СПОСОБ И УСТАНОВКА ДЛЯ ПРОИЗВОДСТВА ЖИДКИХ И ГАЗООБРАЗНЫХ КИСЛОРОДСОДЕРЖАЩИХ ПРОДУКТОВ НИЗКОТЕМПЕРАТУРНЫМ РАЗДЕЛЕНИЕМ ВОЗДУХА

1. Способ производства жидкого кислородсодержащего продукта (LOX) и газообразного кислородсодержащего продукта (GOX) низкотемпературным разделением воздуха (AIR) в системе дистилляционных колонн (S) установки разделения воздуха, которая включает в себя разделительную колонну высокого давления (S1) и разделительную колонну низкого давления (S2), причем для получения жидкого кислородсодержащего продукта (LOX) жидкую фракцию с первым, более высоким, значением содержания кислорода отбирают из разделительной колонны (S2) системы дистилляционных колонн (S) и в жидком виде выводят из установки разделения воздуха, а для получения газообразного кислородсодержащего продукта (GOX) жидкую фракцию со вторым, более низким, значением содержания кислорода отбирают из той же разделительной колонны (S2) системы дистилляционных колонн (S), испаряют в колонне смешивания (S3) за счет воздуха, подаваемого в колонну смешивания, нагревают в основном теплообменнике (E1) за счет охлаждаемого исходного воздуха и затем в виде газа выводят из установки разделения воздуха, причем:- первый частичный поток общего потока воздуха расширяется в первом детандере (X1) с совершением работы до рабочего давления в разделительной колонне высокого давления (S1) и поступает в разделительную колонну высокого давления (S1);- второй частичный поток общего потока воздуха применяют в качестве воздуха, подаваемого в колонну смешивания, при этом:- второй частичный поток общего потока воздуха расширяется во втором детандере (X2) с совершением работы до давления в колонне смешивания и поступает в нижнюю часть колонны смешивания (S3);- оба детандера характеризуются разными значениями температуры на входе;- один из двух РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК F25J 3/04 (11) (13) 2015 112 309 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2015112309, 29.08.2013 (71) Заявитель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ (DE) Приоритет(ы): (30) Конвенционный приоритет: (72) ...

Verfahren und Vorrichtung zur Lufttrennung

Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff durch Tieftemperaturzerlegung von Luft

Das Verfahren und die Vorrichtung zur Gewinnung von Druckstickstoff durch Tieftemperaturzerlegung von Luft in einem Destillationssäulen-System. Das Destillationssäulen-System weist eine Hochdrucksäule (4), eine Niederdrucksäule (6) sowie einen Hauptkondensator (5) und einen Niederdrucksäulen-Kopfkondensator (7) aufweist, die beide als Kondensator-Verdampfer ausgebildet sind. Verdichtete und gereinigte Einsatzluft (1) wird in einem Hauptwärmetauscher (2) abgekühlt und zum mindestens größten Teil gasförmig in die Hochdrucksäule (4) eingeleitet (3). Ein sauerstoffangereicherter Flüssigstrom (11, 13) wird aus der Hochdrucksäule (4) entnommen und in die Niederdrucksäule eingeleitet. Ein gasförmiger Stickstoffstrom (17, 26A, 26B, 27) wird aus der Hochdrucksäule (4) entnommen, im Hauptwärmetauscher (2) angewärmt und als gasförmiges Druckstickstoffprodukt (28, 31) abgezogen. Der Verdampfungsraum des Niederdrucksäulen-Kopfkondensators (7) ist als Forced-Flow-Verdampfer ausgebildet. Die Hochdrucksäule ...

Lufttrennung

Ammonia synthesis

An ammonia production process in which excess nitrogen and traces of carbon oxides are removed from raw ammonia synthesis gas firstly by application of partial condensation and secondly by application of washing action provided by carbon-oxides-free liquified gas, rich in nitrogen, which is derived from a cryogenic process used preferentially for separation of hydrogen from the ammonia synthesis loop purge gas as produced in processes which use excess of nitrogen above stoichiometric requirements in the circulating gas in the synthesis loop.

SEPARATION OF NITROGEN FROM METHANE-CONTAINING GAS STREAMS

Separation of nitrogen from methane-containing gas streams

A process for separating nitrogen from e.g. natural gas 2 by separating the gas in a first distillation column K1 at superatmospheric pressure to obtain an overhead vapour stream 18 having a nitrogen content greater than that of the feed gas mixture, reducing the pressure of said overhead stream e.g. in valve 20, separating it in a second distillation column K2 and recovering a nitrogen depleted product stream from one or both of the condensate streams 16 and 42 from the distillation steps, and wherein part or all of the reboil for the second distillation column is provided by effecting indirect heat exchange between the liquid column bottoms 10 and the overhead vapour stream 18, with at least partial condensation of the latter. ...

Nitrogen removal with iso-pressure open refrigeration natural gas liquids recovery.

A process for recovery of natural gas liquids is disclosed, the process including: fractionating a gas stream comprising nitrogen, methane, ethane, and propane and other C3+ hydrocarbons into at least two fractions including a light fraction comprising nitrogen, methane, ethane, and propane, and a heavy fraction comprising propane and other C3+ hydrocarbons; separating the light fraction into at least two fractions including a nitrogen-enriched fraction and a nitrogen-depleted fraction in a first separator; separating the nitrogen-depleted fraction into a propane-enriched fraction and a propane-depleted fraction in a second separator; feeding at least a portion of the propane-enriched fraction to the fractionating as a reflux; recycling at least a portion of the propane-depleted fraction to the first separator. In some embodiments, the nitrogen-enriched fraction may be separated in a nitrogen removal unit to produce a nitrogen- depleted natural gas stream and a nitrogen-enriched natural ...

PROCEDURE AND DEVICE FOR THE SEPARATION OF A MIXTURE FROM HYDROGEN AND CARBON MONOXIDE

PROCEDURE FOR THE PRODUCTION OF A KRYPTON XENON CONCENTRATE AND A GASEOUS OXYGEN PRODUCT.

PROCEDURE AND DEVICE FOR THE LIQUID AIR SEPARATION BY RECTIFICATION.

PROCEDURE FOR WINNING A KRYPTON XENON CONCENTRATE FROM A LIQUID MIXTURE.

LIQUID AIR SEPARATION PROCEDURE AND - PLANT WITH MIXTURE COLUMN AND KRYPTON XENON PRODUCTION

PROCEDURE AND DEVICE FOR THE LUFTTRENNUNG

Hydrocarbon gas processing

A process and an apparatus for recovering heavier hydrocarbons from a hydrocarbon gas stream is disclosed. The stream is cooled and divided into first and second streams. The first stream is further cooled and divided into first and second portions. The first and second portions are expanded to the fractionation tower pressure and supplied to the tower at upper mid-column feed positions after the expanded second portion is heated. The second stream is expanded to tower pressure and supplied at a mid-column feed position. A distillation vapor stream is withdrawn above the feed point of the second stream, combined with a portion of the tower overhead vapor stream, compressed to higher pressure, and cooled to condense at least a part of it, forming a condensed stream. At least a portion of the condensed stream is expanded to tower pressure and directed to the tower as its top feed.

CRYOGENIC SEPARATION OF SYNTHESIS GAS

A process and apparatus for separating a feed containing hydrogen, carbon monoxide, methane, and optionally nitrogen to form a product gas having a desired H2:CO molar ratio and optionally a hydrogen product gas and a carbon monoxide product gas. The feed is partially con-densed to form a hydrogen-enriched vapor fraction and a carbon monox-ide-enriched liquid fraction. The hydrogen-enriched vapor fraction and carbon monoxide-enriched liquid fraction are combined in a regulated manner to form an admixture, which is cryogenically separated to form the product mixture having the desired H2:CO molar ratio.

HYDROCARBON GAS PROCESSING

A process for the recovery of ethane, ethylene, propane, propylene, and heavier hydrocarbon components from a hydrocarbon gas stream Is disclosed. The stream is cooled and divided into first and second streams. The first stream is further cooled to condense substantially all of it and is thereafter expanded to the fractionation tower pressure, heated, and supplied to the fractionation tower at an upper mid-column feed position. The second stream is expanded to the tower pressure and is then supplied to the column at a mid-column feed position. A distillation vapor stream is withdrawn from the column above the feed point of the second stream and is then directed into heat exchange relation with the expanded cooled first stream and the tower overhead vapor stream to cool the distillation vapor stream and condense at least a part of it, forming a condensed stream.

DIVIDING WALL COLUMN WITH A HEAT PUMP

Systems and methods for separating a multi-component flu-id are provided. The method can include introducing a multi-component fluid to a dividing wall column. The multi-component fluid can be heated to provide a first product, a second product, an intermediate distillate, and a process fluid. At least a portion of the first product can be compressed to provide a compressed first product. Heat can be indirectly transferred from the compressed first product to at least a portion of the intermediate distil-late to provide a heated intermediate distillate. The heated intermediate distillate can be recycled to the dividing wall column. The compressed first product can be expanded.

SYSTEM AND METHOD FOR SEPARATING NATURAL GAS LIQUID AND NITROGEN FROM NATURAL GAS STREAMS

A system and method for removing nitrogen and producing a high pressure methane product stream and an NGL product stream from natural gas feed streams where at least 90%, and preferably at least 95%, of the ethane in the feed stream is recovered in the NGL product stream. The system and method of the invention are particularly suitable for use with feed streams in excess of 5 MMSCFD and up to 300 MMSCFD and containing around 5% to 80% nitrogen. The system and method preferably combine use of strategic heat exchange between various process streams with a high pressure rectifier tower and the ability to divert all or a portion of a nitrogen rejection unit feed stream to optionally bypass a nitrogen fractionation column to reduce capital costs and operating expenses.

COPRODUCTION OF A NORMAL PURITY AND ULTRA HIGH PURITY VOLATILE COMPONENT FROM A MULTI-COMPONENT STREAM

CARBON DIOXIDE RECOVERY PROCESS

A process for recovering CO2 from a mixture of light hydrocarbons, e.g. light hydrocarbons produced from a CO2 injection enhanced oil recovery. The mixture is distilled in a distributive zone with CO2 produced overhead and in the bottoms. The overhead and bottoms produced from the distributive zone are then fed to first and second concentrating distillation zones, respectively. The first concentrating zone produces a bottoms product rich in CO2 and an overhead product rich in methane and lean in CO2. The second concentrating zone is refluxed with lean oil and produces a CO2 distillate and a CO2-lean bottoms product. In various embodiments, at least a section of each of the concentrating zones are placed in a single column, the CO2 product streams are taken as a side draw, vapor from the first concentrating zone is used in an open cycle heat pump to heat the second concentrating zone, the distributive zone is thermally coupled with one or both of the concentrating zones, and the distributive ...

HYDROCARBON GAS PROCESSING

HYDROCARBON GAS PROCESSING

КРИОГЕННАЯ СИСТЕМА ДЛЯ УДАЛЕНИЯ КИСЛОТНЫХ ГАЗОВ ИЗ ПОТОКА ГАЗООБРАЗНЫХ УГЛЕВОДОРОДОВ

Представлена система для удаления кислотных газов из потока сырьевого газа. Система содержит криогенную дистилляционную колонну. Криогенная дистилляционная колонна имеет зону регулируемого замораживания, которая принимает холодную распыляемую жидкость, состоящую главным образом из метана. Колонна принимает и затем разделяет поток сырьевого газа на поток газообразного верхнего метанового погона и, по существу, твердый материал, состоящий из диоксида углерода. Система содержит коллекторную тарелку под зоной регулируемого замораживания. Коллекторная тарелка принимает, по существу, твердый материал, когда он осаждается в зоне регулируемого замораживания. Система также имеет фильтр. Фильтр принимает, по существу, твердый материал и затем разделяет его на твердый материал, состоящий в основном из диоксида углерода, и жидкий материал, содержащий метан. Твердый материал может быть нагрет как жидкость и продан, тогда как жидкий материал возвращают в криогенную дистилляционную колонну.

СПОСОБЫ И УСТАНОВКА ДЛЯ ИЗВЛЕЧЕНИЯ ГАЗОКОНДЕНСАТНЫХ ЖИДКОСТЕЙ

В рассматриваемых установках и способах извлечения NGL из исходных газов с содержанием диоксида углерода, равным приблизительно 2% или более, используются конфигурации с регулированием температуры, которые обеспечивают высокий уровень и универсальное извлечение этана и более тяжелых компонентов, в то же время при осуществлении способа предотвращается замерзание диоксида углерода. Когда исходный газ содержит значительную долю компонентов С3+ и имеет умеренное содержание диоксида углерода, можно применять конфигурацию с одной колонной и промежуточным конденсатором флегмы, в то время как для исходных газов с высоким содержанием диоксида углерода и относительно низкой концентрацией компонентов С3+ можно применять конфигурации с двумя колоннами.

HYDROCARBON GAS PROCESSING

СПОСОБ И УСТАНОВКА ДЛЯ ПРОИЗВОДСТВА ИНЕРТНЫХ ГАЗОВ И КИСЛОРОДА ПУТЕМ КРИОГЕННОЙ ПЕРЕГОНКИ ВОЗДУХА

Изобретение касается способа и установки для производства инертных газов и кислорода путем криогенной перегонки воздуха. Способ производства инертных газов и кислорода путем перегонки в системе колонн, которая содержит по крайней мере одну колонну (К01) среднего давления, одну колонну (К02) низкого давления и одну вспомогательную колонну (К05), состоит в: слитии промежуточного потока (LR1) на промежуточном уровне колонны среднего давления и перемещении его в колонну низкого давления; сливе потока (LR2), обогащенного кислородом по сравнению с промежуточным потоком, из колонны среднего давления и его перемещении в резервуар вспомогательной колонны; сливе обогащенного азотом потока (WN2) из верха колонны низкого давления; сливании потока обогащенной кислородом жидкости (CL) из резервуара колонны низкого давления в виде продукта, как вариант, после этапа испарения, для того, чтобы образовался газообразный продукт; и сливе из вспомогательной колонны обогащенного кислородом потока (ПРОДУКТЫ ОЧИСТКИ ...

