partially evaporating said air in the heat exchanger, optionally additional heating of said air in the heat exchanger, and sending at least a portion of this air to the second compressor. 115-. (canceled)16. A process for the separation of air by cryogenic distillation in a system of columns comprising a first column and a second column operating at a lower pressure than the first column , the process comprising the steps of:i) compressing all of the feed air in a first compressor up to a first outlet pressure of at most one bar greater than and preferably substantially equal to the pressure of the first column;ii) sending a first part of the air under the first outlet pressure to a second compressor, and compression of the air to a second outlet pressure;iii) cooling and condensation of at least a part of the air under the second outlet pressure in the heat exchanger;iv) sending an air gas flow under the first outlet pressure to the system of columns, without more forceful compression, and separation of the air in the system of columns;v) withdrawing the liquid from the system of columns, pressurizing the liquid and vaporizing the ...

SYSTEM AND METHOD FOR PRECOOLING IN HYDROGEN OR HELIUM LIQUEFACTION PROCESSING

Described herein are systems and processes for precooling hydrogen or helium gas streams for liquefaction using liquid nitrogen having reduced energy consumption and amount of liquid nitrogen usage. The systems include a stream of pressurized liquid nitrogen, at least one turboexpander, and at least one heat exchanger. 1. A method for precooling hydrogen or helium gas using a liquid nitrogen stream , the method comprising:a. providing a pressurized liquid nitrogen stream containing liquid nitrogen at a pressure between about 15 bar(a) and about 70 bar(a);b. passing the pressurized liquid nitrogen stream and a partially-cooled hydrogen or helium gas stream through a first heat exchanger that exchanges heat between the pressurized liquid nitrogen stream and the partially-cooled hydrogen or helium gas stream to provide a first partially-warmed nitrogen stream and a precooled hydrogen or helium gas stream;c. passing the first partially-warmed nitrogen stream through one or more turboexpanders that lowers the temperature and pressure of the partially-warmed nitrogen stream to provide a cold nitrogen stream; andd. passing the cold nitrogen stream through the first heat exchanger and through a second heat exchanger to provide the precooled hydrogen or helium gas stream, and a fully-warmed nitrogen gas stream.2. The method of claim 1 , wherein step (d) comprises: passing the cold nitrogen stream through the first heat exchanger that exchanges heat between the cold nitrogen stream and the partially-cooled hydrogen or helium gas stream to provide a second partially-warmed nitrogen gas stream and the precooled hydrogen or helium gas stream; and passing the second partially-warmed nitrogen gas stream through the second heat exchanger that exchanges heat between the second partially-warmed nitrogen gas stream and a warm hydrogen or helium gas stream to provide a fully-warmed nitrogen gas stream and the partially-cooled hydrogen or helium gas stream.3. The method of claim 2 , ...

Integration of hydrogen liquefaction with gas processing units

A method of liquefying hydrogen, including dividing a hydrogen stream into at least a first fraction and a second fraction, introducing the first fraction into a refrigeration cycle of a hydrogen liquefaction unit, thereby liquefying a product hydrogen stream, withdrawing one or more warm hydrogen stream(s) from the hydrogen liquefaction unit, and returning the one or more warm hydrogen stream to the hydrogen stream, wherein the second fraction is combined with a high-pressure nitrogen stream to form an ammonia synthesis gas stream.

INTEGRATION OF HYDROGEN LIQUEFACTION WITH GAS PROCESSING UNITS

A method including, compressing a first hydrogen stream, and expanding a portion to produce a hydrogen refrigeration stream, cooling a second hydrogen stream thereby producing a cool hydrogen stream, wherein at least a portion of the refrigeration is provided by a nitrogen refrigeration stream, further cooling at least a portion of the cool hydrogen stream thereby producing a cold hydrogen stream, and a warm hydrogen refrigeration stream wherein at least a portion of the refrigeration is provided by the hydrogen refrigeration stream, compressing the warm hydrogen refrigeration stream, mixing the balance of the compressed first hydrogen stream with a high-pressure gaseous nitrogen stream to form an ammonia synthesis gas stream, and wherein the first hydrogen stream and the warm hydrogen refrigeration stream are compressed in the same compressor. 1. A method comprising:compressing a first hydrogen stream, and expanding a portion to produce a hydrogen refrigeration stream,cooling a second hydrogen stream thereby producing a cool hydrogen stream, wherein at least a portion of the refrigeration is provided by a nitrogen refrigeration stream,further cooling at least a portion of the cool hydrogen stream thereby producing a cold hydrogen stream, and a warm hydrogen refrigeration stream, wherein at least a portion of the refrigeration is provided by the hydrogen refrigeration stream,compressing the warm hydrogen refrigeration stream,mixing the balance of the compressed first hydrogen stream with a high-pressure gaseous nitrogen stream to form an ammonia synthesis gas stream, andwherein the first hydrogen stream and the warm hydrogen refrigeration stream are compressed in the same compressor.2. The method of claim 1 , wherein the portion of the first hydrogen stream is removed downstream of the compressor.3. The method of claim 1 , wherein the portion of the first hydrogen stream is withdrawn between compression stages of the compressor.4. The method of claim 1 , wherein the ...

PROCESS AND PLANT FOR THE LIQUEFACTION OF AIR AND FOR THE STORAGE AND RECOVERY OF ELECTRICAL ENERGY

A process and plant for the liquefaction of air in which a stream of pressurized air is provided at a first pressure level and is compressed by means of a compressor to a second pressure level, a first partial stream, a second partial stream and a third partial stream are formed from air of the stream of pressurized air after the compression to the second pressure level, air of the first partial stream is cooled down using cold that is produced by means of an expansion of air of the second partial stream and the third partial stream and is at least partially liquefied, and feed air that is compressed to the first pressure level and air of the second partial stream and the third partial stream that is provided at the first pressure level are used for providing the stream of pressurized air at the first pressure level. 1. A process for the liquefaction of air in which a stream of pressurized air is provided at a first pressure level and is compressed using a compressor to a second pressure level , a first partial stream , a second partial stream and a third partial stream are formed from air of the stream of pressurized air after the compression to the second pressure level , air of the first partial stream is cooled down using cold that is produced by means of an expansion of air of the second partial stream and the third partial stream and is at least partially liquefied , and both feed air that is compressed to the first pressure level and air of the second partial stream and the third partial stream that is provided at the first pressure level are used for providing the stream of pressurized air at the first pressure level , the air of the second partial stream being successively cooled down to a first temperature level , allowed to expand from the second pressure level to the first pressure level and heated with respect to the first partial stream , and the air of the third partial stream being successively cooled down to a second temperature level below the ...

