СИСТЕМА И СПОСОБ ДЛЯ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА

Изобретение относится к технологии сжижения и разделения природного газа. Сжижающая система (1) для природного газа включает блок удаления воды из исходного газообразного материала, первый расширитель (3), который производит энергию посредством использования природного газа под давлением в качестве газообразного материала; первый охлаждающий блок (11, 12), который охлаждает газообразный материал, имеющий пониженное давление посредством расширения в первом расширителе; дистилляционный блок (15) для уменьшения содержания или удаления тяжелого компонента, содержащегося в газообразном материале, посредством дистилляции газообразного материала, охлажденного первым охлаждающим блоком; первый компрессор (4) для сжатия газообразного материала, из которого частично или полностью удалены тяжелые компоненты посредством дистилляционного блока, за счет использования энергии, производимой в первом расширителе; и сжижающий блок (21) для сжижения газообразного материала, сжатого первым компрессором, посредством ...

СПОСОБ И УСТАНОВКА ОБРАЗОВАНИЯ ГАЗА ИЗ ВОЗДУХА В ГАЗООБРАЗНОЙ И ЖИДКОЙ ФОРМЕ ВЫСОКОЙ ГИБКОСТИ МЕТОДОМ КРИОГЕННОЙ ДИСТИЛЛЯЦИИ

FIELD: machine building. SUBSTANCE: cooling and heating plant for air flow designed for air separation column system and coming from it contains exchange line (7), the first turbine (21), subsidiary turbine (27), subsidiary compressor for increasing pressure of compressed air (13). Exchange line includes channel for receiving the first flow of purified air interconnected to subsidiary compressor for increasing compressed air pressure, channel connected to pressure pipeline of subsidiary compressor for increasing compressed air pressure and the first turbine, two channels for receiving two fluids (35, 37) that are heated, channel for receiving the second flow of purified air connected to the suction element of subsidiary turbine, note that pressure pipeline of subsidiary turbine is connected to, at least, one channel of heated air. The said channels are connected in such a way so that during operation the temperature of subsidiary turbine suction was higher than the temperature of the first turbine suction and the temperature of subsidiary turbine suction was higher than the temperature of the subsidiary compressor suction. EFFECT: use of invention allows increasing cooling efficiency and increasing the volume of fluid produced. 5 cl, 2 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 479 806 (13) C2 (51) МПК F25J 3/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2009137758/06, 12.03.2008 (24) Дата начала отсчета срока действия патента: 12.03.2008 (72) Автор(ы): ГИЙЯР Ален (FR), ЛЕБО Патрик (FR), ПОНТОН Ксавье (FR) (73) Патентообладатель(и): Л'ЭР ЛИКИД СОСЬЕТЕ АНОНИМ ПУР Л'ЭТЮД Э Л'ЭКСПЛУАТАСЬОН ДЕ ПРОСЕДЕ ЖОРЖ КЛОД (FR) (43) Дата публикации заявки: 20.04.2011 Бюл. № 11 2 4 7 9 8 0 6 (45) Опубликовано: 20.04.2013 Бюл. № 11 (56) Список документов, цитированных в отчете о поиске: FR 2688052 A1, 03.09.1993. US 2006/277944 A1, 14.12.2006. US 5157926 A, 27.10.1992. US 5806341 A, 15.09.1998. SU 645007 A1, 30.01. ...

СИСТЕМА И СПОСОБ ДЛЯ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА (ВАРИАНТЫ)

Изобретение относится к области сжижения природного газа. Сжижающая система (1) для природного газа включает первый расширитель (3), который производит энергию посредством использования природного газа под давлением в качестве газообразного материала, первый охлаждающий блок (11, 12), дистилляционный блок (15), первый компрессор (4) для сжатия газообразного материала, из которого частично или полностью удалены тяжелые компоненты посредством дистилляционного блока, за счет использования энергии, производимой в первом расширителе, и сжижающий блок (21). В результате использования энергии, производимой расширителем посредством расширения газообразного материала, увеличивается давление на выпуске компрессора, и уменьшается требуемая охлаждающая способность холодильника. 9 н. и 22 з.п. ф-лы, 3 табл.,10 ил. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 668 303 C1 (51) МПК F25J 3/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК F25J 1/0022 (2018.05); F25J 1/0035 (2018.05); F25J 1/0052 (2018.05); F25J 1/0055 (2018.05); F25J 1/0082 (2018.05); F25J 1/0085 (2018.05); F25J 1/0087 (2018.05); F25J 1/021 (2018.05); F25J 1/0216 (2018.05); F25J 1/0239 (2018.05) (21)(22) Заявка: 2016144151, 26.12.2014 26.12.2014 Дата регистрации: Приоритет(ы): (30) Конвенционный приоритет: 26.12.2013 JP 2013-270011; 13.03.2014 JP 2014-050786 Номер и дата приоритета первоначальной заявки, из которой данная заявка выделена: 2016130314 26.12.2013 2 6 6 8 3 0 3 R U (56) Список документов, цитированных в отчете о поиске: US 4004430 A, 25.01.1977. US 2013/ 125582 A1, 23.05.2013. RU 2088866 C1, 27.08.1997. US 4445916 A, 01.05.1984. US3520143 A, 14.07.1970. Адрес для переписки: 129090, Москва, ул. Б. Спасская, 25, стр. 3, ООО "Юридическая фирма Городисский и Партнеры" (54) СИСТЕМА И СПОСОБ ДЛЯ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА (ВАРИАНТЫ) (57) Реферат: Изобретение относится к области сжижения посредством дистилляционного блока, за счет природного газа. Сжижающая ...

СПОСОБ НИЗКОТЕМПЕРАТУРНОГО РАЗДЕЛЕНИЯ ВОЗДУХА И УСТАНОВКА РАЗДЕЛЕНИЯ ВОЗДУХА

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2016 147 700 A (51) МПК F25J 3/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2016147700, 06.12.2016 (71) Заявитель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ (DE) Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): ЛАУТЕНШЛАГЕР Тобиас (DE) 07.12.2015 EP 15003482.5 Адрес для переписки: 129090, Москва, ул. Б. Спасская, 25, стр. 3, ООО "Юридическая фирма Городисский и Партнеры" Стр.: 1 A 2 0 1 6 1 4 7 7 0 0 R U A (57) Формула изобретения 1. Способ низкотемпературного разделения воздуха с использованием установки (100) разделения воздуха, которая имеет систему (10) дистилляционных колонн с действующей на уровне давления колонны высокого давления колонной (11) высокого давления и действующей на уровне давления колонны низкого давления колонной (12) низкого давления, причем способ включает стадии, при которых - весь подаваемый в систему (10) дистилляционных колонн воздух сначала сжимают до исходного уровня давления, который на величину по меньшей мере 4 и до 20 бар превышает уровень давления колонны высокого давления, - часть сжатого до исходного уровня давления воздуха подвергают первому повышению давления на находящемся выше 0°С первом уровне температуры, и затем двум дополнительным повышениям давления на находящемся ниже первого уровня температуры уровне температуры, и затем с использованием дроссельного клапана (14) расширяют в колонне (11) высокого давления, и - из колонны (12) низкого давления отбирают охлажденную до низкой температуры, обогащенную кислородом жидкость, подвергают повышению давления в глубоко охлажденном состоянии, подогревают и испаряют, и выводят из установки (100) разделения воздуха, отличающийся тем , что - для первого повышения давления применяют первый бустер (2), который приводят в действие с использованием первой расширительной машины (9), в которой дополнительная часть сжатого до исходного уровня давления воздуха, который затем подается в колонну ...

СИСТЕМА И СПОСОБ ДЛЯ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2016 130 315 A (51) МПК F25J 1/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2016130315, 26.12.2014 (71) Заявитель(и): ТИЙОДА КОРПОРЕЙШН (JP) Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): КИККАВА Йосицуги (JP), САКАИ Коитиро (JP) 26.12.2013 JP 2013-270011; 13.03.2014 JP 2014-050786 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 26.07.2016 JP 2014/006502 (26.12.2014) (87) Публикация заявки PCT: A WO 2015/098125 (02.07.2015) Адрес для переписки: 129090, Москва, ул. Б.Спасская, 25, строение 3, ООО "Юридическая фирма Городисский и Партнеры" R U (57) Формула изобретения 1. Система для сжижения природного газа, которая охлаждает природный газ для производства сжиженного природного газа, включающая: первый расширитель для расширения природного газа под давлением в качестве газообразного материала; первый охлаждающий блок для охлаждения газообразного материала; дистилляционный блок для уменьшения содержания или удаления тяжелого компонента, содержащегося в газообразном материале посредством дистилляции газообразного материала, охлажденного первым охлаждающим блоком; первый компрессор для приема верхней фракции газообразного материала, от которой тяжелый компонент частично или полностью отделен дистилляционным блоком; и сжижающий блок для сжижения газофазного компонента, отделенного от сжатого газообразного материала, сжатого первым компрессором, посредством теплообмена с хладагентом. 2. Система для сжижения природного газа по п. 1, в которой сжатый газообразный материал предварительно охлаждается посредством введения в сжижающий блок, и система дополнительно включает первый разделяющий газовую и жидкую фазы резервуар для отделения газофазного компонента от сжатого газообразного материала, Стр.: 1 A 2 0 1 6 1 3 0 3 1 5 (54) СИСТЕМА И СПОСОБ ДЛЯ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА 2 0 1 6 1 3 0 3 1 5 (86) Заявка PCT: R U (43) Дата публикации заявки: 31.01. ...

Pump for cryogenic fluid, especially fluid gained during an air distillation process, such as liquid oxygen, has labyrinth seal to prevent contamination of cryogenic fluid by flow of operating fluid from motor to pump impeller

The pump has a labyrinth seal arrangement(35) to prevent contamination of the cryogenic fluid(3) by flow of operating fluid(15) from the motor to the pump impeller(21). The pump is immersed in the cryogenic fluid to be pumped, and the pressurized operating fluid is supercooled. The hydraulic motor has a drive wheel(13) driven by the operating fluid and seated upon the same shaft(27) upon which is mounted the pump impeller. The shaft is seated in bearings(29,31) lubricated by the operating fluid. Independent claims are also included for the following: (a) a use for the pump, which is in an air distillation plant; (b) a pump unit with two pumps; (c) a plant for air distillation, incorporating the proposed pump.

Gas Mixture Fractionating Plants

... 1,151,659. Cold separation of gas mixtures. MESSER GRIESHEIM G.m.b.H. 2 May, 1967 [4 May, 1966], No. 20314/67. Heading F4P. In a low temperature compressed gas mixture separation plant wherein part of the cold requirements are met by expansion in a turbine 17, Fig. 2, of the compressed gas mixture, the turbine shaft 28 is directly connected through pinion gearing 24, 26 located between a rotary compressor and a drive motor 11 therefor and which motor is thus assisted by the turbine. The output drive shaft of the motor 11 carries a gear wheel 26, Fig. 3, which drives pinions 23, 25 on shafts 18, 19 of two pairs of rotary compressors 12, 15 and 13, 14 respectively arranged in series and the turbine shaft 28 is connected by clutches 12, 22 to turbines 16, 17 arranged in parallel having supply and exhaust lines 35, 36.

Pump for a cryogenic liquid

PRODUCTION OF OXYGEN BY THE TWO-STAGE LOW-TEMPERATURE RECTIFICATION OF AIR

... 1516478 Air rectification LINDE AG 5 Aug 1976 [6 Aug 1975] 32609/76 Heading F4P In a rectification process in which air is cooled in heat exchangers 2 and fed to the h.p. stage 4 of a two-stage rectification column, and product oxygen is withdrawn from the 1.p. stage 6 via line 5 and heated in a further heat exchanger 8 by a gas stream 11 being fed to the h.p. stage 4, a compensating gas stream 17 is withdrawn from the h.p. stage 4 heated, at least in part, in the h.e.'s 2 recooled in h.e. 8 and expanded in at least one turbine 21. As shown, the gas stream 17 is an air mixture, a portion 20 of which is warmed in parallel with the oxygen product in h.e. 8 before rejoining the balance at 22. A nitrogen stream 9 taken from the top of the h.p. stage 4 forms the gas stream ] 1 after warming in h.e.'s 2 and compression at 10, the stream 11 then being expanded back into h.p. stage 4. Two streams 12, 13 are taken from h.p. stage 4, cooled and expanded into 1.p. stage 6 and gaseous nitrogen is removed ...

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

Systems and methods for using multiple cryogenic hydraulic turbines

There is provided a system and method for producing liquefied natural gas (LNG). An exemplary method includes flowing a high-pressure stream of LNG through a first series of liquid turbines. The exemplary method also includes generating electricity by reducing the pressure of the high-pressure stream of LNG to form a low-pressure stream of LNG. The exemplary method additionally includes bypassing any one the liquid turbines that has a failure while continuing to produce electricity from the first series.

SCALABLE CAPACITY LIQUEFIED NATURAL GAS PLANT

Procédé et installation pour la production d'oxygène gazeux

METHODS AND CONFIGURATION AND DISCHARGE OF ETHANE EXTRACTION OF ETHANE

СПОСОБ РАЗДЕЛЕНИЯ ВОЗДУХА КРИОГЕННОЙ ДИСТИЛЛЯЦИЕЙ И СПОСОБ ФОРМИРОВАНИЯ СТРУИ КИСЛОРОДА ВЫСОКОГО ДАВЛЕНИЯ

Способ разделения воздуха криогенной дистилляцией, в котором согласно первому этапу в установке для разделения воздуха весь воздух, предназначенный для дистилляции, сжимают в главном компрессоре, при этом первую струю воздуха сжимают в по крайней мере главном компрессоре, очищают и охлаждают в теплообменной линии, потом подают в колонну среднего давления колонны двукратной дистилляции, при этом в колонне среднего давления указанную струю воздуха разделяют на обогащенную азотом струю и обогащенную кислородом струю, причем струю жидкого кислорода выводят из колонны низкого давления, указанную струю сжимают до получения высокого давления и испаряют в теплообменной линии для формирования первой обогащенной кислородом газовой струи высокого давления, при этом по крайней мере одну часть воздуха, сжатую в главном компрессоре, сжижают и сжиженную часть подают в колонну двукратной дистилляции, и также получают вторую обогащенную кислородом газовую струю, тем не менее при более низком давлении, чем ...

СПОСОБ КРИОГЕННОЙ ДИСТИЛЛЯЦИИ И УСТАНОВКА ДЛЯ РАЗДЕЛЕНИЯ ВОЗДУХА

Изобретение относится к способу и установке для разделения воздуха с помощью криогенной дистилляции. Согласно изобретению во всем воздухе давление доводят до высокого давления, большего среднего давления, и очищают. Часть потока (11) очищенного воздуха охлаждают в теплообменной линии (9), а потом разделяют на две фракции (13, 15). Каждая из фракций расширяется в турбине (17, 19), при этом давление на входе двух турбин больше среднего давления, по крайней мере, на 5 бар. Более того, давление на выходе, по крайней мере, одной из двух турбин, по сути, равно среднему давлению. По крайней мере, часть воздуха, которая расширилась, по крайней мере, в одной из турбин, подается в колонну (100) среднего давления двойной или тройной колонны. Поэтому холодный бустер-компрессор (23), механически соединенный с одной (19) из турбин, втягивает воздух, который был охлажден в основной теплообменной линии, и выпускает указанный воздух при температуре, большей температуры на входе. Таким образом, сжатую текучую ...

Method for producing a gas from pressurised air by means of cryogenic distillation

The invention relates to a method for separating air by means of cryogenic distillation in a system of columns, in which two single-stage air superchargers (15, 25) are connected in series and coupled to two turbines (17, 27) which expand the air that was not supercharged. The superchargers supercharge the cooled high-pressure air in an exchange line in which the oxygen from the system of columns is vaporised.

PROCESS AND INSTALLATION OF LIQUEFACTION AND SEPARATION Of AIR

APPARATUS AND METHOD FOR AIR SEPARATION BY CRYOGENIC DISTILLATION

METHOD AND APPARATUS FOR SEPARATING AIR BY CRYOGENIC DISTILLATION

Dans un procédé de séparation d'air par distillation cryogénique, de l'air (1,7) est comprimé à une première pression, épuré, refroidi dans un échangeur de chaleur (17) et envoyé pour être séparé dans un système de colonnes (31,33), au moins une partie (9) de l'air épuré sort à un niveau intermédiaire de l'échangeur de chaleur, est surpressée dans au moins un surpresseur (13,15), ayant un taux de compression variable à une température intermédiaire de l'échangeur de chaleur, est renvoyée à l'échangeur de chaleur pour se refroidir et est envoyée au système de colonnes et si le taux de compression du surpresseur ou d'au moins un des surpresseurs ou des surpresseurs est au dessus d'un seuil, on ne soutire pas de débit d'oxygène gazeux (55) du système de colonnes et si le taux de compression du surpresseur ou d'au moins un des surpresseurs ou des surpresseurs est en dessous du seuil, un débit d'oxygène gazeux est soutiré du système de colonnes et se réchauffe dans l'échangeur de chaleur.

PUMP FOR a CRYOGENIC LIQUID LIKE AND COLUMN PUMPING INSTALLATION FRACTIONATING TEAMS Of SUCH a PUMP

L'invention concerne une pompe (1) pour un liquide cryogénique (3), notamment de l'oxygène liquide. Elle comprend un moteur hydraulique (9) alimenté par un liquide moteur (15) sous pression et entraînant une roue de pompage (21) dudit liquide cryogénique (3), et des moyens d'étanchéité relative (33) empêchant la contamination du liquide cryogénique (3) par le liquide moteur (15). The invention relates to a pump (1) for a cryogenic liquid (3), in particular liquid oxygen. It comprises a hydraulic motor (9) supplied by a motor liquid (15) under pressure and driving a pumping wheel (21) of said cryogenic liquid (3), and relative sealing means (33) preventing contamination of the cryogenic liquid. (3) by the motor liquid (15).

