СПОСОБ ПОЛУЧЕНИЯ БИОМЕТАНА ПУТЕМ ОЧИСТКИ БИОГАЗА ИЗ ХРАНИЛИЩ НЕОПАСНЫХ ОТХОДОВ И УСТАНОВКА ДЛЯ ОСУЩЕСТВЛЕНИЯ СПОСОБА

FIELD: oil and gas industry; chemical or physical processes. SUBSTANCE: invention relates to a method of producing biomethane by cleaning biogas from non-hazardous waste (NHWSF) storages and to an apparatus for carrying out said method. Method of producing biomethane by cleaning biogas from non-hazardous waste storage includes compressing initial gas stream, introducing a stream of gas to be purified into at least one adsorber, filled with adsorbents capable of reversible adsorption of VOC. It includes subjecting the VOC depleted gas flow leaving the adsorber to at least one stage of membrane separation in order to partially separate CO 2 and O 2 from the gas flow. That is followed by introduction of a retentate obtained at the stage of membrane separation into at least one adsorber filled with adsorbents capable of reversible adsorption of the greater part of remaining CO 2 . Exposing CO 2 -exhausted gas stream leaving the adsorber, capable of reversible adsorption of a greater portion of remaining CO 2 , a cryogenic separation step in a distillation column in order to separate O 2 and N 2 from the gas stream. And extraction of CH 4 -rich stream obtained at cryogenic separation stage. EFFECT: invention provides a gaseous stream enriched with methane, content of methane in which meets the needs of its use and to the extent possible limits exposure of methane (CH 4 ) emissions to atmosphere (strong greenhouse effect); also provides cleaning biogas from storage of non-hazardous wastes in order to obtain biomethane, which meets the requirements for pumping into a network of distribution of natural gas, or for local use as motor fuel. 14 cl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 721 698 C2 (51) МПК B01D 53/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01D 53/00 (2020.02) (21)(22) Заявка: 2018122940, 10.11.2016 (24) Дата начала отсчета срока действия патента: Дата регистрации: 21.05.2020 R U 10.11 ...

СПОСОБ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА

FIELD: machine building. SUBSTANCE: invention refers to gas liquefaction method with high methane content; it contains the stages at which gas flow is created; some portion of gas is extracted from the flow to be used as cooling agent; cooling agent is compressed; the obtained compressed cooling agent is cooled with cooling fluid medium having the ambient temperature; cooled compressed cooling agent is subject to additional cooling and expanded; cooling agent is supplied to heat exchange zone; gas flow is passed through the above heat exchange zone for cooling of at least some portion of gas by indirect heat exchange with expanded and additionally cooled cooling agent; thus forming the cooled fluid flow. As per the other versions, in order to improve the efficiency, in addition, auxiliary cooling can be performed after one or more other compression stages. EFFECT: use of invention will allow reducing the consumed power of gas liquefaction plant. 12 cl, 3 dwg, 4 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 458 296 (13) C2 (51) МПК F25J 1/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2009144777/06, 04.03.2008 (24) Дата начала отсчета срока действия патента: 04.03.2008 (73) Патентообладатель(и): ЭКСОНМОБИЛ АПСТРИМ РИСЕРЧ КОМПАНИ (US) R U Приоритет(ы): (30) Конвенционный приоритет: 03.05.2007 US 60/927,340 (72) Автор(ы): МИНТА Моузес (US) (43) Дата публикации заявки: 10.06.2011 Бюл. № 16 2 4 5 8 2 9 6 (45) Опубликовано: 10.08.2012 Бюл. № 22 (56) Список документов, цитированных в отчете о поиске: WO 2007/021351 А1, 22.02.2007. RU 2144649 С1, 20.01.2000. RU 2175099 С2, 20.10.2001. US 2005056051 A1, 17.03.2005. US 6023942 A, 15.02.2000. 2 4 5 8 2 9 6 R U (86) Заявка PCT: US 2008/002861 (04.03.2008) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 03.12.2009 (87) Публикация заявки РСТ: WO 2008/136884 (13.11.2008) Адрес для переписки: 129090, Москва, ул. Б.Спасская, 25, стр.3, ООО " ...

СПОСОБ СЖИЖЕНИЯ ГАЗА НА ШЕЛЬФЕ ИЛИ ПОБЕРЕЖЬЕ АРКТИЧЕСКИХ МОРЕЙ

FIELD: heating. SUBSTANCE: method is implemented on installation consisting of two contours, of which the first one is intended for gas decontamination, extraction of heavy hydrocarbons and nitrogen, and natural-gas liquefaction, the second one being a coolant flow contour wherein coolant flow, subsequent to compression and cooling, is divided into two streams in the ratio of 1:19 to 1:33 in a division unit. A bigger flow of coolant is directed to the heat exchanger for cooling, a smaller one being directed, through a throttle gate, to a stripping column cube. After that, the both coolant flows are subject to blending subsequent to pressure equalising. The method allows for reducing cost of natural gas liquefaction due to cooling of liquefied gas before and after its compression, and cooling of the coolant after its compression with cold water from the Arctic seas and inflowing rivers bays with water temperature not exceeding 277 K, and optimisation of coolant streams distribution. Also, the present method allows for reducing the amount of equipment needed and carrying out decontamination of natural gas supplied for liquefaction from mercury and its compounds. EFFECT: reduced power inputs; optimised coolant streams distribution; reduced amount of equipment needed; decontamination of natural gas supplied for liquefaction from mercury and its compounds. 2 cl, 1 dwg ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß RU (19) (11) 2 344 359 (13) C1 (51) ÌÏÊ F25J 1/00 (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÎÏÈÑÀÍÈÅ ÈÇÎÁÐÅÒÅÍÈß Ê ÏÀÒÅÍÒÓ (21), (22) Çà âêà: 2007125075/06, 04.07.2007 (24) Äàòà íà÷àëà îòñ÷åòà ñðîêà äåéñòâè ïàòåíòà: 04.07.2007 (45) Îïóáëèêîâàíî: 20.01.2009 Áþë. ¹ 2 Àäðåñ äë ïåðåïèñêè: 115583, Ìîñêâà, à/ 130, Îòäåë èíòåëëåêòóàëüíîé ñîáñòâåííîñòè ÎÎÎ "ÍÈÈ ïðèðîäíûõ ãàçîâ è ãàçîâûõ òåõíîëîãèéÂÍÈÈÃÀÇ" 2 3 4 4 3 5 9 äàâëåíèé â íèõ, ñìåøèâàþò. Ïðè ðåàëèçàöèè ñïîñîáà ñíèæàþòñ ýíåðãîçàòðàòû íà ñæèæåíèå ïðèðîäíîãî ãàçà çà ñ÷åò îõëàæäåíè ...

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

FIELD: chemistry. SUBSTANCE: present invention relates to a method of liquefying hydrogen. Proposed method comprises steps of cooling feed gas stream containing hydrogen at pressure of at least 1.5 MPa abs (15 bar abs) To temperature below critical temperature of hydrogen at stage of first cooling to produce liquid product flow. According to the invention, the flow of the supplied gas is cooled by means of a closed cycle of the first cooling with the flow of the first high-pressure coolant containing hydrogen, where the flow of the first high-pressure coolant is divided into two partial flows. First partial flow is expanded to low pressure thus obtaining cold for cooling of pre-cooled fed gas below critical pressure of hydrogen, and compressed to medium pressure. Second partial flow is expanded to near average pressure and directed to the first partial flow of medium pressure. EFFECT: technical result is higher efficiency and reduced capital costs. 15 cl, 3 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 718 378 C1 (51) МПК F25J 1/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК F25J 1/001 (2020.02); F25J 1/0042 (2020.02); F25J 1/005 (2020.02); F25J 1/0052 (2020.02); F25J 1/0055 (2020.02); F25J 1/0062 (2020.02); F25J 1/0065 (2020.02); F25J 1/0067 (2020.02); F25J 1/0072 (2020.02); F25J 1/0092 (2020.02); F25J 1/0095 (2020.02); F25J 1/0214 (2020.02); F25J 1/0215 (2020.02); F25J 1/0221 (2020.02); F25J 1/025 (2020.02); F25J 1/0259 (2020.02); F25J 1/0268 (2020.02); F25J 1/0279 (2020.02); F25J 1/0288 (2020.02); F25J 1/0291 (2020.02); F25J 1/0292 (2020.02); F25J 1/0294 (2020.02) 2018116437, 20.10.2016 (24) Дата начала отсчета срока действия патента: 20.10.2016 (73) Патентообладатель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЬШАФТ (DE) 02.04.2020 Приоритет(ы): (30) Конвенционный приоритет: 27.10.2015 EP 15003070.8 (45) Опубликовано: 02.04.2020 Бюл. № 10 C 1 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 28.05.2018 (86) ...

Способ получения жидкого осушенного диоксида углерода и устройство для его осуществления

Изобретение может быть использовано при производстве глубоко осушенного жидкого диоксида углерода (ДУ). ЦЕЛЬ ИЗОБРЕТЕНИЯ - СНИЖЕНИЕ ЭНЕРГОЗАТРАТ. УСТРОЙСТВО ДЛЯ ГЛУБОКОЙ ОСУШКИ ДУ выполнено в виде фильтра-осушител  13 и установлено на линии 11 выдачи продукта потребителю после запорного вентил  12. Накопительное устройство состоит из двух последовательно установленных изотермических емкостей 7 и 8, соединенных между собой линией 9 с запорным вентилем 10. Паровое пространство второй по ходу подачи продукта изотермической емкости 8 соединено дополнительной линией 20 с запорным вентилем 21 с одной из ступеней компрессора 1. Фильтр-осушитель 13 может быть соединен линией с запорным вентилем с выходом одной из ступеней компрессора перед теплообменником. Последовательно сжимают газообразный ДУ многоступенчатым компрессором 1 до давлени  не менее 6,5 МПа, в отделителе 3 отдел ют капельную влагу, в конденсаторе 4 конденсируют ДУ и охлаждают его при дросселировании. Накапливают сдросселированный жидкий ДУ в емкост х 7 и 8 и выдают продукт потребителю. Охлаждение при дросселировании осуществл ют в емкости 8 до т-ры не ниже 251 К и дополнительно отвод т в одну из ступеней компрессора 1 часть газовой фазы из емкости 8 дл  охлаждени  в последней жидкого ДУ до т-ры не выше 233 К, а на выходе из емкости 8 отдел ют образовавшиес  при охлаждении кристаллы льда дл  глубокой осушки. Отводима  часть газовой фазы перед подачей в компрессор 1 м.б. направлена на теплообмен с ДУ, подаваемымна дросселирование. Часть теплого газообразного ДУ после второй ступени компрессора 1 поступает в фильтр-осушитель 13, где очищаетс  ото льда без использовани  специального источника энергии. 2 с. и 2з.п.ф-лы, 1 ил. The invention can be used in the production of deeply dried liquid carbon dioxide (DU). OBJECTIVE OF THE INVENTION - REDUCED ENERGY CONSUMPTION. The DEVICE FOR DEEP DRYING DU is made in the form of filter drier 13 and is installed on line 11 to deliver the product to the consumer after the ...

Verfahren zum Kühlen eines Gases in einer Vorrichtung zur Nutzung von Luft und eine Vorrichtung zur Durchführung des Verfahrens.

Verfahren und Vorrichtung zur Verbesserung von Rückgewinnung von Kohlendioxyd

Carbon dioxide purification

A carbon dioxide (CO2) separation process wherein CO2 is separated from a gaseous feed stream 140 comprising CO2 and at least one other gas having a lower boiling point than CO2. The process comprises the steps of: (i) cooling and partially condensing (200A, 200B) the feed stream; (ii) passing the cooled and partially condensed feed stream to a vapour-liquid separator 210 to produce a vapour stream 215 having reduced CO2 content relative to the feed stream and a liquid stream 220 having increased CO2 content relative to the feed stream; and (iii) dividing the liquid stream from (ii) into at least two streams 240, 245; and (iv) expanding and heating at least one of the at least two liquid streams. The cooling in step (i) is provided at least in part by heat exchange during heating of the liquid stream. Advantageously the separation process uses heat integration techniques to improve the efficiency of the process and to minimise the power requirements for downstream compression.

Liquefaction of nitrogen in regasificaton of liquid methane

... 910,489. Liquefaction and revaporization of gases. CONCH INTERNATIONAL METHANE Ltd. March 29, 1961 [June 16, 1960], No. 11540/61. Class 8(2). Liquefaction of gaseous nitrogen entering the system at atmospheric pressure, through a line 14, Fig. 1, is effected by cooling in a heat exchanger 7 traversed by pressurized liquid methane issuing from a pump 4 and which is thereby vaporized, compressing the so-cooled nitrogen gas at 15 and condensing it in an exchanger 13 cooled by feed liquid methane at atmospheric pressure; the resulting compressed methane gas leaving exchanger 7 being warmed in an exchanger 9 and expanded in a turbine 10 which provides a source of power to drive the pump 4 and compressor 15. As shown the nitrogen issuing from compressor 15 is further compressed at 18 before passing to the condenser 13, the heat of compression being removed by liquid methane exchangers 5, 6. Also turbine 10 discharges through an exchanger 11 traversed by waste hot water before final expansion ...

GAS SUPPLY SYSTEMS FOR GAS ENGINES

PROCEDURE AND DEVICE FOR THE BACK LIQUEFACTION OF A GAS FLOW

Power generating system and corresponding method

The present disclosure provides an integrated power generating system and method and liquefied natural gas (LNG) vaporization system and method. More particularly, heat from a CO ...

Process and apparatus for separating a gas rich in carbon dioxide by distillation

In a process for separating a gas rich in carbon dioxide by distillation, the gas rich in carbon dioxide is cooled in a heat exchanger (3) and is sent to a distillation column (5), a gas (6) depleted in carbon dioxide is withdrawn from the top of the column and a liquid (7) enriched in carbon dioxide is withdrawn from the bottom of the column, a gas enriched in carbon dioxide is compressed in a compressor (17) down to a first pressure and at least one portion of the gas enriched in carbon dioxide originating from the compressor is expanded from the first pressure to a second pressure lower than the first pressure, for example the pressure of the column, and the expanded gas is used to heat the bottom of the column.

SYSTEM AND METHOD FOR POWER STORAGE AND RELEASE

Systems and methods for storing and releasing energy comprise directing inlet air into a vertical cold flue assembly, cooling the air and removing a portion of moisture. The air is directed out of the cold flue assembly and compressed. The remaining moisture is substantially removed. The air is cooled in a main heat exchanger such that it is substantially liquefied using refrigerant loop air. The substantially liquefied air is directed to a storage apparatus. In energy release mode, working loop air warms the released liquid air such that the released liquid air is substantially vaporized, and the released liquid air cools the working loop air such that the working loop air is substantially liquefied. The substantially vaporized air is directed to a combustion chamber and combusted with a fuel stream. A portion of expanded combustion gas may be used to heat and substantially vaporize the released liquid air.

NATURAL GAS LIQUEFACTION PROCESS

The invention relates to a process for liquefying a gas stream rich in me thane, said process comprising: (a) providing said gas stream; (b) withdrawi ng a portion of said gas stream for use as a refrigerant; (c) compressing sa id refrigerant; (d) cooling said compressed refrigerant with an ambient temp erature cooling fluid; (e) subjecting the cooled, compressed refrigerant to supplemental cooling; (f) expanding the refrigerant of (e) to further cool s aid refrigerant, thereby producing an expanded, supplementally cooled refrig erant; (g) passing said expanded, supplementalIy cooled refrigerant to a hea t exchange area; and, (h) passing said gas stream of (a) through said heat e xchange area to cool at least part of said gas stream by indirect heat excha nge with said expanded, supplementally cooled refrigerant, thereby forming a cooled gas stream. In further embodiments for improved efficiencies, additi onal supplemental cooling may be provided after one or more other compressio n steps ...

SYSTEM AND METHOD FOR LIQUID AIR PRODUCTION, POWER STORAGE AND POWER RELEASE

Systems and methods for storing and releasing energy comprising directing inlet air into a vertical cold flue assembly, a portion of moisture being removed from the air within the cold flue assembly. The air is directed out of the cold flue assembly and compressed. The remaining moisture is substantially removed and the carbon dioxide is removed from the air by adsorption. The air is cooled in a main heat exchanger such that it is substantially liquefied using refrigerant loop air. The substantially liquefied air is directed to a storage apparatus. The refrigerant loop air is cooled by a mechanical chiller and by a plurality of refrigerant loop air expanders. In energy release mode, working loop fluid warms the released liquid air such that the released liquid air is substantially vaporized, and the released liquid air cools the working loop fluid such that the working loop fluid is substantially liquefied. A portion of the released liquid air is directed to the at least one generator and ...

PROCESS FOR COMPRESSING A GAS ASSOCIATED WITH A UNIT FOR SEPARATING A GAS MIXTURE

In a process for compressing a gas, associated with a unit (5) for separating a gas mixture, the compressor (1, 2, 7) comprises a number of stages less than that which would be necessary to produce an optimal compressor of the isothermal type compressing the same flow rate of the said gas to the same pressure. The compressor may compress the gas mixture to be separated or a product of the separation.

Liquefaction of neon with turboexpander

Neon is liquified under medium pressure by cooling it through indirect heat exchange with liquid nitrogen after which it is divided into a minor portion which is turboexpanded and used as the basic cold source to cool the remainder of the medium pressure neon, which latter is finally throttle expanded to effect liquefaction. The use of a turbo expander for the liquefaction of neon is more advantageous than the use of hydrogen and helium, as in the first case the sound velocity is small, which offers the possibility to realise the cycle with isentropic expansion of the gas without the known shortcoming inherent to ram expansion mechanics.