Method and apparatus for power storage

Cryogenic energy storage systems, and particularly methods for capturing cold energy and re-using that captured cold energy, are disclosed. The systems allow cold thermal energy from the power recovery process of a cryogenic energy storage system to be captured effectively, to be stored, and to be effectively utilised. The captured cold energy could be reused in any co-located process, for example to enhance the efficiency of production of the cryogen, to enhance the efficiency of production of liquid natural gas, and/or to provide refrigeration. The systems are such that the cold energy can be stored at very low pressures, cold energy can be recovered from various components of the system, and/or cold energy can be stored in more than one thermal store.

METHOD AND INSTALLATION FOR STORING AND RECOVERING ENERGY

The invention relates to a method for storing and recovering energy, according to which a condensed air product (LAIR) is formed in an energy storage period, and in an energy recovery period, a pressure flow is formed and is expanded to produce energy using at least part of the condensed air product (LAIR) without a supply of heat from an external heat source. The method comprises inter alia, for the formation of the condensed air product (LAIR): the compression of air (AIR) in an air conditioning unit (), at least by means of an adiabatically operated compressor device (); the formation of a first and a second sub-flow downstream of the adiabatically driven compressor device (), said flows being formed from the air (AIR) that has been compressed in said device and the guiding of the first and second sub-flows in parallel through a first thermal store () and through a second thermal store (), in which stores heat produced during the compression of the air (AIR) is at least partially stored. For the formation of the pressure flow, a vaporized product (HPAIR) is produced inter alia from at least one part of the condensed air product (LAIR). During the energy-producing expansion process, the pressure flow is guided through a first expansion device () and a second expansion device () and is thus expanded in each device. Heat stored in the first heat store device () is transferred to the pressure flow upstream of the first expansion device () and heat stored in the second heat store device () is transferred to the pressure flow upstream of the second expansion device (). The invention also relates to an installation (). 1. A method for storing and recovering energy in which , in an energy storage period , an air liquefaction product is formed and , in an energy recovery period , a pressurized stream is formed and expanded to perform work by using at least part of the air liquefaction product without a supply of heat from an external heat source , the method comprising , ...

PROCESS AND APPARATUS FOR GENERATING ELECTRIC ENERGY

The invention provides a process and apparatus to generate electric energy in a system comprising a power station and air treatment plant. The power station has a first gas expansion unit connected to a generator. The air treatment plant has an air compression unit, heat exchanger system and tank for liquid. In a first operating mode, feed air is compressed in the air compression unit and cooled in the heat exchanger system. A storage fluid containing less than 40 mol % of oxygen is produced and stored as low-temperature liquid in the tank for liquid. In a second operating mode, low-temperature liquid is taken from the tank for liquid and vaporized or pseudovaporized under superatmospheric pressure. The gaseous high-pressure storage fluid produced in this way is expanded in a gas expansion unit. The (pseudo)vaporization of the low-temperature liquid is carried out in the heat exchanger system of the air treatment plant. 23132. The method as claimed in claim 1 , characterized in that the auxiliary air is further compressed in at least two cold compressors ( claim 1 , ) claim 1 , which are connected in parallel.310410421. The method as claimed in claim 1 , characterized in that the power station has a gas turbine system with combustion chamber claim 1 , gas turbine expander and generator claim 1 , and at least part of the gaseous high-pressure storage fluid () is expanded in the gas turbine expander of a gas turbine system claim 1 , wherein the storage fluid () is fed to the gas turbine system downstream of the (pseudo-)vaporization ().4. The method as claimed in claim 1 , characterized in that the gas expansion unit has a hot-gas turbine system which has at least one heater and one hot-gas turbine.5. The method as claimed in claim 3 , characterized in that the gaseous high-pressure storage fluid is expanded in two steps claim 3 , wherein the first step is carried out as a work-performing expansion in the hot-gas turbine system and the second step is carried out in ...

Method for Thermally Assisted Electric Energy Storage

A proposed method for thermally assisted electric energy storage is characterized by a significant increase in round-trip efficiency through a profitable use of waste heat energy streams from the co-located power generation and industrial facilities, combustion of renewable or fossil fuels, or harnessing the renewable energy sources. In the charge operation mode it is achieved by superheating and expansion of recirculating air stream in the liquid air energy storage with self-producing a part of power required for air liquefaction. In the discharge operation mode it is attained through the repeated and efficient use of a stream of discharged air in auxiliary power production cycle. 1. A method for thermally assisted electric energy storage (TAEES) , comprising in combination:pressurizing a process air, as a sum of fresh and recirculating air streams, up to an intermediate pressure with use of mechanically or electrically driven intercooled compressor train consuming an external power during TAEES charge;succeeding TAEES operation using the principle of at least one turbo expander-compressor based open air auto-refrigeration cycle and including:a) compressing the process air up to a top cycle pressure by the boost compressor;b) pre-cooling the entire process air;c) work-expanding the most part of pre-cooled process air down to a bottom cycle pressure and a corresponding its deep cooling;d) harnessing an expansion work for driving the said boost compressor;e) liquefying the rest of process air at a top cycle pressure and its expanding with a final cooling down to the bottom cycle pressure and temperature;f) separating the liquid and gaseous phases of the rest of process air;g) forming a recirculating air stream at a bottom cycle pressure as a mixture of the deeply-cooled most part of process air and a gaseous phase of the rest of process air;h) further sequential using a cold thermal energy of recirculating air for liquefying the rest of process air and pre-cooling ...