Scalable capacity liquefied natural gas plant

Apparatus and Process for Liquefying Gases

A liquefier device which may be a retrofit to an air separation plant or utilized as part of a new design. The flow needed for the liquefier comes from an air separation plant running in a maxim oxygen state, in a stable mode. The three gas flows are low pressure oxygen, low pressure nitrogen, and higher pressure nitrogen. All of the flows are found on the side of the main heat exchanger with a temperature of about 37 degrees Fahrenheit. All of the gasses put into the liquefier come out as a subcooled liquid, for storage or return to the air separation plant. This new liquefier does not include a front end electrical compressor, and will take a self produced liquid nitrogen, pump it up to a runnable 420 psig pressure, and with the use of turbines, condensers, flash pots, and multi pass heat exchangers. The liquefier will make liquid from a planned amount of any pure gas oxygen or nitrogen an air separation plant can produce.

Liquefaction system using a turboexpander

The subject matter disclosed herein relates to a liquefaction system. Specifically, the present disclosure relates to systems and methods for condensing a pressurized gaseous working fluid, such as natural gas, using at least one turboexpander in combination with other cooling devices and techniques. In one embodiment, a turboexpander may be used in combination with a heat exchanger using vapor compression refrigeration to condense natural gas.

СПОСОБ РАЗДЕЛЕНИЯ ВОЗДУХА НА СОСТАВНЫЕ ЧАСТИ ПРИ ПОМОЩИ КРИОГЕННОЙ ДИСТИЛЛЯЦИИ

... 1. Способ разделения воздуха на составные части при помощи криогенной дистилляции в установке разделения воздуха, имеющей в своем составе систему колонн, при котором: ! i) в соответствии с первым процессом: ! а) сжимают в главном компрессоре (1, 44) весь объем воздуха, предназначенный для дистилляции; ! b) направляют первый поток воздуха, сжатого по меньшей мере в главном компрессоре, очищенного и охлажденного в линии (6, 42, 9) теплообмена, в колонну (8, 50, 100) среднего давления сдвоенной колонны; ! с) разделяют поток воздуха на потоки, обогащенные азотом и обогащенные кислородом, в колонне среднего давления; ! d) направляют эти потоки, обогащенные азотом и обогащенные кислородом в колонне среднего давления, в колонну (9, 51, 200) низкого давления упомянутой сдвоенной колонны непосредственно или косвенным образом; ! е) извлекают поток, обогащенный азотом, из колонны низкого давления и нагревают его в линии теплообмена; ! f) извлекают поток жидкого кислорода из колонны низкого давления ...

Verfahren und Anordnung zum Betrieb von Gaszerlegungsanlagen

Method and apparatus for treating a hydrocarbon stream and method of cooling a hydrocarbon stream

Method and apparatus for treating a mixed hydrocarbon feed stream (10), such as a natural gas stream. The mixed hydrocarbon feed stream (10) is expanded into a mixed-phase hydrocarbon stream (20), which is separated the to provide at least a light overhead stream (30) and a heavy bottom stream (50). The light overhead stream (30) is compressed in one or more first compressors (16) to provide one or more first compressed light streams (40) and further compressed in one or more second compressors (22) to provide one or more further compressed light streams (60). One or more first compressor recycle lines (42) extend around the or each first compressor (16), and one or more second compressor recycle lines (32) having one or more in-line coolers (34) extend around the or each second compressor (22). The method and apparatus may be used in a method of cooling an initial hydrocarbon stream (100).

AIR SEPARATION PROCESS

Method and apparatus for treating a hydrocarbon stream and method of cooling a hydrocarbon stream

Method for treating a hydrocarbon stream

PROCESS AND APPARATUS OF PRODUCTION OF GAS OF THE AIR IN GAS FORM AND LIQUID HAVE HIGH FLEXIBILITY BY CRYOGENIC DISTILLATION

Dans un procédé de production d'au moins un gaz de l'air par distillation cryogénique dans un système de colonnes, selon un premier mode de fonctionnement, une turbine auxiliaire (27) aspire une fraction gazeuse d'un débit d'air ayant été préalablement détendue dans une première turbine (21), la pression d'aspiration de la turbine auxiliaire diffère de moins de 2 bar abs de la moyenne pression, la pression de refoulement de la turbine auxiliaire est supérieure ou substantiellement égale à la pression atmosphérique,;au moins une partie du débit d'air détendu dans la turbine auxiliaire est réchauffée dans une ligne d'échange (7) ou renvoyée à un système de colonnes et une partie (32) des constituants de l'air est produite comme produit final sous forme liquide et dans un deuxième mode de fonctionnement, le débit d'air traité dans la turbine auxiliaire est réduit et la production de liquide comme produit final est diminuée.

CRYOGENIC SYSTEM FOR PRODUCING ELEVATED PRESSURE NITROGEN

A cryogenic air separation system for producing elevated pressure nitrogen wherein a portion of the nitrogen product fed to the product compressor (110) downstream of the primary heat exchanger (101) is withdrawn as refrigerant nitrogen from the product compressor (110), preferably from an intermediate point of the product compressor (110), and turboexpanded to generate refrigeration for the system.

Process for separating hydrogen from an olefin hydrocarbon effluent vapor stream

One or more specific embodiments disclosed herein includes a method for separating hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream, employing a single heat exchanger, multiple gas-liquid separators, multiple expander/compressor sets, and a rectifier attached to a liquid product drum.

DEVICE AND METHOD FOR LIQUEFYING A FLUID SUCH AS HYDROGEN AND/OR HELIUM

Disclosed is a device for liquefying a fluid, comprising a fluid circuit to be cooled, the device comprising a heat exchanger assembly in heat exchange with the fluid circuit to be cooled, at least one first cooling system in heat exchange with at least a portion of the heat exchanger assembly, the first cooling system being a refrigerator having a cycle for refrigerating a cycle gas mainly comprising helium, said refrigerator comprising in series in a cycle circuit: a mechanism for compressing the cycle gas, at least one member for cooling the cycle gas, a mechanism for expanding the cycle gas, and at least one member for reheating the expanded cycle gas, wherein the compression mechanism includes at least four compression stages in series composed of a centrifugal compressor assembly, the compression stages being mounted on shafts that are rotationally driven by a motor assembly, the expansion mechanism comprising at least three expansion stages in series composed of a set of centripetal ...

METHOD AND DEVICE FOR PRODUCING A GASEOUS PRESSURIZED OXYGEN PRODUCT BY CRYOGENIC SEPARATION OF AIR

The invention relates to a method and device used to produce a gaseous oxygen pressurized product by cryogenic separation of air in a distillation column system, which has at least one separation column. Feed air is compressed in an air compressor. A first partial flow (2, 4, 6, 7) of the compressed feed air is expanded to perform work (5, 8). A second partial flow (3) of the compressed feed air (1) is cooled and liquefied or pseudo-liquefied and subsequently introduced into the distillation column system. A liquid oxygen product flow (51) is removed from the distillation column system, brought in the liquid state to a first elevated pressure (52), evaporated or pseudo-evaporated at said first elevated pressure by indirect heat exchange (10) with the second partial flow (3) of the compressed feed air, heated to approximately the ambient temperature (10) and finally withdrawn in the form of a gaseous product flow (55). The evaporated or pseudo-evaporated oxygen product flow (53) is brought further to a second elevated pressure that is higher than the first elevated pressure in a cold compressor (13). The product flow (54) is heated (10) under said second elevated pressure to approximately the ambient temperature. At least part of the mechanical energy generated during the work-performing expansion (5, 8) of the first partial flow (3) is used to drive the cold compressor (13).

METHOD AND APPARATUS FOR THE PRODUCTION OF GAS FROM AIR IN HIGHLY FLEXIBLE GASEOUS AND LIQUID FORM BY CRYOGENIC DISTILLATION

СПОСОБ РАЗДЕЛЕНИЯ ВОЗДУХА ПОСРЕДСТВОМ НИЗКОТЕМПЕРАТУРНОЙ ПЕРЕГОНКИ И УСТАНОВКА ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

Изобретение относится к способу и установке для разделения воздуха посредством низкотемпературной перегонки. Согласно изобретению повышают давление всего воздуха до высокого давления, большего, чем среднее давление, и очищают его. Охлаждают в теплообменнике (9) часть потока (11) очищенного воздуха и затем разделяют ее на две фракции (13, 15). Расширяют в турбодетандере (17, 19) каждую из фракций, при этом давление на входе двух турбодетандеров, по меньшей мере, на 5 бар больше, чем среднее давление. Кроме того, давление на выходе, по меньшей мере, одного из двух турбодетандеров по существу равно среднему давлению. Часть воздуха, который был расширен в одном из турбодетандеров, направляют в колонну среднего давления (100) колонны двукратного или трехкратного разделения. После этого в низкотемпературный компрессор (23), который механически соединен с одним (19) из турбодетандеров, подают воздух, который был охлажден в основном теплообменнике, и нагнетают воздух при температуре больше, чем ...

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`”ВУ“” 2016130315” АЗ Дата публикации: 01.03.2018 Форма № 18 ИЗ,ПМ-2011 Федеральная служба по интеллектуальной собственности Федеральное государственное бюджетное учреждение «Федеральный институт промышленной собственности» ж 9 (ФИПС) ОТЧЕТ О ПОИСКЕ 1. . ИДЕНТИФИКАЦИЯ ЗАЯВКИ Регистрационный номер Дата подачи 2016130315/06(047183) 26.12.2014 РСТ/Р2014/006502 26.12.2014 Приоритет установлен по дате: [ ] подачи заявки [ ] поступления дополнительных материалов от к ранее поданной заявке № [ ] приоритета по первоначальной заявке № из которой данная заявка выделена [ ] подачи первоначальной заявки № из которой данная заявка выделена [ ] подачи ранее поданной заявки № [Х] подачи первой(ых) заявки(ок) в государстве-участнике Парижской конвенции (31) Номер первой(ых) заявки(ок) (32) Дата подачи первой(ых) заявки(ок) (33) Код страны 1. 2013-27001 26.12.2013 ]Р 2. 2014-050786 13.03.2014 ]Р Название изобретения (полезной модели): [ЖХ] - как заявлено; [ ] - уточненное (см. Примечания) СИСТЕМА И СПОСОБ ДЛЯ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА Заявитель: ТИЙОДА КОРПОРЕЙШН, ]Р 2. ЕДИНСТВО ИЗОБРЕТЕНИЯ [Х] соблюдено [ ] не соблюдено. Пояснения: см. Примечания 3. ФОРМУЛА ИЗОБРЕТЕНИЯ: [Х] приняты во внимание все пункты (см. Примечания) [ ] приняты во внимание следующие пункты: [ ] принята во внимание измененная формула изобретения (см. Примечания) 4. КЛАССИФИКАЦИЯ ОБЪЕКТА ИЗОБРЕТЕНИЯ (ПОЛЕЗНОЙ МОДЕЛИ) (Указываются индексы МПК и индикатор текущей версии) Е25.7 1/02 (2006.01) Е25.] 3/00 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) Е25) 1/00, 1/02, 3/00, 3/02 5.2 Другая проверенная документация в той мере, в какой она включена в поисковые подборки: 5.3 Электронные базы данных, использованные при поиске (название базы, и если, возможно, поисковые термины): Езрасепе, Рабеагсв, КОРТО 6 ДОКУМЕНТЫ, ОТНОСЯЩИЕСЯ К ПРЕДМЕТУ ПОИСКА Кате- Наименование документа с указанием (где необходимо) частей, Относится к гория* относящихся к предмету поиска пункту ...

СПОСОБ РАЗДЕЛЕНИЯ ВОЗДУХА ПОСРЕДСТВОМ НИЗКОТЕМПЕРАТУРНОЙ ПЕРЕГОРОДКИ И УСТАНОВКА ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß RU (19) (11) 2006 129 296 (13) A (51) ÌÏÊ F25J 3/04 (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÇÀßÂÊÀ ÍÀ ÈÇÎÁÐÅÒÅÍÈÅ (21), (22) Çà âêà: 2006129296/06, 07.01.2005 (30) Êîíâåíöèîííûé ïðèîðèòåò: 12.01.2004 FR 04 50067 (43) Äàòà ïóáëèêàöèè çà âêè: 20.02.2008 Áþë. ¹ 5 (72) Àâòîð(û): ÄÅ ÁÎ Ïàòðèê (FR) (87) Ïóáëèêàöè PCT: WO 2005/073651 (11.08.2005) R U (54) ÑÏÎÑÎÁ ÐÀÇÄÅËÅÍÈß ÂÎÇÄÓÕÀ ÏÎÑÐÅÄÑÒÂÎÌ ÍÈÇÊÎÒÅÌÏÅÐÀÒÓÐÍÎÉ ÏÅÐÅÃÎÐÎÄÊÈ È ÓÑÒÀÍÎÂÊÀ ÄËß ÅÃÎ ÎÑÓÙÅÑÒÂËÅÍÈß (57) Ôîðìóëà èçîáðåòåíè 1. Ñïîñîá ðàçäåëåíè âîçäóõà ïîñðåäñòâîì íèçêîòåìïåðàòóðíîé ïåðåãîíêè â óñòàíîâêå, ñîäåðæàùåé âîçäóõîðàçäåëèòåëüíóþ êîëîííó (100, 200) äâóêðàòíîãî èëè òðåõêðàòíîãî ðàçäåëåíè , êîëîííà êîòîðîãî, ðàáîòàþùà ïðè áîëåå âûñîêîì äàâëåíèè (100), ðàáîòàåò ïðè òàê íàçûâàåìîì ñðåäíåì äàâëåíèè, è òåïëîîáìåííèê (9), ïðè êîòîðîì: à) ïîâûøàþò äàâëåíèå âñåãî âîçäóõà äî âûñîêîãî äàâëåíè , ïî âûáîðó, ïî ìåíüøåé ìåðå, íà 5 áàð âûøå ñðåäíåãî äàâëåíè è î÷èùàþò åãî, ïî âûáîðó, ïðè ýòîì âûñîêîì äàâëåíèè, b) îõëàæäàþò â òåïëîîáìåííèêå îäíó ÷àñòü ïîòîêà î÷èùåííîãî âîçäóõà è çàòåì ðàçäåë þò åå íà äâå ôðàêöèè, ñ) ðàñøèð þò êàæäóþ ôðàêöèþ â òóðáîäåòàíäåðå (17, 19), d) îáåñïå÷èâàþò äàâëåíèå íà âõîäå äâóõ òóðáîäåòàíäåðîâ (äàâëåíè íà âõîäå äâóõ òóðáîäåòàíäåðîâ), êîòîðîå, ïî ìåíüøåé ìåðå, íà 5 áàð âûøå ñðåäíåãî äàâëåíè , å) îáåñïå÷èâàþò äàâëåíèå íà âûõîäå, ïî ìåíüøåé ìåðå, îäíîãî èç äâóõ òóðáîäåòàíäåðîâ, ïî ñóùåñòâó ðàâíîå ñðåäíåìó äàâëåíèþ, f) íàïðàâë þò, ïî ìåíüøåé ìåðå, îäíó ÷àñòü âîçäóõà, ðàñøèðåííîãî â, ïî ìåíüøåé ìåðå, îäíîì èç òóðáîäåòàíäåðîâ, â êîëîííó ñðåäíåãî äàâëåíè êîëîííû äâóêðàòíîãî èëè òðåõêðàòíîãî ðàçäåëåíè , g) ïîäàþò â íèçêîòåìïåðàòóðíûé ïîäæèìàþùèé êîìïðåññîð (23), ìåõàíè÷åñêè ñîåäèíåííûé ñ îäíèì èç äâóõ òóðáîäåòàíäåðîâ, âîçäóõ, êîòîðûé ïîäâåðãàëè îõëàæäåíèþ â òåïëîîáìåííèêå, è íàãíåòàþò êîìïðåññîðîì âîçäóõ ïðè òåìïåðàòóðå âûøå òåìïåðàòóðû íà Ñòðàíèöà: 1 RU A 2 0 0 6 1 2 9 2 9 6 A Àäðåñ äë ïåðåïèñêè: 129010, Ìîñêâà, óë. Á.Ñïàññêà , 25 ...

Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft

Das Verfahren und die Vorrichtung dienen zur Tieftemperaturzerlegung von Luft in einem Destilliersäulen-System (50), das mindestens eine Trennsäule (14, 15) aufweist. Ein Hauptluftstrom (1, 5) wird in einem Luftverdichter (2) auf einen ersten Druck verdichtet und anschließend in einer Reinigungsvorrichtung (4) gereinigt. Ein erster Luftstrom (6), der aus mindestens einem Teil des gereinigten Hauptluftstroms (5) gebildet wird, wird in einem Nachverdichter (7) auf einen zweiten Druck nachverdichtet, der höher als der erste Druck ist. Der nachverdichtete erste Luftstrom (8) wird in einem Hauptwärmetauscher (9) abgekühlt. Aus dem abgekühlten nachverdichteten ersten Luftstrom (10) werden ein Drosselstrom (11) und ein Turbinenstrom (18, 70, 21) abgezweigt. Der Drosselstrom (11) wird in dem Hauptwärmetauscher verflüssigt oder pseudo-verflüssigt und anschließend einer Entspannungseinrichtung (12) zugeführt. Der entspannte Drosselstrom (13) wird in das Destilliersäulen-System (50) eingeleitet. Der ...

Pump for a cryogenic liquid

Apparatus and process for liquefying gases

A liquefier device to be utilized with an air separation plant running in a maxim oxygen state, in a stable mode. The three gas flows to the liquefier from the plant are low pressure oxygen, low pressure nitrogen, and higher pressure nitrogen gas flows. All of the flows are found on the side of the main heat exchanger with a temperature of about 37 degrees Fahrenheit. All of the gases exit the liquefier as a subcooled liquid, for storage or return to the plant. The liquefier does not include a front end electrical compressor, and will take a self-produced liquid nitrogen, pump it up to a runnable 420 psig pressure, and with the use of turbines, condensers, flash pots, and multi pass heat exchangers. The liquefier will make liquid from a planned amount of any pure gas oxygen or nitrogen an air separation plant can produce.