HYDROCARBON GAS PROCESSING

СПОСОБЫ И КОНФИГУРАЦИИ ДЛЯ ИЗВЛЕЧЕНИЯ ГАЗОКОНДЕНСАТНЫХ ЖИДКОСТЕЙ (NGL)

В рассматриваемых установках и способах извлечения NGL из исходных газов с содержанием диоксида углерода, равным приблизительно 2% или более, используются конфигурации с регулированием температуры, которые обеспечивают высокий уровень и универсальное извлечение этана и более тяжелых компонентов, в то же время при осуществлении способа предотвращается замерзание диоксида углерода. Когда исходный газ содержит значительную долю компонентов С3+ и имеет умеренное содержание диоксида углерода, можно применять конфигурацию с одной колонной и промежуточным конденсатором флегмы, в то время как для исходных газов с высоким содержанием диоксида углерода и относительно низкой концентрацией компонентов С3+ можно применять конфигурации с двумя колоннами.

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 ...

METHOD AND PLANT FOR EXTRACTION OF THE PRODUCT SEPARATION, CONTAINING MAINLY HYDROCARBONS WITH TWO CARBON ATOMS

CRYOGENIC SYSTEM FOR REMOVING ACID GASSES FROM A HYDROCARBON GAS STREAM

METHOD AND APPARATUS FOR PREPARATION NITROGEN-HYDROGEN MIX AND AMMONIA

For producing one or a plurality of air products and air separation apparatus

GENERATING PROCESS AND STATION OF CARBON MONOXIDE AND HYDROGEN

Prod of hydrogen by cracking hydrocarbons

PROCESS AND INSTALLATION FOR PRODUCTION COMBINEE Of a MIXTURE OF SYNTHESED' AMMONIA AND Carbon monoxide

PROCESS AND INSTALLATION FOR PRODUCTION COMBINEE Of a MIXTURE OF SYNTHESED' AMMONIA AND Carbon monoxide

PROCESS AND INSTALLATION FOR PRODUCTION COMBINEE Of a MIXTURE OF SYNTHESED' AMMONIA AND Carbon monoxide

PROCESS AND INSTALLATION FOR PRODUCTION COMBINEE Of a MIXTURE OF SYNTHESED' AMMONIA AND Carbon monoxide

AIR FRACTIONATION PROCESS AND INSTALLATION WITH MIXING COLUMN AND KRYPTON-XENON RECOVERY

PURPOSE: Provided are a process for low-temperature fractionation of air in a distillation column system and a corresponding apparatus, which operate economically and have a relatively high krypton and/or xenon yield. CONSTITUTION: The process comprises the steps of: introducing a first feed air stream(4) into the distillation column system for nitrogen-oxygen separation; pressurizing an oxygen-rich fraction(22) removed from the distillation column system for nitrogen-oxygen separation in liquid form(23) and introducing the oxygen-rich fraction(25) to a mixing column(26); introducing a heat transfer medium stream, in particular a second feed air stream(43), into the lower region of the mixing column(26) and bringing the heat transfer medium stream into countercurrent contact with the oxygen-rich fraction(22,25); removing a gaseous top product from the upper region of the mixing column(26); introducing a liquid(38,39,40,41) from the lower or middle region of the mixing column into the distillation ...

INTEGRATED OLEFIN RECOVERY PROCESS

Methods and apparatus for the integration of a fractionation process and an olefin refrigeration system, wherein the fractionation process olefin effluent is supplied to the refrigeration system, can eliminate a fractionation process condenser and reflux drum typically present. A plurality of bottoms streams can be collected from the fractionation process. The olefin refrigerant can be supplied to alternate olefin refrigerant consumers, as desired. A column in the fractionation process can be refluxed with an olefin stream from refrigeration system, and olefin product can be collected or exported via line.

METHOD AND INSTALLATION FOR PRODUCING CARBON MONOXIDE BY CRYOGENIC DISTILLATION

The invention relates to a method for producing carbon monoxide by cryogenic distillation. Said method comprises the following steps: a gaseous mixture (1) containing carbon monoxide, hydrogen and nitrogen is cooled and partially condensed to produce a cooled and partially condensed gaseous mixture; the cooled and partially condensed gaseous mixture (5) is separated in order to produce a gas enriched with hydrogen and a liquid enriched with carbon monoxide (11); a flow of the liquid enriched with carbon monoxide is sent to a product stripper (17) in order to produce hydrogen-depleted liquid carbon monoxide (19) and hydrogen-enriched gaseous carbon monoxide (RSD); a flow of the hydrogen-depleted carbon monoxide is sent to a first intermediate level of a distillation column (23); a liquid flow enriched with methane (27) compared to the flow supplied to the distillation column is drawn off from the bottom of the distillation column; a flow (29) enriched with carbon monoxide is drawn off at ...

Process and apparatus for the production of hydrocarbon compounds from methane

Higher molecular weight hydrocarbon compounds or oxygenates are produced from a gas comprising methane in a process comprising the steps of generating synthesis gas ("syngas") comprising carbon monoxide and hydrogen by reaction of a gas comprising methane with steam and/or an oxidant gas comprising oxygen, producing higher molecular weight hydrocarbon compounds or oxygenates in a syngas conversion process, removing offgas comprising unreacted hydrogen and unreacted carbon monoxide from said syngas conversion process and separating cryogenically unreacted hydrogen from said offgas or from a gas derived therefrom to produce separated hydrogen product that is substantially free of unreacted carbon monoxide and a first cryogenic liquid comprising unreacted carbon monoxide. The unreacted hydrogen is preferably separated from the offgas in a liquid methane wash column.

System and method for separating natural gas liquid and nitrogen from natural gas streams

A system and method for removing nitrogen and producing a high pressure methane product stream and an NGL product stream from natural gas feed streams where at least 90%, and preferably at least 95%, of the ethane in the feed stream is recovered in the NGL product stream. The system and method of the invention are particularly suitable for use with feed streams in excess of 5 MMSCFD and up to 300 MMSCFD and containing around 5% to 80% nitrogen. The system and method preferably combine use of strategic heat exchange between various process streams with a high pressure rectifier tower and the ability to divert all or a portion of a nitrogen rejection unit feed stream to optionally bypass a nitrogen fractionation column to reduce capital costs and operating expenses.

Hydrocarbon gas processing

A process and an apparatus are disclosed for recovering ethane, ethylene, and heavier hydrocarbon components from a hydrocarbon gas stream. The stream is cooled, expanded to lower pressure, and supplied to a first fractionation tower at a mid-column feed position. A distillation liquid stream is withdrawn from the first fractionation tower below the feed position of the expanded stream, heated, and directed into a second fractionation tower that produces an overhead vapor stream and a bottom liquid stream. The overhead vapor stream is cooled to condense it, with a portion of the condensed stream directed to the second fractionation tower as its top feed and the remainder directed to the first fractionation tower at a lower column feed position. The bottom liquid stream from the second fractionation tower is cooled and directed to the first fractionation tower as its top feed.

MANUFACTUR OF CARBON DIOXIDE INCLUDING RECOVERY OF NITROGEN AND ARGON BY-PRODUCT

PURPOSE: To produce carbon dioxide, nitrogen and optionally argon from combustion exhaust gas. CONSTITUTION: This method for producing carbon dioxide and nitrogen from combustion exhaust gas containing less than about 10 wt.% oxygen comprises multiple steps of (a) treating the combustion exhaust gas containing about less than 10 wt.% oxygen to remove particulate matter, (b) compressing the exhaust gas to a pressure in the range from about 25 psia to 200 psia, (c) purifying the exhaust gas to remove trace contaminants, (d) separating the exhaust gas to obtain a carbon dioxide rich fraction and a nitrogen rich fraction, (e) liquefying the carbon dioxide rich fraction and distilling off volatile contaminants to produce pure carbon dioxide, (f) purifying the nitrogen rich fraction to remove contaminants, and (g) cryogenically fractionally distilling the nitrogen rich fraction to produce pure nitrogen. Argon can be produced simultaneously. The combustion exhaust gas in the process is available ...

СПОСОБ ПОЛУЧЕНИЯ СТЕХИОМЕТРИЧЕСКОЙ АЗОТОВОДОРОДНОЙ СМЕСИ, СПОСОБ ПОЛУЧЕНИЯ АММИАКА С ЕЕ ИСПОЛЬЗОВАНИЕМ И УСТРОЙСТВА ДЛЯ РЕАЛИЗАЦИИ УКАЗАННЫХ СПОСОБОВ

FIELD: chemistry. SUBSTANCE: inventions can be used in chemical industry. The method of producing a stoichiometric hydronitric mixture for synthesis of ammonia involves conversion of natural gas and subsequent purification of the obtained synthetic gas. When purifying synthetic gas, the operation of removing methane and argon from the synthetic gas is combined with the operation for condensation of excess nitrogen by absorbing methane and argon with the condensed excess nitrogen. The absorption process takes place in vertical pipes of an absorber-condenser in counter flow with the purified synthetic gas moving in the pipes from bottom up. The space between the pipes is cooled by throttling the condensate, and the absorber-condenser pipes are fitted with apparatus for swirling the stream of condensate. The obtained purified hydronitric mixture can be used in the ammonia synthesis method. EFFECT: invention enables to completely extract methane and argon impurities from synthetic gas with incidental production of an argon product and liquefied methane, and also enables to considerably reduce ammonia synthesis pressure from 300 to 170 atm, which reduces power consumption in production of ammonia. 19 cl, 3 tbl, 2 dwg, 4 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 438 975 (13) C1 (51) МПК C01C C01B C01B B01D 1/04 (2006.01) 3/02 (2006.01) 3/52 (2006.01) 53/14 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2010130346/05, 21.07.2010 (24) Дата начала отсчета срока действия патента: 21.07.2010 (73) Патентообладатель(и): ООО "Проектный офис" (RU) (45) Опубликовано: 10.01.2012 Бюл. № 1 2 4 3 8 9 7 5 (56) Список документов, цитированных в отчете о поиске: RU 2331575 C2, 20.08.2008. RU 2286942 C2, 10.11.2006. GB 901580 A, 18.07.1962. Производство аммиака. /Под ред. В.П. Семенова. - М.: Химия, 1985, с.24-25, 142-143, 147, 151. 2 4 3 8 9 7 5 R U (54) СПОСОБ ПОЛУЧЕНИЯ СТЕХИОМЕТРИЧЕСКОЙ АЗОТОВОДОРОДНОЙ СМЕСИ, СПОСОБ ...

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 Vorrichtung zur Gewinnung eines Krypton-/Xenon-Konzentrats durch Tieftemperaturzerlegung von Luft

Verfahren zur Herstellung von reinstem Stickstoff

Process and apparatus for the production of hydrocarbon compounds from methane

Nitrogen removal with iso-pressure open refrigeration natural gas liquids recovery

PROCEDURE FOR THE PRODUCTION OF PUREST NITROGEN

DEVICE AND PROCEDURE FOR THE LUFTTRENNUNG BY CRYOGENIC DISTILLATION

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

TREATMENT OF NATURAL GAS

Nitrogen removal with iso-pressure open refrigeration natural gas liquids recovery

SYSTEM AND PROCESS FOR THE RECOVERY OF PROPYLENE AND ETHYLENE FROM REFINERY OFFGASES

A system and process for the recovery of ethylene and propylene from a gas stream, such as a refinery offgas stream. The process comprises withdrawing, cooling, and recovering an overhead vapor stream from a single distillation column (20). The process includes withdrawing a liquid C3+, C4+, C5+ or C6+ bottoms product stream (4) and recycling (5) a portion of the bottoms stream (4) to maintain an overhead column condenser (28) at temperature refrigeration levels of above - 140 .degree.F and withdrawing a vapor side stream rich in propylene or ethylene-propylene.

RECOVERY OF C3+HYDROCARBONS

... "THE RECOVERY OF C3+ HYDROCARBONS" In the recovery of C3+ hydrocarbons from a feed stream containing hydrogen and C1 to at least C5 hydrocarbons, e.g., a refinery waste gas, comprising cooling and partially condensing the feed stream; separating the partially condensed feed stream into a liquid fraction and a gaseous fraction; expanding the gaseous fraction, and fractionating the liquid fraction in a rectification column to obtain product stream consisting essentially of C3+ hydrocarbons and a residual gas stream product containing predominantly C2- hydrocarbons, one improvement comprises passing (a) the gaseous fraction prior to expansion; (b) the liquid fraction prior to rectification; and (c) the gaseous fraction after expansion, in indirect heat exchanger relationship with the feed stream to be cooled. Other improvements comprise separate removal of C1 and C2 fractions from the hydrogen gas; the use of a C5+ fraction as a feed to the rectification column and/or as a scrubbing liquid ...

A METHOD AND A PLANT FOR THE RECOVERY OF A SEPARATION PRODUCT CONTAINING PREDOMINANTLY HYDROCARBONS WITH TWO CARBON ATOMS

The invention relates to a method (100) for producing a separation product, containing predominantly hydrocarbons with two carbon atoms, using a separation feed which contains predominantly methane, hydrogen and hydrocarbons with two carbon atoms, wherein the methane content of the separation feed is up to 20% and the separation feed is provided in a gaseous state. According to the invention, the separation feed is partially condensed once at a first pressure level by cooling from a first temperature level to a second temperature level, while producing exactly one first liquid fraction and exactly one first gas fraction; at least one part of the first gas fraction is partially condensed once at the first pressure level by means of further cooling from the second temperature level to a third temperature level, while obtaining exactly one second liquid fraction and exactly one second gas fraction; at least one part of the second gas fraction is subject to a counter flow absorption in the ...