SYSTEM AND METHOD FOR COMPRESSOR INTERCOOLER

A method includes compressing an air flow to a first pressure, transferring heat from the air flow to a liquefaction fluid via an intercooler heat exchanger, compressing the air flow to a second pressure greater than the first pressure, combusting the air flow and a fuel to generate a combustion product flow, and driving a turbine with the combustion product flow. The turbine is configured to drive machinery of a liquefaction system. The liquefaction fluid includes at least one of a pre-cooling fluid, a refrigerant, and a liquefied product of the liquefaction system. 1. A system comprising: a first compressor stage configured to compress an air flow to a first pressure;', 'a second compressor stage configured to compress the air flow to a second pressure greater than the first pressure; and', 'a turbine disposed along an axis of the gas turbine system;, 'a gas turbine system comprising a body comprising a plurality of channels configured to receive a cooling fluid; and', 'a plurality of fins extending from the body, wherein the air flow is configured to flow over the plurality of fins, and the intercooler heat exchanger is configured to transfer heat from the air flow to the cooling fluid; and, 'an intercooler heat exchanger disposed between the first compressor stage and the second compressor stage, wherein the intercooler comprisesa liquefaction system indirectly coupled to the intercooler heat exchanger, wherein the liquefaction system comprises a liquefaction fluid, and the liquefaction fluid is configured to receive heat from the cooling fluid.2. The system of claim 1 , comprising a working fluid system coupled to the intercooler heat exchanger and to the liquefaction system claim 1 , wherein the working fluid system comprises a working fluid heat exchanger and a pumping system claim 1 , the pumping system is configured to circulate the cooling fluid from the intercooler heat exchanger to the working fluid heat exchanger claim 1 , and the working fluid heat ...

STAGED CRYOGENIC STORAGE TYPE SUPERCRITICAL COMPRESSED AIR ENERGY STORAGE SYSTEM AND METHOD

The present disclosure provides a supercritical compressed air energy storage system. The supercritical compressed air energy storage system includes a supercritical liquefaction subsystem, an evaporation and expansion subsystem, a staged cryogenic storage subsystem, a heat storage and heat exchange subsystem, and a cryogenic energy compensation subsystem, the staged cryogenic storage subsystem being used for implementing the staged storage and release of cryogenic energy, improving efficiency of recovering cryogenic energy during energy release and energy storage, and thereby improving cycle efficiency of the system. The present disclosure does not need to provide any inputs of additional cryogenic energy and heat energy input externally, and has the advantages of high cycle efficiency, low cost, independent operation, environmental friendliness, and no limitation on terrain conditions, and it is suitable for large-scale commercial applications. 1. A staged cryogenic storage type supercritical compressed air energy storage system , comprising a supercritical liquefaction subsystem for converting input gaseous air into liquid air and an evaporation and expansion subsystem for converting liquid air into gaseous air , wherein the staged cryogenic storage type supercritical compressed air energy storage system further comprises:a staged cryogenic storage subsystem for storing and/or releasing cryogenic energy when the gaseous air or the liquid air is converted.2. The system according to claim 1 , wherein the staged cryogenic storage subsystem comprises at least one liquefaction cold box claim 1 , at least one deep cooling cryogenic storage cycle claim 1 , and at least one intermediate cooling cryogenic storage cycle claim 1 ,wherein the deep cooling cryogenic storage cycle is connected with the liquefaction cold box for storing/releasing cryogenic energy from a deep cooling temperature to a normal temperature,wherein the intermediate cooling cryogenic storage cycle is ...

LIQUEFACTION APPARATUS

A liquefaction apparatus that automatically adjusts the load on the liquefaction apparatus correspondingly with an upper limit value of contracted power in different time slots, and which is capable of maximizing the amount of liquefied product produced and of achieving optimum operating efficiency is provided. In certain embodiments, the liquefaction apparatus can include: a production amount calculation unit 91 for obtaining an actual production amount of a liquefied product; a predicted power calculation unit 92 for obtaining a predicted power amount after a predetermined time has elapsed, on the basis of an integrated power value obtained by integrating a usage power; and a power demand control unit 93 for comparing the predicted power amount and a moving average of instantaneous power, and controlling a discharge flow rate of a compressor 3 in such a way as to come infinitely close to a target value, without exceeding the target value, and while using the larger value of the predicted power amount and the moving average of instantaneous power as a value being controlled. 1. A liquefaction apparatus comprising:a predicted power calculation unit configured to obtain a predicted power amount after a predetermined time has elapsed, on the basis of an integrated power value obtained by integrating a usage power; anda power demand control unit configured to compare the predicted power amount and a moving average of instantaneous power, and wherein the power demand control unit is further configured to control a discharge flow rate of a compressor in such a way as to come infinitely close to a target value, without exceeding the target value, and while using the larger value of the predicted power amount and the moving average of instantaneous power as a value being controlled.2. The liquefaction apparatus according to claim 1 , wherein the liquefaction apparatus comprises:an expansion turbine; andan expansion turbine inlet nozzle for controlling an inlet pressure of ...

Small-Scale Hydrogen Liquefaction System Equipped with Cryocooler

Disclosed is a small-scale hydrogen liquefaction system using cryocoolers. The system includes: a pre-cooling heat exchanger for pre-cooling gaseous hydrogen using liquid nitrogen; a first cryocooler that primarily cools the gaseous hydrogen, pre-cooled by the pre-cooling heat exchanger; a heat exchanger attached to a cold head of the first-cryocooler; an n-th cryocooler (wherein n is a natural number equal to or greater than two) that is connected in series with the first cryocooler and cools the gaseous hydrogen, primarily cooled by the first cryocooler, to a liquefaction temperature of 20.3 K; a condensation plate arranged to be in contact with the n-th cryocooler to liquefy the gaseous hydrogen, cooled to the temperature of 20.3 K by the n-th cryocooler; and a low-temperature chamber providing an accommodation space to accommodate the pre-cooling heat exchanger, the first cryocooler, and the n-th cryocooler. 1. A small-scale hydrogen liquefaction system employing multiple cryocoolers connected in series with each other to liquefy gaseous hydrogen through multiple cooling stages , the system comprising:a pre-cooling heat exchanger for pre-cooling gaseous hydrogen using liquid nitrogen;a first cryocooler that receives the gaseous hydrogen pre-cooled by the pre-cooling heat exchanger and primarily cools the gaseous hydrogen;a heat exchanger attached to a cold head of the first cryocooler;an n-th cryocooler that is connected in series with the first cryocooler and cools the primarily cooled gaseous hydrogen to a liquefaction temperature of 20.3 K (wherein n is a natural number equal to or greater than 2);a condensation plate arranged to be in contact with the n-th cryocooler to liquefy the gaseous hydrogen, which is cooled to the liquefaction temperature of 20.3 K by the n-th cryocooler; anda low-temperature chamber providing an accommodation space to accommodate the pre-cooling heat exchanger, the first cryocooler, and the n-th cryocooler therein.2. The small-scale ...