LIQUEFACTION OF INDUSTRIAL AND HYDROCARBON GAS

Method and device for condensing a carbon dioxide-rich gas stream

COMPRESSOR OF GAS, APPARATUS OF SEPARATION Of a GAS MIXTURE INCORPORATING SUCH a COMPRESSOR AND PROCESS OF SEPARATION Of a GAS MIXTURE INCORPORATING SUCH a COMPRESSOR

APPARATUS AND METHOD FOR COMPRESSING AND/OR COOLING AS WELL AS PURIFICATION OF A GAS RICH IN CARBON DIOXIDE CONTAINING WATER

Carbon dioxide separating method for iron and steel industry, involves receiving flow enriched in carbon dioxide from absorption unit, sending it towards homogenization unit and subjecting carbon dioxide to intermediate compression stage

The method involves receiving a flow enriched in carbon dioxide (6) from an absorption unit (3) containing 40 to 95 percentage of carbon dioxide. The carbon dioxide is sent towards a gas homogenization unit (17) for attenuating a cyclic variation of pressure, flow and/or gas composition and is subjected to an intermediate compression stage (7) before the entry of the carbon dioxide in a cryogenic unit (9). An independent claim is also included for an integrated installation for the production of carbon dioxide from a gas supply containing carbon dioxide.

POWER GENERATING SYSTEM AND CORRESPONDING METHOD

Sätt och system för återvinning av värme från gaskomprimering

METHOD AND DEVICE FOR GENERATING TWO PURIFIED PARTIAL AIR STREAMS

The invention relates to a method and device for generating two purified partial air streams under different pressures. A total air stream (1) is compressed to a first total air pressure. The compressed total air stream (5) is cooled with cooling water under the first total air pressure by way of heat exchange (4, 6). The heat exchange with cooling water for cooling the total air stream (5) is carried out as a direct heat exchange in a first direct contact cooler (6), at least in part. The cooled total air stream (9) is divided into a first partial air stream (10) and a second partial air stream (11). The first partial air stream (10) is purified in a first purification device (18) under the first total air pressure, generating the first purified partial air stream (19). The second partial air stream (11) is re-compressed to a higher pressure (12), which is higher than the first total air pressure. The re-compressed second partial air stream (14) is cooled with cooling water in a second ...

Method and apparatus for reliquefying natural gas

Natural gas boiling off from LNG storage tanks located on board a sea-going vessel, is compressed in a plural stage compressor. At least part of the flow of compressed natural gas is sent to a liquefier operating on a Brayton cycle in order to be reliquefied. The temperature of the compressed natural gas from the final stage is reduced to below 0° C. by passage through a heat exchanger. The first compression stage is operated as a cold compressor and the resulting cold compressed natural gas is employed in the heat exchanger to effect the necessary cooling of the flow from the compression stage. Downstream of its passage through the heat exchanger the cold compressed natural gas flows through the remaining stages of the compressor. If desired, a part of the compressed natural gas may be supplied to the engines of the sea-going vessel as a fuel.

METHOD OF COOLING BOIL OFF GAS AND AN APPARATUS THEREFOR

The disclosure relates to a method and apparatus for cooling, preferably liquefying a boil off gas (BOG) stream from a liquefied cargo in a floating transportation vessel, said liquefied cargo having a boiling point of greater than −110° C. at 1 atmosphere and comprising a plurality of components, said method comprising at least the steps of: compressing a boil off gas stream ( 01 ) from said liquefied cargo in two or more stages of compression comprising at least a first stage ( 65 ) and a final stage ( 75 ) to provide a compressed BOG discharge stream ( 06 ), wherein said first stage ( 65 ) of compression has a first stage discharge pressure and said final stage ( 75 ) of compression has a final stage suction pressure and one or more intermediate, optionally cooled, compressed BOG streams ( 02, 03, 04 ) are provided between consecutive stages of compression; cooling the compressed BOG discharge stream ( 06 ) to provide a cooled vent stream ( 51 ) and a cooled compressed BOG stream ( 08 ); expanding, optionally after further cooling, a portion of the cooled compressed BOG stream ( 08 ) to a pressure between that of the first stage discharge pressure and the final stage suction pressure to provide an expanded cooled BOG stream ( 33 ); heat exchanging the expanded cooled BOG stream ( 33 ) against the cooled vent stream ( 51 ) to provide a further cooled vent stream ( 53 ).

METHOD AN APPARATUS FOR SUPPLYING A COMBUSTION CHAMBER WITH NITROGEN

Carbon dioxide production system with integral vent gas condenser

СПОСОБ ОЖИЖЕНИЯ ДИОКСИДА УГЛЕРОДА

FIELD: heating systems, drying. SUBSTANCE: carbon dioxide liquefying method involves its compression in two-stage compressor and pump compression, moisture separation, drying and cooling. Liquefaction and supercooling of carbon dioxide leaving the second stage of compressor is performed in double-section condenser-supercooler due to cold of low pressure liquid ammonia supplied to the left section of condenser-supercooler, and due to heat consumed for gasification of carbon dioxide in the right section of condenser-supercooler, to which liquid low-temperature carbon dioxide is pumped from liquid nitrogen tank under pressure of 15 MPa. EFFECT: reducing energy consumption for carbon dioxide liquefaction. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 376 537 (13) C1 (51) МПК F25J 1/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21), (22) Заявка: 2008137902/06, 22.09.2008 (24) Дата начала отсчета срока действия патента: 22.09.2008 (45) Опубликовано: 20.12.2009 Бюл. № 35 (73) Патентообладатель(и): ОАО "Тольяттиазот" (RU) подаваемого в левую секцию конденсатора-переохладителя, и затрат тепла на газификацию диоксида углерода в правой секции конденсатора-переохладителя, в которую жидкий низкотемпературный диоксид углерода перекачивается насосом из изотермической емкости под давлением 15 МПа. Достигаемый технический результат снижение энергозатрат на ожижение диоксида углерода. 1 ил. R U 2 3 7 6 5 3 7 (57) Реферат: Способ ожижения диоксида углерода включает его компримирование в двухступенчатом компрессоре и сжатие в насосе, влагоотделение, осушку и охлаждение. Ожижение и переохлаждение выходящего из второй ступени компрессора диоксида углерода производится в двухсекционном конденсаторе-переохладителе за счет холода жидкого аммиака низкого давления, Ñòð.: 1 ru C 1 C 1 (54) СПОСОБ ОЖИЖЕНИЯ ДИОКСИДА УГЛЕРОДА 2 3 7 6 5 3 7 Адрес для переписки: 445653, Самарская обл., г. Тольятти, Поволжское ш., 32, ...

СПОСОБ И УСТРОЙСТВО ДЛЯ СЖИЖЕНИЯ ТОПОЧНОГО ГАЗА ОТ СЖИГАТЕЛЬНЫХ УСТАНОВОК

1. Способ производства жидкого COиз газообразных продуктов сгорания, в котором топочный газ (3) сжимают в первом компрессоре (1), затем охлаждают в первом охладителе (5) и частично конденсируют по меньшей мере на двух ступенях (9, 21) разделения, где по меньшей мере две ступени (9, 21) разделения охлаждают расширяющимся отходящим газом (23) и расширяющимся жидким CO(3.1, 3.3) и где первый охладитель (5) питают охлажденной водой с первой ступени разделения (см. фиг.1).2. Способ по п.1, отличающийся тем, что первая ступень (9) разделения включает первый теплообменник (11) и первый барабанный сепаратор (13), и в котором первый теплообменник (11) охлаждают расширяющимся CO(3.1) из первого барабанного сепаратора (13).3. Способ по п.1, отличающийся тем, что вторая ступень (21) разделения включает второй теплообменник (17) и второй барабанный сепаратор (19), и в котором второй теплообменник (17) охлаждают расширяющимся CO(3.3) из второго барабанного сепаратора (19) (см. фиг.1).4. Способ по п.1, отличающийся тем, что вторая ступень (21) разделения включает второй теплообменник (17) и стриппер (37) CO, что поток жидкого CO(3.5) из первой ступени (9) разделения поступает в стриппер (37) COнепосредственно, и что поток (3.2) COиз первой ступени (9) разделения поступает в стриппер (37) COчерез второй теплообменник (17) (см. фиг.2).5. Способ по п.1, отличающийся тем, что жидкий COрасширяется до первого уровня давления (указатель 12) и до второго уровня давления (указатель 11) и поступает в первую или вторую ступень второго компрессора (25) после прохождения по меньшей мере одной из ступеней разделения (9, 21) (см. фиг.1-5).6. Способ по п.1, отличающийся тем, что топочный газ сжимают в первом компрессоре (1), охлаждают в перв� РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК F25J 3/06 (11) (13) 2012 149 433 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2012149433/06, 19.04.2011 (71) Заявитель(и): АЛЬСТОМ ТЕКНОЛОДЖИ ЛТД (CH) ...

Verfahren und Vorrichtung zur Verbesserung von Rückgewinnung von Kohlendioxyd

Method for recovering energy of liquefaction expended in decomposing air after liquefaction

In this method, the individual constituents of air are obtained in liquid form and subsequently further processed in gaseous form. The cold content of at least one of the liquid air constituents is output again to air for its liquefaction. This cold content is preferably given off to the air to be liquefied at the site of the reuse of the said liquid air constituent, without applying a refrigerating (cooling, cold producing) machine. The liquid air obtained is preferably returned into the air separation plant.

VERFAHREN ZUR RUECKGEWINNUNG VON BEI DER LUFTZERLEGUNG NACH VERFLUESSIGUNG AUFGEWENDETER VERFLUESSIGUNGSENERGIE

INTEGRATED PROCEDURE AND INTEGRATED PLANT FOR THE CRYOGENIC ADSORPTION AND SEPARATION FOR THE PRODUCTION OF CO2

SYSTEM FOR THE COLD COMPRESSION OF AN AIR FLOW WITH COOLING BY NATURAL GAS

PROCEDURE AND DEVICE FOR THE COMPRESSION OF GASES.

INTEGRATED LIQUID AIR SEPARATION AND KRAFTANLAGE

APPARATUS FOR COMPRESSING GAS

System and method for liquid air production, power storage and power release

Systems and methods for storing and releasing energy comprising directing inlet air into a vertical cold flue assembly, a portion of moisture being removed from the air within the cold flue assembly. The air is directed out of the cold flue assembly and compressed. The remaining moisture is substantially removed and the carbon dioxide is removed from the air by adsorption. The air is cooled in a main heat exchanger such that it is substantially liquefied using refrigerant loop air. The substantially liquefied air is directed to a storage apparatus. The refrigerant loop air is cooled by a mechanical chiller and by a plurality of refrigerant loop air expanders. In energy release mode, working loop fluid warms the released liquid air such that the released liquid air is substantially vaporized, and the released liquid air cools the working loop fluid such that the working loop fluid is substantially liquefied. A portion of the released liquid air is directed to the at least one generator and ...

Method and installation for liquefying flue gas from combustion installations

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 - ...

Method and system for the small-scale production of liquified natural gas (LNG) from low-pressure gas

A system for the production of LNG from low-pressure feed gas sources, at small production scales and at lower energy input costs. A system for the small-scale production of cold compressed natural gas (CCNG). A method of dispensing natural gas from stored CCNG, comprising: dispensing CCNG from a CCNG storage tank; pumping the CCNG by a cryogenic liquid pump to a pressure suitable for compressed natural gas dispensing and storage in on vehicle compressed natural gas storage tanks; recovering cold from the CCNG by heat exchange with natural gas feeding the natural gas production plant to replace dispensed product. A system for the storage, transport, and dispensing of natural gas, comprising: means for handling natural gas in a CCNG state where the natural gas is a non-liquid, but is dense-enough to allow for pumping to pressure by a cryogenic liquid pump. C:2a :\C17 cIcx -'- 4 0 c C-4~e O ccswW0 3MIS- Oj Ifl~qX ~O 3 ...

Method and device for oxygen production by low-temperature separation of air at variable energy consumption

The method and the device serve to produce oxygen by the low-temperature separation of air at variable energy consumption. A distillation column system comprises a high-pressure column (34), a low-pressure column (35) and a main condenser (36), a secondary condenser (26) and a supplementary condenser (37). Gaseous nitrogen (41, 42) from the high-pressure column (34) is liquefied in the main condenser (36) in indirect heat exchange with an intermediate liquid (43) from the low-pressure column (35). A first liquid oxygen stream (70) from the bottom of the low-pressure column (35) is evaporated in the secondary condenser (26) in indirect heat exchange with feed air (25b) to obtain a gaseous oxygen product (72). The supplementary condenser serves as a bottom heating device for the low-pressure column (35) and is heated by means of a first nitrogen stream (44) from the distillation column system, which nitrogen stream was compressed previously in a cold compressor (45). In a second operating ...

SYSTEM AND METHOD FOR POWER STORAGE AND RELEASE

Systems and methods for storing and releasing energy comprise directing inlet air into a vertical cold flue assembly, cooling the air and removing a portion of moisture. The air is directed out of the cold flue assembly and compressed. The remaining moisture is substantially removed. The air is cooled in a main heat exchanger such that it is substantially liquefied using refrigerant loop air. The substantially liquefied air is directed to a storage apparatus. In energy release mode, working loop air warms the released liquid air such that the released liquid air is substantially vaporized, and the released liquid air cools the working loop air such that the working loop air is substantially liquefied. The substantially vaporized air is directed to a combustion chamber and combusted with a fuel stream. A portion of expanded combustion gas may be used to heat and substantially vaporize the released liquid air.

ALKALINITY CONTROL AGENT SUPPLY METHOD AND APPARATUS FOR COMPRESSOR IMPURITY SEPARATION MECHANISM

Exhaust gas (2), which has been pressurized and cooled by a compressor impurity separation mechanism (100) and had impurities removed, is further cooled by a refrigerator-type heat exchanger (9). Condensation (D4) caused by the cooling in the refrigerator-type heat exchanger (9) is ejected, and the condensation (D4) is supplied to the upstream side of an after-cooler (5a) of at least the foremost stage of an impurity separation device (6a) as an alkalinity control agent (10).

POWER GENERATING SYSTEM AND CORRESPONDING METHOD

The present disclosure provides an integrated power generating system and method and liquefied natural gas (LNG) vaporization system and method. More particularly, heat from a CO2 containing stream (15) from the power generating system and method can be used to heat (21) the LNG for re-gasification (44) as gaseous CO2 from CO2 containing stream is liquefied (55). The liquefied CO2 can be captured and/or recycled back to a combustor (1) in the power generating system and method.

AIR COMPRESSION SYSTEM AND METHOD

An air compression system and method for an air separation plant in which air is compressed in a series of compression stages and a temperature swing adsorption unit adsorbs water vapor and carbon dioxide. The temperature swing adsorption unit is situated at a location of the compression stages such that air pressure upon entry into the adsorbent beds is between about 400 psia and about 600 psia. Each of the adsorbent beds of the unit have a minimum transverse cross-sectional flow area that will set the air velocity of the air to a level below that at which adsorbent bed fluidization would occur. Such operation allows fabrication costs of the adsorbent beds to be reduced because less adsorbent and smaller adsorbent beds are required while power consumption will be at a minimum.

DEVICE FOR COMPRESSING A GASEOUS MEDIUM AND SYSTEMS COMPRISING SUCH DEVICE

The invention relates to a device for compressing a gaseous medium, comprising a compressor unit provided with a medium inlet, an outlet for the compressed medium and with means for the atomising of a liquid evaporation agent in the medium, characterised in that the atomising means comprise at least one flash atomisation unit, arranged and mounted such that the atomised evaporation agent fragmentises by means of the formation of gas in the atomised evaporation agent, to systems for generating energy and for separating gasses, which are provided with such a compression device.

СПОСОБ И УСТАНОВКА ДЛЯ СЖИЖЕНИЯ ДИОКСИДА УГЛЕРОДА

Установка для сжижения диоксида углерода, включающая проточный канал для прохода диоксида углерода от входного отверстия к выходному отверстию. Канал включает множество компрессоров (2, 5, 8) и охлаждающих устройств (4, 7, 9, 10,13), расположенных последовательно, расширительную камеру (14, 15) в указанном проточном канале, причем камера расположена ниже по потоку от конечного компрессора (8) и охлаждающего устройства (9, 10, 13). Установка также включает канал (16) рециркуляции, размещенный для возврата газообразного диоксида углерода из указанной расширительной камеры (15) в указанный проточный канал (3) выше по потоку от указанного конечного компрессора (8) и охлаждающего устройства (9, 10, 13).

CRYOGENIC METHOD AND SYSTEM OF AIR SEPARATION

METHOD OF STEP COMPRESSION OF GAS

СПОСОБ И УСТАНОВКА ДЛЯ СЖИЖЕНИЯ ДИОКСИДА УГЛЕРОДА

Установка для сжижения диоксида углерода, включающая проточный канал для прохода диоксида углерода от входного отверстия к выходному отверстию. Канал включает множество компрессоров (2, 5, 8) и охлаждающих устройств (4, 7, 9, 10, 13), расположенных последовательно, расширительную камеру (14, 15) в указанном проточном канале, причем камера расположена ниже по потоку от конечного компрессора (8) и охлаждающего устройства (9, 10, 13). Установка также включает канал (16) рециркуляции, размещенный для возврата газообразного диоксида углерода из указанной расширительной камеры (15) в указанный проточный канал (3) выше по потоку от указанного конечного компрессора (8) и охлаждающего устройства (9, 10, 13).

Food grade liquid carbon dioxide product in the production method for the reduction of carbon dioxide emissions

SEPARATION OF AIR AND LIQUEFACTION OF ITS COMPONENTS

Proceeded of liquid production of nitrogen and liquid methane gasification

Method and installation for air distillation.

DEVICE FOR SEPARATING A WASTE GAS OF A BOILER OXY-COMBUSTION

Un appareil de séparation d'un gaz résiduaire d'une chaudière à oxycombustion contenant du dioxyde de carbone, du mercure et de la vapeur d'eau comprend un compresseur pour comprimer le gaz résiduaire, des moyens pour récupérer de l'eau condensée du compresseur, des moyens pour envoyer le gaz résiduaire comprimé à un appareil de séparation à basse température par condensation partielle et/ou par distillation, des moyens pour sortir un fluide enrichi en dioxyde de carbone de l'appareil de séparation, des moyens pour sortir un débit de purge contenant du mercure de l'appareil de séparation.