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

A system and method for cryogenic purification of a hydrogen, nitrogen, methane and argon containing feed stream to produce a methane free, hydrogen and nitrogen containing synthesis gas and a methane rich fuel gas, as well as to recover an argon product stream, excess hydrogen, and excess nitrogen is provided. The disclosed system and method are particularly useful as an integrated cryogenic purifier in an ammonia synthesis process in an ammonia plant. The excess nitrogen is a nitrogen stream substantially free of methane and hydrogen that can be used in other parts of the plant, recovered as a gaseous nitrogen product and/or liquefied to produce a liquid nitrogen product.

HELIUM RECOVERY FROM STREAMS CONTAINING HELIUM, CARBON DIOXIDE, AND AT LEAST ONE OF NITROGEN AND METHANE

Systems and methods are provided for recovering helium from a feed comprising helium, carbon dioxide, and at least one of nitrogen and methane. The feed is separated in a first separator to form helium-enriched stream and a CO2-enriched stream, The helium-enriched stream is separated in a pressure swing adsorption unit to form a helium-rich product stream and a helium-lean stream. At least a portion of the helium-lean stream is recycled to the first separator with the feed. In some embodiments, a membrane separation unit is used to enhance helium recovery.

NITROGEN REMOVAL WITH ISO-PRESSURE OPEN REFRIGERATION NATURAL GAS LIQUIDS RECOVERY

A process for recovery of natural gas liquids is disclosed, the process including: fractionating a gas stream comprising nitrogen, methane, ethane, and propane and other c3+ hydrocarbons into at least two fractions including a light fraction comprising nitrogen, methane, ethane, and propane, and a heavy fraction comprising propane and other c3+ hydrocarbons; separating the light fraction into at least two fractions including a nitrogen-enriched fraction and a nitrogen-depleted fraction in a first separator; separating the nitrogen-depleted fraction into a propane-enriched fraction and a propane-depleted fraction in a second separator; feeding at least a portion of the propane-enriched fraction to the fractionating as a reflux; recycling at least a portion of the propane-depleted fraction to the first separator. In some embodiments, the nitrogen-enriched fraction may be separated in a nitrogen removal unit to produce a nitrogen-depleted natural gas stream and a nitrogen-enriched natural ...

HYBRID TURBO EXPANDER AND REFRIGERATED LEAN OIL ABSORBER SYSTEM

METHOD AND APPARATUS FOR REMOVING NITROGEN FROM A CRYOGENIC HYDROCARBON COMPOSITION

Nitrogen is removed from a cryogenic hydrocarbon composition. A least a first portion of the cryogenic hydrocarbon composition is fed to a nitrogen stripper column as a first nitrogen stripper feed stream. A nitrogen-stripped liquid is drawn from the nitrogen stripper column. A liquid hydrocarbon product stream and a process vapour are produced comprising at least a step of depressurizing the nitrogen-stripped liquid to a flash pressure. The process vapour is compressed, and selectively split into a stripping portion and a non-stripping portion. A stripping vapour stream comprising at least the stripping portion is passed into the nitrogen stripper column. A vapour fraction is discharged as off gas, comprising a discharge fraction of overhead vapour from the nitrogen stripper column and comprising at least the bypass portion from the non-stripping portion of the compressed vapour, which bypasses a stripping section positioned in the nitrogen stripper column.

PROCESS AND PLANT FOR THE COMBINED PRODUCTION OF AN AMMONIA SYNTHESIS MIXTURE AND CARBON MONOXIDE

In the process of the invention, an ammonia synthesis mixture and carbon monoxide are produced. The hydrogen is purified in a nitrogen-washing column (61). The carbon monoxide is recovered cryogenically from a first liquid fraction (51) collected at the base of the said washing column (61), in a medium-pressure stripping column (62), then in a low-pressure distillation column (63). A second liquid fraction (52) is drawn from a position intermediate between the base and head of the washing column (61).

WIFI CLIENT CONTINUOUSLY TRACKS THE HEAT LOAD AND LOAD BY DEHYDRATION SUPPLIED TO FLOW, COMING IN THE PROCESS OF CRYOGENIC DISTILLATION

METHOD AND APPARATUS FOR SEPARATING AIR BY CRYOGENIC DISTILLATION

GENERATING PROCESS AND STATION OF CARBON MONOXIDE BY CRYOGENIC DISTILLATION

APPARATUS AND PROCESS OF SEPARATION Of AIR BY CRYOGENIC DISTILLATION

Cryogenic distillation process to remove nitrogen from a synthesis gas containing carbon monoxide by cooling and partially condensing the gaseous mixture

Un procédé de production de monoxyde de carbone par distillation cryogénique comprend les étapes de refroidir et condenser partiellement un mélange gazeux (1) contenant du monoxyde de carbone, de l'hydrogène et de l'azote pour produire un mélange gazeux refroidi et partiellement condensé, séparer le mélange gazeux refroidi et partiellement condensé (5) pour produire un gaz enrichi en hydrogène et un liquide enrichi en monoxyde de carbone, envoyer un débit du liquide enrichi en monoxyde de carbone à une colonne d'épuisement (17) pour produire du monoxyde de carbone liquide dépourvu en hydrogène et du monoxyde de carbone gazeux enrichi en hydrogène, envoyer un débit du monoxyde de carbone dépourvu en hydrogène à un premier niveau intermédiaire d'une colonne de distillation (23), soutirer en cuve de la colonne de distillation un débit liquide enrichi en méthane (27) par rapport au débit alimentant la colonne de distillation, soutirer en un deuxième point intermédiaire un débit (29) riche en ...

METHOD AND INSTALLATION FOR COMBINED PRODUCTION OF A MIXTURE OF HYDROGEN AND NITROGEN AND CARBON MONOXIDE BY CRYOGENIC DISTILLATION AND WASHING

Procédé pour la production combinée d'un mélange d'hydrogène et d'azote, de monoxyde de carbone par distillation et lavage cryogéniques dans lequel on introduit un liquide riche en méthane (45) à un premier niveau intermédiaire d'une colonne de lavage (15) comme premier liquide de lavage et on introduit au moins un liquide riche en azote (73) à un niveau supérieur au premier niveau de la colonne de lavage comme deuxième liquide de lavage et on soutire un mélange d'hydrogène et d'azote comme gaz de tète (27) de la colonne de lavage.

GENERATING PROCESS AND STATION Of OXYGEN AND RARE GASES BY CRYOGENIC DISTILLATION Of AIR

Dans un procédé de production d'oxygène et de gaz rares par distillation dans un système de colonnes comprenant au moins une colonne moyenne pression (K01), une colonne basse pression (K02) et une colonne auxiliaire (K05) , on soutire un débit intermédiaire (LR1) d'un niveau intermédiaire de la colonne moyenne pression et on l'envoie à la colonne basse pression, on soutire un débit, enrichi en oxygène par rapport au débit intermédiaire, de la colonne moyenne pression et on l'envoie en cuve de la colonne auxiliaire on soutire un débit riche en azote (WN2) de la tête de la colonne basse pression on soutire un débit liquide riche en oxygène (OL) de la cuve de la colonne basse pression en tant que produit, éventuellement après une étape de vaporisation pour former un produit gazeux on soutire de la colonne auxiliaire un débit enrichi en oxygène (PURGE), également enrichi en krypton et en xénon par rapport au deuxième débit enrichi en oxygène et on envoie un débit liquide contenant au moins ...

PROCESS AND INSTALLATION FOR PRODUCTION COMBINEE Of a MIXTURE OF SYNTHESED' AMMONIA AND Carbon monoxide

PROCESS AND INSTALLATION FOR PRODUCTION COMBINEE Of a MIXTURE OF SYNTHESED' AMMONIA AND Carbon monoxide

PROCESS AND INSTALLATION FOR PRODUCTION COMBINEE Of a MIXTURE OF SYNTHESED' AMMONIA AND Carbon monoxide

CRYOGENIC SEPARATION OF SYNTHESIS GAS

Gas production system

APPARATUS AND METHOD FOR SEPARATING AIR BY CRYOGENIC DISTILLATION

In a method for separating air by cryogenic distillation in a double column comprising a medium-pressure column (20) and a low-pressure column (21), cooled and purified compressed gaseous air (1) is sent to a first level of the medium-pressure column, cooled and purified compressed liquid air (3) is sent to a second level of the medium-pressure column, a liquid (5) enriched in oxygen, krypton and xenon is tapped from the bottom of the medium-pressure column, a liquid (6) is tapped from the medium-pressure column at a level somewhere between the first and second levels, and sent to the low-pressure column, the liquid enriched in oxygen, krypton and xenon is partially vaporized to form an intermediate gas and an intermediate liquid, a first liquid stream (10) rich in oxygen is tapped from the low-pressure column, a second liquid stream (11) rich in oxygen is tapped from the low-pressure column at a level lower than the intermediate level and the intermediate liquid is sent from the vaporizer ...

METHOD AND SYSTEM FOR THE SEPARATION OF A MIXTURE CONTAINING CARBON DIOXIDE, HYDROCARBON, AND HYDROGEN

The invention provides a method and system for the separation of a mixture containing H2, hydrocarbon, and CO2. The generated mixture is introduced into a distillation column having a side stream to generate a top stream comprising H2, a middle (volatility) stream comprising hydrocarbon; and a bottom stream comprising CO2. In a preferred embodiment, the mixture further comprises N2 which is obtained in the top stream. In a most preferred embodiment, the H2 and the N2 are present in a molar ratio of 3 H2 :1 N2. The generated H2 and N2 may be used for the synthesis of ammonia. Thus, the invention also proves a method and system for the generation of ammonia.

Krypton gas mixture for insulated windows

A mixture of noble gases having desirable insulative properties for use as a window fill gas is derived from an air separation process without substantial further separation or concentration of the noble gases in the mixtures. The mixture of noble gases is processed to form the fill gas using relatively economical catalytic oxidation processes and drying techniques to provide a suitable fill gas. The processed noble gas or fill gas may contain from about 89 to 95% krypton, 5 to 8% xenon and 0.5 to 2% contaminants including oxygen, nitrogen, hydrocarbons and other constituents typically found in air separation processing.

Method for obtaining an air product in an air separating system with temporary storage, and air separating system

A method for obtaining an air product in an air separating system in which a liquid fraction is obtained from feed air and used to provide the air product and in which the liquid fraction is temporarily stored in a tank arrangement. A tank arrangement with at least two tanks is used, and the liquid fraction is fed to at least one of the tanks and/or is removed from at least one of the tanks in order to provide the air product. In the process, the liquid fraction is not fed to and removed from any one of the tanks at the same time, and the composition of the liquid fraction in a tank is ascertained prior to each removal of the liquid fraction from the tank. An air separating system is also described.

Process and device for the recovery of Argon by cryogenic separation of air

Das Verfahren und die Vorrichtung dienen zur Gewinnung von Argon durch Tieftemperaturzerlegung von Luft in einem Destilliersystem, das ein Destilliersäulen-System (4, 5) zur Stickstoff-Sauerstoff-Trennung mit einer Niederdrucksäule (5) sowie eine Mischsäule (39) und eine Rohargon-Rektifikation (61) aufweist. Ein erster Einsatzluftstrom (1, 3) wird in das Destilliersäulen-System (4, 5) zur Stickstoff-Sauerstoff-Trennung eingeführt. Eine erste sauerstoffreiche Fraktion (29, 31, 33) wird in flüssigem Zustand aus der Niederdrucksäule (5) entnommen und auf die Mischsäule (39) aufgegeben. Eine Unrein-Sauerstoff-Fraktion (47) wird aus dem oberen Bereich der Mischsäule (39) abgezogen. Eine erste flüssige Fraktion (43, 44) wird aus dem unteren Bereich der Mischsäule (39) abgezogen und in das Destilliersäulen-System (4, 5) zur Stickstoff-Sauerstoff-Trennung eingeleitet. Ein Wärmeträgerstrom (40, 41, 42), insbesondere ein zweiter Einsatzluftstrom, wird in den unteren Bereich der Mischsäule (39) eingeleitet ...

СПОСОБ И УСТРОЙСТВО ДЛЯ КОМБИНИРОВАННОГО ПОЛУЧЕНИЯ СМЕСИ ВОДОРОДА И АЗОТА, А ТАКЖЕ МОНООКСИДА УГЛЕРОДА ПРИ ПОМОЩИ КРИОГЕННОЙ ДИСТИЛЛЯЦИИ И КРИОГЕННОЙ ПРОМЫВКИ

Способ комбинированного получения смеси водорода и азота, а также монооксида углерода при помощи криогенной дистилляции и криогенной промывки, в котором обогащенную метаном жидкость (45) вводят на первый промежуточный уровень скрубберной колонны (15) в качестве первой промывной жидкости, и по меньшей мере одну обогащенную азотом жидкость (73) вводят на уровень выше первого уровня скрубберной колонны в качестве второй промывной жидкости, и смесь водорода и азота отводят в виде верхнего газа (27) из скрубберной колонны. 2 н. и 8 з.п. ф-лы, 3 ил.