SYSTEMS AND METHODS FOR USING MULTIPLE CRYOGENIC HYDRAULIC TURBINES

There is provided a system and method for producing liquefied natural gas (LNG). An exemplary method includes flowing a high-pressure stream of LNG through a first series of liquid turbines. The exemplary method also includes generating electricity by reducing the pressure of the high-pressure stream of LNG to form a low-pressure stream of LNG. The exemplary method additionally includes bypassing any one the liquid turbines that has a failure while continuing to produce electricity from the first series.

PROCEDE ET INSTALLATION DE LIQUEFACTION ET DE SEPARATION D'AIR

L'INVENTION CONCERNE UN PROCEDE ET UNE INSTALLATION DE LIQUEFACTION ET DE SEPARATION D'AIR COMPORTANT UNE TOUR A HAUTE PRESSION 21 ET UNE TOUR A BASSE PRESSION 22. L'INVENTION EST CARACTERISEE EN CE QUE LA TOUR A HAUTE PRESSION 21 ET LA TOUR A BASSE PRESSION 22 SONT DIVISEES EN DEUX SEGMENTS, EN CE QUE LES GAZ SORTANT EN TETE DES SEGMENTS RESPECTIFS DE LA TOUR A HAUTE PRESSION 21 PEUVENT ECHANGER DE LA CHALEUR AVEC DES LIQUIDES DE CIRCULATION OU DE L'OXYGENE LIQUIDE SORTANT EN BAS DES SEGMENTS RESPECTIFS DE LA TOUR A BASSE PRESSION 22. APPLICATION A LA PRODUCTION D'OXYGENE, D'AZOTE ET D'ARGON SOUS FORME GAZEUSE ET LIQUIDE.

APPARATUS AND METHOD FOR AIR SEPARATION BY CRYOGENIC DISTILLATION

APPARATUS AND METHOD FOR AIR SEPARATION BY CRYOGENIC DISTILLATION

APPARATUS AND METHOD FOR SEPARATING AIR BY CRYOGENIC DISTILLATION

PROCESS AND INSTALLATION FOR the PRODUCTION Of OXYGEN BY CORRECTION OF the AIR AT LOW TEMPERATURE AND UNDER TWO PRESSURE STAGES

PROCESS AND DEVICE OF PRODUCTION OF GASES OF AIR UNDER GASEOUS AND LIQUID FORM WITH HIGH FLEXIBILITY FOR CRYOGENIC DESTILLATION

METHOD AND DEVICE FOR PRODUCING A GASEOUS PRESSURIZED OXYGEN PRODUCT BY CRYOGENIC SEPARATION OF AIR

The invention relates to a method and device used to produce a gaseous oxygen pressurized product by cryogenic separation of air in a distillation column system, which has at least one separation column. Feed air is compressed in an air compressor. A first partial flow (2, 4, 6, 7) of the compressed feed air is expanded to perform work (5, 8). A second partial flow (3) of the compressed feed air (1) is cooled and liquefied or pseudo-liquefied and subsequently introduced into the distillation column system. A liquid oxygen product flow (51) is removed from the distillation column system, brought in the liquid state to a first elevated pressure (52), evaporated or pseudo-evaporated at said first elevated pressure by indirect heat exchange (10) with the second partial flow (3) of the compressed feed air, heated to approximately the ambient temperature (10) and finally withdrawn in the form of a gaseous product flow (55). The evaporated or pseudo-evaporated oxygen product flow (53) is brought ...

METHOD AND DEVICE FOR SEPARATING AIR BY CRYOGENIC DISTILLATION

Method for separating air by cryogenic distillation, wherein air is compressed in a compressor and is subsequently sent to a heat exchanger, with the air cooled in the exchanger being sent to a check valve downstream of the heat exchanger and subsequently to a turbine, the valve being positioned so that air from a short-circuiting duct cannot return to the exchanger from the compressor.

Patent RU2016130314A3

`”ВУ“” 2016130314” АЗ Дата публикации: 01.03.2018 Форма № 18 ИЗ,ПМ-2011 Федеральная служба по интеллектуальной собственности Федеральное государственное бюджетное учреждение «Федеральный институт промышленной собственности» ж 9 (ФИПС) ОТЧЕТ О ПОИСКЕ 1. . ИДЕНТИФИКАЦИЯ ЗАЯВКИ Регистрационный номер Дата подачи 2016130314/06(047182) 26.12.2014 РСТ/ЛР2014/006501 26.12.2014 Приоритет установлен по дате: [ ] подачи заявки [ ] поступления дополнительных материалов от к ранее поданной заявке № [ ] приоритета по первоначальной заявке № из которой данная заявка выделена [ ] подачи первоначальной заявки № из которой данная заявка выделена [ ] подачи ранее поданной заявки № [Х] подачи первой(ых) заявки(ок) в государстве-участнике Парижской конвенции (31) Номер первой(ых) заявки(ок) (32) Дата подачи первой(ых) заявки(ок) (33) Код страны 1. 2013-27001 26.12.2013 ]Р 2. 2014-050786 13.03.2014 ]Р Название изобретения (полезной модели): [ЖХ] - как заявлено; [ ] - уточненное (см. Примечания) СИСТЕМА И СПОСОБ ДЛЯ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА Заявитель: ТИЙОДА КОРПОРЕЙШН, ]Р 2. ЕДИНСТВО ИЗОБРЕТЕНИЯ [Х] соблюдено [ ] не соблюдено. Пояснения: см. Примечания 3. ФОРМУЛА ИЗОБРЕТЕНИЯ: [Х] приняты во внимание все пункты (см. Примечания) [ ] приняты во внимание следующие пункты: [ ] принята во внимание измененная формула изобретения (см. Примечания) 4. КЛАССИФИКАЦИЯ ОБЪЕКТА ИЗОБРЕТЕНИЯ (ПОЛЕЗНОЙ МОДЕЛИ) (Указываются индексы МПК и индикатор текущей версии) Е25.] 3/00 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) Е25. 3/00, 3/02, 1/00 5.2 Другая проверенная документация в той мере, в какой она включена в поисковые подборки: 5.3 Электронные базы данных, использованные при поиске (название базы, и если, возможно, поисковые термины): 6. ДОКУМЕНТЫ, ОТНОСЯЩИЕСЯ К ПРЕДМЕТУ ПОИСКА Кате- Наименование документа с указанием (где необходимо) частей, Относится к гория* относящихся к предмету поиска пункту формулы № 1 2 3 А 05 4004430 А (ТОММОУ$ СО ), 25.01.1977 ...

Patent RU2018120350A3

ВИ“? 2018120350” АЗ Дата публикации: 08.11.2021 Форма № 18 ИЗ,ПМ-2011 Федеральная служба по интеллектуальной собственности Федеральное государственное бюджетное учреждение 5 «Федеральный институт промышленной собственности» (ФИПС) ОТЧЕТ О ПОИСКЕ 1. . ИДЕНТИФИКАЦИЯ ЗАЯВКИ Регистрационный номер Дата подачи 2018120350/12(032080) 01.06.2018 Приоритет установлен по дате: [ ] подачи заявки [ ] поступления дополнительных материалов от к ранее поданной заявке № [ ] приоритета по первоначальной заявке № из которой данная заявка выделена [ ] подачи первоначальной заявки № из которой данная заявка выделена [ ] подачи ранее поданной заявки № [Х] подачи первой(ых) заявки(ок) в государстве-участнике Парижской конвенции (31) Номер первой(ых) заявки(ок) (32) Дата подачи первой(ых) заявки(ок) (33) Код страны 1. 17020238.6 02.06.2017 ЕР* Название изобретения (полезной модели): [Х] - как заявлено; [ ] - уточненное (см. Примечания) Способ получения одного или более продуктов из воздуха и установка по разделению воздуха Заявитель: ЛИНДЕ АКЦИЕНГЕЗЕЛЬШАФТ, РЕ 2. ЕДИНСТВО ИЗОБРЕТЕНИЯ [Х] соблюдено [ ] не соблюдено. Пояснения: см. Примечания 3. ФОРМУЛА ИЗОБРЕТЕНИЯ: [Х] приняты во внимание все пункты (см. Примечания) [ ] приняты во внимание следующие пункты: [ ] принята во внимание измененная формула изобретения (см. Примечания) 4. КЛАССИФИКАЦИЯ ОБЪЕКТА ИЗОБРЕТЕНИЯ (ПОЛЕЗНОЙ МОДЕЛИ) (Указываются индексы МПК и индикатор текущей версии) Е25.7 3/04 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) Е257 3/00-3/04 5.2 Другая проверенная документация в той мере, в какой она включена в поисковые подборки: 5.3 Электронные базы данных, использованные при поиске (название базы, и если, возможно, поисковые термины): Езрасепеь Соозе, РАТЕМТСОРЕ, Рабеагсв, КОРТО, ОЗРТО 6. ДОКУМЕНТЫ, ОТНОСЯЩИЕСЯ К ПРЕДМЕТУ ПОИСКА Кате- Наименование документа с указанием (где необходимо) частей, Относится к гория* относящихся к предмету поиска пункту формулы № 1 2 3 А 0$ 2004 ...

СИСТЕМА И СПОСОБ ДЛЯ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА

Способ получения одного или более продуктов из воздуха и установка по разделению воздуха

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2018 120 350 A (51) МПК F25J 3/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2018120350, 01.06.2018 (71) Заявитель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЬШАФТ (DE) Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): ГОЛУБЕВ Дмитрий (DE) 02.06.2017 EP 17020238.6 Адрес для переписки: 191036, Санкт-Петербург, а/я 24, "НЕВИНПАТ" Стр.: 1 A 2 0 1 8 1 2 0 3 5 0 R U A (57) Формула изобретения 1. Способ получения одного или более продуктов из воздуха с помощью установки (100) по разделению воздуха, имеющей систему (14-17) ректификационных колонн, которая включает колонну (14) высокого давления и колонну (15) низкого давления, а также основной теплообменник (9) и основной воздушный компрессор (1), в котором - общее количество воздуха, подаваемого в систему (14-17) ректификационных колонн сжимают в основном воздушном компрессоре (1) до первого уровня давления, причем колонну (15) высокого давления эксплуатируют при втором уровне давления, который по меньшей мере на 300 кПа (3 бар) ниже первого уровня давления, и - газообразную, насыщенную азотом текучую среду извлекают из колонны (15) высокого давления при втором уровне давления и нагревают в газообразном состоянии без предварительного сжижения, отличающийся тем, что - первое частичное количество газообразной насыщенной азотом текучей среды нагревают до первого уровня температуры от -150 до -100°С, в частности от -140 до -120°С, подают при первом уровне температуры в бустер (12) и с помощью бустера (12) дополнительно сжимают до третьего уровня давления, причем - указанное первое частичное количество после сжатия до третьего уровня давления нагревают до второго уровня температуры выше первого уровня температуры и постоянно извлекают из установки (100) по разделению воздуха. 2. Способ по п. 1, в котором второе частичное количество газообразной насыщенной азотом текучей среды нагревают совместно с первым частичным количеством до первого ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ ГАЗООБРАЗНОГО СЖАТОГО КИСЛОРОДНОГО ПРОДУКТА НИЗКОТЕМПЕРАТУРНЫМ РАЗДЕЛЕНИЕМ ВОЗДУХА

1. Способ получения газообразного сжатого кислородного продукта низкотемпературным разделением воздуха в системе дистилляционных колонн, содержащей по меньшей мере одну разделительную колонну, при котором- сжимают рабочий воздух в воздушном компрессоре,- первый частичный поток (2, 4, 6, 7) сжатого рабочего воздуха расширяют (5, 8) с производством работы,- второй частичный поток (3) сжатого рабочего воздуха (1) охлаждают и подвергают сжижению или псевдо-сжижению, и затем направляют в систему дистилляционных колонн,- сжиженный поток (51) кислородного продукта выводят из системы дистилляционных колонн, в жидком состоянии доводят до первого повышенного давления (52), при этом первом повышенном давлении подвергают испарению или псевдо-испарению путем косвенного теплообмена (10) со вторым частичным потоком (3) сжатого рабочего воздуха, нагревают (10) примерно до температуры окружающей среды и, наконец, выводят в виде газообразного потока (55) продукта,отличающийся тем, что- испаренный или, соответственно, псевдо-испаренный поток (53) кислородного продукта в холодном компрессоре (13) доводят до второго повышенного давления, которое является более высоким, чем первое повышенное давление, и- поток (54) продукта при этом втором повышенном давлении нагревают (10) примерно до температуры окружающей среды, причем- по меньшей мере, часть механической энергии, полученной при расширении (5, 8) с производством работы первого частичного потока (3), используют для привода холодного компрессора (13).2. Способ по п.1, отличающийся тем, что расширение (5, 8) первого частичного потока (2, 4, 6, 7) с производством работы проводят в двух параллельно или последователь РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК F25J 3/04 (11) (13) 2012 108 588 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2012108588/06, 10.08.2010 (71) Заявитель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ (DE) Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): РЭТБОУН Томас ( ...

VERFAHREN UND VORRICHTUNG ZUR HERSTELLUNG VON SAUERSTOFF DURCH ZWEISTUFIGE TIEFTEMPERATURREKTIFIKATION VON LUFT

VERFAHREN ZUR LUFTZERLEGUNG

Improvements in and relating to the production of oxygen

... 976,352. Cold separation of air. PETROCARBON DEVELOPMENTS Ltd. March 29, 1961 [April 4, 1960], No. 11892/60. Heading F4P. In a two-stage air rectification process for the production of gaseous oxygen both columns 13, 14 operate at superatmospheric pressure and effluent nitrogen issuing from the head of the low-pressure column 14 through a line 23 is expanded in a turbine 17 and the cold so produced is used to cool exchangers 10, 11 traversed by the compressed feed air freed of water vapour and carbon dioxide; product gaseous oxygen being discharged from the column 14 through a line 22. Prior to expansion, the effluent nitrogen is warmed in an exchanger 12 which serves to cool liquid nitrogen passing from the upper portion of the high-pressure column 13 through a line 24 and expansion valve 16 to the column 14. Product oxygen may be further compressed by the power brake 171 of the turbine 17. In a modification the effluent nitrogen also serves to cool the oxygen-rich liquid passing ...

Method and apparatus for treating a hydrocarbon stream and method of cooling a hydrocarbon stream

PROCEDURE AND DEVICE FOR THE VERY LOW-TEMPERATURE DISMANTLING OF AIR

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

By using the power generated by an expander by an expansion of material gas, the outlet pressure of a compressor is increased, and a requirement on the cooling capacity of a cooler is reduced. The liquefaction system (1) for natural gas comprises a first expander (3) for generating 5 power by expanding natural gas under pressure as material gas; a first cooling unit (11, 12) for cooling the material gas depressurized by expansion in the first expander; a distillation unit (15) for reducing or eliminating a heavy component in the material gas by distilling the material gas cooled by the first cooling unit; a first compressor (4) for compressing the material gas from which the heavy component was reduced or eliminated by the distillation unit by using the power generated in the first expander; a 0 second heat exchanger for exchanging heat between the material gas introduced into the first compressor and the material gas compressed by the first compressor; and a liquefaction unit (21) for liquefying the material gas compressed by the first compressor by exchanging heat with a refrigerant. No N N N) N r0 , > r> -Q0 (U C --------

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

... [Problem] To use the motive power generated in an expander by means of the expansion of a raw material gas to increase the discharge pressure of a compressor, and to decrease the cooling power required of a cooler. [Solution] A natural gas liquefying system (1) that is characterized by being provided with: a first expander (3) that generates motive power by expanding a raw material gas that is a natural gas obtained by pressurization; first coolers (11, 12) that cool the raw material gas that is decompressed by expansion in the first expander; a distilling device (15) that distills the raw material gas that is cooled by the first coolers and thereby reduces or eliminates the heavy components of the raw material gas; a first compressor (4) that uses the motive force generated in the first expander to compress the raw material gas from which the heavy components are reduced or eliminated in the distilling device; and a liquefying device (21) that liquefies, by means of a heat exchange with ...

Systems and Methods for Using Multiple Cryogenic Hydraulic Turbines

There is provided a system and method for producing liquefied natural gas (LNG). An exemplary method includes flowing a high-pressure stream of LNG through a first series of liquid turbines. The exemplary method also includes generating electricity by reducing the 5 pressure of the high-pressure stream of LNG to form a low-pressure stream of LNG. The exemplary method additionally includes bypassing any one the liquid turbines that has a failure while continuing to produce electricity from the first series. 102 104106 -1 108 112) 2 14 REATED LNG TO GAS NAT. GAS NGPATCARGO GSLNG PLANT _____ TREAT MENT PLANT COOLING/CONDENSATION ...

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

... [Problem] To use the motive power generated in an expander by means of the expansion of a raw material gas to increase the discharge pressure of a compressor, and to decrease the cooling power required of a cooler. [Solution] A natural gas liquefying system (1) that is characterized by being provided with: a first expander (3) that generates motive power by expanding a raw material gas that is a natural gas obtained by pressurization; first coolers (11, 12) that cool the raw material gas that is decompressed by expansion in the first expander; a distilling device (15) that distills the raw material gas that is cooled by the first coolers and thereby reduces or eliminates the heavy components of the raw material gas; a first compressor (4) that uses the motive force generated in the first expander to compress the raw material gas from which the heavy components are reduced or eliminated in the distilling device; and a liquefying device (21) that liquefies, by means of a heat exchange with ...

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 (102,112) to a pressure of at least 138 bara (2,000 psia) to form a compressed natural gas stream (114). The compressed natural gas stream is cooled (116) to form a cooled compressed natural gas stream (118). The cooled compressed natural gas stream is expanded in at least one work producing natural gas expander (120) to a pressure that is less than 207 bara (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 (122). The chilled natural gas stream is liquefied.