COMPRESSION CIRCUIT OF A GASEOUS FLUID AT LOW PRESSURE AND LOW TEMPERATURE.

Process and together of compression of a gas

L'eau de refroidissement de l'appareil de compression (1) est réfrigérée par un appareil (18) de réfrigération à l'air. De l'eau d'appoint plus fraîche que l'eau traitée par cet appareil passe d'abord dans un échangeur de chaleur (8) monté sur la conduite de refoulement de l'appareil de compression, puis alimente l'appareil de réfrigération (18). Application aux installations de distillation d'air. The cooling water of the compression apparatus (1) is cooled by an air-cooled apparatus (18). Make-up water cooler than the water treated by this device first passes through a heat exchanger (8) mounted on the discharge line of the compression device, then feeds the refrigeration device ( 18). Application to air distillation installations.

Process of obtaining pure oxygen and installation for its implementation

Humid air flow compressing method for separating air by cryogenic distillation, involves sending part of condensed water to upstream of compression stage, where water partially enters stage at liquid state and is partly vaporized in stage

PROCESS AND APPARATUS OF SEPARATION Of a GAS RICH IN CARBON DIOXIDE BY DISTILLATION

Dans un procédé de séparation d'un gaz riche en dioxyde de carbone par distillation, on refroidit le gaz riche en dioxyde de carbone dans un échangeur de chaleur (3) et on l'envoie dans une colonne de distillation (5), on soutire un gaz (6) appauvri en dioxyde de carbone de la tête de la colonne et un liquide (7) enrichi en dioxyde de carbone de la cuve de la colonne, on comprime un gaz enrichi en dioxyde de carbone dans un compresseur (17) jusqu'à une première pression et on détend au moins une partie du gaz enrichi en dioxyde de carbone provenant du compresseur depuis à la première pression jusqu'à une deuxième pression plus basse que la première pression, par exemple la pression de la colonne, et on utilise le gaz détendu pour chauffer la cuve de la colonne.

PROCESS AND APPARATUS OF REHEATING OF NITROGEN INTEND TO REGENERATE a UNIT Of ADSORPTION Of a UNIT OF SEPARATION Of AIR

Dans un procédé de réchauffage de l'azote destiné à régénérer une unité d'adsorption (13) d'une unité de séparation d'air, de l'air destiné à une unité de séparation d'air (11) est comprimé dans un compresseur (C1, C2, C3) produisant un débit d'air comprimé réchauffé, le débit d'air comprimé réchauffé chauffe un fluide dans un circuit fermé pour produire un fluide réchauffé et de l'air comprimé refroidi, l'air comprimé refroidi est envoyé à l'unité d'adsorption pour être épuré en eau et en dioxyde de carbone et l'air épuré est envoyé à l'unité de séparation d'air, le fluide réchauffé réchauffe de l'azote gazeux (15) provenant de l'unité de séparation d'air pour produire de l'azote réchauffé (16), et pour refroidir le fluide (21) produisant un fluide refroidi, le fluide refroidi étant de nouveau réchauffé contre le débit d'air comprimé et l'azote réchauffé est envoyé à l'unité d'épuration pour la régénérer, le fluide du circuit fermé est vaporisé par échange de chaleur indirect avec le débit ...

Air separation method for producing pure oxygen, involves cooling air at pressure to form reheated nitrogen, sending cooled air to gas turbine to form released nitrogen flow, and sending air to thermokinetic compressor

Dans un procédé de séparation d'air dans lequel au moins un débit d'air est comprimé dans un compresseur adiabatique (11) à une première pression est refroidi dans un premier échangeur (15) à la première pression, une partie de l'air à la première pression est envoyée à la distillation, une autre partie de l'air (16) à la première pression est surpressée à une deuxième pression dans un surpresseur adiabatique (18), refroidie dans le premier échangeur et séparé par distillation cryogénique pour former un débit d'oxygène (25) et un débit d'azote (23) dans lequel le débit riche en azote se réchauffe dans le premier échangeur où se refroidit l'air à la première pression pour former un débit d'azote réchauffé, détendu dans une turbine (27) pour former un débit d'azote détendu, réchauffé dans le premier échangeur et envoyé à un compresseur thermocinétique (29).

METHOD AND RECOVERY UNIT CONDENSATE WATER FROM AN AIR COMPRESSOR

Dans un procédé de récupération de condensat d'eau d'au moins un compresseur d'air (C), de l'air contenant de l'eau est comprimé dans l'au moins un compresseur jusqu'à une pression supérieure à 4 barg,, de l'eau condensée (1,3) est récupérée du compresseur, traitée et envoyée alimenter au moins une chaudière (AB) produisant de la vapeur d'eau (9), comme eau d'appoint, au moins une partie de la vapeur d'eau produite par la ou les chaudières est envoyée à au moins une turbine à vapeur (ST) qui entraîne le ou au moins un des compresseur(s) et au moins une partie de l'air comprimé dans au moins un des compresseurs est envoyée à au moins un appareil de séparation d'air (ASU) par distillation cryogénique comme gaz d'alimentation.

Method for carbon dioxide recovery from a feed stream

본 발명은 저농도의 CO 2 를 함유하는 유입 저온 공급 스트림으로부터 CO 2 를 회수하는 방법에 관한 것이며, 이 방법은 다음의 단계들을 포함한다. 유입 공급 스트림은 열교환기를 통과하여 유입 공급 스트림의 압축된 흐름에 대하여 압축된 흐름을 냉각한다. 압축된 흐름은 추가로 냉각되어 고압으로 압축되고, 증류 칼럼으로 공급되어 여기서 CO 2 를 함유하는 배기 가스 및 고순도의 바닥물 액체 CO 2 로 전환된다. 바닥물 액체 CO 2 의 제 1 부분은 팽창되어 제 1 냉각된 액체 CO 2 냉매 흐름을 형성하고, 이는 배기 가스에 대하여 증발하여 이로부터 응축된 CO 2 를 회수한다. 그 다음에 응축된 CO 2 는 증류 칼럼 내로 재유입된다. 바닥물 액체 CO 2 의 제 2 부분은 팽창되어 제 2 냉각된 액체 CO 2 냉매 흐름을 형성하고, 이는 이후 CO 2 생성물을 과냉각시키는데 사용된다. The present invention relates to a method for recovering CO 2 from an inlet cold feed stream containing low concentrations of CO 2 , which method comprises the following steps. The inlet feed stream passes through a heat exchanger to cool the compressed stream against the compressed stream of the inlet feed stream. The compressed stream is further cooled, compressed to high pressure, and fed to a distillation column where it is converted to exhaust gas containing CO 2 and high purity bottoms liquid CO 2 . The first portion of the bottoms liquid CO 2 is expanded to form a first cooled liquid CO 2 refrigerant stream, which evaporates to the exhaust gas to recover condensed CO 2 therefrom. The condensed CO 2 is then reintroduced into the distillation column. The second portion of the bottoms liquid CO 2 expands to form a second cooled liquid CO 2 refrigerant stream, which is then used to supercool the CO 2 product.

Método para a redução do consumo de energia em um processo de refrigeração e/ou liquefação

INSTALACAO E PROCESSO PARA A SEPARACAO DE AR PARA RECUPERACAO DE OXIGENIO LIQUIDO E NITROGENIO LIQUIDO

Integrated energy recovery system

The present invention relates to the recovery of heat energy, e.g., the heat of compression, from the production of pressurized gases, in particular nitrogen (N2), but also other gases such as compressed dry air. This invention is directed to a system and method for increasing the efficiency in use of energy by recovering energy normally wasted in one device and using the energy in another device needing the energy. In particular, this invention is directed to recovering the heat of compression from a gas generation plant to warm cooling water that is also used as feed water to an ultra pure water generation plant.

CRYOGENIC AIR SEPARATION METHOD AND SYSTEM

The present invention relates to a cryogenic air separation process that provides high pressure oxygen for an oxy-fired combustion of a fuel (e.g., a carbonaceous fuel). The air separation process can be directly integrated into a closed cycle power production process utilizing a working fluid, such as CO2. Beneficially, the air separation process can eliminate the need for inter-cooling between air compression stages and rather provide for recycling the adiabatic heat of compression into a process step in a further methods wherein an additional heat supply is beneficial.

METHOD OF TREATING A HYDROCARBON STREAM COMPRISING METHANE, AND AN APPARATUS THEREFOR

A wet hydrocarbon stream (510) comprising at least methane and water is dried thereby forming an effluent stream (560) and a wet disposal stream (590). Before drying the wet hydrocarbon stream (510) is cooled by indirectly heat exchanging against the effluent stream (560) followed by indirectly heat exchanging against an auxiliary refrigerant stream (250). The effluent stream (560) is subsequently passed to a further heat exchanger (535) where the effluent stream (560) is cooled against an evaporating refrigerant stream which is subsequently discharged from the further heat exchanger (535) as a spent refrigerant stream (240). A refrigerant stream in compressed condition is formed by compressing the spent refrigerant (240) and the auxiliary refrigerant stream that is discharged from the indirectly heat exchanging with the wet hydrocarbon stream (510), whereby allowing direct heat exchanging between the discharged auxiliary refrigerant stream (265) and the spent refrigerant stream (240) before ...

System and method for liquid air production, power storage and power release

Systems and methods for releasing and replacing stored energy comprise capturing inlet air from the ambient environment so the inlet air flows in a first general direction. Released liquid air flows in a second general direction, the second general direction being substantially opposite to the first general direction. The released liquid air is pumped to pressure, and the released liquid air and inlet air flow past each other such that heat exchange occurs. The inlet air warms the released liquid air such that the released liquid air is substantially vaporized, and the released liquid air cools the inlet air. Moisture and carbon dioxide are removed from the inlet air, and the inlet air is compressed and cooled such that the inlet air is substantially liquefied. The substantially liquefied air replaces a portion of the released liquid air; and the substantially vaporized released liquid air is combusted with fuel to produce electricity.

Process for regeneration of adsorbers

Adsorbers are loaded with impurities removed from a compressed gas stream and are regenerated by a gas heated by the heat of compression of the gas stream. A heat reservoir or accumulator is employed instead of a conventional shell and tube type heat exchanger.

System and method for liquid air production, power storage and power release

Systems and methods for storing and releasing energy comprising directing inlet air into a vertical cold flue assembly, a portion of moisture being removed from the air within the cold flue assembly. The air is directed out of the cold flue assembly and compressed. The remaining moisture is substantially removed and the carbon dioxide is removed from the air by adsorption. The air is cooled in a main heat exchanger such that it is substantially liquefied using refrigerant loop air. The substantially liquefied air is directed to a storage apparatus. The refrigerant loop air is cooled by a mechanical chiller and by a plurality of refrigerant loop air expanders. In energy release mode, working loop fluid warms the released liquid air such that the released liquid air is substantially vaporized, and the released liquid air cools the working loop fluid such that the working loop fluid is substantially liquefied. A portion of the released liquid air is directed to the at least one generator and ...

METHOD AND APPARATUS FOR PRODUCING HIGH-PRESSURE NITROGEN

A method for producing a high-pressure gas from an air separation unit including the steps of introducing a cold air feed into a distillation column system (20) under conditions effective for separating the cold air feed into a first air gas (22) and a second air gas; withdrawing the first and second air gases from the distillation column system and warming said first and second air gases in a main heat exchanger (10), wherein the first air gas is withdrawn from the distillation column system at a medium pressure; splitting the first air gas into a first fraction (24) and a second fraction (26); expanding the first fraction in a turbine (30); and compressing the second fraction in a booster (40) to a pressure that is higher than the medium pressure, wherein the booster is powered by the turbine ...

СПОСОБ РЕКУПЕРАЦИИ ЭНЕРГИИ

... 1. Способ рекуперации энергии при сжатии газа компрессорной установкой (1), имеющей две или более ступеней сжатия, каждая из которых образована компрессором (2, 3), при этом по потоку после каждого из, по меньшей мере, двух указанных компрессоров расположен теплообменник (4, 5) с первой и второй частями, причем через первую часть направляют сжатый газ из ступени сжатия, расположенной по потоку перед теплообменником, а через вторую часть направляют охлаждающий агент, чтобы извлечь часть теплоты сжатия из сжатого газа, при этом охлаждающий агент последовательно направляют через вторую часть, по меньшей мере, двух теплообменников (4, 5), причем последовательность, в соответствии с которой охлаждающий агент направляют через теплообменники (4, 5), выбирают таким образом, чтобы температура на входе в первую часть, по меньшей мере, одного последующего теплообменника была выше или равна температуре на входе в первую часть предшествующего теплообменника, при рассмотрении в направлении потока охлаждающего ...

СПОСОБ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА

... 1. Способ сжижения потока газа с высоким содержанием метана, содержащий этапы, при которых: ! (а) создают поток газа с абсолютным давлением менее 1200 фунтов на кв. дюйм (8273,709 кПа); ! (b) отбирают часть газа из потока для использования в качестве хладагента; ! (с) сжимают этот хладагент до давления, превышающего его давление на этапе (а) для получения сжатого хладагента; ! (d) охлаждают полученный сжатый хладагент косвенным теплообменом с охлаждающей текучей средой, имеющей температуру окружающей среды, до технологической температуры выше приблизительно 35°F (1,7°С); ! (е) подвергают охлажденный сжатый хладагент дополнительному охлаждению для дополнительного понижения его температуры, тем самым получая дополнительно охлажденный сжатый хладагент, имеющий температуру на 10-70°F (6-39°С) ниже, чем технологическая температура, получая дополнительно охлажденный, сжатый хладагент, имеющий температуру 10-60°F (6-15,6°С); ! (f) расширяют хладагент, полученный на этапе (e) для дополнительного ...

Verfahren zur Herstellung von Kohlendioxid

VERFAHREN ZUR VERFLUESSIGUNG VON LUFT UND VERFLUESSIGUNG DEREN KOMPONENTEN

"GASKOMPRESSIONSANLAGE"

Carbon dioxide recovery

Method and apparatus for compressing gas

The fuel required to provide the energy for compressing a gas can be reduced by compressing the gas substantially adiabatically through a pressure ratio of at least 2.5:1 in a compressor, cooling the hot compressed gas by heat exchange with water at superatmospheric pressure, further heating the water to produce super-heated steam and using the superheated steam to drive the compressor. The total amount of fuel consumed can be considerably less than that used for compressing gas conventionally (i.e. substantially isothermally).

Method and Equipment for Liquefaction of Neon with Turboexpander

... 1,186,432. Turbines. NAUTCHNO-IZSLEDOVATELSKI SEKTOR PRI PHISITCHESKIA FAKULTET NA SOFIISKI UNIVERSITET. April 3, 1967 [April 1, 1966], No. 6881/67. Heading F1T. [Also in Division F4] A turbo-expander suitable for cooling neon gas for providing refrigeration comprises a turbine rotor 70 mounted on a vertical shaft 62 having radial gas bearings 65 and a lower end thrust gas bearing 68 supplied with compressed neon at 54, 55 and having exhaust outlets 66, 67; the shaft also carrying an energy absorbing fan 69 supplied with neon through an inlet 52 and the compressed neon discharged at 53 is cooled in a nitrogen bath before being returned to the fan inlet.

Improvements in air purification units

Process and apparatus for the conveyance of real gases through a pipeline

A method of conveying a gas such as natural gas over long distances through a pipeline having a number of sections in series with intermediate compressor stations the pressure and temperature of the gas at entry to each pipeline section being such that the drop in pressure of the gas in each pipe section creates a drop in gas temperature and this low temperature gas is used to recool the gas heated by compression before it enters the next pipeline section.

COOLING DEVICE AND - PROCEDURES FOR COOLING A FLUID USING COOLING WATER

Method for recovering energy when commpressing gas by a compressor

Method for recovering energy when compressing a gas with a compressor (1) with two or more compression stages, with each stage realised by a compressor element (2,3), whereby in each case downstream from at least two aforementioned compressor elements there is a heat exchanger (4,5) with a primary and a secondary part, whereby the coolant is guided. successively in series through the. secondary part of at least two heat exchangers (4,5), whereby the sequence in which the coolant is guided through the heat exchangers (4,5) is chosen such that the temperature at the inlet of the primary part of at least one subsequent heat exchanger is higher than or equal to the temperature at the inlet of the primary part of a preceding heat exchanger, as seen in the direction of flow of the coolant, and whereby at least one heat exchanger (4 and/or 17) is provided with a tertiary part for a coolant.

LOW POWER, FREON REFRIGERATION ASSISTED AIR SEPARATION

Liquid oxygen and liquid nitrogen are produced from the separation of air in an installation of reduced size wherein the refrigeration necessary for the operation of the air separation unit is produced from the use of a single compander and a freon refrigeration unit affixed to a split-out stream of the main heat exchanger with appropriate recycling and heat exchange. The process for such an installation is also set forth.

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 - ...

METHOD FOR PRODUCING BIOMETHANE BY PURIFYING BIOGAS FROM NON-HAZARDOUS WASTE STORAGE FACILITIES AND FACILITY FOR IMPLEMENTING THE METHOD

Procédé de production de biométhane par épuration de biogaz issus d'installations de stockage de déchets non-dangereux (ISDND)selon lequel: -on comprime le flux gazeux initial, -on introduit le flux de gaz à épurer dans au moins un adsorbeur chargé en adsorbants aptes à adsorber réversiblement les COV, -on soumet le flux gazeux appauvri en COV sortant de l'adsorbeur chargé en adsorbants aptes à adsorber réversiblement les COVà au moins une séparation membranaire pour séparer partiellement le CO2 et l'O2 du flux gazeux, -on introduit le rétentat issu de la séparation membranaire dans au moins un adsorbeur chargé en adsorbants aptes à adsorber réversiblement la majeure partie du CO2 restant, -on soumet le flux gazeux appauvri en CO2,sortant de l'adsorbeur chargé en adsorbants aptes à adsorber réversiblement la majeure partie du CO2 restant à une séparation cryogénique dans une colonne de distillation pour séparer l'O2 et l'N2 du flux gazeux, -on récupère le flux riche en CH4 issu de la séparation ...