METHOD FOR COOLING A PROCESS FLOW

A method of cooling a process stream with an auxiliary stream is described, wherein the exchange of heat between the process stream and the auxiliary stream is effected in a first heat exchanger and a second heat exchanger connected downstream thereof. 1. A method of cooling a process stream with an auxiliary stream , wherein an exchange of heat between the process stream and the auxiliary stream is effected in a first heat exchanger and a second heat exchanger connected downstream thereof ,characterized in thata) the process stream is divided into two or more substreams,b) flow rates of the substreams are regulatable by means of one valve each,c) only a first substream is cooled down with the auxiliary stream in the first and second heat exchangers, andd) the other substream(s) is/are mixed into the cooled first substream and a process stream thus formed is cooled again in the second heat exchanger, and, in the case of division into more than two substreams, the process stream is cooled again in the second heat exchanger after each substream has been mixed in,e) wherein the flow rates of the substreams are regulated such that the temperatures of the process streams to be cooled in the second heat exchanger, on entry into the second heat exchanger, differ from one another by not more than 10 K, andf) wherein at least one of the valves that regulates the flow rates of the substreams is fully opened.2. The method as claimed in claim 1 , characterized in that the flow rates of the substreams are regulated such that the temperatures of the process streams to be cooled in the second heat exchanger claim 1 , on entry into the second heat exchanger claim 1 , differ from one another by not more than 5 K.3. The method as claimed in claim 1 , characterized in that the first heat exchanger and/or the second heat exchanger take the form of a plate heat exchanger.4. The method as claimed in claim 1 , characterized in that the process stream to be cooled is selected from the ...

Energy storage and recovery methods, systems, and devices

A method for energy storage and recovery is based on the liquid air energy storage (LAES) operated at the pressure relationship such that the pressure of discharge air is greater than the charge air to provide a high round-trip efficiency. External cold source and cold thermal energy storage are used in a LAES to achieve a decrease in the LAES capital costs. A demand for a supplemental cold energy provided by external sources may be minimized. These features alone or in combination may result in reduced power demand required for cooling.

METHOD AND APPARATUS FOR RECOVERY OF CONDENSABLE GASES FROM LIQUID STORAGE TANKS

A method and apparatus for recovering boil-off gas from a head space of a liquid storage tank having a fluid contained therein is provided. The method can include the steps of withdrawing the boil-off gas from the storage tank and introducing said boil-off gas to a heat exchanger using a vapor flow inducer; cooling the boil-off gas in the heat exchanger by using cold energy from vaporization of liquid nitrogen to form a cooled fluid; and introducing the cooled fluid to the liquid storage tank, thereby reducing the temperature within the liquid storage tank. 1. A method for recovering boil-off gas from a head space of a liquid storage tank having a fluid contained therein , the method comprising the steps of:(a) measuring a condition selected from the group consisting of outside temperature, temperature within the liquid storage tank, pressure within the liquid storage tank, liquid level within the liquid storage tank, heat absorption by the liquid storage tank, and combinations thereof;(b) withdrawing the boil-off gas from the liquid storage tank and introducing said boil-off gas to a heat exchanger using a vapor flow inducer, wherein the vapor flow inducer is configured to adjust the flow rate of the boil-off gas introduced to the heat exchanger based on the condition measured in step (a);(c) cooling the boil-off gas in the heat exchanger by using cold energy from a flow of nitrogen to form a cooled fluid, wherein the heat exchanger is in fluid communication with an outlet of a liquid nitrogen storage tank, such that the heat exchanger is configured to receive a flow of nitrogen from the liquid nitrogen storage tank; and(d) introducing the cooled fluid to the liquid storage tank, thereby reducing the temperature within the liquid storage tank,wherein the flow rate of the boil-off gas withdrawn from the liquid storage tank to the heat exchanger and/or the flow rate of the nitrogen from the liquid nitrogen storage tank is adjusted, such that during the cooling step ( ...

SYSTEMS AND METHODS FOR NATURAL GAS COOLING

A system for natural gas cooling using nitrogen. The system can include a nitrogen liquefier and a natural gas cooler. The nitrogen liquefier can provide liquid nitrogen to the natural gas cooler. One or more heat exchangers of the natural gas cooler can include a gaseous nitrogen output that is in fluid communication with the nitrogen liquefier. In response to receiving gaseous nitrogen at the nitrogen liquefier, from the one or more heat exchangers, a production rate of the the nitrogen liquefier is adjusted. 1. A system for natural gas cooling using nitrogen , the system comprising: one or more gaseous nitrogen input conduits in fluid communication with one or more gaseous nitrogen sources;', 'one or more liquid nitrogen output conduits; and', 'one or more compressors in fluid communication with the one or more gaseous nitrogen input conduits,, 'a nitrogen liquefier, the nitrogen liquefier comprisingwherein the nitrogen liquefier is adapted to convert gaseous nitrogen supplied by the one or more gaseous nitrogen sources into liquid nitrogen that is provided to the one or more liquid nitrogen output conduits; one or more natural gas input conduits in fluid communication with one or more natural gas sources;', 'one or more cooled liquid natural gas output conduits; and', 'one or more heat exchangers in fluid communication with: i) the one or more gaseous nitrogen input conduits of the nitrogen liquefier;', 'and ii) the one or more cooled liquid natural gas output conduits,, 'a natural gas cooler, the natural gas cooler comprisingwherein the natural gas cooler is adapted to reduce a temperature of natural gas from the one or more natural gas sources forming a cooled liquid natural gas that is provided to the one or more cooled liquid natural gas output conduits, andwherein the system is configured such that, in response to a change in a production rate of cooled liquid natural gas being produced in the one or more heat exchangers, a production rate of liquid ...