Cryogenic distillation method and system for air separation

Separation of air by cryogenic distillation involves use of double or triple separation column and operating at high pressure

Dans un procédé de séparation d'air par distillation cryogénique, tout l'air est porté à une haute pression plus supérieure à la moyenne pression et épuré, une partie du débit d'air épuré est refroidie dans la ligne d'échange (9) et est ensuite divisée en deux fractions, chaque fraction se détend dans une turbine (17, 19), la pression d'admission des deux turbines étant supérieure d'au moins 5 bars à la moyenne pression, la pression de refoulement d'au moins une des deux turbines est sensiblement égale à la moyenne pression, on envoie au moins une partie de l'air détendu dans au moins une des turbines à la colonne moyenne pression (100) d'une double ou triple colonne, un surpresseur froid (23) mécaniquement relié à une (19) des turbines de détente aspire de l'air, qui a subi un refroidissement dans la ligne d'échange principale, et refoule l'air à une température supérieure à la température d'admission, et le fluide ainsi comprimé est réintroduit dans la ligne d'échange principale dans ...

Air separating method, involves sending residual oxygen directly to atmosphere through tower in direct contact with water at hot end of exchange line and cold compressor that uses part of refrigerated power of turbine

A DEFROSTING METHOD OF AN APPARATUS FOR SEPARATING AIR BY CRYOGENIC DISTILLATION AND APPARATUS ADAPTED TO BE DEGIVRE BY THIS METHOD

Atmospheric air fractionating process - has separate condensation-vaporisation zone receiving oxygen enriched liquid

METHOD AND APPARATUS FOR PRODUCING A GAS PRESSURIZED AIR BY CRYOGENIC DISTILLATION

PROCESS AND APPARATUS FOR THE SEPARATION OF AIR BY CRYOGENIC DISTILLATION

A process for the separation of air by cryogenic distillation in a distillation system including at least a high pressure column (43) and a low pressure column (45) is disclosed, wherein air is compressed in a main compressor (3), compressed air is cooled in a heat exchange line (41), cooled, compressed and purified air is sent from the heat exchange line (41) to the high pressure column (43), in a first mode of operation, at least 90% of the air compressed in the main compressor (3) is further compressed to a first pressure at least 30 bars higher than the pressure of the high pressure column (43), the air at the first pressure is sent to the heat exchange line (41), cooled and divided in two, one part being liquefied and sent to the distillation system and one part being expanded in at least one turboexpander (29A, 29B) before being sent to the high pressure column (43) and in a second mode of operation, at most 70% of the air compressed in the main compressor (3) is further compressed ...

METHOD AND APPARATUS FOR TREATING A HYDROCARBON STREAM AND METHOD OF COOLING A HYDROCARBON STREAM

Method and apparatus for treating a mixed hydrocarbon feed stream (10), such as a natural gas stream. The mixed hydrocarbon feed stream (10) is expanded into a mixed-phase hydrocarbon stream (20), which is separated the to provide at least a light overhead stream (30) and a heavy bottom stream (50). The light overhead stream (30) is compressed in one or more first compressors (16) to provide one or more first compressed light streams (40) and further compressed in one or more second compressors (22) to provide one or more further compressed light streams (60). One or more first compressor recycle lines (42) extend around the or each first compressor (16), and one or more second compressor recycle lines (32) having one or more in-line coolers (34) extend around the or each second compressor (22). The method and apparatus may be used in a method of cooling an initial hydrocarbon stream (100).

APPARATUS AND METHOD FOR SUPPLYING LIQUID FUEL GAS

An apparatus and a method for supplying a liquid fuel gas having a high energy efficiency, which is efficiently using the coldness of the LNG and being capable of ensuring a supply amount of the liquid fuel gas according to the fluctuation in the composition or the demanded amount of the LNG serving as a source material with little need of the external energy, wherein the LNG supplied from a source material supplying portion 1 is vaporized via coldness releasing process through a first heat exchanger, a second heat exchanger, a third heat exchanger, a vaporizer, and an expander, and the vaporized LNG is passed through the second heat exchanger and a gas-liquid separator to form a gas-liquid mixture to be guided as the source material into the distillation tower; a branching portion is disposed in a flow passageway for guiding out the gas component from the tower top portion of the distillation tower, one gas component A derived from branching at the branching portion is supplied out via ...

CRYOGENIC SYSTEM FOR PRODUCING ELEVATED PRESSURE NITROGEN

A cryogenic air separation system for producing elevated pressure nitrogen wherein a portion of the nitrogen product fed to the product compressor (110) downstream of the primary heat exchanger (101) is withdrawn as refrigerant nitrogen from the product compressor (110), preferably from an intermediate point of the product compressor (110), and turboexpanded to generate refrigeration for the system.

PROCESS FOR SEPARATING AIR BY CRYOGENIC DISTILLATION

According to a first step in an air separation unit, all the air intended for distillation is compressed in a main compressor (1), a first stream of air, compressed in at least the main compressor, purified and cooled in a heat exchange line (6), is sent to the medium-pressure column (8) of a double column, said stream of air is divided into a nitrogen-enriched stream and an oxygen-enriched stream in the medium-pressure column, a liquid oxygen stream (16) is withdrawn from the low-pressure column, said stream is pressurized up to a high pressure and vaporized in the heat exchange line in order to form a first high-pressure oxygen-rich gas stream, at least one portion (24) of the air compressed in the main compressor is liquefied and the liquefied portion is sent to the double column, and a second oxygen-rich gas stream (115) is also produced, but at a lower pressure than the first oxygen-rich gas stream, and, in a second step, the air liquefaction pressure is increased by adjusting the ...

Air-rectification process and apparatus

An air-rectification system comprises a two-stage low-temperature separation column of the LINDE-FRANKL type connected to a heat exchanger whereby air is cooled on passage through the heat exchanger and is introduced into the high-pressure stage of the column, oxygen and nitrogen are fed from the high-pressure stage to a low-pressure stage of the column and are separated therein to form low-temperature product oxygen and nitrogen which are warmed by passage separately through the heat exchanger, and a gas stream, representing a heat-balancing stream (balance stream) is drawn from the rectification column and passed through the heat exchanger, in which one of the gas streams between the heat exchanger and the rectification column is subject to low-temperature compression. The compressed gas stream may be the balance gas stream, the incoming air after cooling in the heat exchanger or one of the product gas streams.

СПОСОБ РАЗДЕЛЕНИЯ ВОЗДУХА НА СОСТАВНЫЕ ЧАСТИ ПРИ ПОМОЩИ КРИОГЕННОЙ ДИСТИЛЛЯЦИИ

FIELD: process engineering. SUBSTANCE: in compliance with first process, entire air volume to be subjected to distillation is compressed in main compressor (1). First airflow compressed in the main compressor, purified and cooled in heat exchange line (6) is directed into medium-pressure dual column (8). Airflow is separated into flows enriched with oxygen and nitrogen in aforesaid medium-pressure column. Fluid oxygen flow (16) is extracted from low-pressure column, flow pressure is increased and it is evaporated in heat exchange line to form the first gaseous high-pressure flow enriched with oxygen. Fraction (24) of air compressed in the main compressor is liquefied and directed into dual column to produce second gaseous flow (115), enriched in oxygen but with pressure lower than that of aforesaid first gaseous flow (115). In compliance with the second process, air liquefying pressure is increased by adjusting main compressor blade system. Second gaseous flow enriched in oxygen is reduced, thus, increasing extraction of the first gaseous flow enriched in oxygen. EFFECT: perfected process, simpler design. 21 cl, 4 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 387 934 (13) C2 (51) МПК F25J 3/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21), (22) Заявка: 2008128818/06, 14.12.2006 (24) Дата начала отсчета срока действия патента: 14.12.2006 (43) Дата публикации заявки: 20.01.2010 (45) Опубликовано: 27.04.2010 Бюл. № 12 (56) Список документов, цитированных в отчете о поиске: US 5941098 A, 24.08.1999. SU 167595 A1, 18.01.1965. US 5291737 A, 08.03.1994. US 5596885 A, 28.01.1997. FR 2831249 A1, 25.04.2003. EP 1586838 A1, 19.10.2005. 2 3 8 7 9 3 4 R U (86) Заявка PCT: FR 2006/051350 (14.12.2006) C 2 C 2 (85) Дата перевода заявки PCT на национальную фазу: 15.07.2008 (87) Публикация PCT: WO 2007/068858 (21.06.2007) Адрес для переписки: 129090, Москва, ул.Б.Спасская, 25, стр.3, ООО "Юридическая ...

СПОСОБ И УСТРОЙСТВО ДЛЯ НИЗКОТЕМПЕРАТУРНОГО РАЗДЕЛЕНИЯ ВОЗДУХА

Изобретение относится к способу и устройству низкотемпературного разделения воздуха. Способ и устройство служат в установке для разделения воздуха, которая содержит основной воздушный компрессор, основной теплообменник и систему дистилляционных колонн с колонной высокого давления и колонной низкого давления. Способ реализуется следующим образом: подаваемый воздух сжимается в основном воздушном компрессоре до первого давления, которое выше, чем рабочее давление колонны высокого давления, первая часть сжатого воздушного потока как первый воздушный поток при первом давлении охлаждается в основном теплообменнике и сжижается или псевдосжижается, затем расширяется и вводится в систему дистилляционных колонн, вторая часть сжатого воздушного потока как второй воздушный поток дополнительно сжимается в воздушном дополнительном компрессоре до второго давления, которое выше, чем первое давление, и по меньшей мере частично дополнительно сжимается в первом приводимом турбиной дополнительном компрессоре ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ ГАЗОВ ИЗ ВОЗДУХА В ГАЗООБРАЗНОМ И ЖИДКОМ СОСТОЯНИИ С ВЫСОКОЙ ГИБКОСТЬЮ ПУТЕМ КРИОГЕННОЙ ДИСТИЛЛЯЦИИ

1. Способ получения, по меньшей мере, одного газа из воздуха путем криогенной дистилляции в системе колонн, включающей в себя, по крайней мере, одну колонну среднего давления, работающую в режиме среднего давления, одну колонну низкого давления, действующую под низким давлением, термически связанные между собой, в котором в первом и во втором варианте функционирования ! а) общий объем подаваемого сжатого воздуха (1) доводят до высокого давления, которое не менее чем на 5 бар выше давления колонны среднего давления, и очищают под этим высоким давлением, называемым основным давлением; ! б) это основное давление при необходимости изменяют в зависимости от производственных требований; ! в) первую порцию воздуха, подаваемого под давлением не ниже основного давления, охлаждают в линии обмена до ее средней температуры и расширяют, по меньшей мере, в первой турбине (21); ! г) в случае необходимости вторую порцию подаваемого воздуха расширяют, по меньшей мере, во второй турбине (21В), в которой условия впуска и выпуска отличаются не более чем на 5 бар и не более чем на 15°C от давления и температуры первой турбины или равны им; ! д) в случае необходимости работу первой или третьей турбины, по меньшей мере, частично, используют для работы, необходимой вспомогательному компрессору для повышения давления сжатого воздуха (13); ! е) давление впуска первой турбины (21) по существу значительно выше, чем среднее давление, а в случае необходимости превосходит основное давление; ! ж) давление на выходе первой турбины превышает среднее давление или равно ему, в предпочтительном варианте исполнения по существу равно среднему давлению; ! з) во вспом� РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2009 137 781 (13) A (51) МПК F25J 3/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2009137781/06, 26.02.2008 (71) Заявитель(и): Л`ЭР ЛИКИД СОСЬЕТЕ АНОНИМ ПУР Л`ЭТЮД Э Л`ЭКСПЛУАТАСЬОН ДЕ ПРОСЕДЕ ЖОРЖ КЛОД (FR) Приоритет ...

СПОСОБ ВЫДЕЛЕНИЯ

... 1. Способ выделения фракции с высоким содержанием компонентов C2, C2/CO2, C2+ или C3+ из фракции с высоким содержанием углеводородов, в котором фракцию с высоким содержанием углеводородов подвергают одно- или многостадийному сбросу давления, осуществляют ректификационную отгонку метана, а из обедненной по метану фракции, полученной после отгонки метана, ректификацией выделяют компоненты C2, C2/CO2, C2+ или C3+, отличающийся тем, что зона нагревания (E2) в нижней части колонны ректификационной отгонки метана (M) связана через контур охлаждения C3 (V4, E4, E5, 20-27) с зоной охлаждения (E3) в верхней части колонны ректификационной отгонки компонентов C2, C2/CO2, C2+ или C3+ (E). ! 2. Способ по п.1, отличающийся тем, что контур охлаждения C3 (V4, 20-27) выполнен одноступенчатым. ! 3. Способ по п.1 или 2, отличающийся тем, что теплообмен между хладагентом контура охлаждения C3 и нагреваемой средой в нижней части колонны, а также охлаждаемой средой в верхней части колонны осуществляют в отдельных ...

Systems and methods for using multiple cryogenic hydraulic turbines

There is provided a system and method for producing liquefied natural gas (LNG). An exemplary method includes flowing a high-pressure stream of LNG through a first series of liquid turbines. The exemplary method also includes generating electricity by reducing the pressure of the high-pressure stream of LNG to form a low-pressure stream of LNG. The exemplary method additionally includes bypassing any one the liquid turbines that has a failure while continuing to produce electricity from the first series.

Method and apparatus for controlling a compressor and method of cooling a hydrocarbon stream

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 (102,112) to a pressure of at least 138 bara (2,000 psia) to form a compressed natural gas stream (114). The compressed natural gas stream is cooled (116) to form a cooled compressed natural gas stream (118). The cooled compressed natural gas stream is expanded in at least one work producing natural gas expander (120) to a pressure that is less than 207 bara (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 (122). The chilled natural gas stream is liquefied.

INTEGRATION OF INDUSTRIAL GAS SITE WITH LIQUID HYDROGEN PRODUCTION

The method for producing liquid hydrogen (346) can include the steps of: introducing pressurized natural gas (302) from a high pressure natural gas pipeline (300) to a gas processing unit under conditions effective for producing a purified hydrogen stream (315); and introducing the purified hydrogen stream to a hydrogen liquefaction unit under conditions effective to produce a liquid hydrogen stream (346), wherein the hydrogen liquefaction unit provides a warm temperature cooling and a cold temperature cooling to the purified hydrogen stream, wherein the warm temperature cooling is provided by utilizing letdown energy of a pressurized stream selected from the group consisting of a nitrogen stream (320) sourced from a nitrogen pipeline, a natural gas stream (2) sourced from the high pressure natural gas pipeline (300), an air gas (86) sourced from an air separation unit (ASU), and combinations thereof, wherein the cold temperature is provided by utilizing letdown energy of the purified hydrogen ...

METHOD FOR SEPARATING AIR BY CRYOGENIC DISTILLATION

METHOD FOR OPERATING AIR SEPARATION PLANT

Integration of industrial gas site with liquid hydrogen production

The method for producing liquid hydrogen can include the steps of: introducing pressurized natural gas from a high pressure natural gas pipeline to a gas processing unit under conditions effective for producing a purified hydrogen stream; and introducing the purified hydrogen stream to a hydrogen liquefaction unit under conditions effective to produce a liquid hydrogen stream, wherein the hydrogen liquefaction unit provides a warm temperature cooling and a cold temperature cooling to the purified hydrogen stream, wherein the warm temperature cooling is provided by utilizing letdown energy of a pressurized stream selected from the group consisting of a nitrogen stream sourced from a nitrogen pipeline, a natural gas stream sourced from the high pressure natural gas pipeline, an air gas sourced from an air separation unit, and combinations thereof, wherein the cold temperature is provided by utilizing letdown energy of the purified hydrogen stream.

Process for Separating Hydrogen from an Olefin Hydrocarbon Effluent Vapor Stream

One or more specific embodiments disclosed herein includes a method for separating hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream, employing a single heat exchanger, multiple gas-liquid separators, multiple expander/compressor sets, and a rectifier attached to a liquid product drum. 1. A process for the separation of hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream from a dehydrogenation unit , which process comprises:a. cooling a compressed effluent vapor stream in a heat exchanger;b. separating hydrogen from olefin and heavy paraffinic components in the cooled compressed effluent vapor stream in a first separator to provide a first vapor stream and a first liquid stream;c. cooling the first vapor stream in the heat exchanger;d. separating hydrogen from olefin and heavy paraffinic components in the cooled first vapor stream in a second separator to provide a second vapor stream and a second liquid stream;e. warming the second vapor stream in the heat exchanger;f. isentropically expanding the second vapor stream, wherein the pressure and temperature of the second vapor stream is lowered;g. dividing the second vapor stream into a first split stream and a second split stream;h. warming the first split stream in the heat exchanger;i. compressing the first split stream;j. cooling the first split stream in a first discharge cooler;k. withdrawing a gas product;l. cooling a liquid paraffinic stream in the heat exchanger;m. combining the cooled liquid paraffinic stream with the second split stream to provide a combined feed;n. vaporizing the combined feed in the heat exchanger;o. withdrawing the vaporized combined feed;p. lowering the pressure of the first liquid stream in a control valve;q. partially vaporizing the first liquid stream in the heat exchanger;r. flashing the partially vaporized first liquid stream in a liquid product drum to provide a hydrogen-rich gas, which travels to a rectifier connected to the liquid ...

METHOD AND APPARATUS FOR CONTROLLING A COMPRESSOR AND METHOD OF COOLING A HYDROCARBON STREAM

Systems And Methods For Using Multiple Cryogenic Hydraulic Turbines

There is provided a system and method for producing liquefied natural gas (LNG). An exemplary method includes flowing a high-pressure stream of LNG through a first series of liquid turbines. The exemplary method also includes generating electricity by reducing the pressure of the high-pressure stream of LNG to form a low-pressure stream of LNG. The exemplary method additionally includes bypassing any one the liquid turbines that has a failure while continuing to produce electricity from the first series. 1. A method for generating electricity from liquid turbines , comprising:{'sup': 'st', 'flowing a high-pressure liquid stream through a first plurality of n liquid turbines coupled in a first series, wherein, after a first turbine in the series, an inlet of each of the second through the n-1liquid turbines is coupled to an outlet of a proceeding liquid turbine;'}generating electricity from the first series by removing energy from the high-pressure liquid stream to form a low-pressure liquid stream;bypassing any one of the first plurality of liquid turbines that has a failure while continuing to produce electricity with the remaining turbines of the first series; andoperating the first plurality of liquid turbines in the first series that are not bypassed to maintain a pressure and flow rate of the low-pressure liquid stream.2. The method of claim 1 , further comprising:maintaining the total electrical output from the first series as a constant value when a liquid turbine is bypassed.3. The method of claim 1 , further comprising:maintaining the temperature of the low-pressure liquid stream from the first series when a liquid turbine is bypassed.4. The method of claim 1 , further comprising:removing a portion of the high-pressure liquid stream prior to the first series;{'sup': 'st', 'flowing the portion through a second plurality of n liquid turbines coupled in a second series, wherein, after a first turbine in the series, an inlet of each of the second through the n- ...