METHOD FOR COMPRESSING A GAS IN STAGES

The invention relates to a method for gradual sealing of a gas in a compressor arrangement (100, 200, 300, 400) having a plurality of compression stages (I-VI), sequentially connected to each other via a main line (1), in which compression stages the gas conducted through the main line (1) is compressed from a suction-side pressure level to a pressure-side pressure level and heated from a suction-side temperature level to a pressure-side temperature level via said compression, wherein a return volume of the gas conducted through the main line (1) is extracted at least temporarily from the main line (1) downstream of one of the compression stages (V), supplied to a decompression, and supplied back into the main line (1) upstream of the same compression stage (V). According to the invention, the pressure-side pressure level of the compression stage (V), downstream of which the return volume is extracted from the main line (1), is a supercritical pressure level, the decompression of the return ...

APPARATUS FOR PREPARING PURE CARBON DIOXIDE (CO2) FROM A GASEOUS CARBON DIOXIDE CONTAINING PRODUCT

The invention relates to an apparatus for preparing pure carbon dioxide (CO2) from a gaseous CO2 containing product, which apparatus comprises a processing line which comprises at least an inlet for the gaseous product, means for removing water-soluble impurities from the product, compression means for compressing and pressurising the product, cleaning means for removing further impurities from the product, as well as storage means for collecting and storing the purified CO2, which elements are interconnected by means of suitable piping. According to the invention, the compression means comprise at least one screw compressor so as to provide an apparatus for preparing pure carbon dioxide from a gaseous CO2 containing product which has a higher efficiency, which is of simpler, cheaper construction and which is easy to maintain.

PROCESS AND APPARATUS FOR THE LIQUEFACTION OF CARBON DIOXIDE

Apparatus for carbon dioxide liquefaction comprising a flow channel for carbon dioxide passage from an inlet port to an outlet port. The channel comprises a plurality of compressors (2, 5, 8) and coolers (4, 7, 9, 10, 13) arranged in series with an expansion chamber (14, 15) in said flow channel downstream of the final compressor (8) and cooler (9, 10, 13). The apparatus also comprises a recirculation channel (16) arranged to return gaseous carbon dioxide from said expansion chamber (15) into said flow channel (3) upstream of said final compressor (8) and cooler (9, 10, 13).

METHOD AND INSTALLATION FOR LIQUEFYING FLUE GAS FROM COMBUSTION INSTALLATIONS

A plant for CO2 separation is described that has a high security level, minimized energy consumption and can deliver liquid CO2 from the flue gas of a fossil fired power plant at different purity levels.

METHOD AND INSTALLATION FOR LIQUEFYING FLUE GAS FROM COMBUSTION INSTALLATIONS

A plant for CO2 separation is described that has a high security level, minimized energy consumption and can deliver liquid CO2 from the flue gas of a fossil fired power plant at different purity levels.

METHOD AND APPARATUS FOR ENHANCING CARBON DIOXIDE RECOVERY

A process and an apparatus for producing substantially pure carbon dioxide from a carbon dioxide feed containing from about 80% to about 95% volume of carbon dioxide.

APPARATUS OF RECUPERATION Of ENERGY FOR INSTALLATION OF GAS COMPRESSOR

Mixed Refrigerant System and Method

A system and method for cooling a gas using a mixed refrigerant includes a compressor system and a heat exchange system, where the compressor system may include an interstage separation device or drum with no liquid outlet, a liquid outlet in fluid communication with a pump that pumps liquid forward to a high pressure separation device or a liquid outlet through which liquid flows to the heat exchanger to be subcooled. In the last situation, the subcooled liquid is expanded and combined with an expanded cold temperature stream, which is a cooled and expanded stream from the vapor side of a cold vapor separation device, and subcooled and expanded streams from liquid sides of the high pressure separation device and the cold vapor separation device, or combined with a stream formed from the subcooled streams from the liquid sides of the high pressure separation device and the cold vapor separation device after mixing and expansion, to form a primary refrigeration stream. 1. A system for cooling a gas with a mixed refrigerant comprising:a. a main heat exchanger including a warm end and a cold end with a feed stream cooling passage extending therebetween, the feed stream cooling passage being adapted to receive a feed stream at the warm end and to convey a cooled product stream out of the cold end, said main heat exchanger also including a low pressure liquid cooling passage, a high pressure vapor cooling passage, a high pressure liquid cooling passage, a cold separator vapor cooling passage, a cold separator liquid cooling passage and a refrigeration passage;b. a mixed refrigerant compressor system including a compressor first section having an inlet in fluid communication with an outlet of the refrigeration passage and an outlet, a first section cooler having an inlet in fluid communication with the outlet of the compressor first section and an outlet, an interstage separation device having an inlet in fluid communication with the outlet of the first section cooler and ...

Carbon Dioxide Capture from Flu Gas

A method for capturing carbon dioxide from a flue gas includes (i) removing moisture from a flue gas to yield a dried flue gas; (ii) compressing the dried flue gas to yield a compressed gas stream; (iii) reducing the temperature of the compressed gas stream to a temperature Tusing a first heat exchanger; (iv) reducing the temperature of the compressed gas stream to a second temperarature Tusing a second heat exchanger stream, where T Подробнее

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 ...

Method And Device For Condensing A Carbon Dioxide-Rich Gas Stream

The invention relates to a method for condensing a carbon dioxide-rich gas stream, wherein a stream of water heated by an exchange of heat with the carbon dioxide-rich stream, which is at least partially condensed, is sent to at least one compressor () for compressing the carbon dioxide-rich stream or a fluid, the carbon dioxide-rich stream of which is derived, in order to at least partially cool at least one stage of said compressor. 111-. (canceled)12. A method for condensing a gas stream rich in carbon dioxide , in which method a stream of water is heated up by exchange of heat with the stream rich in carbon dioxide which at least partially condenses , wherein the heated stream is sent to:i) at least one compressor of the stream rich in carbon dioxide and/orii) at least one compressor of a fluid from which the stream rich in carbon dioxide is derived in order to at least partially cool at least one stage of the at least one compressor.13. The method as claimed in claim 12 , in which the stream of water heated while the respective compressor is being cooled claim 12 , is cooled and returned at least in part in order to cool the stream rich in carbon dioxide that is to be condensed.14. The method as claimed in claim 12 , in which the fluid compressed in the compressor is treated by distillation and/or by amine scrubbing and/or by permeation and/or by adsorption to form the stream rich in carbon dioxide.15. The method as claimed in claim 12 , in which the water heated by condensation of carbon dioxide is at a first temperature and is sent to the respective compressor at a temperature substantially equal to the first temperature.16. The method as claimed in claim 12 , in which the water heated by condensation of carbon dioxide is divided into two portions claim 12 , one portion being sent to a compressor of the stream rich in carbon dioxide which will then be condensed claim 12 , and the other portion being sent to the compressor of the fluid from which the stream ...

METHODS AND CONFIGURATIONS FOR LNG LIQUEFACTION

Embodiments relate generally to systems and methods for pre-cooling a natural gas stream to a liquefaction plant. A system may comprise a compressor configured to receive a first natural gas stream at a first pressure and produce a second natural gas stream at a second pressure; an exchanger, wherein the exchanger is configured to receive the second natural gas stream as the second pressure and cool the second natural gas stream to produce a cooled natural gas stream; and an expander, wherein the expander is configured to receive the cooled natural gas stream and expand the cooled natural gas stream from the second pressure to a third pressure. 1. A system for pre-cooling a natural gas stream to a liquefaction plant , the system comprising:a compressor configured to receive a first natural gas stream at a first pressure and produce a second natural gas stream at a second pressure;an exchanger, wherein the exchanger is configured to receive the second natural gas stream at the second pressure and cool the second natural gas stream to produce a cooled natural gas stream; andan expander, wherein the expander is configured to receive the cooled natural gas stream and expand the cooled natural gas stream from the second pressure to a third pressure.2. The system of claim 1 , wherein the exchanger is an ambient air exchanger configured to exchange heat between the second natural gas stream at the second pressure and an ambient air stream.3. The system of claim 1 , further comprising:a second compressor configured to receive a natural gas feed stream at a fourth pressure and produce a fourth natural gas stream at the first pressure, wherein the first pressure is higher than the fourth pressure; anda second exchanger, wherein the second exchanger is configured to receive the fourth natural gas stream at the first pressure and cool the natural gas stream to produce the first natural gas stream.4. The system of claim 3 , wherein the natural gas stream at the third pressure is ...

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.

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.

Carbon dioxide capturing apparatus using cold heat of liquefied natural gas and power generation system using same

A carbon dioxide capturing apparatus using cold heat of liquefied natural gas (LNG) includes a heat exchanger to cool primary coolant using heat exchange between the primary coolant and the LNG; a chiller connected to the heat exchanger and configured to discharge capturing coolant colder than the primary coolant by performing a heat exchange between the capturing coolant and a cooling material; and a capturing cooler configured to capture carbon dioxide contained in flue gas by performing a heat exchange between the capturing coolant discharged from the chiller and the flue gas. A power generation system includes an LNG storage facility; a power generation facility discharging flue gas; a unit for heat exchange between the LNG and a coolant to regasify the LNG and cool the coolant; and a unit for capturing carbon dioxide contained in the flue gas by heat exchange between the discharged flue gas and the coolant.

Pre-Cooling of Natural Gas by High Pressure Compression and Expansion

A method of producing liquefied natural gas (LNG) is disclosed. A natural gas stream is provided from a supply of natural gas. The natural gas stream is compressed in at least two serially arranged compressors to a pressure of at least 2,000 psia to form a compressed natural gas stream. The compressed natural gas stream is cooled to form a cooled compressed natural gas stream. The cooled compressed natural gas stream is expanded in at least one work producing natural gas expander to a pressure that is less than 3,000 psia and no greater than the pressure to which the at least two serially arranged compressors compress the natural gas stream, to thereby form a chilled natural gas stream. The chilled natural gas stream is liquefied. 1. A method of producing liquefied natural gas (LNG) , the method comprising:providing a natural gas stream from a supply of natural gas;compressing the natural gas stream in at least two serially arranged compressors to a pressure of at least 2,000 psia to form a compressed natural gas stream;cooling the compressed natural gas stream to form a cooled compressed natural gas stream;expanding, in at least one work producing natural gas expander, the cooled compressed natural gas stream to a pressure that is less than 3000 psia and no greater than the pressure to which the at least two serially arranged compressors compress the natural gas stream, to thereby form a chilled natural gas stream; andliquefying the chilled natural gas stream.2. The method of claim 1 , wherein liquefying the chilled natural gas stream is performed in one or more single mixed refrigerant (SMR) liquefaction trains.3. The method of claim 1 , wherein liquefying the chilled natural gas stream is performed in one or more expander-based liquefaction modules claim 1 , and wherein the expander-based liquefaction module is one of a nitrogen gas expander-based liquefaction module and a feed gas expander-based liquefaction module.4. The method of claim 3 , wherein the feed gas ...

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 ...

METHOD AND SYSTEM FOR SEPARATING CARBON DIOXIDE FROM FLUE GAS

A method for separating carbon dioxide from flue gas to generate a high purity CO2 stream. 1. A method for separating carbon dioxide from flue gas , the method comprising:compressing the flue gas,cooling the compressed flue gas in at least a heat exchanger;providing the cooled compressed gas to a separator to generate a carbon dioxide rich liquid stream and a carbon dioxide lean gas stream;providing the carbon dioxide rich liquid stream and the carbon dioxide lean gas stream to a distillation column to generate a non-condensable gas stream and a carbon dioxide liquid stream;providing the carbon dioxide liquid at a cold side of a reboiler to generate a purified carbon dioxide liquid stream;expanding the purified carbon dioxide liquid and supplying the expanded carbon dioxide liquid to the at least a heat exchanger for cooling the at least a heat exchanger;providing the expanded carbon dioxide liquid from the at least a heat exchanger to a high-pressure compressor to generate a compressed carbon dioxide vapor;providing at least a part of the compressed carbon dioxide vapor from the high-pressure compressor to a warm side of the reboiler to generate a cooled carbon dioxide liquid;expanding the cooled carbon dioxide liquid and passing the cooled carbon dioxide liquid through the at least a heat exchanger for cooling the at least a heat exchanger; andforwarding the purified carbon dioxide liquid and the cooled carbon dioxide liquid to the at least a heat exchanger.2. The method according to claim 1 , further comprising:cooling the flue gas in at least two heat exchangers connected in series,splitting the purified carbon dioxide liquid in at least two streams,expanding each of the streams to a given pressure to generate at least two expanded carbon dioxide liquids streams having different temperatures,supplying each expanded carbon dioxide liquid stream to one of the at least two heat exchangers.3. The method according to claim 1 , further comprising:expanding the cooled ...

Hydrocarbon Distillation

Systems and methods are provided for increasing the efficiency of liquefied natural gas production and heavy hydrocarbon distillation. In one embodiment, air within an LNG production facility can be utilized as a heat source to provide heat to HHC liquid for distillation in a HHC distillation system. The mechanism of heat transfer from the air can be natural convection. In another embodiment, heat provided by natural gas, or compressed natural gas, can be used for HHC distillation. In other embodiments, various other liquids can be used to transfer heat to HHC liquid for distillation. 119-. (canceled)20. A system for producing liquefied natural gas (LNG) and electrical power , comprising:a LNG production facility configured to receive a natural gas feedstock and to form liquefied natural gas from the natural gas feedstock, wherein the LNG production facility receives electrical power from an external power source; anda power generation facility configured to create electrical power using the natural gas feedstock or an additional fuel source and to provide a first portion of the electrical power to the LNG production facility.21. The system of claim 20 , wherein the external power source includes one of a local power grid and a battery bank.22. The system of claim 20 , wherein the additional fuel source includes a fuel vapor received from the LNG production facility claim 20 , the fuel vapor collected while reducing a pressure of the liquefied natural gas within the LNG production facility.23. The system of claim 20 , wherein the additional fuel source includes one of petroleum fuel claim 20 , diesel fuel claim 20 , propane claim 20 , and kerosene.24. The system of claim 20 , wherein the power generation facility is further configured to provide a second portion of the electrical power for storage in batteries or to a local power grid.25. The system of claim 20 , wherein waste heat generated at the power generation facility can be provided to the LNG production ...

COMPRESSING SYSTEM, AND GAS COMPRESSING METHOD

A compressing system includes a compression section that compresses a target gas to an intermediate pressure, which is equal to or higher than a critical pressure and lower than a target pressure to generate an intermediate supercritical fluid, a cooling section that cools the intermediate supercritical fluid generated in the compression section to near a critical temperature to generate an intermediate supercritical pressure liquid, and a pumping section that compresses the intermediate supercritical pressure liquid generated in the cooling section to a pressure that is equal to or higher than the target pressure. At least one of the intermediate supercritical pressure liquid compressed in the pumping section, a low-temperature liquid generated by extracting the intermediate supercritical pressure liquid on the upstream side of the pumping section to reduce pressure to near the critical pressure, and an external cooling medium is used as a cooling medium in the cooling section. 16-. (canceled)7. A gas compressing method that compresses carbon dioxide as a target gas to a pressure that is equal to or higher than a target pressure higher than a critical pressure , the gas compressing method comprising:a compression step of compressing the carbon dioxide to an intermediate pressure, which is equal to or higher than the critical pressure and is lower than the target pressure;a first cooling step of cooling the carbon dioxide compressed in the compression step to generate an intermediate supercritical fluid;a second cooling step of cooling the intermediate supercritical fluid cooled in the first cooling step to a temperature range of ±20° C. from a critical temperature of the carbon dioxide to generate an intermediate supercritical pressure liquid;a pressure-reduction step of reducing the pressure of a portion of the intermediate supercritical pressure liquid extracted a main flow thereof after the second cooling step to generate a low-temperature liquid; anda pumping ...

Hydrocarbon Distillation

Systems and methods are provided for increasing the efficiency of liquefied natural gas production and heavy hydrocarbon distillation. In one embodiment, air within an LNG production facility can be utilized as a heat source to provide heat to HHC liquid for distillation in a HHC distillation system. The mechanism of heat transfer from the air can be natural convection. In another embodiment, heat provided by natural gas, or compressed natural gas, can be used for HHC distillation. In other embodiments, various other liquids can be used to transfer heat to HHC liquid for distillation. 1. A system for producing liquefied natural gas (LNG) and separating heavy hydrocarbon components , comprising:a LNG production facility configured to receive and liquefy a natural gas feedstock, the LNG production facility having a refrigerant fluid configured to accept heat from the natural gas feedstock; anda distillation column coupled to the LNG production facility and having a first heat exchanger configured to transfer heat to a liquid containing heavy hydrocarbon components such that the liquid boils to form vapor thereby allowing the heavy hydrocarbon components to be separated and collected, the heat being transferred from at least one of a heated fluid comprising at least a portion of at least one of the natural gas feedstock, the refrigerant fluid, and an ambient air.2. The system of claim 1 , wherein the heat being transferred from the heated fluid is delivered to the first heat exchanger from a second heat exchanger.3. The system of claim 1 , wherein heat is transferred from the heated fluid by natural convection.4. The system of claim 1 , wherein heat is transferred from the heated fluid by forced convection.5. The system of claim 1 , further comprising heat pipes that are configured to aid in transferring heat from the heated fluid to the liquid.6. The system of claim 1 , wherein the first heat exchanger is a reboiler.7. The system of claim 2 , wherein the first and ...