СПОСОБ РАЗДЕЛЕНИЯ УГЛЕВОДОРОДСОДЕРЖАЩЕЙ ГАЗОВОЙ СМЕСИ

FIELD: chemistry. SUBSTANCE: method includes the following steps: a) dehydrating the mixture, b) cooling the mixture, c) feeding the mixture through a first fractionation column (7) to obtain a first stream (105) rich in hydrocarbons and a second stream (106) containing hydrocarbons dissolved in CO 2 , d) feeding components of the first stream (105) for separation in a revolving gas stream in a nozzle to separate components into a third stream (107) rich in components heavier than methane, and a fourth stream (108) rich in said components, e) heating the third stream (107), f) using one part of the third stream (107) as an output gas (114), g) cooling the other part (115) of the third stream (107) and mixing said part with the first stream (105) and feeding the obtained mixture (117) to step d), h) feeding the second stream (108) and the fourth stream (108) into a second fractionation column (12) to separate a fifth stream (109) rich in C3+ hydrocarbons, a sixth stream (110) rich in CO 2 and a seventh stream (111) rich in methane, i) mixing the seventh stream (111) with the initial gas mixture (101) and feeding components to step (a). EFFECT: reduced loss of target components and high cost effectiveness of the method. 7 cl, 3 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК B01D 53/00 (13) 2 568 215 C1 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2014140948/05, 10.10.2014 (24) Дата начала отсчета срока действия патента: 10.10.2014 (73) Патентообладатель(и): Общество с ограниченной ответственностью "ЭНГО Инжиниринг" (RU) (45) Опубликовано: 10.11.2015 Бюл. № 31 2 5 6 8 2 1 5 R U (54) СПОСОБ РАЗДЕЛЕНИЯ УГЛЕВОДОРОДСОДЕРЖАЩЕЙ ГАЗОВОЙ СМЕСИ (57) Реферат: Изобретение относится к технологии нагрев третьего потока (107), f) использование переработки углеводородсодержащих газовых одной части третьего потока (107) в качестве смесей, а именно к низкотемпературной сепарации выходного газа (114), g) охлаждение ...

СПОСОБ И УСТРОЙСТВО ДЛЯ УДАЛЕНИЯ АЗОТА ИЗ КРИОГЕННОЙ УГЛЕВОДОРОДНОЙ КОМПОЗИЦИИ

1. Способ удаления азота из криогенной углеводородной композиции, содержащей азот- и метансодержащую жидкую фазу, причем данный способ включает:- обеспечение криогенной углеводородной композиции, содержащей азот- и метансодержащую жидкую фазу;- подачу первого потока сырья для колонны отпаривания азота при давлении отпаривания в колонну отпаривания азота, содержащую по меньшей мере одну внутреннюю секцию отпаривания, расположенную внутри колонны отпаривания азота, причем указанный первый поток сырья для колонны отпаривания азота содержит первую порцию криогенной углеводородной композиции;- отведение обедненной азотом жидкости из области сборника колонны отпаривания азота, расположенной ниже секции отпаривания;- получение по меньшей мере потока жидкого углеводородного продукта и технологического пара из обедненной азотом жидкости, включающее по меньшей мере стадию сброса давления обедненной азотом жидкости до давления мгновенного испарения;- сжатие указанного технологического пара до по меньшей мере давления отпаривания, тем самым получая сжатый пар;- селективное деление сжатого пара на отпарную порцию и неотпарную порцию, которая не содержит отпарной порции, при этом неотпарная порция содержит перепускаемую порцию указанного сжатого пара;- пропускание потока отпарного пара в колонну отпаривания азота на уровне, находящемся ниже по вертикали указанной секции отпаривания, причем указанный поток отпарного пара содержит по меньшей мере отпарную порцию указанного сжатого пара;- прохождение промежуточного пара через конденсатор, с помощью которого происходит косвенный теплообмен промежуточного пара с потоком РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК F25J 3/02 (11) (13) 2014 128 669 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2014128669, 10.12.2012 (71) Заявитель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) Приоритет(ы): (30) Конвенционный приоритет: 12.12.2011 EP 11192922.0 (85) Дата начала рассмотрения ...

Extraction of krypton or xenon-enriched mixture

The extraction system is integrated into an air separation plant with a double column (1) having a high-pressure section (2) and a low-pressure section (3). A krypton/xenon-rich fraction is taken from the low-pressure column at (16) and passed into a material exchange column (15). The major portion enters the column near its middle at (25) whilst a minor portion enters the head at (26). The other component of the fraction is oxygen. In an alternative method the fraction is injected in its entirety at (25) whilst almost pure oxygen is injected in the head. Nitrogen (18), as the inert gas, is passed into the base of the column at (19). The krypton/xenon rich mixture then collects at the base of the column and is withdrawn at (23). In the above description all gases are liquefied except that, at the base, an evaporator (21) vaporizes the product, gaseous nitrogen being used as the heat exchange medium.

Verfahren zur Zerlegung von Gasgemischen durch fraktionierte Kondensation unter Druck

Verfahren und Vorrichtung zur Gewinnung von Drucksauerstoff und Krypton/Xenon durch Tieftemperaturzerlegung von Luft

Argon production by low temperature air decomposition has the low-pressure column above the high-pressure column and the condensor below the oxygen-enriched fraction feed height to the low-pressure column

Argon production by low temperature air decomposition is effected in a specified arrangement with the low-pressure column (3) positioned above the high-pressure column (2) and with the crude argon condensor (13) positioned below the height (32) at which the first oxygen-rich fraction (33) is introduced (48) into the low-pressure column (3). Argon production by low temperature air decomposition is effected with the low-pressure column (3) positioned above the high-pressure column (2) and with the crude argon condensor (13) positioned below the height (32) at which the first oxygen-rich fraction (33) is introduced (48) into the low-pressure column (3), the process being of the type in which (A) air (28) is fed into a distillation system having a high-pressure (2) and a low-pressure (3) column; (B) an argon fraction (4) is withdrawn from the low-pressure column (3) and fed into a rectifier which has at least one crude argon column (5, 9); (C) a gas (20) from the crude argon rectifier is condensed ...

Nitrogen removal with iso-pressure open refrigeration natural gas liquids recovery

Air separation

Nitrogen removal with iso-pressure open refrigeration natural gas liquids recovery

Mixing and Heat Integration of Melt Tray Liquids in a Cryogenic Distillation Tower

A cryogenic distillation tower for separating a feed stream. The tower includes a distillation section. A controlled freeze zone section is situated above the distillation section and forms a solid from the feed stream. The controlled freeze zone section includes a spray assembly in an upper section and a melt tray assembly in a lower section. The melt tray assembly includes at least one vapor stream riser that directs the vapor from the distillation section into liquid retained by the melt tray assembly, and one or more draw-off openings positioned to permit a portion of the liquid to exit the controlled freeze zone section. The portion of the liquid indirectly exchanges heat with a heating fluid. One or more return inlets return the portion of the liquid to the melt tray assembly after it has been heated in the heat exchanger. 1. A cryogenic distillation tower for separating a feed stream , the distillation tower comprising:a distillation section permitting vapor to rise upwardly therefrom;one or more lines for directing the feed stream into the distillation tower; a spray assembly in an upper section of the controlled freeze zone, and', at least one vapor stream riser that directs the vapor from the distillation section into liquid retained by the melt tray assembly, and', 'one or more draw-off openings positioned to permit a portion of the liquid retained by the melt tray assembly to exit the controlled freeze zone section;, 'a melt tray assembly in a lower section of the controlled freeze zone, wherein the melt tray assembly includes'}], 'a controlled freeze zone section situated above the distillation section, the controlled freeze zone constructed and arranged to form a solid from the feed stream, the controlled freeze zone section including'}a heat exchanger arranged to heat the portion of the liquid through indirect heat exchange with a heating fluid; andone or more return inlets that return the portion of the liquid to the melt tray assembly after the ...

Helium Recovery From Streams Containing Helium, Carbon Dioxide, and at least one of Nitrogen and Methane

Systems and methods are provided for recovering helium from a feed comprising helium, carbon dioxide, and at least one of nitrogen and methane. The feed is separated in a first separator to form helium-enriched stream and a CO-enriched stream. The helium-enriched stream is separated in a pressure swing adsorption unit to form a helium-rich product stream and a helium-lean stream. At least a portion of the helium-lean stream is recycled to the first separator with the feed. In some embodiments, a membrane separation unit is used to enhance helium recovery. 1. A method for recovering helium from a feed stream containing helium , carbon dioxide and at least one of methane and nitrogen , the method comprising:{'sub': 2', '2, 'introducing a separator feed stream into a separator, the separator feed stream comprising at least a portion of the feed stream, separating the separator feed stream into a first helium-enriched stream and a first CO-enriched stream, and withdrawing the first helium-enriched stream and the first CO-enriched stream from the separator;'}introducing a pressure swing adsorption unit feed stream into a pressure swing adsorption unit, the pressure swing adsorption unit feed stream comprising at least a portion of the first helium-enriched stream, separating the pressure swing adsorption unit feed stream into a helium-rich product stream and a helium-lean stream, and withdrawing the helium-rich product stream and the helium-lean stream from the pressure swing adsorption unit;compressing a compressor feed stream in a compressor to form a compressor effluent stream, the compressor feed stream comprising the helium-lean stream and a helium-enriched permeate stream;introducing a first portion of the compressor effluent stream into a membrane separation unit, separating the first portion of the compressor effluent stream to form the helium-enriched permeate stream and a helium-depleted non-permeate stream, and withdrawing the helium-enriched permeate stream ...

PROCESS AND APPARATUS FOR PRODUCTION OF CARBON MONOXIDE BY PARTIAL CONDENSATION

A process for separating a mixture of hydrogen, methane and carbon monoxide by cryogenic distillation. The mixture is cooled in a first heat exchanger and is partially condensed in at least one second heat exchanger which is a bottom reboiler of a first or second column of the column system and at least one portion of the liquid produced by the partial condensation is sent to an intermediate level of the first column. 1. A process for separating a mixture of hydrogen , methane and carbon monoxide by cryogenic distillation in a column system comprising a first column and a second column , comprising:i. cooling the mixture in a first heat exchanger and partially condensing at least one portion thereof in at least one second heat exchanger which is a bottom reboiler of the second column of the column system and at least one portion of the liquid produced by the partial condensation, or a liquid derived therefrom, by at least one step of partial condensation is sent to an intermediate level of the first column, only the at least one portion of the mixture and bottom liquid from the second column exchanging heat in the second heat exchanger, the vaporized bottom liquid being sent back to the column from which it originates,ii. withdrawing a hydrogen-enriched overhead gas from the first column and reheating the hydrogen-enriched overhead gas in the first heat exchanger,iii. withdrawing a liquid enriched in carbon monoxide and in methane from the bottom of the first column and sending it to at least one intermediate level of the second column,iv. withdrawing a methane-rich liquid from the bottom of the second column and withdrawing a fluid rich in carbon monoxide from the top of the second column, andv. producing refrigeration to keep the process cold by means of a refrigeration cycle.2. The process according to claim 1 , in which a portion of the cooled mixture is sent to the second heat exchanger which is a reboiler of the first column.3. The process according to claim 1 ...

PROCESS AND DEVICE FOR THE CRYOGENIC SEPARATION OF SYNTHESIS GAS

The invention relates to a process and device for the cryogenic separation of a methane-containing feed gas predominantly consisting of hydrogen and carbon monoxide, that is partially condensed in this case by cooling, in order to obtain a hydrogen-containing first liquid phase predominantly consisting of carbon monoxide and methane, from which first liquid phase, in an Hseparation column that is heated via a circulation heater, a second liquid phase is generated by separating off hydrogen, from which second liquid phase, in a CO/CHseparation column, a carbon monoxide-rich gas phase is obtained having a purity that permits release thereof as carbon monoxide product. It is characteristic in this case that a low-methane material stream is withdrawn from the Hseparation column and is then applied to the CO/CHseparation column as reflux. 1151811922829263412. Process for the cryogenic separation of a methane-containing feed gas () predominantly consisting of hydrogen and carbon monoxide , that is partially condensed in this case by cooling , in order to obtain a hydrogen-containing first liquid phase () predominantly consisting of carbon monoxide and methane , from which first liquid phase , in an Hseparation column (T) that is heated via a circulation heater () , a second liquid phase () is generated by separating off hydrogen () , from which second liquid phase , in a CO/CHseparation column (T) , a carbon monoxide-rich gas phase () is obtained having a purity that permits release thereof as carbon monoxide product () , characterized in that a low-methane material stream ( , ) is withdrawn from the Hseparation column (T) and is then applied to the CO/CHseparation column (T) as reflux.22612. Process according to claim 1 , characterized in that the low-methane material stream () is withdrawn in the gaseous state from the Hseparation column (T) and liquefied by cooling before introduction thereof into CO/CHseparation column (T).3261. Process according to claim 1 , ...

System and Method for Natural Gas Liquid Production with Flexible Ethane Recovery or Rejection

A system and method for processing an NGL product stream from a natural gas feed stream in either an ethane retention or ethane rejection mode utilizing heat exchange of particular process streams. In ethane rejection mode, there are preferably two stages of heat exchange between the feed stream and a first separator bottoms stream and a side stream withdrawn from a fractionation tower is cooled through heat exchange with both the fractionation tower and second separator overhead streams, and optionally with an external refrigerant, resulting in 5-15% ethane and at least 97% propane recovery. In ethane retention mode, a portion of the feed stream and portions of a first separator overhead and bottoms streams are preferably separately cooled through heat exchange with other process streams, including the entireties of a recycled residue gas and fractionation column overhead streams, resulting in around 99% ethane and around 100% propane recovery. 1. A system for processing a feed stream comprising methane , ethane , propane , and other components in either an ethane rejection mode or ethane retention mode to produce an NGL product stream and a residue gas stream , system comprising:a first separator wherein the feed stream is separated into a first overhead stream and a first bottoms stream;a fractionation column wherein the first overhead stream and first bottoms stream are separated into a second overhead stream and a second bottoms stream, wherein the residue gas stream comprises the second overhead stream and the NGL product stream comprises the second bottoms stream;a first heat exchanger for cooling at least a first portion of the feed stream prior to the first separator through heat exchange with a first set of other streams;a second heat exchanger for warming the second overhead stream prior to the first heat exchanger through heat exchange with a second set of other streams;wherein the first set of other streams comprises (1) the first bottoms stream, the ...