HYDROGEN LIQUEFACTION DEVICE

An example hydrogen liquefaction apparatus is disclosed. The apparatus includes an outer container; a liquefaction container positioned at least partially within the outer container; a heat pipe positioned within the liquefaction container. The head pipe includes a condensing portion, an evaporating portion, an inner tube portion containing a working fluid and operatively coupling the condensing portion to the evaporating portion, and an outer tube portion surrounding the inner tube portion and defining a dual tube region between the outer tube and the inner tube. Also included is a cryocooler in thermal communication with the liquefaction container, a pre-cooling tube, and an ortho-para converting part having a catalyst configured to induce an ortho-para conversion of gaseous hydrogen within the pre-cooling tube. 1. A hydrogen liquefaction apparatus , comprising:an outer container;a liquefaction container positioned at least partially within the outer container;a heat pipe positioned within the liquefaction container and comprising a condensing portion, an evaporating portion, an inner tube portion containing a working fluid and operatively coupling the condensing portion to the evaporating portion, and an outer tube portion surrounding the inner tube portion and defining a dual tube region between the outer tube and the inner tube;a cryocooler in thermal communication with the liquefaction container and configured to cool the condensing portion of the heat pipe;a pre-cooling tube positioned at least partially within the dual tube region and comprising an inlet port for receiving gaseous hydrogen and an outlet port for discharging gaseous hydrogen into the liquefaction container; andan ortho-para converting part positioned at least partially within the pre-cooling tube, the ortho-para converting part comprising a catalyst configured to induce an ortho-para conversion of gaseous hydrogen within the pre-cooling tube.2. The hydrogen liquefaction apparatus of claim 1 , ...

METHOD AND FACILITY FOR STORING AND DISTRIBUTING LIQUEFIED HYDROGEN

A method for storing and distributing liquefied hydrogen using an installation having a storage facility for liquid hydrogen, a source of gaseous hydrogen, a liquefier having an inlet connected to the source and an outlet connected to the liquid hydrogen storage facility, the storage facility having a liquid withdrawal pipe having an end connected to the liquid hydrogen storage facility and an end configured to be connected to at least one mobile tank, the method having a stage of liquefying gaseous hydrogen and a stage of transferring the liquefied hydrogen to the storage facility, wherein the liquefied hydrogen has a temperature below the bubble point of hydrogen at the storage pressure and further having a stage of transfer of liquid hydrogen directly to the tank at a temperature between the saturation temperature at the pressure of the liquid and a temperature above the solidification temperature of the hydrogen. 1. A method for storing and distributing liquefied hydrogen using an installation comprising a storage facility for liquid hydrogen at a predetermined storage pressure , a source of gaseous hydrogen , a liquefier comprising an inlet connected to the source and an outlet connected to the liquid hydrogen storage facility , the storage facility comprising a liquid withdrawal pipe comprising an end connected to the liquid hydrogen storage facility and an end configured to be connected to at least one mobile tank , the method comprising a stage of liquefying gaseous hydrogen supplied by the source and a stage of transferring the liquefied hydrogen to the storage facility , wherein the hydrogen liquefied by the liquefier and transferred to the storage facility has a temperature below the bubble point of hydrogen at the storage pressure and further comprising a stage of transfer of liquid hydrogen produced by the liquefier directly to the tank at a temperature between the saturation temperature at the pressure of the liquid and a temperature above the ...

INTEGRATED REFUELING STATION

A system comprising: 1. A system comprising:(a) a liquid natural gas compression module having a compressed liquid natural gas conduit;{'sub': '2', '(b) an active magnetic regenerative refrigerator Hliquefier module;'}{'sub': 2', '2', '2, '(c) at least one Hgas source fluidly coupled to the active magnetic regenerative refrigerator Hliquefier module via an Hgas conduit; and'}{'sub': '2', '(d) a heat exchanger that receives the compressed liquid natural gas conduit and the Hgas conduit.'}2. The system of claim 1 , further comprising:(e) a fuel cell;{'sub': 2', '2, 'wherein the fuel cell has an inlet fluidly coupled to the liquid natural gas compression module via a methane conduit and an Hgas outlet fluidly coupled to the Hgas conduit.'}3. The system of claim 1 , further comprising:(f) a liquid natural gas storage tank fluidly coupled to the liquid natural gas compression module;(g) a liquid natural gas vehicle dispenser fluidly coupled to the liquid natural gas storage tank;(h) a compressed liquid natural gas vehicle dispenser fluidly coupled to the liquid natural gas compression module;{'sub': 2', '2, '(i) a liquid Hvehicle dispenser fluidly coupled to the active magnetic regenerative refrigerator Hliquefier module; and'}{'sub': 2', '2, '(j) a compressed Hvehicle dispenser fluidly coupled to the active magnetic regenerative refrigerator Hliquefier module.'}4. The system of claim 1 , wherein the active magnetic regenerative refrigerator Hliquefier module comprises (i) a high magnetic field section in which a heat transfer fluid flows from a cold side to a hot side through at least one magnetized bed of at least one magnetic refrigerant claim 1 , (ii) a first no heat transfer fluid flow section in which the bed is demagnetized claim 1 , (iii) a low magnetic or demagnetized field section in which the heat transfer fluid flows from a hot side to a cold side through the demagnetized bed claim 1 , (iv) a second no heat transfer fluid flow section in which the bed is ...

Small-Scale Hydrogen Liquefaction System Equipped with Cryocooler

Disclosed is a small-scale hydrogen liquefaction system using cryocoolers. The system includes: a gas supply line to supply a gaseous hydrogen; n cryocoolers each connected to the gas supply line to be connected in parallel and configured such that the gaseous hydrogen supplied from the gas supply line is divided into n portions, and the n portions flow through the n cryocoolers, respectively, and are cooled to a liquefaction temperature, wherein n is a natural number equal to or greater than 2; n heat exchangers each attached to a cold head of each of the n cryocoolers; and a low-temperature chamber providing an accommodation space to accommodate the n cryocoolers therein. 1. A small-scale hydrogen liquefaction system employing multiple cryocoolers to liquefy gaseous hydrogen through multiple cooling stages , the system comprising:a gas supply line to supply a gaseous hydrogen;n cryocoolers each connected to the gas supply line to be connected in parallel and configured such that the gaseous hydrogen supplied from the gas supply line is divided into n portions, and the n portions flow through the n cryocoolers, respectively, and are cooled to a liquefaction temperature, wherein n is a natural number equal to or greater than 2;n heat exchangers each attached to a cold head of each of the n cryocoolers; anda low-temperature chamber providing an accommodation space to accommodate the n cryocoolers therein.2. The small-scale hydrogen liquefaction system according to claim 1 , further comprising:a pre-cooling heat exchanger for pre-cooling the gaseous hydrogen supplied from the gas supply line, using liquid nitrogen, wherein the pre-cooling heat exchanger is connected between the gas supply line and the n cryocoolers and is configured to provide the pre-cooled gaseous hydrogen to each of the n cryocoolers.3. The small-scale hydrogen liquefaction system according to claim 1 , further comprising:m cryocoolers having the first cryocooler to m-th cryocooler and connected ...