SYSTEM AND METHOD FOR ENHANCED ARGON RECOVERY FROM A FEED STREAM COMPRISING HYDROGEN, METHANE, NITROGEN AND ARGON

A system and method for argon and nitrogen extraction from a feed stream comprising hydrogen, methane, nitrogen and argon, such as tail gas of an ammonia production plant is provided. The disclosed system and method provides for nitrogen-argon rectification and the methane rejection within a column system comprised of at least one distillation column. Nitrogen and argon are further separated and to produce liquid products. An argon stripping column arrangement is disclosed where residual argon is further removed from the methane-rich fuel gas and recycled back to the feed stream.

Air compression system and method

An air compression system and method for an air separation plant in which air is compressed in a series of compression stages and a temperature swing adsorption unit adsorbs water vapor and carbon dioxide. The temperature swing adsorption unit is situated at a location of the compression stages such that air pressure upon entry into the adsorbent beds is between about 400 psia and about 600 psia. Each of the adsorbent beds of the unit have a minimum transverse cross-sectional flow area that will set the air velocity of the air to a level below that at which adsorbent bed fluidization would occur. Such operation allows fabrication costs of the adsorbent beds to be reduced because less adsorbent and smaller adsorbent beds are required while power consumption will be at a minimum.

CO2 SEPARATION & LIQUEFACTION SYSTEM AND METHOD

A CO2 separation and liquefaction system such as might be used in a carbon capture and sequestration system for a fossil fuel burning power plant is disclosed. The CO2 separation and liquefaction system includes a first cooling stage to cool flue gas with liquid CO2, a compression stage coupled to the first cooling stage to compress the cooled flue gas, a second cooling stage coupled to the compression stage and the first cooling stage to cool the compressed flue gas with a CO2 melt and provide the liquid CO2 to the first cooling stage, and an expansion stage coupled to the second cooling stage to extract solid CO2 from the flue gas that melts in the second cooling stage to provide the liquid CO2. 1. A CO2 separation and liquefaction system comprising:a first cooling stage to cool flue gas with liquid CO2;a compression stage coupled to the first cooling stage to compress the cooled flue gas;a second cooling stage coupled to the compression stage and the first cooling stage to cool the compressed flue gas with a CO2 melt and provide the liquid CO2 to the first cooling stage; andan expansion stage coupled to the second cooling stage to extract solid CO2 from the flue gas that melts in the second cooling stage to provide the liquid CO2.2. The CO2 separation and liquefaction system of further comprising:a compressor located upstream from the first cooling stage; anda heat exchanger, cooled by an ambient environment, and coupled in series between the compressor and the first cooling stage.3. The CO2 separation and liquefaction system of wherein the first cooling stage cools the flue gas with an N2 rich flue stream created by the solid CO2 extraction.4. The CO2 separation and liquefaction system of wherein the expansion stage comprises:a plurality of heat exchangers coupled in series to extract the solid CO2 from the flue gas, anda plurality of expanders coupled in series and downstream from the plurality of heat exchangers; andwherein each of the heat exchangers is ...

NATURAL GAS LIQUEFACTION SYSTEM

A natural gas liquefaction system includes a piping rack for supporting a raw material gas transporting pipe for transporting the raw material gas; a pre-cooling heat exchanger for pre-cooling the raw material gas with a first refrigerant; a first refrigerant compressor for compressing the first refrigerant; a plurality of first air-cooled heat exchangers disposed on a top of the piping; a liquefier for liquefying the raw material gas which has been cooled by the pre-cooling heat exchanger, wherein the piping rack has a widened section along a part of a length of the piping rack, wherein the pre-cooling heat exchanger and the first refrigerant compressor are disposed on either side of the widened section of the piping rack, and are connected to each other via a first refrigerant transporting pipe extending in a direction intersecting a lengthwise direction of the piping rack for transporting the first refrigerant. 1. A natural gas liquefaction system for cooling a natural gas supplied as a raw material gas to produce a liquefied natural gas , comprising:a piping rack for supporting a raw material gas transporting pipe for transporting the raw material gas;a pre-cooling heat exchanger for pre-cooling the raw material gas with a first refrigerant;a first refrigerant compressor for compressing the first refrigerant;a plurality of first air-cooled heat exchangers disposed on a top of the piping rack for cooling the first refrigerant compressed by the first refrigerant compressor;a liquefier for liquefying the raw material gas by further cooling the raw material gas which has been cooled by the pre-cooling heat exchanger;a second refrigerant compressor for compressing a second refrigerant used for cooling the raw material gas in the liquefier;a plurality of second air-cooled heat exchangers disposed on the top of the piping rack for cooling the second refrigerant compressed by the second refrigerant compressor; anda refrigerant heat exchanger for cooling the second ...

LARGE-SCALE HYDROGEN LIQUEFACTION BY MEANS OF A HIGH PRESSURE HYDROGEN REFRIGERATION CYCLE COMBINED TO A NOVEL SINGLE MIXED-REFRIGERANT PRECOOLING

The present invention relates to a method for liquefying hydrogen, the method comprises the steps of: cooling a feed gas stream comprising hydrogen with a pressure of at least 15 bar(a) to a temperature below the critical temperature of hydrogen in a first cooling step yielding a liquid product stream. According to the invention, the feed gas stream is cooled by a closed first cooling cycle with a high pressure first refrigerant stream comprising hydrogen, wherein the high pressure first refrigerant stream is separated into at least two partial streams, a first partial stream is expanded to low pressure, thereby producing cold to cool the precooled feed gas below the critical pressure of hydrogen, and compressed to a medium pressure, and wherein a second partial stream is expanded at least close to the medium pressure and guided into the medium pressure first partial stream. 2212425. The method according to claim 1 , wherein said first refrigerant stream () is further separated at least into a third partial stream () claim 1 , and optionally a fourth partial stream () claim 1 , wherein{'b': 24', '25', '54', '55', '56', '57', '31', '32, 'said third partial stream (), and optionally said fourth partial stream (), is expanded in a third expansion device (, ), and optionally a fourth expansion device (, ), respectively, yielding a partially expanded third partial stream (), and optionally a partially expanded fourth partial stream (),'}{'b': 31', '30', '32', '33, 'said partially expanded third partial stream () and said partially expanded first partial stream (), and optionally said expanded fourth partial stream (), are merged to form a combined partially expanded partial stream (), and'}{'b': 33', '35', '34, 'said combined partially expanded partial stream () and said partially expanded second partial stream () are merged to form said partially expanded first refrigerant stream ().'}32353292952302922292222. The method according to claim 1 , wherein said first partial ...

SYSTEM AND METHOD FOR ENHANCED ARGON RECOVERY FROM A FEED STREAM COMPRISING HYDROGEN, METHANE, NITROGEN AND ARGON

A system and method for argon and nitrogen extraction from a feed stream comprising hydrogen, methane, nitrogen and argon, such as tail gas of an ammonia production plant is provided. The disclosed system and method provides for nitrogen-argon rectification and the methane rejection within a column system comprised of at least one distillation column. Nitrogen and argon are further separated and to produce liquid products. An argon stripping column arrangement is disclosed where residual argon is further removed from the methane-rich fuel gas and recycled back to the feed stream. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. (canceled)14. (canceled)15. (canceled)16. (canceled)17. (canceled)18. (canceled)19. (canceled)20. (canceled)21. (canceled)22. (canceled)23. (canceled)24. (canceled)25. (canceled)26. (canceled)27. A system for recovery of argon from a feed stream comprising hydrogen , nitrogen , methane and argon , the system comprising:a conditioning circuit configured for conditioning the feed stream to a temperature suitable for rectification and at pressure less than or equal to about 400 psia;at least one rectifying column configured to receive the conditioned feed stream and produce an argon depleted, nitrogen rich vapor stream, an argon enriched side draw, and a methane-rich liquid stream;an argon stripping column configured to receive the methane rich liquid stream and strip argon from the methane rich liquid stream using the argon depleted, nitrogen rich vapor stream and produce an argon depleted methane rich liquid from the bottom of the argon stripping column and an argon containing overhead gas from the top of the argon stripping column;a recycle circuit configured for extracting the argon containing overhead gas from the argon stripping column and mixing the argon containing overhead gas with the feed stream; anda distillation column ...

Thermoelectric power generating module, and thermoelectric power generating device, anti-freezing vaporizer, and vaporized fuel gas liquefaction process device including same

Provided are a thermoelectric power generation module, a thermoelectric power generation apparatus including the same, an anti-icing vaporization device including the same, and an apparatus for a vaporized fuel gas liquefaction process including the same. The thermoelectric power generation module includes: a pipe through which a fluid flows; and a thermoelectric power generator configured to surround the pipe and to produce power due to a temperature difference between the fluid and outside air.

Large-scale hydrogen liquefaction by means of a high pressure hydrogen refrigeration cycle combined to a novel single mixed-refrigerant precooling

The present invention relates to a method for liquefying hydrogen, the method comprises the steps of: cooling a feed gas stream comprising hydrogen with a pressure of at least 15 bar(a) to a temperature below the critical temperature of hydrogen in a first cooling step yielding a liquid product stream. According to the invention, the feed gas stream is cooled by a closed first cooling cycle with a high pressure first refrigerant stream comprising hydrogen, wherein the high pressure first refrigerant stream is separated into at least two partial streams, a first partial stream is expanded to low pressure, thereby producing cold to cool the precooled feed gas below the critical pressure of hydrogen, and compressed to a medium pressure, and wherein a second partial stream is expanded at least close to the medium pressure and guided into the medium pressure first partial stream.

Process

Lower power, freon refrigeration assisted air separation

Liquid oxygen and liquid nitrogen are produced from the separation of air in an installation of reduced size wherein the refrigeration necessary for the operation of the air separation unit is produced from the use of a single compander and a freon refrigeration unit affixed to a split-out stream of the main heat exchanger with appropriate recycling and heat exchange. The process for such an installation is also set forth.

Method and system for the small-scale production of liquified natural gas (LNG) from low-pressure gas

A method and system for the small-scale production of LNG. The method comprising: configuring a prime mover to be operable communication with a multi-stage compressor; configuring the prime mover to be in fluid communication with an ammonia absorption chiller; configuring the ammonia absorption chiller to be in fluid communication with the multi-stage compressor; operating the ammonia absorption chiller using waste heat from a prime mover; pre-cooling a first stream of natural gas using cooled fluid from the ammonia absorption chiller; cooling a first portion of the first stream of natural gas, using an expansion valve, into a two-phase stream; cooling a second portion of the first stream to liquefied natural gas, using the two-phase stream as a cooling fluid; delivering the second portion of the first stream as LNG to a low-pressure LNG tank; cooling a third portion of the first stream of natural gas in a turbo-expander; separating liquid heavies out of the third portion of the first stream of natural gas; and delivering the liquid heavies to a pressure tank.

System and method for cooling a bog stream

A system for cooling a boil-off gas (BOG) stream prior to compression in a boil-off reliquefaction plant, comprising a line (10) for feeding BOG into a compressor (11; 11') prior to heat exchange with a closed-loop refrigeration system. The refrigeration system comprising compressors (2, 3, 4) and expanders(8, 9) and a number of heat ex-changers for heat exchange with the BOG stream. The expanders (8, 9) are arranged in series. A precooler in the feed line (10) is fluidly connected (32, 33) to the closed-loop refrigeration system, whereby said BOG is pre-cooled in heat exchange with a portion of the coolant in the closed-loop refrigeration system prior to said compression.

Process to convert low grade heat source into power using dense fluid expander

A process to convert heat into power is set forth wherein, to make the cycle more suitable to low grade heat, the working fluid remains substantially in the liquid state after being heat exchanged against the heat source and a dense fluid expander is used in place of a conventional vapor expander to subsequently work expand the liquid working fluid.

System And Method For Cooling A Bog Stream

A system for cooling a boil-off gas (BOG) stream prior to compression in a boil-off reliquefaction plant, comprising a line ( 10 ) for feeding BOG into a compressor ( 11; 11 ″) prior to heat exchange with a closed-loop refrigeration system. The refrigeration system comprising compressors ( 2, 3, 4 ) and expanders( 8, 9 ) and a number of heat ex-changers for heat exchange with the BOG stream. The expanders ( 8, 9 ) are arranged in series. A precooler in the feed line ( 10 ) is fluidly connected ( 32, 33 ) to the closed-loop refrigeration system, whereby said BOG is pre-cooled in heat exchange with a portion of the coolant in the closed-loop refrigeration system prior to said compression.

Process to convert low grade heat source into power using dense fluid expander

A process to convert heat into power is set forth wherein, to make the cycle more suitable to low grade heat, the working fluid remains substantially in the liquid state after being heat exchanged against the heat source and a dense fluid expander is used in place of a conventional vapor expander to subsequently work expand the liquid working fluid.

耦合余热制冷技术和膨胀深冷分离技术的聚烯烃装置排放气回收系统

本发明公开一种耦合余热制冷技术和膨胀深冷分离技术的聚烯烃装置排放气回收系统。该系统包括：压缩冷凝单元，接收来自聚烯烃装置的排放气，经过两次压缩、冷凝及气液分离过程，回收排放气中的重质烃；深冷分离单元，接收压缩冷凝单元的气相组成，通过膨胀自冷回收低碳烃类；吸收制冷单元，采用溴化锂溶液中间介质，回收压缩冷凝单元的热能制得低温冷量输送到深冷分离单元。本发明通过回收排放气压缩过后的压缩热，产生7℃冷量，用于排放气深冷过程，并通过膨胀过程，降低排放气自身温度，实现自冷，进一步减少聚烯烃装置排放气回收过程的热能排放和冷量需求。

液化天然气的汽化系统和方法

本发明公开了使液化天然气(LNG)汽化的方法和系统，其使用冷凝气体流来调节LNG的总热值(GHV)，从而在汽化时获得满足管线或其它商业规格的天然气产品。冷凝气体可为空气、氮气，或者在一些实施方案中为NGL，如乙烷、丙烷或丁烷，或其它可燃烃如二甲基醚(DME)，取决于期望的GHV变化。在一些实施方案中，所述方法和系统使用一体化的空气分离设备来产生用作冷凝气体的氮气，其中热传递介质的冷流，如水、乙二醇、其它普通热传递流体或其混合物在LNG的汽化过程中通过热传递而获得，用来预冷却空气分离设备的空气进料，或者用来冷却与之相关的其它过程流。

用于通过蒸馏分离富二氧化碳气体的方法和设备

本发明涉及一种通过蒸馏分离富二氧化碳气体的方法，所述富二氧化碳气体在热交换器(3)中被冷却并且被送至蒸馏塔(5)，从塔顶提取贫二氧化碳气体(6)并且从塔底提取富二氧化碳液体(7)，在压缩机(17)中将富二氧化碳气体压缩至第一压力并且源自所述压缩机的所述富二氧化碳气体的至少一部分从第一压力膨胀至比所述第一压力低的第二压力、例如塔中的压力，并且膨胀的气体用于加热塔底。

一种利用外循环气波制冷回收聚烯烃装置排放气的方法

本发明提供了一种利用外循环气波制冷回收聚烯烃装置排放气的方法，包括至少一个压缩装置、至少一个换热装置和至少一个气液分离装置的压缩分离步骤，其用于接收来自聚烯烃反应系统的排放气，将其压缩并气液分离，分别输出第一回收产品和第一气相成分；包括至少两个换热装置、至少一个气液分离装置的预分离步骤，其用于接收第一气相成分，将其逐级冷却并气液分离，分别输出第三回收产品和第二气相成分；包括至少一个气波制冷装置、至少一个多流股换热装置和至少一个气液分离装置的深冷分离步骤，多流股换热装置用于接收第二气相成分，气波制冷装置提供制冷剂，将第二气相成分深冷并气液分离，分别输出第二回收产品和第四回收产品，并回收产品部分冷量。

Способ для сжижения топочного газа от сжигательных установок

Изобретение относится к способу производства жидкого СО 2 из газообразных продуктов сгорания. Топочный газ сжимают в первом компрессоре, затем охлаждают в первом охладителе и частично конденсируют на двух ступенях разделения. Две ступени разделения охлаждают расширяющимся отходящим газом и расширяющимся жидким СО 2 . Вторая ступень разделения включает второй теплообменник и стриппер CO 2 , в котором поток жидкого CO 2 из первой ступени разделения поступает в стриппер CO 2 непосредственно и поток CO 2 из первой ступени разделения поступает в стриппер СО 2 через второй теплообменник. Жидкий СО 2 в стриппере кипятят ребойлером и из верхней части стриппера СО 2 отходящий газ выделяют, расширяют в регулирующем давление клапане и используют в ступенях разделения для целей охлаждения. Также жидкий СО 2 из ребойлера и стриппера CO 2 собирают в буферном барабане. Технический результат заключается в повышении чистоты сжиженного СО 2 без увеличения потребности в энергии. 11 з.п. ф-лы, 5 ил., 1 табл. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК F25J 3/02 F25J 3/06 (11) (13) 2 557 945 C2 (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2012149433/06, 19.04.2011 (24) Дата начала отсчета срока действия патента: 19.04.2011 (72) Автор(ы): ШТАЛЛЬМАНН Олаф (DE) (73) Патентообладатель(и): АЛЬСТОМ ТЕКНОЛОДЖИ ЛТД (CH) Приоритет(ы): (30) Конвенционный приоритет: R U 21.04.2010 EP 10004249.8 (43) Дата публикации заявки: 27.05.2014 Бюл. № 15 (45) Опубликовано: 27.07.2015 Бюл. № 21 2 5 5 7 9 4 5 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 21.11.2012 C 2 C 2 (56) Список документов, цитированных в отчете о поиске: US 2008/196584 A1 (HA BAO, AIR LIQUIDE PROCESS & CONSTRUCTION), 21.08.2008. DE 19744844 A1 (LINDE AG), 26.03.1998. RU 2175949 C2 (ЗАО "Центр ВМТехнологий"), 20.11.2001. EA 12122 B1 (СТАТОЙЛ АСА, СИНВЕНТ АС, ОРКЛА ЭНДЖИНИРИНГ), 28.08.2009 (86) Заявка PCT: IB 2011/000853 (19.04.2011) R U 2 5 5 7 9 ...