System and Method for Separating Natural Gas Liquid and Nitrogen from Natural Gas Streams

A system and method for removing nitrogen and producing a high pressure methane product stream and an NGL product stream from natural gas feed streams where at least 90%, and preferably at least 95%, of the ethane in the feed stream is recovered in the NGL product stream. The system and method of the invention are particularly suitable for use with feed streams in excess of 5 MMSCFD and up to 300 MMSCFD and containing around 5% to 80% nitrogen. The system and method preferably combine use of strategic heat exchange between various process streams with a high pressure rectifier tower and the ability to divert all or a portion of a nitrogen rejection unit feed stream to optionally bypass a nitrogen fractionation column to reduce capital costs and operating expenses. 1. A system for removing nitrogen from a feed stream comprising nitrogen , methane , ethane , and other components to produce a methane product stream , an NGL product stream , and a nitrogen vent stream the system comprising:a first separator wherein the feed stream is separated into a first overhead stream and a first bottoms stream;a first fractionating column wherein the first overhead stream is separated into a second overhead stream and a second bottoms stream;an expander for expanding the first overhead stream prior to the first fractionating column;a second fractionating column wherein the first bottoms stream and second bottoms stream are separated into a third overhead stream and a third bottoms stream;a third fractionating column wherein at least a first NRU feed stream separated into a fourth overhead stream and a fourth bottoms stream;a first heat exchanger for cooling a first portion of the feed stream prior to the first separator and cooling a first portion of the second overhead stream prior to the third fractionating column through heat exchange with the fourth bottoms stream and a recycle refrigerant stream;a second heat exchanger for cooling the first portion of the second overhead ...

METHOD FOR FLEXIBLE RECOVERY OF ARGON FROM A CRYOGENIC AIR SEPARATION UNIT

A method for flexible production of argon from a cryogenic air separation unit is provided. The disclosed cryogenic air separation unit is capable of operating in a ‘no-argon’ or ‘low-argon’ mode when argon demand is low or non-existent and then switching to operating in a ‘high-argon’ mode when argon is needed. The recovery of the argon products from the air separation unit is adjusted by varying the percentages of dirty shelf nitrogen and clean shelf nitrogen in the reflux stream directed to the lower pressure column. The cryogenic air separation unit and associated method also provides an efficient argon production/rejection process that minimizes the power consumption when the cryogenic air separation unit is operating in a ‘no-argon’ or ‘low-argon’ mode yet maintains the capability to produce higher volumes of argon products at full design capacity to meet argon product demands. 1. A method of producing an argon product in an air separation unit , the method comprising the steps of:producing a stream of compressed and purified air;cooling the compressed and purified air stream in a main heat exchanger system;rectifying the cooled, compressed and purified air stream in a distillation column system configured to produce a plurality of products including one or more oxygen products and the argon product, wherein the distillation column system comprises a higher pressure column and a lower pressure column linked in a heat transfer relationship via a condenser-reboiler and an argon column,extracting a clean shelf nitrogen stream and a dirty shelf nitrogen stream from the distillation column systemsubcooling the clean shelf nitrogen stream and the dirty shelf nitrogen stream in one or more nitrogen subcoolers;directing the subcooled clean shelf nitrogen stream to an uppermost location of the lower pressure column and the subcooled dirty shelf nitrogen stream to another location of the lower pressure column at or below the uppermost location;wherein the air separation ...

SYSTEM AND METHOD FOR FLEXIBLE RECOVERY OF ARGON FROM A CRYOGENIC AIR SEPARATION UNIT

A system and method for flexible production of argon from a cryogenic air separation unit is provided. The cryogenic air separation unit is capable of operating in a ‘no-argon’ or ‘low-argon’ mode when argon demand is low or non-existent and then switching to operating in a ‘high-argon’ mode when argon is needed. The recovery of the argon products from the air separation unit is adjusted by varying the percentages of dirty shelf nitrogen and clean shelf nitrogen in the reflux stream directed to the lower pressure column. The cryogenic air separation unit and associated method also provides an efficient argon production/rejection process that minimizes the power consumption when the cryogenic air separation unit is operating in a ‘no-argon’ or ‘low-argon’ mode yet maintains the capability to produce higher volumes of argon products at full design capacity to meet argon product demands. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. (canceled)14. (canceled)15. (canceled)16. (canceled)17. (canceled)18. (canceled)19. (canceled)20. (canceled)21. (canceled)22. (canceled)23. (canceled)24. (canceled)25. (canceled)26. (canceled)27. (canceled)28. (canceled)29. (canceled)30. An air separation unit comprising:a main air compression system configured for producing a compressed and purified air stream;a main heat exchange system configured to cool the compressed and purified air stream;a distillation column system comprising a plurality of columns including a higher pressure column and a lower pressure column linked in a heat transfer relationship via a condenser-reboiler and an argon column arrangement operatively coupled with the lower pressure column, the distillation column system configured to receive the compressed and purified air stream and produce a clean shelf nitrogen stream, a dirty shelf nitrogen stream from the plurality of columns, one or more oxygen ...

PROCESS AND PLANT FOR THE COMBINATION PRODUCTION OF A MIXTURE OF HYDROGEN AND NITROGEN AND ALSO OF CARBON MONOXIDE BY CRYOGENIC DISTILLATION AND CRYOGENIC SCRUBBING

Process for the combined production of a mixture of hydrogen and nitrogen, and of carbon monoxide by cryogenic distillation and cryogenic scrubbing, wherein a methane-rich liquid is introduced at a first intermediate level of a scrubbing column as first scrubbing liquid and at least one nitrogen-rich liquid is introduced at a level higher than the first level of the scrubbing column as second scrubbing liquid and a mixture of hydrogen and nitrogen is drawn off as overhead gas from the scrubbing column. 110-. (canceled)11. A process for the combined production of a mixture of hydrogen and nitrogen , of carbon monoxide by cryogenic distillation and cryogenic scrubbing , wherein the process comprises the steps of:i) cooling, in a heat exchanger, a gas mixture containing at least hydrogen, carbon monoxide and methane;ii) sending the cooled mixture to a scrubbing column;iii) introducing a methane-rich liquid at a first intermediate level of the scrubbing column as a first scrubbing liquid;iv) introducing at least one nitrogen-rich liquid at a level higher than the first level of the scrubbing column as a second scrubbing liquid;v) withdrawing a mixture of hydrogen and nitrogen as an overhead gas from the scrubbing column;vi) withdrawing a first bottoms liquid from the scrubbing column and then sending said first bottoms liquid to a stripping column;vii) withdrawing a liquid that is level with an intermediate section of the scrubbing column and sending said liquid either to the heat exchanger, or to a stripping column overhead gas line, or to a second stripping column;viii) withdrawing a second bottoms liquid from the stripping column and then sending to a column configured to separate carbon monoxide and methane; andix) withdrawing a fluid rich in carbon monoxide from the separating column;x) withdrawing a third bottoms liquid from the separating column, wherein at least one portion of the third bottoms liquid from the separating column constitutes the methane-rich ...

System and Method for Separating Natural Gas Liquid and Nitrogen from Natural Gas Streams

A system and method for removing nitrogen and producing a high pressure methane product stream and an NGL product stream from natural gas feed streams where at least 90%, and preferably at least 95%, of the ethane in the feed stream is recovered in the NGL product stream. The system and method of the invention are particularly suitable for use with feed streams in excess of 5 MMSCFD and up to 300 MMSCFD and containing around 5% to 80% nitrogen. The system and method preferably combine use of strategic heat exchange between various process streams with a high pressure rectifier tower and the ability to divert all or a portion of a nitrogen rejection unit feed stream to optionally bypass a nitrogen fractionation column to reduce capital costs and operating expenses. 1. A system for removing nitrogen from a feed stream comprising nitrogen , methane , ethane , and other components to produce a methane product stream and an NGL product stream , the system comprising:a first separator wherein the feed stream is separated into a first overhead stream and a first bottoms stream;a first fractionating column wherein the first overhead stream is separated into a second overhead stream and a second bottoms stream;an expander for expanding the first overhead stream prior to the first fractionating column;a second fractionating column wherein the second bottoms stream is separated into a third overhead stream and a third bottoms stream;a third fractionating column wherein at least a first NRU feed stream is separated into a fourth overhead stream and a fourth bottoms stream;a first heat exchanger for cooling a first portion of the feed stream prior to the first separator and cooling a first portion of the second overhead stream prior to the third fractionating column through heat exchange with the fourth bottoms stream and a recycle refrigerant stream;a second heat exchanger for cooling the first portion of the second overhead stream after the first heat exchanger and prior to ...

ALTERNATIVE TWO COLUMN HRU DESIGN WITH RICH REFLUX

The invention relates to a system, method and apparatus for removing heavies from natural gas. Natural gas and an external rich reflux gas feed are processed in a single column refluxed absorber. A bottoms stream is routed to a first heat exchanger and then to a stabilizer column where an overhead stream from the stabilizer column is routed through a condenser for partial separation into an overhead stream. A rich solvent may be introduced to the stabilizer column. The overhead stream is routed through a condenser for partial separation into a stabilizer reflux and a second overhead stream lights. The second overhead stream lights is routed to a heat exchanger and then routed to a partial condenser where the stream is separated into a heavies rich reflux stream, a distillate stream and heavies treated natural gas stream. The rich reflux is routed through a heat exchanger and the rich reflux is pumped to the single column refluxed absorber to be introduced into the single column refluxed absorber as the external rich reflux gas feed. 1. A method for natural gas processing comprising:introducing a natural gas feed to a single column refluxed absorber;introducing an external rich reflux gas feed to the single column refluxed absorber;processing the natural gas feed and the external rich reflux gas feed in the single column refluxed absorber to produce a first bottoms stream and a first overhead stream, wherein the first bottoms stream and the first overhead stream are separate streams upon expulsion from the single column refluxed absorber, wherein the first bottoms stream is routed to a first heat exchanger and then to a stabilizer column and the first overhead stream is routed through a condenser for partial separation of the first overhead stream into heavies-treated natural gas;routing the heavies treated natural gas to storage of heavies treated natural gas;introducing a rich solvent to the stabilizer column;processing the first bottoms stream and the rich solvent ...

MIXED REFRIGERANT SYSTEM FOR NATURAL GAS PROCESSING

A simplified mixed refrigerant system for natural gas processing which eliminates the need for storing, mixing and adjusting the individual hydrocarbon components of the refrigerant thereby rendering what are normally complex systems more practical for the natural gas liquid recovery industry. 1. A method for recovering natural gas liquids (NGL) from a natural gas stream , comprising:receiving a natural gas stream into an inlet of a heat exchanger associated with a heat exchanger section;cooling the received natural gas stream using a mixed refrigerant circulated by a refrigerant loop to form a cooled and partially condensed natural gas stream;receiving the cooled and partially condensed natural gas stream in a separator to form an overhead gas stream and a liquid stream;stabilizing at least a portion of the liquid stream from the separator in a liquid stabilization system, wherein the liquid stream passes through a distillation column, the distillation column having a plurality of trays and a plurality of taps, each tap of the plurality of trays being in fluid communication with a tray of the plurality of trays;sending an overhead stream from the distillation column to the heat exchanger section;drawing a portion of the cooled NGL stream using at least one tap; andsending the portion of drawn cooled NGL stream to the refrigerant loop.2. The method of claim 1 , wherein the mixed refrigerant circulates in the heat exchanger via a sub-cooler line and an evaporation pass line claim 1 , and further comprising:dropping a pressure of the mixed refrigerant using a pressure reduction device connected between the sub-cooler line and the evaporation pass line;completely vaporizing the mixed refrigerant in the evaporation pass line;receiving and compressing the completely vaporized mixed refrigerant in a compressor associated with the refrigerant loop;cooling the compressed mixed refrigerant using at least one cooler; andsending the cooled compressed mixed refrigerant to the ...

CYROGENIC SEPARATION OF LIGHT OLEFINS AND METHANE FROM SYNGAS

In accordance with the present invention, disclosed herein is a method comprising the steps for separating syngas and methane from C2-C4 hydrocarbons. Also disclosed herein, are systems utilized to separate syngas and methane from C2-C4 hydrocarbons. 1. A method comprising the steps of:a) providing a first product stream comprising syngas, methane, and C2-C4 hydrocarbons, wherein the first product stream has a first temperature;b) lowering the first temperature of the first product stream to a second temperature in a first heat exchange unit;c) separating at least a portion of the syngas from the first product stream in a cryogenic separation unit, thereby producing a second product stream comprising methane and C2-C4 hydrocarbons;d) separating at least a portion of the methane in the second product stream in a demethanizer, thereby producing a third product stream comprising C2-C4 hydrocarbons;e) recycling the at least a portion of the separated syngas to a Fischer-Tropsch reactor; andf) recycling the at least a portion of the separated methane to a syngas generation unit.2. The method of , further comprises the step of separating at least a portion of Hfrom the at least a portion of the separated syngas in a methane wash unit , thereby producing a methane wash product comprising methane and carbon monoxide , wherein at least a portion of separated methane in the method of is used to wash the at least a portion of the separated syngas in the methane wash unit.3. The method of claim 1 , wherein the separated syngas has a third temperature claim 1 ,wherein the method further comprises the steps of:{'sub': '2', 'lowering the third temperature of at least a portion of the separated syngas to a fourth temperature via a Nrefrigeration loop and a second heat exchange unit; and'}recycling energy from the portion of the separated syngas with the fourth temperature to the first product stream comprising syngas, methane, and C2-C4 hydrocarbons via the first heat exchange unit ...