INTEGRATION OF INDUSTRIAL GAS SITE WITH LIQUID HYDROGEN PRODUCTION

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

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 FOR THE INTEGRATION OF LIQUEFIED NATURAL GAS AND SYNGAS PRODUCTION

An integrated method for the production of liquefied natural gas (LNG) and syngas is provided. The method can include the steps of: utilizing letdown energy of a high pressure natural gas stream that is withdrawn from a natural gas pipeline to provide a warm temperature cooling; utilizing a refrigeration cycle to provide a cold temperature cooling, wherein the refrigeration cycle comprises a refrigerant recycle compressor that is powered utilizing a steam turbine; and cooling a second high pressure natural gas stream using the warm temperature cooling and the cold temperature cooling to produce an LNG product stream. The second high pressure natural gas stream is withdrawn from the natural gas pipeline, and the steam turbine is powered by high pressure steam that is produced from a syngas production facility. 1. A method for the production of liquefied natural gas (“LNG”) , the method comprising the steps of:a) operating a syngas production facility that is configured to convert a first natural gas stream into a syngas stream, wherein the syngas production facility is further configured to produce a pressurized steam, wherein the pressurized steam is fed to a steam turbine, wherein during said operating step, the syngas production facility uses a second natural gas stream at a lower pressure than the first natural gas stream;b) cooling and liquefying a third natural gas stream using refrigeration provided by at least two different sources to produce an LNG product stream;c) providing a first source for the refrigeration used in step b) by expanding the second natural gas stream in a natural gas expander and then warming the second natural gas stream, prior to being used in the syngas production facility in step a), against the third natural gas stream; andd) providing a second source for the refrigeration used in step b) using a nitrogen refrigeration cycle, wherein the nitrogen refrigeration cycle comprises a nitrogen recycle compressor and at least one turbine, ...

METHOD FOR STARTING UP A CRYOGENIC AIR SEPARATION UNIT AND ASSOCIATED AIR SEPARATION UNIT

In a process for starting up an air separation unit, which is at a temperature of above 0° C., the air separation unit comprising a main air compressor for compressing the feed air, a booster driven by a turbine and a venting conduit connected downstream of the booster and upstream of the main heat exchanger wherein in order to start up the air separation unit, once the turbine is operating at said given speed, the venting conduit is opened to send at least part of the air compressed in the booster from the booster outlet to the atmosphere. 115-. (canceled)16. A process for starting up an air separation unit which is at a temperature of above 0° C. , the air separation unit comprising:a main air compressor for compressing the feed air,a main heat exchanger,a conduit for sending compressed air from the main air compressor to the main heat exchanger to be cooled,a booster,a conduit for sending at least part of the compressed air cooled in the main heat exchanger to the booster,means for sending air to the main heat exchanger from the booster, there being no means for cooling the air downstream of the booster and upstream of the main heat exchanger,a column system,at least one turbine connected to receive compressed air from the main air compressor and possibly from the booster, the at least one turbine being connected to the column system to provide air to be distilled in the column system,a conduit from removing an oxygen enriched product from the column system and sending the oxygen enriched product to be warmed in the main heat exchanger,a conduit from removing an nitrogen enriched product from the column system and sending the nitrogen enriched product to be warmed in the main heat exchanger;wherein, during normal operation, the air separation unit is configured such that air is sent from the main air compressor to the heat exchanger, cooled in the heat exchanger, compressed in the booster, cooled in the heat exchanger and separated in the column system, air is ...

Energy recovery from reduction in pressure of a dense phase hydrocarbon fluid

Disclosed are processes in which the pressure of a dense phase fluid stream containing hydrocarbons is reduced to produce a two-phase fluid stream, and energy is recovered. The process includes passing the dense phase fluid stream at a pressure greater than the cricondenbar pressure of the dense phase fluid stream through an expander where the dense phase fluid stream is expanded isentropically such that a two phase fluid stream having a pressure lower than the pressure of the dense phase fluid stream leaves the expander. The expander is coupled to a rotating mechanical power user, such that the expander drives the rotating mechanical power user. The process further includes passing the two phase fluid stream leaving the expander to a separator such that the two phase fluid stream is separated into a vapor phase stream and a liquid phase stream. The composition or quantity of liquid formed can be adjusted to control the dew point of the gas produced from the dense-phase fluid.

Process for Separating Hydrogen from an Olefin Hydrocarbon Effluent Vapor Stream

One or more specific embodiments disclosed herein includes a method for separating hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream, employing a single heat exchanger, multiple gas-liquid separators, multiple expander/compressor sets, and a rectifier attached to a liquid product drum. 1. A process for the separation of hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream from a dehydrogenation unit , which process comprises:a. cooling a compressed effluent vapor stream in a heat exchanger, wherein the heat exchanger comprises a warm section and a cold section;b. separating hydrogen from olefin and heavy paraffinic components in the cooled compressed effluent vapor stream in a first separator to provide a first vapor stream and a first liquid stream;c. cooling the first vapor stream in the heat exchanger;d. separating hydrogen from olefin and heavy paraffinic components in the cooled first vapor stream in a second separator to provide a second vapor stream and a second liquid stream;e. warming the second vapor stream in the heat exchanger;f. isentropically expanding, in a high-pressure expander, the second vapor stream, wherein the pressure and temperature of the second vapor stream are lowered;g. warming the second vapor stream in the heat exchanger;h. compressing, in a high-pressure compressor, the second vapor stream;i. cooling the second vapor stream in a first discharge cooler;j. dividing the second vapor stream into a gas product and a split stream;k. withdrawing a gas product;l. compressing, in a low-pressure compressor, the split stream;m. cooling the split stream in a second discharge cooler and further cooling the split stream in the heat exchanger;n. isentropically expanding, in a low-pressure expander, the split stream, wherein the pressure and temperature of the split stream are lowered;o. cooling a liquid paraffinic stream in the heat exchanger;p. combining the cooled liquid paraffinic stream with the ...

Apparatus and Process for Liquefying Gases

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

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

By using the power generated by an expander by an expansion of material gas, the outlet pressure of a compressor is increased, and a requirement on the cooling capacity of a cooler is reduced. The liquefaction system () for natural gas comprises a first expander () for generating power by using natural gas under pressure as material gas; a first cooling unit () for cooling the material gas depressurized by expansion in the first expander; a distillation unit () for reducing or eliminating a heavy component in the material gas by distilling the material gas cooled by the first cooling unit; a first compressor () for compressing the material gas from which the heavy component was reduced or eliminated by the distillation unit by using power generated in the first expander; and a liquefaction unit () for liquefying the material gas compressed by the first compressor by exchanging heat with a refrigerant. 1. A system for the liquefaction of natural gas that cools the natural gas to produce liquefied natural gas , comprising:a first expander for generating power by expanding natural gas under pressure as material gas;a first cooling unit for cooling the material gas depressurized by expansion in the first expander;a distillation unit for reducing or eliminating a heavy component in the material gas by distilling the material gas cooled by the first cooling unit;a first compressor for compressing the material gas from which the heavy component was reduced or eliminated by the distillation unit by using the power generated in the first expander; anda liquefaction unit for liquefying the material gas compressed by the first compressor by exchanging heat with a refrigerant.2. The system for the liquefaction of natural gas according to claim 1 , further comprising a second cooling unit placed between the first compressor and the liquefaction unit to cool the material gas compressed by the first compressor.3. The system for the liquefaction of natural gas according to claim 1 ...

Process for Separating Hydrogen from an Olefin Hydrocarbon Effluent Vapor Stream

One or more specific embodiments disclosed herein includes a method for separating hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream, employing a integrated heat exchanger, multiple gas-liquid separators, external refrigeration systems, and a rectifier attached to a liquid product drum. 1. A process for the separation of hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream from a dehydrogenation unit , which process comprises:a. introducing a compressed effluent vapor stream into a processing unit;b. cooling the compressed effluent vapor stream in a heat exchanger;c. separating hydrogen from olefin and heavy paraffinic components in the cooled compressed effluent vapor stream in a first separator to provide a first vapor stream and a first liquid stream;d. cooling a first vapor stream in the heat exchanger;e. separating hydrogen from olefin and heavy paraffinic components in the cooled first vapor stream in a second separator to provide a second vapor stream and a second liquid stream;f. dividing the second vapor stream into a first split stream and a second split stream;g. warming the first split stream in the heat exchanger to produce a gas product;h. withdrawing the gas product from the processing unit;i. lowering the pressure of the second split stream in a control valve, wherein the temperature of the second spilt stream is reduced;j. cooling a liquid paraffinic stream in the heat exchanger;k. combining the cooled liquid paraffinic stream with the cooled second split stream to provide a combined feed;l. vaporizing the combined feed in the heat exchanger;m. withdrawing the vaporized combined feed;n. lowering the pressure of the first liquid stream in a control valve;o. partially vaporizing the first liquid stream in the heat exchanger;p. flashing the partially vaporized first liquid stream in a liquid product drum to provide a hydrogen-rich gas, which travels to a rectifier connected to the liquid product drum;q. ...

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 ...

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

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

Systems and Methods for Using Multiple Cryogenic Hydraulic Turbines

There is provided a system and method for producing liquefied natural gas (LNG). An exemplary method includes flowing a high-pressure stream of LNG through a first series of liquid turbines. The exemplary method also includes generating electricity by reducing the pressure of the high-pressure stream of LNG to form a low-pressure stream of LNG. The exemplary method additionally includes bypassing any one the liquid turbines that has a failure while continuing to produce electricity from the first series. 1. A method for generating electricity from liquid turbines , comprising:{'b': '1', 'in a normal mode, flowing a high-pressure liquid stream through a first plurality of n liquid turbines coupled in a first series, wherein, after a first turbine in the series, an inlet of each of a second through an n- liquid turbine is coupled to an outlet of a preceding liquid turbine;'}generating electricity from the first series by removing energy from the high-pressure liquid stream to form a low-pressure liquid stream; andbypassing any one of the first plurality of liquid turbines that has a failure while continuing to produce electricity with the remaining turbines of the first series.2. The method of claim 1 , further comprising:maintaining a total electrical output from the first series as a constant value when a liquid turbine is bypassed.3. The method of claim 1 , further comprising:operating the first plurality of liquid turbines in the first series that are not bypassed to maintain a pressure, temperature, and flow rate of the low-pressure liquid stream from the first series to be the same as a pressure, temperature, and flow rate of the low-pressure liquid stream when operating in the normal mode.4. The method of claim 1 , further comprising:removing a portion of the high-pressure liquid stream prior to the first series;{'b': '1', 'flowing the portion through a second plurality of n liquid turbines coupled in a second series, wherein, after a first turbine in the ...

NITROGEN PROCESS FOR PRODUCTION OF AMMONIA AND LIQUID HYDROGEN

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

Process for Separating Hydrogen from an Olefin Hydrocarbon Effluent Vapor Stream

One or more specific embodiments disclosed herein includes a method for separating hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream, employing a integrated heat exchanger, multiple gas-liquid separators, external refrigeration systems, and a rectifier attached to a liquid product drum. 1. A process for the separation of hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream from a dehydrogenation unit , which process comprises:a. introducing a compressed effluent vapor stream into a processing unit;b. cooling the compressed effluent vapor stream in a heat exchanger;c. separating hydrogen from olefin and heavy paraffinic components in the cooled compressed effluent vapor stream in a first separator to provide a first vapor stream and a first liquid stream;d. cooling the first vapor stream in the heat exchanger;e. separating hydrogen from olefin and heavy paraffinic components in the cooled first vapor stream in a second separator to provide a second vapor stream and a second liquid stream;f. warming the second vapor stream in the heat exchanger to produce a gas product;g. lowering the pressure of the first liquid stream in a first control valve to provide a pressure-reduced first liquid stream;h. dividing the second liquid stream into first liquid split stream and a second liquid split stream;i. lowering the pressure of the first liquid split stream in a second control valve to provide a pressure-reduced first liquid split stream;j. warming the pressure-reduced first liquid split stream in the heat exchanger to provide a partially vaporized stream;k. lowering the pressure of the second liquid split stream in a third control valve to provide a pressure-reduced second liquid split stream;l. flashing the pressure-reduced first liquid stream and the partially vaporized stream in a liquid product drum to provide a hydrogen-rich gas, which travels to a rectifier connected to the liquid product drum;m. combining the hydrogen-rich ...

System and method for liquefaction of natural gas

By controlling an excessive rise in the temperature of the material gas that is introduced into the liquefaction unit following the compression by a compressor, the temperature of the material gas may be adjusted to the temperature level at the introduction point of the liquefaction unit. A system ( 1 ) for the liquefaction of natural gas, comprises a first expander ( 3 ) for expanding natural gas under pressure as material gas; a first cooling unit ( 10, 11, 12 ) for cooling the material gas; a distillation unit ( 15 ) for reducing or eliminating a heavy component in the material gas by distilling the material gas cooled by the first cooler; a first compressor ( 4 ) for receiving a top fraction of the material gas from which the heavy component was reduced or eliminated by the distillation unit; and a liquefaction unit ( 21 ) for liquefying a gas phase component separated from the compressed material gas compressed by the first compressor by exchanging heat with a refrigerant.

SYSTEM AND METHOD FOR LIQUEFACTION OF NATURAL GAS

By using the power generated by an expander by an expansion of material gas, the outlet pressure of a compressor is increased, and a requirement on the cooling capacity of a cooler is reduced. The liquefaction system () for natural gas comprises a first expander () for generating power by using natural gas under pressure as material gas; a first cooling unit () for cooling the material gas depressurized by expansion in the first expander; a distillation unit () for reducing or eliminating a heavy component in the material gas by distilling the material gas cooled by the first cooling unit; a first compressor () for compressing the material gas from which the heavy component was reduced or eliminated by the distillation unit by using power generated in the first expander; and a liquefaction unit () for liquefying the material gas compressed by the first compressor by exchanging heat with a refrigerant. 1. A system for the liquefaction of natural gas that cools the natural gas to produce liquefied natural gas , comprising:a first expander for generating power by expanding natural gas under pressure as material gas;a first cooling unit for cooling the material gas depressurized by expansion in the first expander;a distillation unit for reducing or eliminating a heavy component in the material gas by distilling the material gas cooled by the first cooling unit;a first compressor for compressing the material gas from which the heavy component was reduced or eliminated by the distillation unit by using the power generated in the first expander; anda liquefaction unit for liquefying the material gas compressed by the first compressor by exchanging heat with a refrigerant.2. The system for the liquefaction of natural gas according to claim 1 , further comprising a second cooling unit placed between the first compressor and the liquefaction unit to cool the material gas compressed by the first compressor.3. The system for the liquefaction of natural gas according to claim 1 ...

METHOD AND DEVICE FOR SEPARATING AIR BY CRYOGENIC DISTILLATION

A method for separating air by cryogenic distillation, wherein air is compressed in a first compressor, cooled in a heat exchanger and then separated in a system of columns, liquid oxygen is vaporized in the heat exchanger countercurrent to a flow of pressurized gas which pseudo-condenses, a flow of gas which is air or a gas delivered from the system of columns is expanded in a cryogenic expansion turbine having a single wheel, the turbine having an inlet temperature lower than −100° C., a gas which is air or a gas delivered from the system of columns is compressed in a first booster compressor having a single wheel, with an inlet temperature higher than −50° C., a gas which is air or a gas delivered from the system of columns. 115.-. (canceled)16. A method for separating air by cryogenic distillation , wherein air is compressed in a first compressor , cooled in a heat exchanger and then separated in a system of columns , liquid oxygen is vaporized in the heat exchanger countercurrent to a flow of pressurized gas which pseudo-condenses , a flow of gas which is air or a gas delivered from the system of columns is expanded in a cryogenic expansion turbine having a single wheel , the turbine having an inlet temperature lower than −100° C. , a gas which is air or a gas delivered from the system of columns is compressed in a first booster compressor having a single wheel , with an inlet temperature higher than −50° C. , a gas which is air or a gas delivered from the system of columns , this gas having already been compressed in the first booster compressor , is compressed in a second booster compressor having a single wheel with an inlet temperature lower than −100° C. , the gas compressed in at least the first booster compressor cools in the heat exchanger , contributes to the vaporization of liquid oxygen by exchange of heat in the exchanger , and is pseudo-liquefied on leaving the cold end of the heat exchanger , wherein:a) the work generated by the expansion turbine ...

PROCESS FOR OBTAINING ONE OR MORE AIR PRODUCTS AND AIR SEPARATION PLANT

The invention proposes a process and an air separation plant comprising a rectification column system comprising a high-pressure column, a low-pressure column, a main heat exchanger, and a main air compressor. The total air supplied to the rectification column system is compressed in the main air compressor to a first pressure level. The high-pressure column is operated at a second pressure level, at least 3 bar below the first pressure level. A gaseous, nitrogen-rich fluid is removed from the high-pressure column and warmed up in the gaseous state without prior liquefaction. A first partial quantity of the gaseous, nitrogen-rich fluid is warmed to a first temperature level of −150 to −100° C., supplied at this first temperature level to a booster and compressed further to a third pressure level. The first partial quantity is then warmed to a second temperature level and discharged from the air separation plant. 2121215. Process according to claim 1 , in which a second partial quantity of the gaseous nitrogen-rich fluid is warmed up together with the first partial quantity to the first temperature level claim 1 , supplied at this temperature level to the booster () claim 1 , and compressed further to the third pressure level by using the booster () claim 1 , the second partial quantity after compression to the third pressure level being cooled down to a third temperature level below the first temperature level claim 1 , subsequently expanded to the second pressure level and returned into the high-pressure column ().3100. Process according to claim 2 , in which a third partial quantity of the nitrogen-rich fluid without compression to the third pressure level is warmed up to the first temperature level and discharged permanently from the air separation plant ().4999. Process according to claim 2 , in which the first and second partial quantities are warned up to the first temperature level by using the main heat exchanger () claim 2 , and/or the first partial ...