利用天然气制冷对空气流进行冷压缩的系统

本发明涉及一种利用天然气制冷对空气流进行冷压缩的系统。空气流受到多级压缩，源自含有天然气的制冷剂的制冷被用于级间冷却。通过使用中间冷却介质将制冷从制冷剂传给级间空气流减少了天然气泄漏进入该空气流的可能性。被压缩空气流可供给一种深冷空气分离装置，该空气分离装置包括基于液化天然气的液化器装置，从该液化器装置中提取出用作所述制冷剂的冷天然气流。

一种天然气原料气加工装置

本发明提供了一种天然气原料气加工装置，包括依次连接的原料气预分离器、压缩装置、制冷分离装置和分馏装置，还包括CNG压缩装置，所述制冷分离装置和所述分馏装置都设置有干气出气管，所述CNG压缩装置连接所述制冷分离装置的干气出气管和所述分馏装置的干气出气管。本发明尤其适合在边远油气田或者零星油气井，对于不能进集输管网的天然气进行处理，可大大减少投资，同时可降低生产过程的操作能耗。生产的液化气和稳定轻烃可以作为化工原料及工业或民用燃料，压缩天然气可运至城市，作为天然气汽车燃料，代替城市车用汽柴油，大大地洁净了城市环境，具有良好的经济效益和社会效益。

用稠密流体膨胀器将低级热源转化为动力的工艺

提出了用于将热转化为动力的工艺，其中为使循环更适用于低级热，工作流体在与热源进行热交换后基本保持液态，并且用稠密流体膨胀器代替传统蒸汽膨胀器随后使液体工作流体做功膨胀。

一种回收压缩空气余热的空分系统

本发明公开了一种回收压缩空气余热的空分系统，包括空气流路和纯化模块，还包括除湿再生回路和吸收式制冷循环回路；所述除湿再生回路包括除湿器、第一溶液热交换器、发生器、第一流量控制器和第一溶液泵；所述吸收式制冷循环回路包括所述发生器的高温空气通道、冷凝器、膨胀元件、低温蒸发器、所述除湿器的冷却通道、吸收器、第二溶液泵、第二溶液热交换器、第二流量控制器和节流元件；所述空气流路包括依次连通除湿器的除湿通道、一级空压机、发生器的一级压缩空气预冷流路、第一冷却单元、低温蒸发器的一级通道、二级空压机、发生器的二级压缩空气预冷流路、第二冷却单元以及低温蒸发器的二级通道，最后通入纯化模块。

A kind of shallow cold process for recovering light hydrocarbon method

本发明涉及一种浅冷轻烃回收工艺方法，原料气经过分离后，进压缩机压缩，冷却后分离进压缩机增压，增压后在分离出气体和液烃；气体进四股流板翅式换热器第一管程；经过冷却后，经低温分离器进四股板翅式流换热器第二管程，换热后干气外输；液烃经分配器分成二股，一股液烃进四股流板翅式换热器第三管程，循环回分离器；第二股液烃经进四股流板翅式换热器第四管程；换热后进脱乙烷塔；分离器通过液烃泵脱乙烷塔；脱乙烷塔塔顶气体进分离器；脱乙烷塔塔底混烃进液化气塔；液化气塔塔顶外输液化气；液化气塔塔底外输轻油；该方法比常规的浅冷冷凝+冷油吸收法节省能耗63.3％。

Integrated energy recovery system

Recovery of heat energy, e.g., the heat of compression, from the production of pressurized gases, in particular nitrogen (N), but also other gases such as compressed dry air. This invention is directed to a system and method for increasing the efficiency in use of energy by recovering energy normally wasted in one device and using the energy in another device needing the energy. In particular, this invention is directed to recovering the heat (18, 28, 38) of compression from a gas generation plant to warm cooling water (64, 66, 68, 70) that is also used as feed (76) water to an ultra pure water generation plant.

Patent RU2018122940A3

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2018 122 940 A (51) МПК B01D 53/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2018122940, 10.11.2016 (71) Заявитель(и): ВАГА ЭНЕРДЖИ (FR) Приоритет(ы): (30) Конвенционный приоритет: 24.12.2015 FR 1563357 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 24.07.2018 R U (43) Дата публикации заявки: 24.01.2020 Бюл. № 3 (72) Автор(ы): ПРЭНС Гвенаэль (FR), ЛЕФЕВР Матьё (FR), БРИЕН Пьер (FR), ПАЖЕ Николя (FR) (86) Заявка PCT: (87) Публикация заявки PCT: WO 2017/109305 (29.06.2017) A Адрес для переписки: 123242, Москва, пл. Кудринская, д. 1, а/я 35, "Михайлюк, Сороколат и партнеры патентные поверенные" R U (57) Формула изобретения 1. Способ получения биометана путем очистки биогаза из хранилищ неопасных отходов (NHWSF), согласно которому начальный газовый поток подвергают сжатию, газовый поток, подлежащий очистке, вводят по меньшей мере в один адсорбер, заполненный адсорбентами, способными к обратимой адсорбции VOC, обедненный по VOC газовый поток, выходящий из адсорбера, заполненного адсорбентами, способными к обратимой адсорбции VOC, подвергают по меньшей мере одному мембранному разделению, предусматривающему задействование от 1 до 4 мембранных ступеней, проницаемость которых обеспечивает отделение от газового потока более 90% CO2 и по меньшей мере 30% O2, ретентат, полученный в результате мембранного разделения, вводят по меньшей мере в один адсорбер, заполненный адсорбентами, способными к обратимой адсорбции большей части оставшегося CO2, обедненный по CO2 газовый поток, выходящий из адсорбера, заполненного адсорбентами, способными к обратимой адсорбции большей части оставшегося CO2, подвергают криогенному разделению в дистилляционной колонне с отделением O2 и Стр.: 1 A 2 0 1 8 1 2 2 9 4 0 (54) СПОСОБ ПОЛУЧЕНИЯ БИОМЕТАНА ПУТЕМ ОЧИСТКИ БИОГАЗА ИЗ ХРАНИЛИЩ НЕОПАСНЫХ ОТХОДОВ И УСТАНОВКА ДЛЯ ОСУЩЕСТВЛЕНИЯ СПОСОБА 2 0 1 8 1 2 2 9 4 0 FR 2016/052937 (10.11. ...

Electric power production processing method using combined power cycle according to liquefied natural gas and synthetic fuel gas

기계 및 전기적 전력이 통합된 연소와 스텀터빈에 따른 부분산화공정에 의한 합성연료가스에 따라 생산된다. 가스소비자를 위해 파이프 라인에 공급하기 위한 부산물 기화 액화 천연가스가 부분산화가스화와 가스크리닝 및 정화영역으로부터의 열함유흐름에 따른 열변환에 의해 얻어지고; 연소 및/또는 스팀터빈영역으로부터의 열함유흐름으로부터 임의적으로 상기 부분산화처리와 통합된다. 연소터빈 배기가스로부터의 열이(1) 스팀터빈에서 사용하기 위한 과열스팀과; (2) 농축된 부가적 메탄의 존재여부에 따라 깨끗한 황이 없는 합성연료가스를 포화시킨 미리 가열된 물; (3) 상기 부분산화영역을 위해 미리 가열한 산소가스 및; (4) 기화된 LNG에 따라 이용된다. 공기압축기의 전, 중간, 후단계가 LNG와 함께 간접 가열변환에 의해 냉각됨으로써 따뜻해지거나 기화된다.

Liquid air energy storage and ammonia synthesis integrated device and method

本发明公开了一种液态空气储能与氨气合成集成装置及方法，包括液态空气储能循环系统和氨气合成循环系统，液态空气储能循环系统由空气分离液化单元和空气发电单元组成。用电低谷时段，多余电力驱动空气分离液化单元获取液态氮气，并存储在液态空气储罐；氨气合成循环系统中氮气的来源，一方面可以利用液态空气储罐中的液态氮气，另一方面也可以利用从空分厂中分离的气态氮气。用电高峰时段，液态空气储罐中的液态氮气经过加压预热后，一方面可以作为原料直接供给氨气合成循环系统，另一方面可以经过加热后进入空气透平机组膨胀发电，然后加压供给氨气合成循环系统。

Temperature swing adsorption method

(57)【要約】 【課題】 原料ガスから少なくとも二酸化炭素と水を除 去して精製ガスを作るための温度スイング吸着法を提供 する。 【解決手段】 原料ガスから全ての水と二酸化炭素の少 なくとも大部分とを吸着するのにアルミナを使用する。 随意に、更に二酸化炭素と炭化水素類を除去するため下 流にゼオライトの領域を設ける。

Liquefied air energy storage power generation system coupled with steam-water system of coal-fired power generating unit

本发明涉及一种耦合燃煤发电机组汽水系统的液化空气储能发电系统，包括空气压缩及凝结水加热系统、空气液化储能系统、空气膨胀发电系统及冷量回收储存系统；空气压缩及凝结水加热系统包括空气压缩机及换热器；空气液化储能系统与空气压缩及凝结水加热系统连接；空气膨胀发电系统与空气液化储能系统连接；冷量回收储存系统与空气膨胀发电系统及空气压缩及凝结水加热系统连接。本发明将燃煤发电机组与液化空气储能系统耦合，有效提高了火电厂深度调峰的灵活性，保证了电网整体调频水平，同时还可有效提高燃煤发电机组在深度调峰过程中机组的安全运行水平、降低设备损耗。

Method for carbon dioxide recovery from feed stream

本发明的方法是从含低浓度CO 2 的冷入口进料气流中回收CO 2 ，包括以下步骤。入口进料气流通过一个热交换器，由入口进料气流的压缩气流，以冷却该压缩气流。该压缩气流进一步冷却并压缩至高压，并送入蒸馏塔，在那里转变成含CO 2 的出口气体和高纯塔底液体CO 2 。膨胀第一部分塔底液体CO 2 ，得到第一次冷却的液体CO 2 冷冻剂液流，然后它由出口气体蒸发，从中回收冷凝的CO 2 。然后该冷凝的CO 2 再引入蒸馏塔中。膨胀第二部分塔底液体CO 2 ，得到第二次冷却的液体CO 2 冷冻剂物流，然后用它低温冷却输出的CO 2 产品。

Lng production with nitrogen removal

FIELD: cryogenic technology. SUBSTANCE: invention relates to cryogenic technology. A method and system for liquefying the supplied natural gas stream and removing nitrogen from it are proposed. The natural gas stream is cooled and liquefied in the main heat exchanger due to indirect heat exchange with the first refrigerant, thus forming the first LNG stream. The first LNG stream is expanded and fed into the distillation column. The flow of nitrogen-depleted bottom liquid is diverted from the distillation column to form a second, nitrogen-depleted LNG stream. The flow of nitrogen-enriched steam of the upper fraction is heated in the upper heat exchanger. They are compressed, liquefied due to indirect heat exchange with the first refrigerant, supercooled in the upper heat exchanger due to indirect heat exchange with nitrogen-enriched steam of the upper fraction and the recirculating flow formed from the first part of the heated steam of the upper fraction is expanded and fed it into the distillation column. The upper heat exchanger is separated from the main heat exchanger, and the entire cooling capacity for the upper heat exchanger is provided by heating the flow of nitrogen-enriched steam of the upper fraction. EFFECT: invention makes it possible to simplify the liquefaction system. 20 cl, 5 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 764 820 C1 (51) МПК F25J 1/00 (2006.01) F25J 3/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК F25J 1/0022 (2021.08); F25J 3/0209 (2021.08); F25J 3/0233 (2021.08) (21)(22) Заявка: 2021105989, 10.03.2021 (24) Дата начала отсчета срока действия патента: Дата регистрации: 21.01.2022 13.03.2020 US 16/818,168 (45) Опубликовано: 21.01.2022 Бюл. № 3 2 7 6 4 8 2 0 R U (54) ПРОИЗВОДСТВО СПГ С УДАЛЕНИЕМ АЗОТА (57) Реферат: Изобретение относится к криогенной технике. непрямого теплообмена с первым хладагентом, Предложены способ и система для сжижения переохлаждают в верхнем ...

Process to convert low grade heat source into power using dense fluid expander

提出了用于将热转化为动力的工艺，其中为使循环更适用于低级热，工作流体在与热源进行热交换后基本保持液态，并且用稠密流体膨胀器代替传统蒸汽膨胀器随后使液体工作流体做功膨胀。

Cooling system of multistage gas piston compressor

СИСТЕМА ОХЛАВДЕНИЯ МНОГОСТУПЕНЧАТОГО ГАЗОВОГО ПОРШНЕВОГО КОМПРЕССОРА, содержаща  промежуточ7 ные вод ные охладители между его ступен ми, отличающа с  тем, что, с. целью повышени  экономичности при сжатии влажного газа, система дополнительно содержит абсорбционные холодильные машины в количестве , соответствующем количеству ступеней компрессора, при этом генератор первой холодильной машины установлен после последней ступени компрессора, ее испаритель - перед первой ступенью .компрессора, а генераторы и испарители остальных холодильных машин установлены соответственно перед и после вод ного ладител , установленного между смежными ступен ми. COOLING SYSTEM OF MULTI-STAGE GAS PISTON COMPRESSOR, containing intermediate water coolers between its steps, characterized in that, c. In order to increase the efficiency of compression of a humid gas, the system additionally contains absorption chillers in an amount corresponding to the number of compressor stages, the generator of the first refrigerating machine is installed after the last stage of the compressor, its evaporator is before the first stage of the compressor, and the generators and evaporators of the remaining refrigerating machines installed, respectively, before and after the water ladder, installed between adjacent steps.

Compressor

압축 장치를 개시한다. 본 발명은 유체를 흡입하는 흡입부;와, 흡입부로부터 유입된 유체를 다단으로 압축하는 압축부;와, 압축된 공기를 배출하는 배출부;를 포함하되, 흡입부와, 압축부는 각각 복수로 이루어진 것;을 포함하는 것으로서, 제 1 단의 압축기에 있어서, 동일 단에 복수의 압축기를 설치하여서 유량을 2배 증가시킬 수 있다. A compression apparatus is disclosed. The present invention includes a suction unit for sucking the fluid; and a compression unit for compressing the fluid introduced from the suction unit into multiple stages; and a discharge unit for discharging the compressed air; wherein the suction unit and the compression unit are respectively provided in plurality. It is made; includes, in the compressor of the first stage, by installing a plurality of compressors in the same stage can increase the flow rate twice.

Method and device for generating two purified partial air streams

본 발명은 상이한 압력들 하에서 정화된 두 개의 부분 공기 스트림들을 발생시키기 위한 방법 및 장치에 관한 것이다. 전체 공기 스트림(1)은 제 1 전체 공기 압력으로 압축된다. 압축된 전체 공기 스트림(5)은 열 교환(4, 6)에 의해 제 1 전체 공기 압력 하에서 냉각수에 의해 냉각된다. 전체 공기 스트림(5)을 냉각하기 위한 냉각수와의 열 교환은 적어도 부분적으로 제 1 직접 접촉 냉각기(6)에서의 직접 열 교환으로서 수행된다. 냉각된 전체 공기 스트림(9)은 제 1 부분 공기 스트림(10) 및 제 2 부분 공기 스트림(11)으로 분리된다. 제 1 부분 공기 스트림(10)은 제 1 전체 공기 압력 하에서 제 1 정화 장치(18)에서 정화되고 제 1 정화된 부분 공기 스트림(19)을 발생시킨다. 제 2 부분 공기 스트림(11)은 고압(12)으로 재압축되고 이는 제 1 전체 공기 압력보다 더 높다. 재압축된 제 2 부분 공기 스트림(14)은 직접 열 교환(13,15)에 의해 제 2 직접 접촉 냉각기(15)에서 냉각수에 의해 냉각된다. 냉각된 제 2 부분 공기 스트림(17)은 제 2 정화 장치(30)에서 더 높은 압력 하에서 정화되어, 제 2 정화된 부분 공기 스트림(31)을 발생시킨다. The present invention relates to a method and apparatus for generating two partial air streams purified under different pressures. The entire air stream 1 is compressed to a first total air pressure. The compressed total air stream (5) is cooled by cooling water under a first total air pressure by heat exchange (4, 6). The heat exchange with the cooling water for cooling the total air stream 5 is carried out at least in part as direct heat exchange in the first direct contact cooler 6. The cooled total air stream (9) is separated into a first partial air stream (10) and a second partial air stream (11). The first partial air stream 10 is purified in the first purifier 18 under a first total air pressure and produces a first purified partial air stream 19. The second partial air stream 11 recompresses to a high pressure 12 which is higher than the first total air pressure. The recompressed second partial air stream 14 is cooled by the cooling water in the second direct contact cooler 15 by direct heat exchange 13,15. The cooled second partial air stream 17 is purified at a higher pressure in the second purifier 30 to produce a second purified partial air stream 31.