NITROGEN PRODUCTION METHOD AND NITROGEN PRODUCTION APPARATUS

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

System and method for enhanced recovery of argon and oxygen from a nitrogen producing cryogenic air separation unit

A moderate pressure air separation unit and air separation cycle is disclosed that provides for up to about 96% recovery of argon, an overall nitrogen recovery of 98% or greater and limited gaseous oxygen production. The air separation is configured to produce a first high purity oxygen enriched stream and a second lower purity oxygen enriched stream from the lower pressure column, one of which is used as the refrigerant to condense the argon in the argon condenser, with the resulting vaporized oxygen stream used to regenerate the temperature swing adsorption pre-purifier unit. All or a portion of the first high purity oxygen enriched stream is vaporized in the main heat exchanger to produce the gaseous oxygen products.

HYDROCARBON GAS PROCESSING FEATURING A COMPRESSED REFLUX STREAM FORMED BY COMBINING A PORTION OF COLUMN RESIDUE GAS WITH A DISTILLATION VAPOR STREAM WITHDRAWN FROM THE SIDE OF THE COLUMN

A process and an apparatus are disclosed for the recovery of ethane, ethylene, propane, propylene, and heavier hydrocarbon components from a hydrocarbon gas stream. The stream is cooled and divided into first and second streams. The first stream is further cooled to condense substantially all of it and divided into first and second portions. The first and second portions are expanded to the fractionation tower pressure and supplied to the fractionation tower at upper mid-column feed positions, with the expanded second portion being heated before it enters the tower. The second stream is expanded to the tower pressure and supplied to the column at a mid-column feed position. A distillation vapor stream is withdrawn from the column above the feed point of the second stream, combined with a portion of the tower overhead vapor stream, compressed to higher pressure, and directed into heat exchange relation with the remaining tower overhead vapor stream and the expanded second portion to cool the compressed combined vapor stream and condense at least a part of it, forming a condensed stream. At least a portion of the condensed stream is expanded to the tower pressure and directed to the fractionation tower as its top feed. The quantities and temperatures of the feeds to the fractionation tower are effective to maintain the overhead temperature of the fractionation tower at a temperature whereby the major portion of the desired components is recovered. 1. In a process for the separation of a gas stream containing methane , Ccomponents , Ccomponents , and heavier hydrocarbon components into a volatile residue gas fraction and a relatively less volatile fraction containing a major portion of said Ccomponents , Ccomponents , and heavier hydrocarbon components or said Ccomponents and heavier hydrocarbon components , in which process(a) said gas stream is cooled under pressure to provide a cooled stream;(b) said cooled stream is expanded to a lower pressure whereby it is ...

Reducing Refrigeration and Dehydration Load for a Feed Stream Entering a Cryogenic Distillation Process

A system for conditioning a sour gas feed stream for a cryogenic distillation tower, comprising a dehydration unit configured to separate the sour gas feed stream into a first stream comprising water and a feed stream, and a sequential cooling assembly coupled to both the dehydration unit and the cryogenic distillation tower, wherein the sequential cooling assembly comprises a first stage configured to separate the feed stream into a partially cooled feed stream and a second stream comprising acid gas, a second stage configured to cool the partially cooled feed stream into a cooled feed stream and a third stream comprising acid gas, and a cooled feed stream header coupled to a cryogenic distillation tower feed inlet, wherein the first stage, the second stage, or both are configured to send at least one of the second and third streams to a bottom section of the cryogenic distillation tower. 1. A system for conditioning a sour gas feed stream for a cryogenic distillation tower , comprising:a dehydration unit configured to separate the sour gas feed stream into a first stream comprising water and a feed stream; and a first stage configured to separate the feed stream into a partially cooled feed stream and a second stream comprising acid gas;', 'a second stage configured to cool the partially cooled feed stream into a cooled feed stream and a third stream comprising acid gas; and', 'a cooled feed stream header coupled to a cryogenic distillation tower feed inlet,', 'wherein the first stage, the second stage, or both are configured to send at least one of the second and third streams to a bottom section of the cryogenic distillation tower., 'a sequential cooling assembly coupled to both the dehydration unit and the cryogenic distillation tower, wherein the sequential cooling assembly comprises2. The system of claim 1 , wherein the first stage comprises a first separator coupled to a first cryogenic distillation tower bottom section inlet.3. The system of claim 1 , ...

SYSTEMS AND METHODS FOR REMOVAL OF NITROGEN FROM LNG

A system for the removal of nitrogen from a liquid natural gas (LNG) stream. The system. comprises a feed heat changer and a stripper column. The heat receives the LNG stream and cools the LNG stream via heat exchange with a stripper column side-draw stream to yield a cooled LNG stream and a heated side-draw stream. The stripper column receives the cooled LNG stream at a first tray and the heated side-draw stream. The stripper column produces the stripper column side-draw stream, a stripper column overhead stream, and a stripper column bottom stream. The stripper column side-draw stream is taken from the stripper column at a second tray. The second tray is at least about 15 feet higher than the feed heat exchanger. 1. A system for the removal of nitrogen from a liquid natural gas (LNG) stream , the system comprising:a feed heat exchanger, wherein the heat is configured to receive the LNG stream and to cool the LNG stream via heat exchange with a stripper column side-draw stream to yield a cooled LNG stream and a heated side-draw stream; anda stripper column, wherein the stripper column is configured to receive the cooled LNG stream at a first tray and the heated side-draw stream, and wherein the stripper column is configured to produce the stripper column side-draw stream, a stripper column overhead stream, and a stripper column bottom stream,wherein the stripper column is configured such that the stripper column side-draw stream is taken from the stripper column at a second tray, wherein the second tray is at least about 15 feet higher than the feed heat exchanger.2. The system of claim 1 , further comprising a pressure reduction device claim 1 , wherein the pressure reduction device is configured to reduce the pressure of the stripper column side-draw stream prior to introduction into the feed heat exchanger.3. The system of claim 2 , wherein the pressure reduction device is a valve.4. The system of claim 2 , further comprising a control device claim 2 , wherein ...

Impurity Control For A High Pressure CO2 Purification And Supply System

An apparatus for producing a purified, pressurized liquid carbon dioxide stream includes a distillation column (B) having packing (C) therein and a sump (D) below the packing, the distillation column in fluid communication with the liquid carbon dioxide supply tank for receiving the liquid carbon dioxide stream and the packing stripping volatile impurities from the liquid carbon dioxide stream; a heater (E) in contact with the liquid carbon dioxide stream in the sump (D) for vaporizing the liquid carbon dioxide stream in the sump; a vent in the distillation column (B) from which a first vaporized portion (G) of carbon dioxide vapor in the sump (D) is withdrawn from the distillation column: and a conduit (I) in fluid communication with the sump (D) and from which a second vaporized portion (H) of the carbon dioxide vapor in the sump is withdrawn into the conduit (I) to be introduced into the carbon dioxide vapor feed stream. 1101314182030203130453010513018. In an apparatus for producing a purified , pressurized liquid carbon dioxide stream , including a liquid carbon dioxide supply tank () for distilling off a feed stream comprising carbon dioxide vapor , at least one purifying filter ( ,) for purifying the carbon dioxide vapor feed stream , a condenser () for condensing the carbon dioxide vapor feed stream into an intermediate liquid carbon dioxide stream , a receiver () for accumulating the intermediate liquid carbon dioxide stream , a high-pressure accumulation chamber () for accepting the intermediate liquid carbon dioxide stream from the receiver () , a heater () for heating the high-pressure accumulation chamber () for pressurizing the carbon dioxide liquid contained therein to a delivery pressure , a sensor () for detecting when the high-pressure accumulation chamber () requires replenishment of liquid carbon dioxide () , a flow network having conduits connecting the bulk supply tank , the condenser , the receiver and the high-pressure accumulation chamber and ...

Impurity Control For A High Pressure CO2 Purification And Supply System

A batch process for producing a purified, pressurized liquid carbon dioxide stream, includes withdrawing a liquid carbon dioxide stream (A) from a liquid carbon dioxide supply (); introducing the liquid carbon dioxide stream (A) into a distillation column (B) having packing (C) therein, and stripping volatile impurities from the liquid carbon dioxide stream with the packing; vaporizing the liquid carbon dioxide stream (A) in a sump (D) of the distillation column (B) for providing a carbon dioxide vapor; withdrawing from a vaporized portion (F) of carbon dioxide vapor in the sump (D) a first vapor stream (G) vented from the distillation column (B); withdrawing from the vaporized portion (F) of the carbon dioxide vapor in the sump (D) a second vapor portion (H) vented from the sump into a conduit (I); and introducing the second vapor portion (H) in the conduit (I) into a carbon dioxide vapor feed stream. 1101314182030303030. In a batch process for producing a purified , pressurized liquid carbon dioxide stream including providing a liquid carbon dioxide supply () , introducing a carbon dioxide vapor feed stream into at least one purifying filter ( ,) , condensing the purified vapor feed stream within a condenser () to form an intermediate liquid carbon dioxide stream , accumulating the intermediate liquid carbon dioxide stream in a receiver () , introducing the intermediate liquid carbon dioxide stream into at least on high-pressure accumulation chamber () , heating the high pressure accumulation chamber () to pressurize the intermediate liquid carbon dioxide stream contained therein to a delivery pressure , delivering a pressurized liquid carbon dioxide stream from the high-pressure accumulation chamber () , and discontinuing delivery of the pressurized liquid carbon dioxide stream for replenishing the high pressure accumulation chamber () , wherein the improvement comprises:{'b': '10', 'withdrawing a liquid carbon dioxide stream (A) from the liquid carbon dioxide ...

USE OF DENSE FLUID EXPANDERS IN CRYOGENIC NATURAL GAS LIQUIDS RECOVERY

A system and a process for processing a natural gas liquid feed is provided. In the system, a dense fluid expander is positioned downstream from a subcooler heat exchanger. The subcooler heat exchanger cools one or more reflux streams against an overhead vapor stream and a distillation column positioned downstream from the dense fluid expander. An increase in recovery of natural gas liquids is provided through the use of this system having at least one dense fluid expander. 1. A system for producing natural gas liquid products comprisinga. a dense fluid expander positioned downstream from a subcooler heat exchanger, wherein said subcooler heat exchanger cools one or more reflux streams against an overhead vapor streamb. and a distillation column positioned downstream from said dense fluid expander.2. The system of wherein a backpressure valve is located between said dense fluid expander and said distillation column.3. The system of further comprising a Joules-Thomson valve positioned on a line parallel to said dense fluid expander.4. The system of wherein said dense fluid expander is positioned to accept the liquid feed from said dense fluid expander into an upper portion of said distillation column.5. The system of wherein said distillation column has an upper exit for a residue gas stream and a lower exit for a liquid stream.6. The system of further comprising a recycle line positioned to return a portion of the residual gas stream to said distillation column.7. The system of further comprising a dense fluid expander on said recycle line.8. A process for separating a hydrocarbon mixture into a liquid stream and a vapor stream claim 6 , said process comprising the steps of:a. cooling a hydrocarbon feed to produce a two-phase mixture;b. separating said two-phase mixture into a vapor stream and a liquid stream;c. sending at least a portion of said vapor stream through a subcooler heat exchanger to produce a liquefied stream;d. sending the liquefied stream through a ...

GAS LIQUEFACTION COLUMN

An apparatus and process for the compression, expansion, evaporation, and liquefaction of gases or gaseous mixtures consisting of a gas liquefaction column comprising successive chambers made of balloons resembling those used in pneumatic suspensions, and double-piston bases in between the upper and lower end of each chamber. Some of the double-piston bases are fixed while others in between are mobile. The group of mobile double-piston bases is activated in a linear to-and-fro vertical stroke while the other group of double-piston bases remains stationary. This results in consecutive suction and compression of the chambers, creating a Joule-Thomson effect at each of them. This results in the cooling and liquefaction of the gas or gaseous mixture. The apparatus also comprises humidity extractors, and different types of valves and piping. 11223233232367710910aa. An apparatus and process for the compression , expansion , evaporation , and liquefaction of gases or gaseous mixtures by cooling , consisting of a vertical gas liquefaction column () under vacuum , comprising successive chambers () made of balloons () , and groups of double-piston bases () in between the upper and lower end of each chamber () , some of said double-piston bases () being fixed while others in between being mobile , the group of mobile double-piston bases () is activated in a linear to-and-fro vertical stroke compressing and expanding the balloons () while the other group of double-piston bases () remains stationary , resulting in consecutive compression and suction of said chambers () to create the cooling effect , the double-piston bases () further comprising , at their bottom , a floating ball () that blocks the liquefied gases consecutively formed by the cooling process , and forces said liquefied gases to flow out through each individual conduit of a piping () to different tanks , forcing the opening of a pressure valve situated at the bottom end of said piping () , said apparatus also ...