METHOD FOR STARTING UP AN ARGON SEPARATION COLUMN OF AN APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION AND UNIT FOR IMPLEMENTING THE METHOD

A unit for producing argon by cryogenic distillation, suitable for connection to a double air separation column consisting of first and second columns interconnected thermally, comprises an argon separation column surmounted with a top condenser and a denitrogenation column, means for withdrawing an argon-rich and nitrogen-depleted product (LAR) at the bottom of the denitrogenation column, means for connecting the top of the argon separation column to the denitrogenation column, means for sending a top gas from the argon separation column to the atmosphere, means for withdrawing a nitrogen-rich fluid from the top of the denitrogenation column, an analyser for measuring the nitrogen content at the top of the argon separation column, and means for opening and closing the means for connecting the top of the argon separation column to the denitrogenation column depending on the nitrogen content detected by the analyser.

NITROGEN PROCESS FOR PRODUCTION OF AMMONIA AND LIQUID HYDROGEN

A method of co-producing liquid hydrogen and ammonia, including a hydrogen generator, a nitrogen generator, and a HLU is presented. The method includes pressurizing a hydrogen stream from the hydrogen generator in a hydrogen compressor, dividing the pressurized hydrogen into at least a first portion and a second portion, wherein the first portion includes at least part of the flow of a first refrigeration cycle in the HLU, and the second part comprises at least part of the feed to an ammonia plant. The method also includes pressurizing a nitrogen stream from the nitrogen generator in a HP nitrogen compressor, dividing the pressurized nitrogen stream into at least a first part and a second part, wherein the first part comprises at least part of the flow of a second refrigeration cycle in the HLU, and the second part comprises at least part of the feed to the ammonia plant. 1. A method of co-producing liquid hydrogen and ammonia , comprising a hydrogen generator , a nitrogen generator , and a hydrogen liquefaction unit , the method comprising:pressurizing a hydrogen stream from the hydrogen generator in a HP hydrogen compressor, dividing the pressurized hydrogen stream into at least a first portion and a second portion, wherein the first portion comprises at least part of the flow of a first refrigeration cycle in the hydrogen liquefaction unit, and the second part comprises at least part of the feed to an ammonia plant, andpressurizing a nitrogen stream from the nitrogen generator in a HP nitrogen compressor, dividing the pressurized nitrogen stream into at least a first part and a second part, wherein the first part comprises at least part of the flow of a second refrigeration cycle in the hydrogen liquefaction unit, and the second part comprises at least part of the feed to the ammonia plant2. The method of claim 1 , wherein the HP nitrogen compressor has an inlet pressure and the inlet pressure is between 5 bara and 15 bara.3. The method of claim 2 , wherein the ...

SYSTEM AND METHOD FOR NATURAL GAS AND NITROGEN LIQUEFACTION WITH DUAL OPERATING MODES

Liquefier arrangements configured for co-production of both liquid natural gas (LNG) and liquid nitrogen (LIN) configured to operate in two distinct operating modes are provided. 1. A method of liquefaction to co-produce liquid nitrogen and liquid natural gas , the method comprising the steps of:(i) receiving a gaseous nitrogen feed stream;(ii) compressing the gaseous nitrogen feed stream and one or more gaseous nitrogen recycle streams in a recycle compressor to produce a gaseous nitrogen effluent stream;(iii) further compressing a first portion of the effluent stream in a cold booster compressor to form a part of a primary nitrogen liquefaction stream;(iv) further compressing a second portion of the effluent stream in a warm booster compressor to form either a warm nitrogen recycle stream or another part of the primary nitrogen liquefaction stream;(v) cooling the primary nitrogen liquefaction stream in a first heat exchange passage in a multi-pass brazed aluminum heat exchanger;(vi) expanding a first portion of the cooled primary nitrogen liquefaction stream extracted at a primary intermediate location of the first heat exchange passage in a cold booster loaded turbine to produce a cold turbine exhaust;(vii) warming the cold turbine exhaust and the warm turbine exhaust in one or more heat exchange passages in the multi-pass brazed aluminum heat exchanger, including at least a second heat exchange passage to produce one or more gaseous nitrogen recycle streams;(viii) subcooling the primary nitrogen liquefaction stream to produce the subcooled liquid nitrogen stream;(ix) liquefying a natural gas feed stream in a fifth heat exchange passage of the multi-pass brazed aluminum heat exchanger against a first portion of the at least partially vaporized subcooled liquid nitrogen stream in a fourth heat exchange passage of the multi-pass brazed aluminum heat exchanger and the one or more gaseous nitrogen recycle streams to produce the liquid natural gas, and(x) taking a ...

SYSTEM AND METHOD FOR NATURAL GAS AND NITROGEN LIQUEFACTION WITH DIRECT DRIVE MACHINES FOR TURBINES AND BOOSTERS

Liquefier arrangements configured for co-production of both liquid natural gas (LNG) and liquid nitrogen (LIN) configured to operate using direct drive motor/generator arrangement for the warm and/or cold booster compressors and turbines. Alternatively, the use of a conventional generator with a bull gear in lieu of the direct drive motor/generator arrangement on the warm turbine and warm booster compressor coupling is also disclosed. 1. A method of liquefaction to co-produce liquid nitrogen and liquid natural gas , the method comprising the steps of:(i) receiving a gaseous nitrogen feed stream;(ii) compressing the gaseous nitrogen feed stream and one or more gaseous nitrogen recycle streams in a recycle compressor to produce a gaseous nitrogen effluent stream;(iii) further compressing a first portion of the effluent stream in a cold booster compressor to form a part of a primary nitrogen liquefaction stream and further compressing a second portion of the effluent stream in a warm booster compressor to form a warm nitrogen recycle stream, wherein the warm booster compressor is coupled to a direct drive motor/generator arrangement;(iv) cooling the primary nitrogen liquefaction stream in a first heat exchange passage in a multi-pass brazed aluminum heat exchanger;(v) expanding a first portion of the cooled primary nitrogen liquefaction stream extracted at a primary intermediate location of the first heat exchange passage in a cold booster loaded turbine to produce a cold turbine exhaust;(vi) warming the cold turbine exhaust in a second heat exchange passage in the multi-pass brazed aluminum heat exchanger to form a gaseous nitrogen recycle stream;(vii) cooling the warm nitrogen recycle stream in a third heat exchange passage in the multi-pass brazed aluminum heat exchanger;(viii) expanding the cooled stream exiting the third heat exchange passage in a warm booster loaded turbine to produce a warm turbine exhaust wherein the warm booster loaded turbine is also ...