Gas supply systems for gas engines

극저온 열교환기, 증발가스 예열기를 구비하는 증발가스 압축기 및 압신기(compander)를 구비하는 질소 회로를 포함하고, 증발가스 재액화 설비에 통합되며, 상기 증발가스는 화물 탱크로부터 나오는 액화 천연 가스 또는 재액화 설비로부터 나온 응축물의 액화 천연 가스 형태인, 이중연료 엔진 또는 가스 엔진용 가스 공급 시스템이 개시되어 있다. 상기 가스 공급 시스템에는, 엔진에 의해 연소될 가스로부터 나오는 냉각 듀티를 재액화 설비에서 활용하기 위해, 가스 공급 시스템에는 냉각 듀티를 추출하는 증발기(옵티마이저) 및/또는 냉각 듀티 추출을 최적화하는 데에 사용되는 중간 매체를 가열하는 열원과 하나 이상의 펌프를 포함하는 폐회로 내에 배치되어 있는 증발기가 마련되어 있다. A cryogenic heat exchanger, an evaporative gas compressor with an evaporative gas preheater and a nitrogen circuit with a compander, which are integrated into an evaporative gas reliquefaction plant, which is a liquefied natural gas or ash from a cargo tank. A gas supply system for a dual fuel engine or gas engine, in the form of liquefied natural gas of condensate from a liquefaction plant, is disclosed. In the gas supply system, in order to utilize the cooling duty from the gas to be burned by the engine in the reliquefaction facility, the gas supply system may be used to optimize the evaporator (optimizer) and / or cooling duty extraction that extracts the cooling duty. An evaporator is provided which is arranged in a closed circuit comprising a heat source for heating the intermediate medium used and one or more pumps.

Liquefaction of industrial gas and hydrocarbon gas

Gas compressor plant equipped with power recovering means

Industrial and hydrocarbon gas liquefaction

산업용 가스 또는 가스 혼합물(탄화수소 및/또는 비 탄화수소)의 액화 방법은 액화 공정 중에 상기 가스 또는 가스 혼합물을 냉각시키는 데 사용되는 변형된 수화 암모니아 흡수식 냉동 시스템(ARP)을 사용한다. 상기 가스는 그 임계점 이상으로 압축될 수 있고, 압축열 에너지는 ARP를 작동하는데 필요한 열 에너지의 일부 또는 전부를 제공하기 위하여 회수될 수 있다. 상기 방법은 Joule Thomson (JT) 단열 팽창 과정을 사용하여 특수 극저온 회전 장비가 필요하지 않는다. 수화 암모니아 흡수식 냉동 시스템은 증기 흡수 탑(VAT, vapour absorber tower)을 포함하며, 이는 무수 암모니아 증기가 과냉각된 린(lean) 수화 암모니아 용액에 흡수될 때 시스템 내의 용액의 열 및 응축 에너지 열의 일부 또는 전부를 회수할 수 있다. VAT를 포함하는 변형된 ARP는 암모니아 가스 냉각기 작동 온도가 -71℃로 낮아지도록 10kPa까지 낮은 작동 압력을 달성할 수 있다. The liquefaction process for industrial gases or gas mixtures (hydrocarbons and/or non-hydrocarbons) uses a modified hydrated ammonia absorption refrigeration system (ARP) which is used to cool the gas or gas mixture during the liquefaction process. The gas may be compressed above its critical point, and the thermal energy of compression may be recovered to provide some or all of the thermal energy required to operate the ARP. The method uses a Joule Thomson (JT) adiabatic expansion process and does not require special cryogenic rotating equipment. Hydrated ammonia absorption refrigeration systems include a vapor absorber tower (VAT), which is part or all of the heat and condensation energy heat of the solution in the system when the anhydrous ammonia vapor is absorbed into the supercooled lean hydrated ammonia solution. can be recovered A modified ARP with VAT can achieve operating pressures as low as 10 kPa to bring the ammonia gas cooler operating temperature down to -71°C.

Energy production method

FIELD: production of energy from carbonaceous fuel. SUBSTANCE: fuel gas and sensible heat are produced by partial oxidation of fuel by oxygen or oxygen-containing gas. Sensible heat or large part of this heat is conveyed to energy producing unit together with fuel gas. Energy producing unit is turbine cycle with moisture-laden air. This makes it possible to use one and the same set of internal combustion turbine both when using set in turbine cycle with moisture-laden air and when integrating the set into gasification plant. EFFECT: enlarged operating capabilities of set. 5 cl, 1 dwg (19) 13) ВО ‘” 2 121 588 Сл (51) МК р (02 С 3/28, Е 01 К 23/06 РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 95119997/06, 16.02.1994 (71) Заявитель: Нюкомб Сюнергетикс АБ ($Е) (30) Приоритет: 16.02.1993 ЗЕ 9300500-7 (72) Изобретатель: Ингвар Ландельв ($Е) (46) Дата публикации: 10.11.1998 (73) Патентообладатель: (56) Ссылки: ЦЗ 5117623 А, 1992. ЕР 0103914 А2, Нюкомб Сюнергетикс АБ (ЗЕ) 1984. ЕР 0259114 ВЛ, 19388. 50 59*637 А, 1941. 5Ц 1309913 АЗ, 1984. $Ц 1327795 А, 1986. С1 (54) СПОСОБ ПРОИЗВОДСТВА ЭНЕРГИИ _. Загрузка (57) Реферат: Способ может быть использован для з производства энергии из углеродистого | | [ал 2| | М топлива. Частичным окислением топлива > кислородом или кислородсодержащим газом 4А получают горючий газ и физическую теплоту, 3 3 ззяАагстс ПЧ ГЭ при этом физическую теплоту или большую ее часть передают в энергопроизводящий блок вместе С горючим газом. Энергопроизводящий блок является турбинным циклом с увлажненным воздухом и дает возможность использовать один и тот же агрегат турбины внутреннего сгорания и в случае использования его в турбинном цикле с увлажненным воздухом, и в случае интегрирования его в газификационную установку. 4 з.п. ф-лы, 1 ил. -----= пример 2] р 13 К ----- ыы ъъ%--- 31| 133 — электроэнергия 32 24 нат-Цикл 2? Фиг.1 21215883 КО ззяАагстс ПЧ ГЭ КУЗЗАМ АСЕМСУ ГОК РАТЕМТ$ ...

System and method for cooling a bog stream

증발 재액화 플랜트에서 압축 전에 증발가스 스트림을 냉각하는 시스템은 폐쇄 루프 냉각 시스템과 열교환하기 전에 압축기(11;11'')로 BOG를 급송하기 위한 라인(10)을 포함한다. 상기 폐쇄 루프 냉각 시스템은 압축기들(2,3,4) 및 익스팬더들(8,9) 및 증발가스(BOG) 스트림과의 열 교환을 위한 다수의 열교환기들을 포함한다. 상기 익스팬더들(8,9)은 직렬로 배열된다. 상기 급송 라인(10)의 예냉각기는 상기 폐쇄 루프 냉각 시스템에 스트림적으로 연결(32,33)되어, 상기 BOG가 압축 전에 폐쇄 루프 냉각 시스템의 냉매의 일부와 열교환하여 예냉각된다.

Process and apparatus for the liquefaction of carbon dioxide

유입구부터 유출구까지의 이산화탄소 통과를 위한 플로우 채널을 포함하는 이산화탄소 액화 장치가 개시된다. 상기 채널은 마지막 압축기(8) 및 냉각기(9, 10, 13)의 플로우 채널 하부스트림에 있는 팽창챔버(14, 15)와 일련하여 배열된 다수 압축기(2, 5, 8) 및 냉각기(4, 7, 9, 10, 13)를 포함한다. 또한 상기 장치는 상기 팽창 챔버(15)로부터 상기 마지막 압축기(8) 및 냉각기(9, 10, 13)의 상기 플로우 채널(3) 상부스트림으로 기체상의 이산화탄소를 되돌리도록 배치되는 재순환 채널(16)을 포함한다. 이산화탄소, 액화

Coal bed gas liquefaction system

本实用新型涉及煤层气液化技术领域，尤其涉及一种煤层气液化系统，包括：两级压缩单元，两级压缩单元包括第一压缩机和第二压缩机，第一压缩机与第二压缩机连接，第一压缩机上设置有预处理后的煤层气的入口；冷却单元，冷却单元包括第一水冷器和第二水冷器，第一水冷器设置在第一压缩机与第二压缩机之间，第二水冷器连接在第二压缩机之后；斯特林制冷机，斯特林制冷机进口与第二水冷器连接；储液罐，储液罐的进口与斯特林制冷机出口连接。本实用新型通过外设的斯特林制冷机，提高了制冷效率；通过两级压缩单元压缩增压和冷却单元降温，提高了煤层气中甲烷的液化温度，同时降低了制冷机的冷负荷，从而降低了整个系统的功耗。

The improvement of air cleaning member

一种液态空气能量存储系统，包括空气液化器、用于存储液化空气的液态空气储存设施以及与所述液态空气存储设施联接的功率恢复单元。所述空气液化器包括空气入口、用于净化进气的吸附空气净化单元以及用于液化净化的空气的冷箱。所述功率恢复单元包括：泵，用于加压来自所述液态空气存储设施的液化空气；蒸发器，用于将高压液化空气转换成高压气态空气；膨胀涡轮，该膨胀涡轮能够由所述高压气态空气驱动；发电机，用于从所述膨胀涡轮生成电力；以及排放部，用于排放来自所述膨胀涡轮的低压气态空气。所述排放部联接至所述吸附空气净化单元，使得从所述膨胀涡轮排放的所述低压气态空气的至少一部分能够用于使所述吸附空气净化单元再生。

Configurations and methods for offshore lng regasification and heating value conditioning

Contemplated plant configurations and methods employ a vaporized and supercritical LNG stream at an intermediate temperature that is expanded, wherein refrigeration content of the expanded LNG is used to chill one or more recompressor feed streams and to condense a demethanizer reflux. One portion of the so warmed and expanded LNG is condensed and fed to the demethanizer as reflux, while the other portion is expanded and fed to the demethanizer as feed stream. Most preferably, the demethanizer overhead is combined with a portion of the vaporized and supercritical LNG stream to form a pipeline product.

Heat reuse method for cooler used with compressor

Method and apparatus for compressing and cooling air

本発明は、間接的な熱による交換のための手段を持たない、空気の極低温分離のための設備から上流側で空気を圧縮および冷却するための方法に関し、湿気のある空気がコンプレッサー（３）内で圧縮され、このコンプレッサー内で圧縮された空気が間接的な熱交換を有する第１の交換器（１３）内で冷却され、第１の交換器における冷却から上流側および／或いは下流側で空気から水（１１、１９）が回収され、二酸化炭素および／或いは水の精製された空気を製造するため、第１の交換器内で冷却された空気が精製ユニット（４５）へ送られ、精製された空気が極低温分離設備へ送られ、少なくとも１つのガスが極低温分離設備から回収され、回収された水が設備からのガスと混合され、製造された混合物が混合物内の水の凝固の温度より高い温度であり、ガスと混合された水が第１の交換器内で再加熱される。

Process and apparatus for purification of carbon dioxide

A process for the low temperature purification of CO 2 , wherein CO 2 is separated from a gaseous feed stream comprising at least 30 mol% CO 2 and at least one other gas having a lower boiling point than CO 2 , the process comprising the steps of: (i)cooling and partially condensing the feed stream; (ii)passing the cooled and partially condensed feed stream from step (i) to a vapour-liquid separator to produce a vapour stream having reduced CO 2 content relative the feed stream and a liquid stream having increased CO 2 content relative to the feed stream; (iii)dividing the liquid stream from step (ii) into at least two streams; and (iv)expanding and heating at least one of the at least two streams from step (iii); wherein cooling in step (i) is provided at least in part by heat exchange during heating of the liquid stream in step (iv).

Treatment of flue gas from an oxyfuel combustion process

Carbon monoxide (CO) may be removed from flue gas generated by oxyfuel combustion of a hydrocarbon or carbonaceous fuel, by contacting the flue gas, or a CO-containing gas derived therefrom, at a first elevated temperature, e.g. at least 80° C., and at a first elevated pressure, e.g. at least 2 bar (0.2 MPa), with at least one catalyst bed comprising a CO-oxidation catalyst in the presence of oxygen (O 2 ) to convert CO to carbon dioxide and produce carbon dioxide-enriched gas. The carbon dioxide produced from the CO may be recovered from the carbon dioxide-enriched gas using conventional carbon dioxide recovery techniques. NO in the flue gas may also be oxidized to nitrogen dioxide (NO 2 ) and removed using conventional NO 2 removal techniques, or may be reduced in the presence of a reducing gas to nitrogen (N 2 ) which does not have to be removed from the gas.

Process for feed gas cooling in reboiler during CO2 separation

An improved process for the separation of carbon dioxide from the flue gas of an oxy-combustion power plant is provided. An inlet stream containing carbon dioxide and oxygen is at least partially condensed in the reboiler of a stripping column. The condensed inlet stream is then separated in a separator, thereby producing a first liquid stream and a first gas stream. The first liquid stream is then separated into a top gas stream and a bottom liquid stream in the stripping column. The top gas stream is then warmed by indirect heat exchange in the heat exchanger. The warmed top gas stream is then recycled and combined with the inlet stream.

Method for carbon dioxide recovery from a feed stream

The method of the invention recovers CO₂ from an inlet cold feed stream containing a low concentration thereof, and includes the following steps. An inlet feed stream is passed through a heat exchanger, against a compressed flow of the inlet feed stream, to cool the compressed flow. The compressed flow is further cooled and compressed to a high pressure, fed to a distillation column and there converted into a vent gas including CO₂ and a high purity bottom liquid CO₂. A first portion of the bottom liquid CO₂ is expanded to achieve a first cooled liquid CO₂ refrigerant flow, which is then vaporized against the vent gas to recover condensed CO₂ therefrom. The condensed CO₂ is then reintroduced into the distillation column. A second portion of the bottom liquid CO₂ is expanded to achieve a second cooled liquid CO₂ refrigerant flow, which is then used to subcool the CO₂ product output.

Carbon dioxide and acid gas removal and recovery process for fossil fuel fired power plants

Carbon dioxide production system with integral vent gas condenser

A system for producing carbon dioxide, particularly from a feed which contains significant levels of light contaminants, wherein light overhead from a distillation column is partially condensed against heat exchange fluid containing both carbon dioxide and light contaminants and the resulting heat exchange fluid passed into the feed for the distillation column.

Method and apparatus for enhancing carbon dioxide recovery

A process and an apparatus for producing substantially pure carbon dioxide from a carbon dioxide feed containing from about 80% to about 95% volume of carbon dioxide.

Process and apparatus for separating a gas rich in carbon dioxide by distillation

In a process for separating a gas rich in carbon dioxide by distillation, the gas rich in carbon dioxide is cooled in a heat exchanger (3) and is sent to a distillation column (5), a gas (6) depleted in carbon dioxide is withdrawn from the top of the column and a liquid (7) enriched in carbon dioxide is withdrawn from the bottom of the column, a gas enriched in carbon dioxide is compressed in a compressor (17) down to a first pressure and at least one portion of the gas enriched in carbon dioxide originating from the compressor is expanded from the first pressure to a second pressure lower than the first pressure, for example the pressure of the column, and the expanded gas is used to heat the bottom of the column.

Method and system for separating carbon dioxide from flue gas

The method for separating carbon dioxide from flue gas comprises cooling the compressed flue gas in heat exchangers (3a, 3b) separating a carbon dioxide rich liquid from a carbon dioxide lean gas, supplying the carbon dioxide rich liquid and the carbon dioxide lean gas into a distillation column (8), separating in the distillation column (8) non-condensable gas from carbon dioxide liquid, heating the carbon dioxide liquid (CDL) at a cold side of a reboiler (14) generating a purified carbon dioxide liquid (PCDL), expanding the purified carbon dioxide liquid (PCDL) and supplying the expanded carbon dioxide liquid (ECDL) to the heat exchangers (3a, 3b) for cooling, supplying the expanded carbon dioxide liquid (ECDL) from the heat exchangers (3a, 3b) to a high pressure compressor (25) to generate a compressed carbon dioxide vapor (CCDV), supplying a part of the compressed carbon dioxide vapor (CCDV) from the high pressure compressor (25) to a warm side of the reboiler (14) generating a cooled carbon dioxide liquid (CCDL), expanding the cooled carbon dioxide liquid (CCDL) and passing the cooled carbon dioxide liquid (CCDL) through the heat exchangers (3a, 3b) for cooling. The purified carbon dioxide liquid (PCDL) and the cooled carbon dioxide liquid (CCDL) are directly forwarded to the at least a heat exchanger (3a, 3b).

Carbon dioxide production system with integral vent gas condenser

A system for producing carbon dioxide, particularly from a feed which contains significant levels of light contaminants, wherein light overhead from a distillation column is partially condensed against heat exchange fluid containing both carbon dioxide and light contaminants and the resulting heat exchange fluid passed into the feed for the distillation column.

LCD liquefaction process

Process for feed gas cooling in reboiler during co2 separation

An improved process for the separation of carbon dioxide from the flue gas of an oxy-combustion power plant is provided. An inlet stream containing carbon dioxide and oxygen is at least partially condensed in the reboiler of a stripping column. The condensed inlet stream is then separated in a separator, thereby producing a first liquid stream and a first gas stream. The first liquid stream is then separated into a top gas stream and a bottom liquid stream in the stripping column. The top gas stream is then warmed by indirect heat exchange in the heat exchanger. The warmed top gas stream is then recycled and combined with the inlet stream

LNG Regasification process and liquid air energy storage system

본 발명은 액화가스 공급부에서 액화가스를 공급하는 제1기화 라인; 제1기화 라인에 배치되고 액화가스와 제1작동 유체가 열교환하는 제1열교환기; 제1열교환기를 포함하고 제1작동 유체가 순환하는 제1순환 라인; 제1기화 라인에 배치되고 액화가스와 제2작동 유체가 열교환하는 제2열교환기; 제2열교환기를 포함하고 제2작동 유체가 순환하는 제2순환 라인; 액화가스 공급부와 제1열교환기 사이에서 제1기화 라인과 분기되고, 제1열교환기와 제2열교환기 사이에서 제1기화 라인과 연결되는 제2기화 라인; 제2기화 라인에 배치되고 액화가스와 공기가 열교환하는 제3열교환기; 제3열교환기를 포함하고 공기 공급부와 액체공기 저장부를 연결하는 공기액화 라인; 액체공기 저장부에서 액체공기를 공급하는 공기발전 라인; 및 제1순환 라인, 제2순환 라인 및 공기발전 라인에 각각 설치되어 제1작동 유체, 제2작동 유체 및 액체공기를 이용하여 동력을 발생시키는 제1, 제2, 및 제3 터빈을 포함하는 액체공기 저장 및 발전 시스템으로서, 본 발명의 시스템은, 액화가스 특히, 액화천연가스 재기화 공정 및 액체공기 에너지 저장 기술을 통합하여 에너지 효율을 높이고, 액화천연가스 재기화 공정에서의 천연가스 압력 및 액체공기 에너지의 저장 압력을 조절하여 안전성 및 경제성이 우수하며, 수요에 맞는 유연한 운영이 가능한 액화천연가스 재기화 공정 및 액체공기 에너지 저장 기술이 결합된 시스템을 제공한다. The present invention is a first vaporization line for supplying liquefied gas from the liquefied gas supply; a first heat exchanger disposed in the first vaporization line and exchanging heat between the liquefied gas and the first working fluid; a first circulation line including a first heat exchanger and through which a first working fluid circulates; a second heat exchanger disposed in the first vaporization line and exchanging heat between the liquefied gas and the second working fluid; a second circulation line including a second heat exchanger and through which a second working fluid circulates; a second vaporization line branched from the first vaporization line between the liquefied gas supply unit and the first heat exchanger, and connected to the first vaporization line between the first heat exchanger and the second heat exchanger; a third heat exchanger disposed in the second vaporization line and exchanging heat between liquefied gas and air; an air liquefaction line including a third heat exchanger and connecting the air supply unit and the liquid air storage unit; an air power generation line for supplying liquid air from the liquid air storage unit; and first, second, and third turbines respectively installed in the first circulation line, the ...