Method for obtaining a liquid and a gaseous oxygen-rich air product in an air breakdown apparatus and air breakdown apparatus

Es wird ein Verfahren zur Tieftemperaturzerlegung von Luft vorgeschlagen, bei dem eine Luftzerlegungsanlage (100) mit einem Destillationssäulensystem (6, 7) verwendet wird, das eine auf einem ersten Druckniveau betriebene Hochdrucksäule (61), eine auf einem zweiten, geringeren Druckniveau betriebene Niederdrucksäule (62) und eine Mischsäule (7) umfasst. In die Mischsäule (7), insbesondere unmittelbar oberhalb des Sumpfes, wird ein erster Druckluftstrom (h) gasförmig eingespeist und in der Mischsäule (7) einem sauerstoffreichen Strom (n) entgegengeschickt. Der erste Druckluftstrom (h) wird unter Verwendung von Luft gebildet, die auf ein Ausgangsdruckniveau oberhalb des ersten Druckniveaus verdichtet und danach auf ein erstes Temperaturniveau abgekühlt und in einer ersten drehzahlvariablen Turbine (4) entspannt wird. In die Hochdrucksäule (62) wird ein zweiter Druckluftstrom (g) eingespeist, der ebenfalls unter Verwendung der auf das Ausgangsdruckniveau verdichteten und danach auf das erste Temperaturniveau abgekühlten und in der ersten Turbine (4) entspannten Luft gebildet wird. In die Niederdrucksäule (62) wird hingegen ein dritter Druckluftstrom (f) eingespeist, der unter Verwendung von Luft gebildet wird, die zwar ebenfalls auf das Ausgangsdruckniveau verdichtet wird, danach aber auf ein zweites Temperaturniveau abgekühlt, in einer zweiten drehzahlvariablen Turbine (4) entspannt und weiter auf ein drittes Temperaturniveau abgekühlt wird. Die Luft in der ersten Turbine (4) wird auf das erste und die Luft in der zweiten Turbine (5) auf das zweite Druckniveau entspannt. Die Mischsäule (7) wird auf dem ersten Druckniveau oder einem dritten Druckniveau betrieben, das sich um höchstens 1 bar von dem ersten Druckniveau unterscheidet. Ein flüssiges sauerstoffreiches Luftprodukt wird aus der Luftzerlegungsanlage (100) in flüssigem Zustand ausgeleitet. Eine entsprechende Luftzerlegungsanlage (100) ist ebenfalls Gegenstand der vorliegenden Erfindung. A process is proposed ...

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 and device for recovering a product under pressure by cryogenic air separation

Recovery of pressure product (22) from low temperature air breakdown in a rectifier system, the assembly has a pressure column (3) and a low pressure column (4). Product fraction taken from the rectifier system is converted into a liquid by pressure and evaporated by indirect heat exchange with head product in the mixing column at the main heat exchanger, to be taken off as a pressure product. Recovery of a pressure product (22) from a low temperature air breakdown in a rectifier system, the assembly has a pressure column (3) and a low pressure column (4). An initial flow (50) of compressed clean air (1) is cooled in a main heat exchanger system (2), to be carried by a feed (51) into the pressure column. At least one fraction (5) from the pressure column is relaxed (7) and stored in the low pressure column. A fraction (218a), rich in oxygen, is converted into a liquid in a pressure stage (220) and carried (224,226) to a mixing column (27). A heat carrier (66) enters the lower section of the mixing column, to move through the fraction in a counterflow, and a gas head product (28) is extracted from the upper section of the column. A product fraction taken from the rectifier system is converted into a liquid by pressure, and evaporated by indirect heat exchange with the head product in the mixing column at the main heat exchanger, to be taken off as a pressure product.

Air separation process and apparatus with a mixing column and krypton and xenon recovery

Process for obtaining an ethane-rich fraction for refilling the ethane-containing refrigeration circuit of a liquefaction process for a hydrocarbon-rich fraction

In the generation of an ethane-rich fraction for use as make-up in the cooling circuit in a process for liquefying a hydrocarbon-rich fraction, a side-stream of the already liquefied hydrocarbon fraction is fed to a C1/C2/C3+ fractionating column. An ethane-rich fraction is drawn off from the middle of the fractionating column and mixed with the ethane-bearing cooling medium.

Process for obtaining an ethane-rich fraction for refilling the ethane-containing refrigeration circuit of a liquefaction process for a hydrocarbon-rich fraction

Demixing sidedraws for distillation columns

The present invention provides one or more sidedraws, from the stripping section of a column, of a heavy key component in the presence of a desirable heavier than heavy key component. In addition, the present invention provides one or more sidedraws, from the rectification section of a column, of a light key component in the presence of a desirable lighter than light key component. In prior art columns, an inherent remixing of the components to be separated in downstream columns occurs near the top or bottom of refluxed or reboiled columns respectively. In the prior art, a re-separation of the remixed components from an upstream column must be done in downstream columns. The present invention eliminates or reduces, according to desired optimization, the remixing by removal of the heavy or light key components in the sidedraw stream.

Dephlegmator process with liquid additive

A cryogenic process for the separation of one light gas component from a heavier gas component in a gas feed stream, by injecting a liquid hydrocarbon additive stream into the top or upper portion of a dephlegmator-heat exchanger, to increase the rectification temperature, or to maintain the temperature and reduce the additive flow rate relative to the respective values required with a conventional, single stage condenser.

Verfahren zur Kälteversorgung der Tieftemperaturtrennungsstufe einer Olefinanlage

Es wird ein Verfahren zur Kältemittelversorgung einer Tieftemperaturtrennungsstufe in einer Anlage zur Herstellung von Olefinen aus kohlenwasserstoffhaltigem Einsatz (Olefinanlage) beschrieben. Während der, mit einem front end Deethanizer (3) nach Rohgasverdichtung (1), Vorkühlung und Trocknung (2) beginnenden, Trennsequenz wird zuerst in eine Olefinfraktion mit höchstens zwei Kohlenstoffatomen und eine Olefinfraktion mit mindestens drei Kohlenstoffatomen getrennt. Die Fraktion mit mindestens drei Kohlenstoffatomen wird zur weiteren Trennsequenz für längerkettige Olefine geführt (4). Die Fraktion mit höchstens zwei Kohlenstoffatomen wird über eine zwischengeschaltete katalytische Hydrierungsstufe (5) zur Tieftemperaturtrennungsstufe (6) geführt, die drei Kondensationsstufen im Temperaturbereich von -50°C bis -100°C umfasst. Aus der Tieftemperaturtrennungsstufe werden gasförmiger Wasserstoff (9) und Methan (10) abgeleitet, während die Olefine mit höchstens zwei Kohlenstoffatomen zu einer weiteren Fraktionierungsstufe geführt werden (7). Die Kälteleistung für die Tieftemperaturtrennungsstufe wird durch die Verdampfung eines Teils der im front end Deethanizer entstehenden flüssigen Ethylenfraktion (8) über Wärmetauschern zur Verfügung gestellt. Die verdampfte Ethylenfraktion wird zur Rohgasverdichtung zurückgeführt (11).

Recovery of C3+ hydrocarbons

In the recovery of C 3+ hydrocarbons from a feed stream containing hydrogen and C 1 to at least C 5 hydrocarbons, e.g., a refinery waste gas, comprising cooling and partially condensing the feed stream; separating the partially condensed feed stream into a liquid fraction and a gaseous fraction; expanding the gaseous fraction, and fractionating the liquid fraction in a rectification column to obtain product stream consisting essentially of C 3+ hydrocarbons and a residual gas stream product containing predominantly C 2- hydrocarbons, one improvement comprises passing (a) the gaseous fraction prior to expansion; (b) the liquid fraction prior to rectification; and (c) the gaseous fraction after expansion, in indirect heat exchanger relationship with the feed stream to be cooled. Other improvements comprise separate removal of C 1 and C 2 fractions from the hydrogen gas; the use of a C 5+ fraction as a feed to the rectification column and/or as a scrubbing liquid for separating the partially condensed feed stream.

Method for providing refrigeration to the cryogenic separation stage of an olefin plant

Es wird ein Verfahren zur Kältemittelversorgung einer Tieftemperaturtrennungsstufe in einer Anlage zur Herstellung von Olefinen aus kohlenwasserstoffhaltigem Einsatz (Olefinanlage) beschrieben. Während der, mit einem front end Deethanizer (3) nach Rohgasverdichtung (1), Vorkühlung und Trocknung (2) beginnenden, Trennsequenz wird zuerst in eine Olefinfraktion mit höchstens zwei Kohlenstoffatomen und eine Olefinfraktion mit mindestens drei Kohlenstoffatomen getrennt. Die Fraktion mit mindestens drei Kohlenstoffatomen wird zur weiteren Trennsequenz für längerkettige Olefine geführt (4). Die Fraktion mit höchstens zwei Kohlenstoffatomen wird über eine zwischengeschaltete katalytische Hydrierungsstufe (5) zur Tieftemperaturtrennungsstufe (6) geführt, die drei Kondensationsstufen im Temperaturbereich von -50°C bis -100°C umfasst. Aus der Tieftemperaturtrennungsstufe werden gasförmiger Wasserstoff (9) und Methan (10) abgeleitet, während die Olefine mit höchstens zwei Kohlenstoffatomen zu einer weiteren Fraktionierungsstufe geführt werden (7). Die Kälteleistung für die Tieftemperaturtrennungsstufe wird durch die Verdampfung eines Teils der im front end Deethanizer entstehenden flüssigen Ethylenfraktion (8) über Wärmetauschern zur Verfügung gestellt. Die verdampfte Ethylenfraktion wird zur Rohgasverdichtung zurückgeführt (11). The invention relates to a process for the supply of a cryogenic separation stage in a plant for the production of olefins from hydrocarbon-containing feedstock (olefin plant). During the separation sequence beginning with a front end deethanizer (3) after crude gas compression (1), pre-cooling and drying (2), first an olefin fraction having at most two carbon atoms and an olefin fraction having at least three carbon atoms are separated. The fraction with at least three carbon atoms is led to the further separation sequence for longer-chain olefins (4). The fraction of at most two carbon atoms is passed through an intermediate catalytic hydrogenation ...

Recovery of propylene and ethylene from offgases

A system and process for the recovery of ethylene and propylene from a gas stream, such as a refinery offgas stream. The process comprises withdrawing, cooling, and recovering an overhead vapor stream from a single distillation column (20). The process includes withdrawing a liquid C3+, C4+, C5+ or C6+ bottoms product stream (4) and recycling (5) a portion of the bottoms stream (4) to maintain an overhead column condenser (28) at temperature refrigeration levels of above -140 °F and withdrawing a vapor side stream rich in propylene or ethylene-propylene.

Integrated olefin recovery process

Methods and apparatus for the integration of a fractionation process and an olefin refrigeration system, wherein the fractionation process olefin effluent is supplied to the refrigeration system, can eliminate a fractionation process condenser and reflux drum typically present. A plurality of bottoms streams can be collected from the fractionation process. The olefin refrigerant can be supplied to alternate olefin refrigerant consumers, as desired. A column in the fractionation process can be refluxed with an olefin stream from refrigeration system, and olefin product can be collected or exported via line.

Integrated olefin recovery process

Methods and apparatus for the integration of a fractionation process and an olefin refrigeration system, wherein the fractionation process olefin effluent is supplied to the refrigeration system, can eliminate a fractionation process condenser and reflux drum typically present. A plurality of bottoms streams can be collected from the fractionation process. The olefin refrigerant can be supplied to alternate olefin refrigerant consumers, as desired. A column in the fractionation process can be refluxed with an olefin stream from refrigeration system, and olefin product can be collected or exported via line.

Reducing refrigeration and dehydration load for a feed stream entering a cryogenic distillation process

A system for conditioning a sour gas feed stream for a cryogenic distillation tower. A dehydration unit separates the sour gas feed stream into a first stream including water and a feed stream. A sequential cooling assembly is coupled to both the dehydration unit and the cryogenic distillation tower. The sequential cooling assembly includes: a first stage that separates the feed stream into a partially cooled feed stream and a second stream including acid gas; a second stage that cools the partially cooled feed stream into a cooled feed stream and a third stream including acid gas; and a cooled feed stream header coupled to a cryogenic distillation tower feed inlet. The first stage, the second stage, or both send at least one of the second and third streams to a bottom section of the cryogenic distillation tower.

Hydrocarbon Gas Processing

A process and an apparatus are disclosed for the recovery of ethane, ethylene, propane, propylene, and heavier hydrocarbon components from a hydrocarbon gas stream. The stream is cooled and divided into first and second streams. The first stream is further cooled to condense substantially all of it and divided into first and second portions. The first and second portions are expanded to the fractionation tower pressure and supplied to the fractionation tower at upper mid-column feed positions, with the expanded second portion being heated before it enters the tower. The second stream is expanded to the tower pressure and supplied to the column at a mid-column feed position. A distillation vapor stream is withdrawn from the column above the feed point of the second stream, combined with a portion of the tower overhead vapor stream, compressed to higher pressure, and directed into heat exchange relation with the remaining tower overhead vapor stream and the expanded second portion to cool the compressed combined vapor stream and condense at least a part of it, forming a condensed stream. At least a portion of the condensed stream is expanded to the tower pressure and directed to the fractionation tower as its top feed. The quantities and temperatures of the feeds to the fractionation tower are effective to maintain the overhead temperature of the fractionation tower at a temperature whereby the major portion of the desired components is recovered.

Hydrocarbon gas processing featuring a compressed reflux stream formed by combining a portion of column residue gas with a distillation vapor stream withdrawn from the side of the column

A process and an apparatus are disclosed for the recovery of ethane, ethylene, propane, propylene, and heavier hydrocarbon components from a hydrocarbon gas stream. The stream is cooled and divided into first and second streams. The first stream is further cooled to condense substantially all of it and divided into first and second portions. The first and second portions are expanded to the fractionation tower pressure and supplied to the fractionation tower at upper mid-column feed positions, with the expanded second portion being heated before it enters the tower. The second stream is expanded to the tower pressure and supplied to the column at a mid-column feed position. A distillation vapor stream is withdrawn from the column above the feed point of the second stream, combined with a portion of the tower overhead vapor stream, compressed to higher pressure, and directed into heat exchange relation with the remaining tower overhead vapor stream and the expanded second portion to cool the compressed combined vapor stream and condense at least a part of it, forming a condensed stream. At least a portion of the condensed stream is expanded to the tower pressure and directed to the fractionation tower as its top feed. The quantities and temperatures of the feeds to the fractionation tower are effective to maintain the overhead temperature of the fractionation tower at a temperature whereby the major portion of the desired components is recovered.