COOLING METHOD FOR LIQUEFYING A FEED GAS

The present invention pertains to a cooling method for liquefying a feed gas, comprising the steps of providing a cooling cycle with a refrigerant stream; dividing the refrigerant stream into a first partial stream and a second partial stream; expanding the first partial stream in a first expansion device; and transferring cooling energy from the expanded first partial stream to a feed gas stream to be cooled, particularly comprising hydrogen and/or helium. Further the method comprises the steps of guiding the expanded first partial stream to a suction inlet of an ejector; and guiding the second partial stream to a propellant inlet of the ejector such that, upon expanding the second partial stream in the ejector, the expanded first partial stream is compressed and merged with the expanded second partial stream. 1. Cooling method for liquefying a feed gas , comprising the steps of:providing a cooling cycle with a refrigerant stream;dividing the refrigerant stream into a first partial stream and a second partial stream;expanding the first partial stream in a first expansion device; and, guiding the expanded first partial stream to a suction inlet of an ejector; and,', 'guiding the second partial stream to a propellant inlet of the ejector such that, upon expanding the second partial stream in the ejector, the expanded first partial stream is compressed and merged with the expanded second partial stream., 'transferring cooling energy from the expanded first partial stream to a feed gas stream to be cooled, wherein the method further comprises the steps of2. Method according to claim 1 , wherein claim 1 , by transferring cooling energy from the expanded first partial stream to the feed gas stream to be cooled claim 1 , particularly by means of a first heat exchanger claim 1 , the feed gas stream is cooled to a temperature below the critical temperature of hydrogen claim 1 , particularly below 24 K claim 1 , so as to provide a liquid product stream comprising hydrogen.3. ...

AIR SEPARATION REFRIGERATION SUPPLY METHOD

A method of supplying refrigeration to air separation plants within an air separation plant facility in which a refrigerant stream is produced at cryogenic temperature within a centralized refrigeration system. Streams of the refrigerant at the cryogenic temperature are introduced into the air separation plants such that all or a part of the refrigeration requirements of the air separation plants are supplied by the streams of the refrigerant. 1. A method of supplying refrigeration to air separation plants located within an air separation plant facility , such method comprising:separating air within at least two air separation plants to produce products including a nitrogen-rich vapor stream, wherein the air to be separated in the first of the at least two air separation plants comprises a first compressed air stream that is introduced into a liquid expander and subsequently introduced into at least one of a higher pressure column and a lower pressure column of the first of the at least two air separation plants and a second compressed air stream that is expanded to produce an exhaust stream and the exhaust stream is introduced into the higher pressure column, thereby to impart part of the refrigeration requirements of the first of the at least two air separation plants;withdrawing the nitrogen-rich vapor stream from the first of the at least two air separation plants;liquefying the nitrogen-rich vapor stream within a refrigeration system to produce a nitrogen-rich liquid refrigerant at a cryogenic temperature as a nitrogen-rich liquid; andintroducing one or more streams of the nitrogen-rich liquid refrigerant, while at the cryogenic temperature, directly from the refrigeration system into the other of the at least two air separation plants such that all or a part of the refrigeration requirements of the other of the at least two air separation plants are supplied by the one or more streams of the nitrogen-rich liquid refrigerant.2. The method of claim 1 , wherein ...

PROCESS FOR UTILIZING OF MULTI STAGE COMPRESSORS INTERCOOLERS BLOWDOWN AS A COOLANT FOR PROCESS AIR

A system and a method for processing air prior to separating components of the air are disclosed. The system comprises an air cooler, one or more compression stages operated in series, and one or more intercoolers installed between two adjacent compression stages. A blowdown storage tank is configured to collect water blowdown from one or more intercoolers and provide cooling medium to the air cooler. Atmospheric air is first sprayed by the water blowdown in the air cooler to form a cooled air stream. The cooled air stream is subsequently compressed in the one or more compression stages and cooled by the intercoolers between two adjacent compression stages. The water blowdown from one or more of the intercoolers is collected and recycled as the cooling medium to cool the atmospheric air before it enters the first compression stage. 1. A method of processing air prior to separating components of the air , the method comprising:cooling the air with a cooling medium to produce cooled air;compressing the cooled air in a compressor unit that comprises one or more compression stages and one or more intercoolers to produce compressed process air; andcollecting water blowdown from the one or more intercoolers, wherein the water blowdown is used as the cooling medium.2. The method of claim 1 , wherein the compressor unit is a multi-stage compressor unit.3. The method of claim 2 , wherein the multi-stage compressor unit comprises at least two compression stages and at least one intercooler for cooling compressed air from the at least two compression stages.4. The method of claim 2 , wherein the multi-stage compressor unit comprises at least three compression stages in series and at least two intercoolers for cooling compressed air from the at least three compression stages.5. The method of claim 1 , further comprising claim 1 , before the cooling claim 1 , measuring humidity and temperature of the air claim 1 , wherein the step of cooling the air with a cooling medium is ...

ADVANCED MULTI-LAYER ACTIVE MAGNETIC REGENERATOR SYSTEMS AND PROCESSES FOR MAGNETOCALORIC LIQUEFACTION

An apparatus comprising: 1. A process for liquefying a process gas comprising:introducing a heat transfer fluid into an active magnetic regenerative refrigerator apparatus that comprises dual regenerators located axially opposite to each other, wherein the apparatus comprise (i) a first top regenerator comprising 2 to 16 successive layers, wherein each layer comprises an independently compositionally distinct magnetic refrigerant material having an independent Curie temperature and wherein the first layer of the top regenerator has the highest Curie temperature and the last layer of the top generator has the lowest Curie temperature and (ii) a second bottom regenerator comprising 2 to 16 successive layers, wherein each layer comprises an independently compositionally distinct magnetic refrigerant material having an independent Curie temperature and wherein the first layer of the bottom regenerator has the lowest Curie temperature and the last layer of the bottom regenerator has the highest Curie temperature;flowing the heat transfer fluid through each layer of the first top regenerator and each layer of the second bottom regenerator;diverting a portion of the flowing heat transfer fluid from an outlet of each layer of the first top regenerator to an inlet of the corresponding Curie temperature layer of the second bottom regenerator, except for lowest Curie temperature layer;diverting a bypass portion of the flowing heat transfer fluid from the lowest Curie temperature layer of the first top regenerator into a bypass flow heat exchanger at a first cold inlet temperature;introducing the process gas into the bypass flow heat exchanger at a first hot inlet temperature and at a counterflow with the bypass portion flow, and discharging the process gas or liquid from the bypass flow heat exchanger at a first cold exit temperature; andsimultaneously subjecting all of the layers of the second bottom regenerator to a higher magnetic field while all of the layers of first top ...