一种混合塔制氧方法

本发明公开了一种混合塔制氧方法，步骤如下：1、空气经自洁式空气过滤器过滤后进入空气压缩机压缩，进入空气预冷系统；2、空气在空冷塔中被冷却水以及被水冷塔和冷水机组冷却的冷冻水冷却降温，并经水洗涤，除掉水溶性杂质后进入分子筛纯化系统；3、空气中的水分、二氧化碳等筛除掉后进入分成四路：第一路进入分馏塔内冷却至液化温度‑168℃后分别进入下塔；第二路空气去膨胀机增压端，经冷却器冷却后进入主换热器换热后，经透平膨胀机进行制冷，膨胀后的空气进入上塔精馏；第三路空气在下塔精馏得到液氮和富氧液空，进上塔各物料经精馏后得到液氧、污氮气；第四路作为仪表气。通过上述方式，本发明既生产压力氧，又降低空压机压力，提高提取率。

Process to obtain liquefied natural gas

A process to obtain liquefied natural gas (LNG) which comprises the use of air as refrigerant in an open or closed cycle. The invention also refers to a system to carry out said process and uses thereof.

Process for Separating Hydrogen from an Olefin Hydrocarbon Effluent Vapor Stream

One or more specific embodiments disclosed herein includes a method for separating hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream, employing an integrated heat exchanger, multiple gas-liquid separators, external refrigeration systems, and a rectifier attached to a liquid product drum.

Process to obtain liquefied natural gas

A process to obtain liquefied natural gas (LNG) which comprises the use of air as refrigerant in an open or closed cycle. The invention also refers to a system to carry out said process and uses thereof.

用于空气分离的低温蒸馏方法和系统

本发明涉及一种用于空气分离的低温蒸馏方法。根据本发明，使所有空气处于高压并在高压下被净化，所述高压高于中压至少5巴。一部分净化后的空气流在热交换管路(9)中冷却，然后被分成两小部分。各小部分在涡轮机(17，19)中膨胀，两个涡轮机的入口压力高于中压至少5巴。此外，两个涡轮机中的至少一个的输出压力基本上等于中压。在至少一个涡轮机中膨胀的空气的至少一部分被输送至双塔或三塔的中压塔(100)。然后，机械连接至其中一个涡轮膨胀机(19)的冷增压器(23)吸入在主热交换管路中冷却的空气，并以高于入口温度的温度排出所述空气。这样被压缩的流体被再次引入主热交换管路，在其中至少一部分该流体(33，37)冷凝。另外，来自其中一个塔(200)的至少一种加压液体(25)在热交换管路中在汽化温度被汽化。此外，未连接至冷增压器(23)的涡轮机(17)设有选自以下的能量消耗装置：i)不同于该冷增压器的增压器(5)，其被机械联接并在后面设有冷却器，ii)油阀系统，iii)发电机(61)。

天然气液化系统和方法

通过使用由原料气体的膨胀使膨胀机产生的动力，增大压缩机的出口压力，并降低对于冷却器的冷却容量的要求。天然气液化系统(1)包括：第一膨胀机(3)，其用于通过使用压力状态下的天然气作为原料气体来产生动力；第一冷却单元(11，12)，其用于冷却在所述第一膨胀机中通过膨胀减压的所述原料气体；蒸馏单元(15)，其用于通过蒸馏由所述第一冷却单元冷却的所述原料气体来减少或除去所述原料气体中的重质组分；第一压缩机(4)，其用于通过使用在所述第一膨胀机中所产生的动力来压缩通过所述蒸馏单元从其中减少或除去所述重质组分的所述原料气体；以及液化单元(21)，其用于通过与制冷剂进行热交换来液化由所述第一压缩机压缩的所述原料气体。

工业气体场所与液氢生产的一体化

用于生产液氢的方法(346)可以包括以下步骤：将来自高压天然气管道(300)的加压天然气(302)引入处于有效产生经纯化氢流(315)的条件下的气体处理单元；并且将该经纯化氢流引入处于有效产生液氢流的条件下的氢液化单元(346)，其中，该氢液化单元对该经纯化氢流提供暖温冷却和冷温冷却，其中，该暖温冷却是通过利用选自下组的加压流的泄放能量来提供的，该组由以下组成：源自氮管道的氮流(320)、源自该高压天然气管道(300)的天然气流(2)、源自空气分离单元(ASU)的空气气体(86)、及其组合，其中，通过利用该经纯化氢流的泄放能量来提供该冷温。

argon tail gas recovery and purification device containing methane and hydrocarbon

本发明涉及一种含甲烷、碳氢化合物的氩尾气回收提纯装置，用于回收处理含杂质甲烷、碳氢化合物、CO、H 2 、N 2 的氩尾气，含甲烷、碳氢化合物的氩尾气回收提纯装置与用于净化氩尾气并输出净化后的原料气的前端净化系统相连接，含甲烷、碳氢化合物的氩尾气回收提纯装置包括：用于去除净化后的原料气中的甲烷、碳氢化合物并输出待精馏的粗氩气的脱甲烷和碳氢化合物系统；用于精馏待精馏的粗氩气而得到产品氩气的精馏系统；用于为精馏系统提供热源和冷源、为前端净化系统提供再生气的气体循环系统。本发明能够实现安全、高效的有油氩尾气回收，从而避免氩组分浪费。

Natural gas liquefying system and liquefying method

通过使用由原料气体的膨胀使膨胀机产生的动力，增大压缩机的出口压力，并降低对于冷却器的冷却容量的要求。天然气液化系统(1)包括：第一膨胀机(3)，其用于通过使用压力状态下的天然气作为原料气体来产生动力；第一冷却单元(11，12)，其用于冷却在所述第一膨胀机中通过膨胀减压的所述原料气体；蒸馏单元(15)，其用于通过蒸馏由所述第一冷却单元冷却的所述原料气体来减少或除去所述原料气体中的重质组分；第一压缩机(4)，其用于通过使用在所述第一膨胀机中所产生的动力来压缩通过所述蒸馏单元从其中减少或除去所述重质组分的所述原料气体；以及液化单元(21)，其用于通过与制冷剂进行热交换来液化由所述第一压缩机压缩的所述原料气体。

METHOD AND DEVICE FOR LOW-TEMPERATURE AIR SEPARATION

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2015 126 605 A (51) МПК B01D 53/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2015126605, 02.07.2015 (71) Заявитель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ (DE) Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): ГОЛУБЕВ Дмитрий (DE) 05.07.2014 EP 14002309.4 Адрес для переписки: 129090, Москва, ул. Б. Спасская, 25, стр. 3, ООО "Юридическая фирма Городисский и Партнеры" Стр.: 1 A 2 0 1 5 1 2 6 6 0 5 R U A (57) Формула изобретения 1. Способ низкотемпературного разделения воздуха в установке разделения воздуха, которая содержит основной воздушный компрессор, основной теплообменник (8) и систему дистилляционных колонн с колонной (10) высокого давления и колонной низкого давления, причем - весь подаваемый воздух (1) в основном воздушном компрессоре (3а) сжимается до первого воздушного давления, которое по меньшей мере на 3 бар выше, чем рабочее давление колонны высокого давления, чтобы сформировать сжатый полный воздушный поток (4, 7), - первая часть сжатого полного воздушного потока как первый воздушный поток (100) при первом воздушном давлении охлаждается в основном теплообменнике (8) и сжижается или псевдо-сжижается, затем расширяется (101) и вводится (102, 9) в систему дистилляционных колонн, - вторая часть сжатого полного воздушного потока как второй воздушный поток (200) дополнительно сжимается в воздушном дополнительном компрессоре (3b) до второго воздушного давления, которое выше, чем первое воздушное давление, и по меньшей мере первая часть второго воздушного потока дополнительно сжимается в системе дополнительного сжатия до третьего воздушного давления, которое выше, чем второе воздушное давление, причем система дополнительного сжатия имеет по меньшей мере первый приводимый турбиной дополнительный компрессор (202с), - первый частичный поток второго воздушного потока как третий воздушный поток (210) при первом входном давлении турбины вводится в первую турбину ( ...

Method for producing one or more products from air and air separation unit

FIELD: cryogenic equipment. SUBSTANCE: invention relates to cryogenic equipment; it can be used in air separation. One or more products from the air are obtained using air separation unit (100) having system (14-17) of distillation columns, which includes high-pressure column (14) and low-pressure column (15), as well as main heat exchanger (9) and main air compressor. The total volume of air supplied to system (10-17) of distillation columns is compressed in main air compressor (1) to the first pressure level, and high-pressure column (15) is operated at the second pressure level, which is at least 300 kPa lower than the first pressure level. Gaseous nitrogen-saturated fluid is extracted from high-pressure column (15) at the second pressure level and heated in a gaseous state. The first partial amount of gaseous nitrogen-saturated fluid is heated to the first temperature level from -150 to -100°C, supplied at the first temperature level into booster (12), and, using booster (12), is additionally compressed to the third pressure level. The specified first partial amount after compression to the third pressure level is heated to the second temperature level above the first temperature level and is constantly discharged from unit (100). EFFECT: increased efficiency. 14 cl, 4 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 768 445 C2 (51) МПК F25J 3/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК F25J 3/04024 (2022.02); F25J 3/04054 (2022.02); F25J 3/04175 (2022.02); F25J 3/04296 (2022.02); F25J 3/04351 (2022.02); F25J 3/04412 (2022.02) (21)(22) Заявка: 2018120350, 01.06.2018 01.06.2018 (73) Патентообладатель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЬШАФТ (DE) Дата регистрации: 24.03.2022 Приоритет(ы): (30) Конвенционный приоритет: 02.06.2017 EP 17020238.6 (43) Дата публикации заявки: 03.12.2019 Бюл. № 34 (45) Опубликовано: 24.03.2022 Бюл. № 9 2 7 6 8 4 4 5 R U (54) Способ получения одного или более продуктов из воздуха и ...

Natural gas processing equipment and liquefied natural gas carrier

System and method of production of liquefied natural gas

본 발명은 개방 사이클 또는 폐쇄 사이클 내 냉각제(refrigerant)로써 공기를 사용하는 단계를 포함하는 액화 천연가스의 제조 방법에 관한 것이다. 또한, 상기 본 발명은 상기 처리 공정을 수행하기 위한 시스템에 관한 것이다. The present invention relates to a process for the production of liquefied natural gas comprising the step of using air as a refrigerant in an open cycle or closed cycle. The present invention also relates to a system for performing the process.

Low-temperature air separation method and air separation plant

FIELD: heat exchange.SUBSTANCE: disclosed is a low-temperature air separation method in an air separation plant (100), which has system (10) of distillation columns with high-pressure column (11) and low-pressure column (12). Air supplied to system (10) is compressed to initial pressure level. Part of compressed air is subjected to first pressure increase at first temperature level higher than 0 °C, and then to two additional pressure increases at temperature level below first temperature level, and then expanded in column (11). Enriched with oxygen liquid is extracted from column (22). For the first pressure boost, first booster (2) is used, which is actuated using the first expansion machine (9), in which the additional portion of compressed to the initial air pressure level expands to the pressure level of the low pressure column. For two additional boosts of pressure first booster (5) and second booster (6) are used. Air enters second booster (6) at temperature level whereat it exits first booster (5).EFFECT: technical result is reduction of losses during heat exchange.13 cl, 3 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 721 195 C2 (51) МПК F25J 3/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК F25J 3/04054 (2020.02); F25J 3/0409 (2020.02); F25J 3/04175 (2020.02); F25J 3/04296 (2020.02); F25J 3/04303 (2020.02); F25J 3/04393 (2020.02); F25J 3/04793 (2020.02); F25J 3/04951 (2020.02) (21)(22) Заявка: 2016147700, 06.12.2016 06.12.2016 (73) Патентообладатель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ (DE) Дата регистрации: 18.05.2020 Приоритет(ы): (30) Конвенционный приоритет: 07.12.2015 EP 15003482.5 (43) Дата публикации заявки: 08.06.2018 Бюл. № 16 2 7 2 1 1 9 5 R U Адрес для переписки: 129090, Москва, ул. Б. Спасская, 25, стр. 3, ООО "Юридическая фирма Городисский и Партнеры" (54) СПОСОБ НИЗКОТЕМПЕРАТУРНОГО РАЗДЕЛЕНИЯ ВОЗДУХА И УСТАНОВКА РАЗДЕЛЕНИЯ ВОЗДУХА (57) Реферат: Предлагается способ низкотемпературного ...

Liquid fuel gas supply apparatus and supply method

Patent RU2016147700A3

`”ВУ“” 2016147700” АЗ Дата публикации: 05.03.2020 Форма № 18 ИЗПМ-2011 Федеральная служба по интеллектуальной собственности Федеральное государственное бюджетное учреждение 5 «Федеральный институт промышленной собственности» (ФИПС) ОТЧЕТ О ПОИСКЕ 1. . ИДЕНТИФИКАЦИЯ ЗАЯВКИ Регистрационный номер Дата подачи 2016147700/06(076626) 06.12.2016 Приоритет установлен по дате: [ ] подачи заявки [ ] поступления дополнительных материалов от к ранее поданной заявке № [ ] приоритета по первоначальной заявке № из которой данная заявка выделена [ ] подачи первоначальной заявки № из которой данная заявка выделена [ ] подачи ранее поданной заявки № [Х] подачи первой(ых) заявки(ок) в государстве-участнике Парижской конвенции (31) Номер первой(ых) заявки(ок) (32) Дата подачи первой(ых) заявки(ок) (33) Код страны 1. 15003482.5 07.12.2015 ЕР* Название изобретения (полезной модели): [Х] - как заявлено; [ ] - уточненное (см. Примечания) СПОСОБ НИЗКОТЕМПЕРАТУРНОГО РАЗДЕЛЕНИЯ ВОЗДУХА И УСТАНОВКА РАЗДЕЛЕНИЯ ВОЗДУХА Заявитель: ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ, ОЕ 2. ЕДИНСТВО ИЗОБРЕТЕНИЯ [Х] соблюдено [ ] не соблюдено. Пояснения: см. Примечания 3. ФОРМУЛА ИЗОБРЕТЕНИЯ: [Х] приняты во внимание все пункты (см. п см. Примечания [ ] приняты во внимание следующие пункты: р [ ] принята во внимание измененная формула изобретения (см. Примечания) 4. КЛАССИФИКАЦИЯ ОБЪЕКТА ИЗОБРЕТЕНИЯ (ПОЛЕЗНОЙ МОДЕЛИ) (Указываются индексы МПК и индикатор текущей версии) Е25.7 3/04 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) Е257 3/00-3/04 5.2 Другая проверенная документация в той мере, в какой она включена в поисковые подборки: 5.3 Электронные базы данных, использованные при поиске (название базы, и если, возможно, поисковые термины): Езрасепе, РАТЕМТЗСОРЕ, Рабъеагсв, КОРТО, ИЗРТО 6. ДОКУМЕНТЫ, ОТНОСЯЩИЕСЯ К ПРЕДМЕТУ ПОИСКА Кате- Наименование документа с указанием (где необходимо) частей, Относится к гория* относящихся к предмету поиска пункту формулы № 1 2 3 А 05 5475980 А ( ...

Precooling of natural gas by high pressure compression and expansion

METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION

Dans un procédé de séparation d'air par distillation cryogénique, un débit de gaz est détendu dans une turbine de détente cryogénique à une seule roue, ayant une température d'entrée inférieure à -100°C, un gaz est comprimé dans un premier surpresseur (B1) à une seule roue avec une température d'entrée supérieure à -50°C, de l'air est comprimé dans un deuxième surpresseur (B2) à une seule roue avec une température d'entrée inférieure à -100°C, l'air surpressé dans au moins le premier surpresseur se refroidit dans l'échangeur de chaleur le travail généré par la turbine de détente (T), et éventuellement par une deuxième turbine, est utilisé pour l'étape de compression cryogénique dans le premier surpresseur et pour l'étape de compression dans le deuxième surpresseur et la roue du premier surpresseur, la roue du deuxième surpresseur et la roue de la turbine sont montées sur le même axe de rotation. In a cryogenic distillation air separation process, a gas flow is expanded in a single impeller cryogenic expansion turbine, having an inlet temperature below -100°C, a gas is compressed in a first booster (B1) with a single wheel with an inlet temperature above -50°C, air is compressed in a second booster (B2) with a single wheel with an inlet temperature below -100°C, the air boosted in at least the first booster is cooled in the heat exchanger the work generated by the expansion turbine (T), and possibly by a second turbine, is used for the cryogenic compression stage in the first booster and for the compression stage in the second booster and the wheel of the first booster, the wheel of the second booster and the wheel of the turbine are mounted on the same axis of rotation.

METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION

PUMP FOR A CRYOGENIC LIQUID AND PUMP GROUP AND DISTILLATION COLUMN EQUIPPED WITH SUCH A PUMP

PLANT FOR PRODUCTION OF LARGE QUANTITIES OF OXYGEN AND / OR NITROGEN

METHOD AND APPARATUS FOR PRODUCING PRESSURIZED AIR GAS USING A CRYOGENIC SURPRESSOR

METHOD AND INSTALLATION OF AIR SEPARATION BY CRYOGENIC DISTILLATION

Dans un procédé de séparation d'air par distillation cryogénique, tout l'air est porté à une haute pression plus supérieure d'au moins 5 bars à la moyenne pression et épuré à cette haute pression, une partie du débit d'air épuré est refroidie dans la ligne d'échange (9) et est ensuite divisée en deux fractions, chaque fraction se détend dans une turbine (17, 19), la pression d'admission des deux turbines étant supérieure d'au moins 5 bars à la moyenne pression, la pression de refoulement d'au moins une des deux turbines est sensiblement égale à la moyenne pression, on envoie au moins une partie de l'air détendu dans au moins une des turbines à la colonne moyenne pression (100) d'une double ou triple colonne, un surpresseur froid (23) mécaniquement relié à une (19) des turbines de détente aspire de l'air, qui a subi un refroidissement dans la ligne d'échange principale, et refoule l'air à une température supérieure à la température d'admission, et le fluide ainsi comprimé est réintroduit dans la ligne d'échange principale dans laquelle au moins une partie du fluide se condense, au moins un liquide pressurisé provenant d'une des colonnes est vaporisé dans la ligne d'échange à une température de vaporisation et la turbine non couplée (17) au surpresseur froid est pourvue d'un dispositif de dissipation d'énergie parmi :i) un surpresseur (5) autre que le surpresseur froid et mécaniquement couplé et suivi d'un réfrigérantii) un système à frein d'huileiii) une génératrice électrique (61) In a process of air separation by cryogenic distillation, all the air is brought to a higher pressure at least 5 bars higher than the average pressure and purified at this high pressure, part of the purified air flow is cooled in the exchange line (9) and is then divided into two fractions, each fraction expands in a turbine (17, 19), the inlet pressure of the two turbines being at least 5 bar higher than ...

Device and method for liquefying a fluid such as hydrogen and/or helium

Dispositif de liquéfaction d’un fluide comprenant un circuit (3) de fluide à refroidir, le dispositif (1) comprenant un ensemble d’échangeur(s) (6, 7, 8, 9, 10, 11, 12, 13) de chaleur en échange thermique avec le circuit (3) de fluide à refroidir, au moins un premier système (20) de refroidissement en échange thermique avec au moins une partie de l’ensemble d’échangeur(s) (6, 7, 8, 9, 10, 11, 12, 13) de chaleur, le premier système (20) de refroidissement étant un réfrigérateur à cycle de réfrigération d’un gaz de cycle comprenant majoritairement de l’hélium, ledit le réfrigérateur (20) comprenant, disposés en série dans un circuit (14) de cycle : un mécanisme (15) de compression du gaz de cycle, au moins un organe (16, 5, 6, 8, 10, 12) de refroidissement du gaz de cycle, un mécanisme (17) de détente du gaz de cycle et au moins un organe (13, 12, 11, 10, 9, 8, 7, 6, 5) de réchauffage du gaz de cycle détendu, dans lequel le mécanisme de compression comprend au moins quatre étages de compression (15) en série composés d’un ensemble de compresseur(s) (15) de type centrifuge, les étages de compressions (15) étant monté sur des arbres (19, 190) entraînés en rotation par un ensemble de moteur(s) (18), le mécanisme de détente comprenant au moins trois étages de détente en série composés d’un ensemble de turbines (17) de type centripète, le au moins un organe (16, 5, 6, 8, 10, 12) de refroidissement du gaz de cycle étant configuré pour refroidir le gaz de cycle à la sortie de l’une au moins des turbines (17) et dans lequel au moins une des turbines (17) est accouplée au même arbre (19) qu’au moins un étage de compression (15) de façon à fournir à l’étage de compression (15) du travail mécanique produit lors de la détente. Figure de l’abrégé: Fig. 1 Device for liquefying a fluid comprising a circuit (3) of fluid to be cooled, the device (1) comprising a set of heat exchanger(s) (6, 7, 8, 9, 10, 11, 12, 13) heat in heat exchange with the fluid circuit (3) to be cooled, at ...

Device and method for liquefying a fluid such as hydrogen and/or helium

Disclosed is a device for liquefying a fluid, comprising a circuit (3) for fluid to be cooled, the device (1) comprising a set of one or more heat exchangers (6, 7, 8, 9, 10, 11, 12, 13) exchanging heat with the circuit (3) of fluid to be cooled, at least one first cooling system (20) exchanging heat with at least some of the set of one or more heat exchangers (6, 7, 8, 9, 10, 11, 12, 13), the first cooling system (20) being a refrigerator with refrigeration cycle of a cycle gas mostly comprising helium, the refrigerator (20) comprising, arranged in series in a cycle circuit (14): a cycle gas compression mechanism (15), at least one cycle gas cooling member (16, 5, 6, 8, 10, 12), a mechanism (17) for expansion of the cycle gas and at least one expanded cycle gas heating member (13, 12, 11, 10, 9, 8, 7, 6, 5), wherein the compression mechanism comprises at least four compression stages (15) in series, consisting of a set of one or more centrifuge-type compressors (15), the compression stages (15) being mounted on shafts (19, 190) rotated by a set of one or more motors (18), the expansion mechanism comprising at least three expansion stages in series, consisting of a set of centripetal turbines (17), the at least one cycle gas cooling member (16, 5, 6, 8, 10, 12) being configured to cool the cycle gas at the outlet of at least one of the turbines (17) and wherein at least one of the turbines (17) is coupled to the same shaft (19) as at least one compression stage (15) so as to supply the compression stage (15) with the mechanical work produced during the expansion.

METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION

Dans un procédé de séparation d'air par distillation cryogénique, un débit de gaz est détendu dans une turbine de détente cryogénique à une seule roue, ayant une température d'entrée inférieure à -100°C, un gaz est comprimé dans un premier surpresseur (B1) à une seule roue avec une température d'entrée supérieure à -50°C, de l'air est comprimé dans un deuxième surpresseur (B2) à une seule roue avec une température d'entrée inférieure à -100°C, l'air surpressé dans au moins le premier surpresseur se refroidit dans l'échangeur de chaleur le travail généré par la turbine de détente (T), et éventuellement par une deuxième turbine, est utilisé pour l'étape de compression cryogénique dans le premier surpresseur et pour l'étape de compression dans le deuxième surpresseur et la roue du premier surpresseur, la roue du deuxième surpresseur et la roue de la turbine sont montées sur le même axe de rotation. In a cryogenic distillation air separation process, a gas flow is expanded in a single impeller cryogenic expansion turbine, having an inlet temperature below -100°C, a gas is compressed in a first booster (B1) with a single wheel with an inlet temperature above -50°C, air is compressed in a second booster (B2) with a single wheel with an inlet temperature below -100°C, the air boosted in at least the first booster is cooled in the heat exchanger the work generated by the expansion turbine (T), and possibly by a second turbine, is used for the cryogenic compression stage in the first booster and for the compression stage in the second booster and the wheel of the first booster, the wheel of the second booster and the wheel of the turbine are mounted on the same axis of rotation.

AIR SEPARATION METHOD BY CRYOGENIC DISTILLATION

Selon une première marche dans un appareil de séparation d'air, on comprime dans un compresseur principal (1) de l'air destiné à la distillation, on envoie un premier débit d'air comprimé au moins dans le compresseur principal, épuré et refroidi dans une ligne d'échange (6) à la colonne moyenne pression (8) d'une double colonne, on sépare le débit d'air en des flux enrichis en azote et en oxygène dans la colonne moyenne pression, on soutire un débit d'oxygène liquide (16) de la colonne basse pression, on le pressurise jusqu'à une pression élevée et on le vaporise dans la ligne d'échange pour former un premier débit gazeux riche en oxygène et à pression élevée, on liquéfie au moins une partie (24) de l'air comprimé dans le compresseur principal et on envoie la partie liquéfiée à la double colonne et on produit également un deuxième débit gazeux riche en oxygène (115) mais à une pression moins élevée que le premier débit gazeux riche en oxygène et selon une deuxième marche, on augmente la pression de liquéfaction de l'air dans en réglant les aubages du compresseur principal (1) qui fixe cette pression, on réduit la production du deuxième débit gazeux riche en oxygène et on augmente le soutirage du premier débit gazeux riche en oxygène. According to a first step in an air separation apparatus, air is compressed in a main compressor (1) for distillation, a first compressed air flow is sent at least in the main compressor, purified and cooled. in an exchange line (6) at the medium-pressure column (8) of a double column, the air flow is separated into flows enriched in nitrogen and oxygen in the medium pressure column, a flow rate of liquid oxygen (16) of the low pressure column, pressurized to a high pressure and vaporized in the exchange line to form a first gas flow rich in oxygen and at high pressure, liquefies at least one portion (24) of the compressed air in the main compressor and the liquefied portion is sent to the ...

Method for separation of air by cryogenic distillation for production of gas, involves pressurizing and vaporizing liquid flow in one of two exchange lines, and coupling cold booster with driving mechanism e.g. electrical motor

Dans un procédé de séparation d'air par distillation cryogénique, une partie (9) de l'air, est refroidie dans une première ligne d'échange (A), soutirée à une température intermédiaire de la première ligne d'échange, et surpressée à partir d'au moins la haute pression au moyen d'un surpresseur froid (17), puis est renvoyée dans la première ligne d'échange, et une autre fraction de l'air (7) à au moins la pression P1, est refroidie dans la deuxième ligne d'échange (B) jusqu'au bout froid de celle-ci et envoyée dans au moins une turbine.

METHOD AND APPARATUS FOR GENERATING GAS AIR FROM THE AIR IN A GAS FORM AND LIQUID WITH HIGH FLEXIBILITY BY CRYOGENIC DISTILLATION

Dans un procédé de production d'au moins un gaz de l'air par distillation cryogénique au moins dans un premier mode de fonctionnement, une turbine auxiliaire (27) aspire une fraction gazeuse du débit d'air ayant été refroidie dans la ligne d'échange principale (7), la pression d'aspiration de la turbine auxiliaire est sensiblement supérieure ou substantiellement égale à la moyenne pression, préférablement supérieure ou substantiellement égale à la pression principale et une partie des constituants de l'air est produite sous forme liquide comme produit final et dans un deuxième mode de fonctionnement, le débit d'air traité dans la turbine auxiliaire est réduit et la production de liquide comme produit final est diminuée. In a process for producing at least one gas from the air by cryogenic distillation, at least in a first mode of operation, an auxiliary turbine (27) draws in a gaseous fraction of the air flow which has been cooled in the line of main exchange (7), the suction pressure of the auxiliary turbine is substantially greater than or substantially equal to the medium pressure, preferably greater than or substantially equal to the main pressure and part of the constituents of the air is produced in liquid form as final product and in a second mode of operation, the flow of air treated in the auxiliary turbine is reduced and the production of liquid as final product is reduced.

METHOD AND APPARATUS FOR GENERATING GAS AIR FROM THE AIR IN A GAS FORM AND HIGHLY FLEXIBLE LIQUID BY CRYOGENIC DISTILLATION

Dans un procédé de production d'au moins un gaz de l'air par distillation cryogénique au moins dans un premier mode de fonctionnement, une turbine auxiliaire (27) aspire une fraction gazeuse du débit d'air ayant été refroidie dans la ligne d'échange principale (7), la pression d'aspiration de la turbine auxiliaire est sensiblement supérieure ou substantiellement égale à la moyenne pression, préférablement supérieure ou substantiellement égale à la pression principale et une partie des constituants de l'air est produite sous forme liquide comme produit final et dans un deuxième mode de fonctionnement, le débit d'air traité dans la turbine auxiliaire est réduit et la production de liquide comme produit final est diminuée. In a process for producing at least one air gas by cryogenic distillation at least in a first mode of operation, an auxiliary turbine (27) sucks a gaseous fraction of the air flow having been cooled in the line of main exchange (7), the suction pressure of the auxiliary turbine is substantially greater than or substantially equal to the average pressure, preferably greater than or substantially equal to the main pressure, and part of the constituents of the air is produced in liquid form as final product and in a second mode of operation, the air flow treated in the auxiliary turbine is reduced and the production of liquid as the final product is reduced.

METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION

METHOD FOR DEFROSTING AN AIR SEPARATION APPARATUS BY CRYOGENIC DISTILLATION AND APPARATUS SUITABLE FOR BEING DEFROST BY THIS METHOD

Procédé de séparation d'air par distillation cryogénique dans un appareil de séparation d'air comprenant un système de colonnes (K1, K2), une première turbine (T1) et une deuxième turbine (T2), dans lequel en marche de dégivrage on ferme une conduite commune (13) amenant l'air des deux turbines à une colonne au moyen d'une vanne d'isolement (V11), on envoie un gaz de purge à une température supérieure à 0°C dans les turbines pour les dégivrer mais on n'envoie pas de gaz de purge au système de colonnes.

METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION

Une installation de séparation d'air par distillation cryogénique comprend une double colonne de séparation d'air,une ligne d'échange (91), un surpresseur chaud (C1)et un surpresseur froid (C2), une première turbine (T1) et une deuxième turbine (T2), chacune couplée à un des surpresseurs, des moyens pour porter tout l'air à une haute pression plus élevée que la moyenne pression et des moyens pour l'épurer à cette haute pression, des moyens pour diviser l'air épuré en deux fractions et pour en envoyer une fraction au surpresseur chaud et une fraction au surpresseur froid après refroidissement dans la ligne d'échange, des moyens pour réintroduire la deuxième fraction d'air provenant du surpresseur froid dans la ligne d'échange, des moyens pour envoyer au moins un liquide pressurisé provenant d'une des colonnes dans la ligne d'échange, une vanne (4,5), des moyens pour envoyer de l'air épuré à la haute pression et non surpressé à la ligne d'échange pour s'y refroidir et ensuite à la vanne et des moyens pour envoyer l'air détendu dans la vanne à la distillation et/ou à l'atmosphère. An air separation installation by cryogenic distillation comprises a double air separation column, an exchange line (91), a hot booster (C1) and a cold booster (C2), a first turbine (T1) and a second turbine (T2), each coupled to one of the boosters, means for bringing all the air to a high pressure higher than the medium pressure and means for purging it at this high pressure, means for dividing the purified air in two fractions and to send a fraction to the hot booster and a fraction to the cold booster after cooling in the exchange line, means for reintroducing the second fraction of air from the cold booster in the exchange line, means for sending at least one pressurized liquid from one of the columns in the exchange line, a valve (4,5), means for sending purified air at the high pressure and not overpressured at the line d ...

System and method of production of liquefied natural gas

본 발명은 개방 사이클 또는 폐쇄 사이클 내 냉각제(refrigerant)로써 공기를 사용하는 단계를 포함하는 액화 천연가스의 제조 방법에 관한 것이다. 또한, 상기 본 발명은 상기 처리 공정을 수행하기 위한 시스템에 관한 것이다.

Apparatus for the production of pressurized purified air and a liquid product by cryogenic distillation of air

적어도, 1개 이상의 상부 응축기(C, C1, C2)를 가지는 제1 컬럼(A), 열 교환기(9), 터빈(23), 공기를 제1 압력으로 압축하기 위한 압축기(V), 제1 압력의 공기를 정제하기 위한 정제 수단(P), 제1 압력의 정제된 공기를 제1 분획 및 제2 분획으로 분할하기 위한 도관 수단, 제1 분획을 열 교환기에서 냉각되도록 보내기 위한 도관, 열 교환기에서 냉각된 제1 분획을 증류 컬럼 시스템의 제1 컬럼으로 보내기 위한 도관, 제2 분획을 열 교환기에서 중간 온도로 냉각되도록 보내기 위한 도관, 제2 분획을 중간 온도에서 열 교환기로부터 제거하고 제1 압력의 제2 분획을 터빈으로 보내기 위한 도관, 팽창된 제2 압력의 제2 분획을 열 교환기에서 제2 압력에서 가온되도록 보내기 위한 도관, 가온된 제2 분획을 제2 압력의 생성물 스트림으로서 제거하기 위한 도관, 제1 컬럼으로부터의 산소 풍부 액체를 제1 컬럼의 상기 상부 응축기 하나에서 기화되도록 보내기 위한 도관, 기화된 산소 풍부 액체를 제1 산소 풍부 기체로서 제거하기 위한 도관, 질소 풍부 유체를 제1 컬럼으로부터 제거하기 위한 도관, 및 적어도 1종의 액체 생성물을 증류 컬럼 시스템으로부터 제거하기 위한 도관을 가지며 제1 압력은 제2 압력보다 적어도 3 bar 더 높고 제2 압력은 3 bar abs보다 높은 증류 컬럼 시스템을 포함하는, 공기의 초저온 증류(cryogenic distillation)에 의한 가압 정제 공기 및 액체 생성물의 제조를 위한 장치.

Method and apparatus for the cryogenic separation of air

本发明提出了一种用于低温分离空气的SPECTRA方法，其中用于提取氧的附加的第二精馏塔(12)的塔底液在第二冷凝器蒸发器(121)中蒸发。在所述第二冷凝器蒸发器(121)中，先前在用于冷凝第一精馏塔(11)的塔顶气的第一冷凝器蒸发器(111)中蒸发的气体在先前蒸发的压力水平下冷凝。本发明还涉及一种对应的设备(100,200,300)。

Method and device for the cryogenic decomposition of air

System and method for liquefaction of natural gas

[Problem] To suppress excessive increases in the temperature of a raw material gas that is introduced to a liquefying device after being compressed by a compressor and thereby to easily adjust the temperature level of the raw material gas such that said temperature level nears the temperature level of the site where the gas is introduced to the liquefying device. [Solution] A natural gas liquefying system (1) that is characterized by being provided with: a first expander (3) that expands a raw material gas that is a natural gas obtained by pressurization; first coolers (10, 11, 12) that cool the raw material gas; a distilling device (15) that distills the raw material gas that is cooled by the first coolers and thereby reduces or eliminates the heavy components of the raw material gas; a first compressor (4) into which is introduced an overhead distillate from which the heavy components of the raw material gas have been reduced or eliminated in the distilling device; and a liquefying device (21) that liquefies, by means of a heat exchange with a coolant, the gaseous phase component that is separated from a compressed gas that is compressed in the first compressor.