Method and device for condensing a carbon dioxide-rich gas stream

本发明涉及一种用于冷凝富含二氧化碳的气体流的方法，其中水流通过与富含二氧化碳的流进行热交换而被加热，该富含二氧化碳的流至少部分地冷凝，所述被加热的水流被送至用于压缩富含二氧化碳的流或从中获得富含二氧化碳的流的流体的至少一个压缩机(3，21)，以便至少部分地冷却所述压缩机的至少一个级。

System and method for liquid air production, power storage and power release

본 발명은 유입 공기를 수직방향의 냉각관 조립체 안으로 유입되도록 유도하는 단계와, 공기를 냉각하고 수분 부분을 제거하는 단계를 포함하는 에너지 저장 및 방출 시스템 및 장치에 관한 것이다. 상기 공기는 상기 냉각관 조립체로부터 밖으로 향하여 압축된다. 남아있는 수분은 실질적으로 제거된다. 상기 공기는 냉매 루프 공기를 사용하여 실질적으로 액화되도록 주 열교환기에서 냉각된다. 상기 실질적으로 액화된 공기는 저장 장치로 향한다. 에너지 방출 모드에서, 작동 루프 공기는 상기 방출된 액체 공기가 실질적으로 증발되도록 방출된 액체 공기를 가온시키고, 상기 방출된 액체 공기는 상기 작동 루프 공기가 실질적으로 액화되도록 상기 작동 루프 공기를 냉각시킨다. 상기 실질적으로 증발된 공기는 연소실로 향하여 연소 흐름에 의하여 연소된다. 팽창된 연소가스의 일부는 상기 방출된 액체 공기를 가열하여 실질적으로 증발시키는데 사용될 수 있다.

Energy recovery method

FIELD: power industry. SUBSTANCE: method of energy recovery by gas compression in compressor plant (1) with two or more compression stages. Each stage is formed by a compressor (2, 3). A heat exchanger (4, 4) consisting of first and second part two is placed downstream of each compressor. Cooling agent is fed in sequence through the second part of at least two heat exchangers (4, 5). Sequence of cooling agent passage through heat exchangers (4, 5) is selected so that temperature at the inlet of the first part of at least one next heat exchanger was not lower than temperature at the inlet of previous heat exchanger if viewed along the flow of cooling agent. At least one heat exchanger (4 and/or 17) has a third part for cooling agent. EFFECT: higher energy recovery compared to existing methods of energy recovery. 25 cl, 3 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 511 816 C2 (51) МПК F04D 29/58 (2006.01) F04B 39/06 (2006.01) F04C 29/04 (2006.01) F02C 7/143 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2012125059/06, 27.12.2010 (24) Дата начала отсчета срока действия патента: 27.12.2010 (72) Автор(ы): ЯНСЕНС Стейн Йозеф Рита Йоханна (BE) (73) Патентообладатель(и): АТЛАС КОПКО ЭРПАУЭР, НАМЛОЗЕ ВЕННОТСХАП (BE) Приоритет(ы): (30) Конвенционный приоритет: R U 25.01.2010 BE 2010/0038 (43) Дата публикации заявки: 20.12.2013 Бюл. № 35 (45) Опубликовано: 10.04.2014 Бюл. № 10 2 5 1 1 8 1 6 02.11.2005. GB 1025538 A, (BROWN BOVERI & COMPANY LIMITED), 14.04.1966. GB 105748 A, (ESCHER WYSS & CIE.), 19.07.1917. EP 0015535 A1, (MASCHINENFABRIK AUGSBURG-NURNBERG AKTIENGESELLSCHAFT), 17.09.1980. US 4936109 A, (COLUMBIA ENERGY STORAGE INC), 26.06.1990. SU 1076633 A1, (ВСЕСОЮЗНОЕ НАУЧНОПРОИЗВОДСТВЕННОЕ (см. прод.) C 2 C 2 (56) Список документов, цитированных в отчете о поиске: EP 1591644 A1, (MAN TURBO AG), R U 2 5 1 1 8 1 6 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 15.06.2012 (86) Заявка PCT: BE ...

Compressed air energy storage system coupled and integrated with cryogenic air separation device

本发明提供了一种与深冷空分装置耦合集成的压缩空气储能系统，属于能量储存与利用技术领域。本发明从峰谷电差和分时电价政策出发，将深冷空分与压缩空气储能耦合集成，通过用电负荷削峰填谷大幅降低运行成本。由于关键设备、运行维护、管理模式等方面高度相似，本发明对储能装置和空分装置的空气压缩机整体考虑，减少设计裕量和设备投资；合理利用空分装置产生的废热，提高储能系统的发电效率；在电价高位阶段由压缩空气储能系统直接向空分装置提供带压空气，大幅减少高成本电能的消耗。通过深冷空分装置和压缩空气储能系统的耦合集成，用电高峰阶段与用电低谷阶段的总运行成本可节约45％，压缩空气储能装置的投资回收期约为5年。

Liquefied air energy storage-temperature difference power generation coupling system and working method thereof

一种液化空气储能‑温差发电耦合系统及其工作方法。该系统包括：空气压缩装置、空气液化装置、液态空气加压气化装置、空气膨胀装置、温差发电装置及储热蓄冷装置。其工作方法为：在储能阶段，空气压缩装置、空气液化装置和储热蓄冷装置处于工作状态，消耗外部电能实现空气液化存储及压缩热回收；在释能阶段，为超临界工作模式，液态空气加压气化装置、空气膨胀装置、温差发电装置以及储热蓄冷装置处于工作状态，通过空气膨胀装置和温差发电装置向外供电，并完成液态空气气化潜热回收。本发明在液化空气储能系统中引入半导体温差发电装置，利用压缩余热和膨胀余冷驱动温差发电装置输出额外电能，不仅可以提升系统运行效率，还可以减少废热排放。

Method and apparatus for the reliquefaction of a vapour

기화된 액화 천연 가스는 예를 들어 저장 탱크(10)로부터 흘러 증기 압축 스테이지(40) 및 (42)에서 압축된다. 생성된 압축 증기는 응축기(46)에서 응축되며, 상기 응축물은 탱크(10)로 되돌아간다. 응축기(46)는 브레이튼 사이클(60)에서 흐르는 작동 유체, 예를 들면 질소에 의해 냉각된다. 브레이튼 사이클은 응축기(46)를 통하는 통로의 상기 압축 천연 가스 증기의 상류에 상기 압축된 천연 가스 증기로부터 압축열을 제거하는 열 교환기(86)을 포함한다. 또한, 응축기(46)로부터의 작동 유체 출구와 열 교환기(86)로의 작동 유체 입구를 매개하는 브레이튼 사이클(60)의 영역으로부터 작동 유체의 일부가 회수되고, 그 회수된 작동 유체는 압축 스테이지(40) 및 (42)를 매개하는 천연 가스 증기로부터 압축열을 제거하는 또 다른 열 교환기(88)를 통해 흐른다. 상기 회수된 작동 유체는 브레이튼 사이클(60)로 되돌아간다. The vaporized liquefied natural gas flows, for example, from the storage tank 10 and is compressed in the vapor compression stages 40 and 42. The resulting compressed vapor is condensed in a condenser 46 and the condensate is returned to the tank 10. The condenser 46 is cooled by a working fluid flowing in the Brayton cycle 60, for example nitrogen. The Brayton cycle includes a heat exchanger (86) that removes the heat of compression from the compressed natural gas vapor upstream of the compressed natural gas vapor in the passageway through the condenser (46). A portion of the working fluid is also withdrawn from the region of the Brayton cycle 60 that mediates the working fluid outlet from the condenser 46 and the working fluid inlet to the heat exchanger 86, 40 and 42 through another heat exchanger 88 which removes the heat of compression from the natural gas vapor. The recovered working fluid returns to the Brayton cycle (60).

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 -71 C.

Precooling of natural gas by high pressure compression and expansion

Method and system for the small-scale production of liquified natural gas (lng) from low-pressure gas

A method and system for the small-scale production of LNG. The method comprising: configuring a prime mover to be operable communication with a multi-stage compressor; configuring the prime mover to be in fluid communication with an ammonia absorption chiller; configuring the ammonia absorption chiller to be in fluid communication with the multi-stage compressor; operating the ammonia absorption chiller using waste heat from a prime mover; pre-cooling a first stream of natural gas using cooled fluid from the ammonia absorption chiller; cooling a first portion of the first stream of natural gas, using an expansion valve, into a two-phase stream; cooling a second portion of the first stream to liquefied natural gas, using the two-phase stream as a cooling fluid; delivering the second portion of the first stream as LNG to a low-pressure LNG tank; cooling a third portion of the first stream of natural gas in a turbo-expander; separating liquid heavies out of the third portion of the first stream of natural gas; and delivering the liquid heavies to a pressure tank.

Process for enhanced closed-circuit cooling system

An apparatus and method for cooling a gas stream is provided comprising at least one heat exchanger in which a gas stream is cooled against a cooling liquid, whereby the cooling liquid temperature increases from a first temperature to a second temperature, at least one air cooler for cooling the cooling liquid after passing though the at least one heat exchanger, surface area of the at least one air cooler being designed to decrease temperature of the cooling liquid to the first temperature; a pump; and conduits to form a closed-circuit for the cooling liquid to pass continuously through the at least one heat exchanger and the at least one air cooler. The ratio of surface area of the at least one air cooler to the surface area of the at least one heat exchanger is optionally 12 or lower, and the difference of temperature between the second temperature and first temperature being greater than 15° C.

Method of cooling boil off gas and an apparatus therefor

부유 운송 선박의 액화된 에탄 카고로부터의 보일 오프 가스 스트림을 냉각시키는 방법에 있어서, 상기 방법은 적어도, 압축된 BOG 배출 스트림을 제공하기 위해 적어도 제 1 스테이지 및 최종 스테이지를 포함하는 2 개 또는 그 초과의 압축의 스테이지들에서 상기 액화된 에탄 카고로부터의 보일 오프 가스 스트림을 압축하는 단계 - 상기 제 1 압축 스테이지는 제 1 스테이지 배출 압력을 가지며, 상기 최종 압축 스테이지는 최종 스테이지 흡입 압력을 가지며 그리고 하나 또는 그 초과의 중간의, 선택적으로 냉각된, 압축된 BOG 스트림들이 압축의 연속 스테이지들 사이에 제공됨 -; 냉각되고 압축된 제 1 BOG 스트림을 제공하기 위해서 하나 또는 그 초과의 제 1 냉각제 스트림들에 대해서 압축된 BOG 배출 스트림을 냉각시키는 단계; 냉각되고 압축된 제 2 BOG 스트림을 제공하기 위해서 적어도 하나의 제 2 냉각제 스트림에 대해서 냉각되고 압축된 제 1 BOG 스트림을 냉각시키는 단계; 냉각되고 압축된 제 3 BOG 스트림을 제공하기 위해 제 3 냉각제 스트림에 대해서 냉각되고 압축된 제 2 BOG 스트림을 냉각시키는 단계; 팽창되고 냉각된 제 1 BOG 스트림을 제공하기 위해서 냉각되고 압축된 제 3 BOG 스트림의 일부를 제 1 스테이지 배출 압력과 최종 스테이지 흡입 압력 사이의 압력으로 팽창시키는 단계; 팽창되고 가열된 제 1 BOG 스트림을 제공하기 위해서 제 3 냉각제 스트림으로서 팽창되고 냉각된 제 1 BOG 스트림을 사용하는 단계; 및 팽창되고 가열된 제 1 BOG 스트림을 제 2 냉각제 스트림으로서 사용하는 단계를 포함한다. A method for cooling a boil off gas stream from a liquefied ethane cargo on a floating transport vessel, the method comprising at least: compressing the boil off gas stream from the liquefied ethane cargo in two or more stages of compression comprising at least a first stage and a final stage to provide a compressed BOG effluent stream, the first compression the stage has a first stage discharge pressure, the final compression stage has a final stage suction pressure and one or more intermediate, optionally cooled, compressed BOG streams are provided between successive stages of compression; cooling the compressed BOG effluent stream with respect to the one or more first coolant streams to provide a cooled compressed first BOG stream; cooling the cooled compressed first BOG stream with respect to the at least one second coolant stream to provide a cooled compressed second BOG stream; cooling the cooled compressed second BOG stream relative to the third coolant stream to provide a cooled compressed third BOG stream; expanding a portion of the cooled compressed third BOG stream to a pressure between the first stage outlet pressure and the final stage inlet pressure to ...

Refrigeration device and installation

Dispositif de réfrigération à basse température comprenant un circuit de travail (10) formant une boucle et contenant un fluide de travail, le circuit (10) de travail formant un cycle comprenant en série: un mécanisme (2, 3) de compression, un mécanisme (4, 5, 6) de refroidissement, un mécanisme (7) de détente et un mécanisme (6, 8) de réchauffement, le dispositif (1) comprenant un échangeur (8) de chaleur de réfrigération destiné à extraire de la chaleur à au moins un organe (125) par échange de chaleur avec le fluide de travail circulant dans le circuit (10) de travail, le mécanisme (2, 3) de compression comprenant deux compresseurs (2, 3) distincts, le mécanisme (4, 5, 6) de refroidissement du fluide de travail comprenant deux échangeurs (4, 5) de chaleur de refroidissement disposés respectivement à la sortie des deux compresseurs (2, 3) et assurant un échange de chaleur entre le fluide de travail et un fluide de refroidissement, chaque échangeur (4, 5 ) de chaleur de refroidissement comprenant une entrée (24, 25) de fluide de refroidissement et une sortie (34, 35) de fluide de refroidissement, caractérisé en ce que la sortie (34, 35) de fluide de refroidissement de l’un des deux échangeur (4, 5) de chaleur de refroidissement est raccordée à l’entrée (25, 24) de fluide de refroidissement de l’autre échangeur (5) de chaleur de refroidissement. Figure de l’abrégé : Fig. 1 A low temperature refrigeration device comprising a working circuit (10) forming a loop and containing a working fluid, the working circuit (10) forming a cycle comprising in series: a compression mechanism (2, 3), a (4, 5, 6), an expansion mechanism (7) and a heating mechanism (6, 8), the device (1) comprising a refrigeration heat exchanger (8) intended to extract heat from at least one member (125) by heat exchange with the working fluid circulating in the working circuit (10), the compression mechanism (2, 3) comprising two separate compressors (2, 3), the mechanism (4, 5, 6) for cooling the ...

PROCESS FOR PRODUCING BIOMETHANE BY PURIFYING BIOGAS FROM NON-HAZARDOUS WASTE STORAGE FACILITIES (ISDND) AND INSTALLATION FOR IMPLEMENTING THE METHOD

Procédé de production de bio méthane par épuration de biogaz issus d'installations de stockage de déchets non-dangereux (ISDND) selon lequel : - on comprime le flux gazeux initial, - on introduit le flux de gaz à épurer dans au moins un adsorbeur modulé en pression (PSA) chargé en adsorbants aptes à adsorber réversiblement les COV, - on soumet le flux gazeux à au moins une séparation membranaire pour séparer partiellement le CO2 et l'O2 du flux gazeux, - on introduit le rétentat issu de la séparation membranaire dans au moins un adsorbeur modulé en température (PTSA) chargé en adsorbants aptes à adsorber réversiblement la majeure partie du CO2 restant, - on soumet le flux gazeux à une séparation cryogénique dans une colonne de distillation pour séparer l'O2 et l'N2 du flux gazeux, - on récupère le flux riche en CH4 issu de la séparation cryogénique. Installation pour la mise en œuvre du procédé Process for producing bio methane by biogas purification from non-hazardous waste storage facilities (ISDND) according to which: - the initial gas flow is compressed, - the stream of gas to be purified is introduced into at least one modulated adsorber in pressure (PSA) loaded with adsorbents capable of reversibly adsorbing VOCs, the gaseous stream is subjected to at least one membrane separation to partially separate the CO2 and O2 from the gas stream, and the retentate resulting from the membrane separation is introduced. in at least one temperature-modulated adsorber (PTSA) loaded with adsorbents capable of reversibly adsorbing most of the remaining CO2, the gas stream is subjected to cryogenic separation in a distillation column to separate the O 2 and N 2 from the gaseous flow, - the CH4-rich stream from the cryogenic separation is recovered. Installation for the implementation of the process