ACTIVE MAGNETIC REGENERATIVE PROCESSES AND SYSTEMS EMPLOYING HYDROGEN AS HEAT TRANSFER FLUID AND PROCESS GAS

A process for liquefying a hydrogen process gas comprising: 1. A process for liquefying a hydrogen gas comprising:introducing a hydrogen heat transfer fluid into an active magnetic regenerative refrigerator apparatus that comprises (i) a high magnetic field section in which the hydrogen heat transfer fluid flows from a cold side to a hot side through at least one magnetized bed of at least one magnetic refrigerant, (ii) a first no heat transfer fluid flow section in which the bed is demagnetized, (iii) a low magnetic or demagnetized field section in which the hydrogen heat transfer fluid flows from a hot side to a cold side through the demagnetized bed, and (iv) a second no heat transfer fluid flow section in which the bed is magnetized;continuously introducing the hydrogen heat transfer fluid from the cold side of the low magnetic or demagnetized field section into the cold side of the high magnetic field section;continuously separating a bypass portion of the cold hydrogen heat transfer fluid flowing from the cold side of the low magnetic field or demagnetized section into an expander; andisenthalpically expanding the separated portion of the hydrogen heat transfer fluid to produce liquefied hydrogen.2. The process of claim 1 , wherein the bypass portion constitutes 3 to 12% of the total hydrogen heat transfer fluid exiting the cold side of the low magnetic or demagnetized field section.3. The process of claim 1 , wherein the magnetic refrigerant operates at or below its Curie temperature throughout an entire active magnetic regeneration cycle.4. The process of claim 1 , wherein the process provides a figure of merit (FOM) of at least 0.5.5. The process of claim 1 , wherein the active magnetic regenerative refrigerator apparatus includes a plurality of magnetic refrigerant layers.6. The process of claim 1 , wherein the active magnetic regenerative refrigerator apparatus includes 1 to 16 layers of compositionally distinct magnetic refrigerant materials.7. The ...

Liquid natural gas liquefier utilizing mechanical and liquid nitrogen refrigeration

The present invention relates to a method and system for producing liquefied natural gas (LNG) from a stream of pressurized natural gas which involves a combination of mechanical refrigeration.

RAW MATERIAL GAS LIQUEFYING DEVICE AND METHOD OF CONTROLLING THIS RAW MATERIAL GAS LIQUEFYING DEVICE

A raw material gas liquefying device includes a feed line; a refrigerant circulation line; and a controller. In a refrigerant liquefaction route, a refrigerant flows through a compressor, a heat exchanger, a circulation system JT valve, a liquefied refrigerant storage tank, and the heat exchanger, and returns to the compressor. In a cryogenic energy generation route, the refrigerant flows through the compressor, the heat exchanger, an expansion unit, and the heat exchanger, and returns to the compressor. The controller determines if a refrigerant storage tank liquid level is within an allowable range, manipulates a feed system JT valve opening rate to control refrigerant temperature at the high-temperature-side refrigerant flow path exit side of the heat exchanger, and manipulates the opening rate of the feed system JT valve to control the refrigerant storage tank liquid level so that the refrigerant storage tank liquid level falls into the predetermined allowable range. 1. A raw material gas liquefying device comprising:a feed line in which a raw material gas flows through a raw material flow path of a heat exchanger, a liquefied refrigerant storage tank which stores a liquefied refrigerant therein, and a feed system Joule-Thomson valve in this order;a refrigerant circulation line including a refrigerant liquefaction route and a cryogenic energy generation route, wherein in the refrigerant liquefaction route, a refrigerant flows through a compressor, a high-temperature-side refrigerant flow path of the heat exchanger, a circulation system Joule-Thomson valve, the liquefied refrigerant storage tank, and a first low-temperature-side refrigerant flow path of the heat exchanger in this order, and returns to the compressor, while in the cryogenic energy generation route, the refrigerant flows through the compressor, an expansion unit, and a second low-temperature-side refrigerant flow path of the heat exchanger in this order, and returns to the compressor;a temperature ...

NITROGEN PRODUCTION METHOD AND NITROGEN PRODUCTION APPARATUS

A portion of feed air is expanded and cooled in front of a main heat exchanger, and is used as cold for precooling the remaining unexpanded feed air inside the main heat exchanger. A portion of the feed air precooled inside the main heat exchanger is removed to outside the main heat exchanger, expanded and cooled, and used as cold to cool the remaining unexpanded precooled feed air inside the main heat exchanger. 1. A method for producing a liquid nitrogen product , the method comprising:a precooling step for cooling at least a portion of feed air scrubbed of specified impurities to a first temperature and cooling the precooled feed air;a cooling step for cooling at least a first portion of the feed air cooled by the cooling step to a second temperature lower than the first temperature to produce a low-temperature feed air;a first expanding step for expanding and cooling a second portion of the feed air cooled by the precooling step to produce a first low-temperature air;a second expanding step for expanding and cooling at least a third portion of the feed air to produce a second low-temperature air;a first introducing step for expanding and introducing the feed air cooled by the cooling step into a lower section than a first distilling section in a distillation column having the first distilling section;a condensing step for condensing at least a portion of the gas inside the distillation column by exchanging heat with an oxygen-rich liquid pooled in a lower section of the distillation column by a condensing section arranged in an upper section of the distillation column;a recycled air compressing step for diverting waste gas removed from the condensing section arranged in an upper section of the distillation column and compressing the diverted waste gas;a waste gas heat exchange step for exchanging heat between the not diverted waste gas and either the feed air or the precooled feed air;a second introducing step for introducing the compressed recycled air ...