System and method to produce liquefied natural gas using two distinct refrigeration cycles with an integral gear machine

A system and method for liquefaction of natural gas using two distinct refrigeration circuits having compositionally different working fluids and operating at different temperature levels is provided. The turbomachinery associated with the liquefaction system are driven by a single three-pinion, three-turbine integral gear machine with customized pairing arrangements. The system and method of natural gas liquefaction further includes the conditioning of a lower pressure natural gas containing feed stream to produce a purified, compressed natural gas stream at a pressure equal to or above the critical pressure of natural gas and substantially free of heavy hydrocarbons to be liquefied.

Method and unit for low-temperature air separation

The invention relates to a method for a low-temperature air separation in which an air separation unit (100, 200) is used comprising a heat exchanger (6), a decompression machine (8), a compressor (9) coupled to the decompression machine (8), a first rectification column (11), a second rectification column (12), and a condenser evaporator (5) which is arranged in the lower region of the second rectification column (12). The first rectification column (11) is operated at a first pressure level, and the second rectification column (12) is operated at a second pressure level below the first pressure level. Fluid which is oxygen-enriched compared to atmospheric air is drawn from the first rectification column (11) in the form of one or more first material flows. The fluid is partly or completely heated in a heat exchanger (6), and the heat exchanger (6) is used to cool the head gas of the first rectification column (11). A first fraction of the fluid is then conducted through a decompression machine (8) and is discharged from the air separation unit (100, 200), and a second fraction is conducted through a compressor (9) coupled to the decompression machine (8) and is returned to the first rectification column (11). Furthermore, additional fluid which contains nitrogen and oxygen is drawn from the first rectification column (11) in the form of a second material flow and is fed to the second rectification column (12); oxygen-enriched fluid is formed in the sump of the second rectification column (12) and is drawn from the second rectification column (12) at least partly in the form of a third material flow; and an additional fluid is formed at the head of the second rectification column (12) and is drawn from the second rectification column (12) at least partly in the form of a fourth material flow. The second material flow is supercooled in counter flow with the fourth material flow in a supercooler (10) prior to being fed to the second rectification column (12) and ...

Process for separating hydrogen from an olefin hydrocarbon effluent vapor stream

One or more specific embodiments disclosed herein includes a method for separating hydrogen from an olefin hydrocarbon rich compressed effluent vapor stream, employing a integrated heat exchanger, multiple gas-liquid separators, external refrigeration systems, and a rectifier attached to a liquid product drum.

Atmospheric air fractionating process - has separate condensation-vaporisation zone receiving oxygen enriched liquid

Compressed air is cooled by a nitrogen-enriched gas and separated into high- and low-oxygen content liquids in high-pressure columns. The nitrogen-enriched gas is condensed in a condenser-vaporiser by the oxygen-enriched gas. The liquids are introduced respectively into an intermediate zone and the top of the low-pressure column, where they are separated into a nitrogen-rich gas and an oxygen-rich liquid. Part of the oxygen-enriched liquid is delivered to the vaporisation compartment from which oxygen-enriched gas is extracted. Nitrogen-rich gas is delivered to the condensation compartment as a heater, and extracted liquid is delivered to a fractionating zone. During vaporisation heat exchange occurs between nitrogen rich gas and oxygen rich liquid.

METHOD AND APPARATUS FOR PRODUCING GAS-LIKE AIR AND HIGH-FLEXIBILITY LIQUID AIR GASES BY CRYOGENIC DISTILLATION

Dans un procédé de production d'au moins un gaz de l'air par distillation cryogénique dans un système de colonnes, selon un premier mode de fonctionnement, une turbine auxiliaire (27) aspire une fraction gazeuse d'un débit d'air ayant été préalablement détendue dans une première turbine (21), la pression d'aspiration de la turbine auxiliaire diffère de moins de 2 bar abs de la moyenne pression, la pression de refoulement de la turbine auxiliaire est supérieure ou substantiellement égale à la pression atmosphérique,;au moins une partie du débit d'air détendu dans la turbine auxiliaire est réchauffée dans une ligne d'échange (7) ou renvoyée à un système de colonnes et une partie (32) des constituants de l'air est produite comme produit final sous forme liquide et dans un deuxième mode de fonctionnement, le débit d'air traité dans la turbine auxiliaire est réduit et la production de liquide comme produit final est diminuée. In a process for producing at least one gas from the air by cryogenic distillation in a column system, according to a first mode of operation, an auxiliary turbine (27) sucks a gas fraction from an air flow that has been previously expanded in a first turbine (21), the suction pressure of the auxiliary turbine differs by less than 2 bar abs from the medium pressure, the discharge pressure of the auxiliary turbine is greater than or substantially equal to atmospheric pressure; at least part of the air flow expanded in the auxiliary turbine is heated in an exchange line (7) or returned to a column system and part (32) of the constituents of the air is produced as final product under liquid form and in a second mode of operation, the flow rate of treated air in the auxiliary turbine is reduced and the production of liquid as a final product is reduced.

Procedure and installation of air separation by cryogenic distillation

Procedimiento de separación por destilación criogénica en una instalación que comprende una doble o triplecolumna (100, 200) de separación de aire, en la que la columna que funciona a la presión más elevada (100)funciona a una presión denominada media presión, una línea de intercambio (9) y, además de la doble o triplecolumna, una columna de mezcla (300), en el cual: a) todo el aire es llevado a una alta presión, eventualmente superior al menos en 5 bares a la media presión, yeventualmente depurado a esta alta presión, b) una parte del caudal de aire depurado es enfriada en la línea de intercambio y a continuación es dividida en dosfracciones, c) cada fracción se expande en una turbina (17, 19), d) la presión de admisión de las dos turbinas, respectivamente las presiones de las dos turbinas, son superiores almenos en 5 bares a la media presión, e) la presión de impulsión de al menos una de las dos turbinas es sensiblemente igual a la media presión, f) se envía al menos una parte del aire expandido en al menos una de las turbinas a la columna de media presión deuna doble o triple columna, g) un sobrecompresor frío (23) unido mecánicamente a una de las turbinas de expansión aspira aire, que haexperimentado un enfriamiento en la línea de intercambio, e impulsa aire a una temperatura superior a latemperatura de admisión, y el fluido así comprimido es reintroducido en la línea de intercambio en la cual al menosuna parte del fluido se condensa o seudocondensa, h) al menos un líquido presurizado que proviene de una de las columnas es (seudo) vaporizado en la línea deintercambio a una temperatura de vaporización, y i) la turbina (17) no acoplada al sobrecompresor frío está acoplada a un sobrecompresor (5) seguido de unrefrigerante,y eventualmente j) la temperatura de aspiración del sobrecompresor frío (23) es próxima a la temperatura de vaporización oseudovaporización del líquido, y k) aire que proviene de al menos una de las turbinas (17, 19) es enviado a la columna de ...

Method for obtaining an air product and air decomposition system

Ein Verfahren zur Erzeugung eines Luftprodukts in einer Luftzerlegungsanlage (100) mit einer Wärmetauscheinheit (10), einer Entspannungs-/Verdichtungseinheit (20), einer Rektifikationseinheit (30), einer Flüssigkeitsspeichereinheit (40), einer Kältespeichereinheit (50) sowie einem Hauptluftverdichter (1), umfasst, dass die gesamte, der Rektifikationseinheit (30) zugeführte Luft durch den Hauptluftverdichter (1) geführt und dort zunächst auf ein Druckniveau verdichtet wird, das mindestens 3 bar oberhalb des höchsten Druckniveaus liegt, auf dem die Rektifikationseinheit (30) betrieben wird, unter Verwendung der durch den Hauptluftverdichter (1) geführten Luft in der Rektifikationseinheit (30) eine oder mehrere tiefkalte Flüssigkeiten in einem ersten Betriebsmodus in einer ersten, in einem zweiten Betriebsmodus in einer zweiten und in einem dritten Betriebsmodus in einer dritten Produktionsmenge erzeugt werden, die eine oder die mehreren tiefkalten Flüssigkeiten in dem dritten Betriebsmodus in einer Einspeichermenge, die einer Teilmenge der dritten Produktionsmenge entspricht, in der Flüssigkeitsspeichereinheit (40) eingespeichert und in dem zweiten Betriebsmodus in einer Ausspeichermenge aus der Flüssigkeitsspeichereinheit (40) ausgespeichert werden, die eine oder die mehreren tiefkalten Flüssigkeiten in dem ersten Betriebsmodus in einer ersten, in dem zweiten Betriebsmodus in einer zweiten und in dem dritten Betriebsmodus in einer dritten Verdampfungsmenge verdampft und/oder pseudoverdampft werden, wobei die erste Verdampfungsmenge der ersten Produktionsmenge, die zweite Verdampfungsmenge der zweiten Produktionsmenge zuzüglich der Ausspeichermenge und die dritte Verdampfungsmenge der dritten Produktionsmenge abzüglich der Einspeichermenge entspricht, und unter Verwendung der durch den Hauptluftverdichter (1) geführten Luft in dem zweiten Betriebsmodus ein tiefkalter Fluidstrom, unter Verwendung dessen die Kältespeichereinheit (50) abgekühlt wird, und der sich ...

Integration of industrial gas site with liquid hydrogen production

The method for producing liquid hydrogen (346) can include the steps of: introducing pressurized natural gas (302) from a high pressure natural gas pipeline (300) to a gas processing unit under conditions effective for producing a purified hydrogen stream (315); and introducing the purified hydrogen stream to a hydrogen liquefaction unit under conditions effective to produce a liquid hydrogen stream (346), wherein the hydrogen liquefaction unit provides a warm temperature cooling and a cold temperature cooling to the purified hydrogen stream, wherein the warm temperature cooling is provided by utilizing letdown energy of a pressurized stream selected from the group consisting of a nitrogen stream (320) sourced from a nitrogen pipeline, a natural gas stream (2) sourced from the high pressure natural gas pipeline (300), an air gas (86) sourced from an air separation unit (ASU), and combinations thereof, wherein the cold temperature is provided by utilizing letdown energy of the purified hydrogen stream.

Method and device for separating air by cryogenic distillation

本发明涉及用于通过低温蒸馏来分离空气的方法和装置，其中空气在压缩机(C2)中被压缩并随后送至热交换器(E)，将在交换器中冷却的空气送至在热交换器下游的止回阀(CL3)并随后送至一涡轮机，该阀定位成使得来自短路管道(23)的空气不能从压缩机返回到交换器。

System and method for liquefaction of natural gas

Nitrogen making machine suitable for electronic gas factory

本发明涉及电子气的技术领域，更具体地，涉及一种适用于电子气工厂的制氮机，包括空气过滤及压缩系统、空气预冷系统、空气纯化系统、换热器系统、氧氮精馏系统及后备系统：空气先进入空气过滤器去除杂质，后送往空气压缩机压缩，空气自下而上流出空气冷却塔进入空气纯化系统，纯化后的空气经换热器冷却到液化温度后进入第一塔参与精馏，精馏得到的氮气作为氮气产品送用户，少量液氮送入后备系统，精馏得到的富氧液空可回流至空气纯化系统和空气预冷系统。本发明具有宽泛的负荷调节范围，可节约能耗；氧氮精馏系统采用双塔设计，可提高氮气提取率；吸附器内设置多层填料层，可满足产品气高标准要求；关键设备一用一备，可避免设备宕机对制氮供气的影响。

Process and apparatus for liquifying and fractionating air

Process and apparatus for liquifying and fractionating (separating) air by use of a multiple rectification tower system having a high pressure tower and a low pressure tower. The rectification regions of the high pressure tower and of the low pressure tower are subdivided into an equal number (at least two) of segments and at the head ends of the particular segments of the high pressure tower the gases are conducted through a heat exchange with circulating liquids or liquid oxygen at the bottom ends (trays) of the particular segments of the low pressure tower and the circulating liquids or the liquid oxygen is evaporated. The gases are then condensed, a circulating liquid being obtained for the low pressure tower.

Method and apparatus for separating air by cryogenic distillation

In a method for separating air by cryogenic distillation, compressed air is purified in a purification unit (7), cooled in an exchange line (19) and sent to a column of a system of columns comprising a medium-pressure column (21) and a low-pressure column (23), an oxygen-rich fluid is tapped from the low-pressure column, is heated in the exchange line and sent to the client, a fluid resulting from the distillation is expanded in a turbine (55) and is then used to regenerate the purification unit, the residual nitrogen is sent directly to the atmosphere, possibly through a contact tower in which it is in direct contact with the water, at the hot end of the exchange line and a cold compressor (51) uses at least some of the refrigerating power of the turbine.

Method and apparatus for treating a hydrocarbon stream and method of cooling a hydrocarbon stream

Method and apparatus for treating a mixed hydrocarbon feed stream (10), such as a natural gas stream. The mixed hydrocarbon feed stream (10) is expanded into a mixed-phase hydrocarbon stream (20), which is separated the to provide at least a light overhead stream (30) and a heavy bottom stream (50). The light overhead stream (30) is compressed in one or more first compressors (16) to provide one or more first compressed light streams (40) and further compressed in one or more second compressors (22) to provide one or more further compressed light streams (60). One or more first compressor recycle lines (42) extend around the or each first compressor (16), and one or more second compressor recycle lines (32) having one or more in-line coolers (34) extend around the or each second compressor (22). The method and apparatus may be used in a method of cooling an initial hydrocarbon stream (100).

Apparatus and method for supplying liquid fuel gas

An apparatus and a method for supplying a liquid fuel gas having a high energy efficiency, which is efficiently using the coldness of the LNG and being capable of ensuring a supply amount of the liquid fuel gas according to the fluctuation in the composition or the demanded amount of the LNG serving as a source material with little need of the external energy, wherein the LNG supplied from a source material supplying portion 1 is vaporized via coldness releasing process through a first heat exchanger, a second heat exchanger, a third heat exchanger, a vaporizer, and an expander, and the vaporized LNG is passed through the second heat exchanger and a gas-liquid separator to form a gas-liquid mixture to be guided as the source material into the distillation tower; a branching portion is disposed in a flow passageway for guiding out the gas component from the tower top portion of the distillation tower, one gas component A derived from branching at the branching portion is supplied out via a compressor linked to the expander 41 and a natural gas supplying portion, and the other gas component B derived from branching at the branching portion is guided as a reflux liquid into an upper portion of the distillation tower via the first heat exchanger; the liquid component guided out from the tower bottom portion of the distillation tower is supplied out as an NGL via the third heat exchanger and a natural gas liquid supplying portion.

Refrigeration and / or liquefaction device

Dispositif de réfrigération et/ou de liquéfaction de type cryogénique comprenant un circuit (2) de travail contenant un fluide de travail, le circuit (2) de travail comprenant en série: un mécanisme (5, 6) de refroidissement du fluide de travail, un mécanisme de détente (7) du fluide de travail et un mécanisme de réchauffage (6) du fluide de travail, dans lequel le mécanisme de détente comprend deux turbines (7) de détente de type centripète montées respectivement aux deux extrémités d’un même arbre (8), les deux turbines (7) ayant des aubages (9) orientés de façon opposée selon la direction de l’arbre (8) Figure de l’abrégé : Fig. 2 Cryogenic type refrigeration and / or liquefaction device comprising a working circuit (2) containing a working fluid, the working circuit (2) comprising in series: a mechanism (5, 6) for cooling the working fluid, an expansion mechanism (7) for the working fluid and a heating mechanism (6) for the working fluid, in which the expansion mechanism comprises two expansion turbines (7) of the centripetal type mounted respectively at both ends of the same shaft (8), the two turbines (7) having blades (9) oriented opposite in the direction of the shaft (8) Figure of the abstract: Fig. 2

Staged Regenerative Supercritical Compressed Air Energy Storage System and Method

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 5 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.

Integrated continuous oxygen and nitrogen making device

本实用新型公开的一体式连续制氧制氮装置，包括生产氮气及液氮产品的深冷制氮装置和用于生产氧气产品的变压吸附制氧装置，深冷制氮装置的富氧空气出口与一富氧空气缓冲罐的入口连接，富氧空气缓冲罐的出口与变压吸附制氧装置的入口连接，变压吸附制氧装置的运行由一PLC控制系统控制。该一体式连续制氧制氮装置，将深冷制氮装置、富氧空气缓冲罐和变压吸附制氧装置依次串联，既解决了富氧空气的压力及组成波动问题，实现了氧气、氮气及液氮产品的连续稳定的生产，同时解决了现有深冷制氮装置将富氧空气放空所造成的能量损失问题。该一体式连续制氧制氮装置生产的氮气、氧气纯度高，并能同时生产液氮产品，应用范围大。

Processes and Device for Low Temperature Separation of Air

The process and device serve for the low-temperature separation of air in a distillation-column system includes at least one separation column. A main air stream is compressed in an air compressor at a first pressure and is then purified. A first air stream, which is formed from at least one part of the purified main air stream, is further compressed at a second pressure that is higher than the first pressure. From the further compressed first air stream, a throttling stream and a turbine stream are branched off. The throttling stream is cooled down and liquefied or pseudo-liquefied in a main heat exchanger and is then passed on to expansion equipment. The expanded throttling stream is conducted into the distillation-column system. The turbine stream is cooled down in the main heat exchanger and under an intermediate temperature of the main heat exchanger is conducted into an expansion machine.

Device and method for separating air by low temperature distillation

本发明涉及用于通过低温蒸馏来分离空气的装置。此外，本发明涉及用于通过低温蒸馏来分离空气的方法，其中使待蒸馏空气的至少一部分在空气增压器(C2)中增压，允许压缩空气在至少一个膨胀涡轮机(T2，T1)中膨胀，并且如果增压器的两个点之间的压降低于阈值和/或增压器的流量低于增压器的最小流量，则允许在增压器中增压的空气的一部分在尚未于增压器与膨胀涡轮机之间冷却的情况下膨胀并且将增压且膨胀后的空气在已增压之后在尚未于热交换器中进行冷却的情况下送至所述至少一个涡轮机的上游或下游。