Hydrocarbon Gas Processing

A process and an apparatus are disclosed for the recovery of ethane, ethylene, propane, propylene, and heavier hydrocarbon components from a hydrocarbon gas stream. The stream is cooled and divided into first and second streams. The first stream is further cooled to condense substantially all of it and is thereafter expanded to the fractionation tower pressure and supplied to the fractionation tower at an upper mid-column feed position. The second stream is expanded to the tower pressure and supplied to the column at a mid-column feed position. A distillation vapor stream is withdrawn from the column above the feed point of the first stream, combined with a portion of the tower overhead vapor stream, compressed to higher pressure, and directed into heat exchange relation with the remaining tower overhead vapor stream to cool the compressed combined vapor stream and condense at least a part of it, forming a condensed stream. At least a portion of the condensed stream is expanded to the tower pressure and directed to the fractionation tower as its top feed. The quantities and temperatures of the feeds to the fractionation tower are effective to maintain the overhead temperature of the fractionation tower at a temperature whereby the major portion of the desired components is recovered.

METHOD FOR DETERMINING C (DOWN ARROW) 3 (DOWN ARROW) (DOWN ARROW) + (DOWN ARROW) HYDROCARBONS

System and process for the recovery of propylene and ethylene from refinery offgases

A system and process for the recovery of ethylene and propylene from a gas stream, such as a refinery offgas stream. The process comprises withdrawing, cooling, and recovering an overhead vapor stream from a single distillation column (20). The process includes withdrawing a liquid C3+, C4+, C5+ or C6+ bottoms product stream (4) and recycling (5) a portion of the bottoms stream (4) to maintain an overhead column condenser (28) at temperature refrigeration levels of above -140 °F and withdrawing a vapor side stream rich in propylene or ethylene-propylene.

Integrated olefin recovery process

분류 공정 올레핀 유출물이 냉각 시스템으로 공급되는 분류 공정과 올레핀 냉각 시스템의 통합을 위한 장치 및 방법은 통상의 분류 공정 응축기 및 환류 드럼을 제거할 수 있다. 바닥 스트림의 다수는 분류 공정으로부터 수집될 수 있다. 올레핀 냉매는 필요하면 대체 올레핀 냉매 소비기에 공급될 수 있다. 분류 공정에서 칼럼은 냉각 시스템으로부터 올레핀 스트림이 환류될 수 있으며, 올레핀 제품은 라인을 통하여 배출 혹은 수집될 수 있다. Classification Process The apparatus and method for the integration of the olefin cooling system with the fractionation process in which the olefin effluent is fed to the cooling system can remove the conventional fractionation process condenser and reflux drum. Many of the bottom streams can be collected from the fractionation process. The olefinic refrigerant can be fed to a replacement olefin refrigerant consumer if desired. In the fractionation process, the column may reflux the olefin stream from the cooling system and the olefin product may be discharged or collected through the line.

Method and system for cooling and separating hydrocarbon flow

FIELD: cooling; chemical or physical processes. SUBSTANCE: present invention relates to a method of cooling and separating hydrocarbon flow. Flow of hydrocarbon material (7) is passed through the first stage of cooling and separation to produce upper stream of steam enriched with methane (110), and flow of lean liquid to methane of liquid (10). Flow of lean liquid to methane (10) is passed to fractionation column (200) to obtain bottom condensate flow (210), upper stream enriched with C 1 -C 2 (220) and average flow enriched with C 3 -C 4 (230). Upper part of fractionation column (201) is cooled with condenser (206). Split flow (112) is obtained from upper stream of steam enriched with methane (110), cooled split flow (112') by cooling by expansion of volume of split flow (112). Cooling capacity is provided in upper part of fractionation column (201) by means of cooled split flow (112'). EFFECT: technical result is increased compactness and reduced weight of structure. 14 cl, 3 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 720 732 C1 (51) МПК F25J 3/02 (2006.01) F25J 1/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК F25J 1/0022 (2020.02); F25J 1/0035 (2020.02); F25J 1/0042 (2020.02); F25J 1/0045 (2020.02); F25J 1/0052 (2020.02); F25J 1/0055 (2020.02); F25J 1/0205 (2020.02); F25J 1/0214 (2020.02); F25J 1/0216 (2020.02); F25J 1/0216 (2020.02); F25J 1/0231 (2020.02); F25J 1/0237 (2020.02); F25J 1/0239 (2020.02); F25J 1/0255 (2020.02); F25J 1/0262 (2020.02); F25J 3/0209 (2020.02); F25J 3/0233 (2020.02); F25J 3/0242 (2020.02); F25J 3/0247 (2020.02); F25J 3/061 (2020.02); F25J 3/0635 (2020.02) 2018104986, 08.07.2016 (24) Дата начала отсчета срока действия патента: 08.07.2016 (73) Патентообладатель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) 13.05.2020 Приоритет(ы): (30) Конвенционный приоритет: (56) Список документов, цитированных в отчете о поиске: US 2009107174 A1, 30.04.2009. US 5453559 A, 26.09 ...

System and method for separating gas condensate liquid and nitrogen from natural gas streams

FIELD: gas industry. SUBSTANCE: system and method for removing nitrogen and producing a high-pressure methane product stream and NGL product stream from natural gas feed streams are proposed, where at least 90% of ethane and preferably at least 95% of ethane in the feed stream are extracted into NGL product stream. The system and method of the invention are particularly suitable for use with supply flows over 5 million cubic feet/day (0.1 million m 3 /day) and up to 300 million cubic feet/day (8.5 million m 3 /day) and containing from about 5% to 80% of nitrogen. The system and method preferably combine the use of strategic heat exchange between various technological flows with a high-pressure distillation column and a capability of diverting all or part of the supply flow to a nitrogen removal plant with an optional bypass of a nitrogen fractionation column to reduce capital costs and operating costs. EFFECT: removing nitrogen and producing a high-pressure methane product stream and NGL product stream from natural gas feed streams. 63 cl, 5 dwg, 2 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 766 161 C2 (51) МПК F25J 3/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК F25J 3/0209 (2021.08); F25J 3/0233 (2021.08); F25J 3/0238 (2021.08); F25J 5/005 (2021.08) (21)(22) Заявка: 2019128836, 02.02.2018 (24) Дата начала отсчета срока действия патента: (73) Патентообладатель(и): БАТТС ПРОПЕРТИЗ, ЛТД. (US) Дата регистрации: 08.02.2022 Приоритет(ы): (30) Конвенционный приоритет: 15.02.2017 US 15/433,375 (43) Дата публикации заявки: 16.03.2021 Бюл. № 8 (45) Опубликовано: 08.02.2022 Бюл. № 4 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 16.09.2019 2 7 6 6 1 6 1 (56) Список документов, цитированных в отчете о поиске: US 4331461 A, 25.05.1982. RU 128924 U1, 10.06.2013. US 2014/182331 A1, 03.07.2014. US 2012/324943 A1, 27.12.2012. US 4948405 A, 14.08.1990. R U 02.02.2018 (72) Автор(ы): БАТТС, Рэйберн, К. ...

Patent RU2019128836A3

ВИ“? 2019128836” АЗ Дата публикации: 19.07.2021 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 2019128836/12(056693) 02.02.2018 РСТЛО52018/016561 02.02.2018 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. 15/433,375 15.02.2017 05 Название изобретения (полезной модели): [Х] - как заявлено; [ ] - уточненное (см. Примечания) СИСТЕМА И СПОСОБ ДЛЯ ОТДЕЛЕНИЯ ГАЗОКОНДЕНСАТНОЙ ЖИДКОСТИ И АЗОТА ИЗ ПОТОКОВ ПРИРОДНОГО ГАЗА Заявитель: БАТТС ПРОПЕРТИЗ, ЛТД., 0$ 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 3/02 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) Е257 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): 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$ 4331461 А (РНПЛАР РЕТКОГЕОМ ...

Система и способ для отделения газоконденсатной жидкости и азота из потоков природного газа

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2019 128 836 A (51) МПК F25J 3/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2019128836, 02.02.2018 (71) Заявитель(и): БАТТС ПРОПЕРТИЗ, ЛТД. (US) Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): БАТТС, Рэйберн, К. (US) 15.02.2017 US 15/433,375 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 16.09.2019 R U (43) Дата публикации заявки: 16.03.2021 Бюл. № 8 (86) Заявка PCT: (87) Публикация заявки PCT: WO 2018/151954 (23.08.2018) A 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 удаления азота из сырьевого потока, содержащего азот, метан, этан и другие компоненты, с образованием потока метанового продукта и потока NGLпродукта, причем система включает в себя: первый сепаратор, в котором сырьевой поток разделяется на первый головной поток и первый кубовый поток; первую фракционирующую колонну, в которой первый головной поток разделяется на второй головной поток и второй кубовый поток; детандер для расширения первого головного потока перед первой фракционирующей колонной; вторую фракционирующую колонну, в которой второй кубовый поток разделяется на третий головной поток и третий кубовый поток; третью фракционирующую колонну, в которой первый поток подачи NRU и второй поток подачи NRU разделяются на четвертый головной поток и четвертый кубовый поток; первый теплообменник для охлаждения первой части потока подачи перед первым сепаратором и охлаждения первой части второго головного потока перед третьей фракционирующей колонной посредством теплообмена с четвертым кубовым потоком и рециркулирующим потоком хладагента; Стр.: 1 A 2 0 1 9 1 2 8 8 3 6 (54) СИСТЕМА И СПОСОБ ДЛЯ ОТДЕЛЕНИЯ ГАЗОКОНДЕНСАТНОЙ ЖИДКОСТИ И АЗОТА ИЗ ПОТОКОВ ПРИРОДНОГО ГАЗА 2 0 1 9 1 2 8 8 3 6 US 2018/016561 (02.02.2018) A 2 0 1 9 1 2 8 8 3 6 A R U 2 0 1 9 1 2 8 8 3 6 Стр.: ...

중압 극저온 공기 분리 유닛으로부터의 질소 및 아르곤의 고 회수율을 위한 시스템 및 방법

아르곤의 최대 약 96% 회수율 및 98% 이상의 전체 질소 회수율을 제공하는 중압 공기 분리 유닛 및 공기 분리 사이클이 개시된다. 공기 분리는 아르곤 응축기 내에서 아르곤을 응축시키기 위한 냉매로서 사용되는 고 순도 산소 부화 스트림을 생성하도록 구성되며, 이때 생성되는 기화된 산소 스트림은 온도 스윙 흡착 사전정화기 유닛을 재생하는 데 사용된다. 아르곤 회수가 아르곤 슈퍼스테이지식 칼럼의 사용에 의해 용이해진다.

用于从中压低温空气分离单元实现氮和氩的高回收率的系统和方法

本发明公开了一种中压空气分离单元和空气分离循环，该中压空气分离单元和空气分离循环提供最多至约96％的氩回收率和98％或更大的总氮回收率。该空气分离被构造为产生高纯度富氧流，该高纯度富氧流用作制冷剂以在氩冷凝器中冷凝氩，并且所得气化的氧流用于再生变温吸附预纯化器单元。使用氩超级塔来促进氩回收。

分离含烃气态混合物的方法

本发明涉及用于处理含烃气态混合物的技术，并且特别是涉及气体组分的低温分离，并且本发明可以被用于处理油井气体或天然气。技术结果包括减少目标组分的损失和增加方法的效率。

질소 생성 극저온 공기 분리 유닛으로부터의 아르곤 및 산소의 향상된 회수율을 위한 시스템 및 방법

아르곤의 최대 약 96% 회수율, 98 퍼센트 이상의 전체 질소 회수율 및 제한된 기체 산소 생성을 제공하는 중압 공기 분리 유닛 및 공기 분리 사이클이 개시된다. 공기 분리는 저압 칼럼으로부터 제1 고 순도 산소 부화 스트림 및 제2 보다 낮은 순도의 산소 부화 스트림을 생성하도록 구성되고, 그 중 하나가 아르곤 응축기 내에서 아르곤을 응축시키기 위한 냉매로서 사용되며, 이때 생성되는 기화된 산소 스트림은 온도 스윙 흡착 사전-정화기 유닛을 재생하는 데 사용된다. 제1 고 순도 산소 부화 스트림의 전부 또는 일부분이 기체 산소 생성물을 생성하도록 주 열 교환기 내에서 기화된다.

超高纯度氮气和氧化发生器装置

本发明提供了一种以空气作为原料同时生产超高纯度氮气和超高纯度氧气的装置。将原料气加入第一蒸馏柱6的底部15,从上部蒸馏部分12和中部蒸馏部分13之间回收超高纯度液氮,从中部蒸馏部分13和下部蒸馏部分14之间回收没有高沸点组分的液体空气,将在底部15中收集的富氧液体空气通过膨胀阀31降压,然后将其送入氮气冷却器8作为冷却剂。在通过膨胀阀33降低所述的液体空气部分的压力后,将其送入第二蒸馏柱7,在此,从顶部21分离低沸点组分并从底部23回收超高纯度液氧。通过膨胀阀32对所述液体空气剩余部分降压,然后将其送入氮气冷却器作为冷却剂部分。因此,调节了流过下部蒸馏部分14的回流液的量并调节了加入第二蒸馏柱7的所述液体空气的量。

탄화수소 가스 처리

탄화수소 가스 스트림으로부터 에탄, 에틸렌 및 그보다 무거운 탄화수소 성분을 회수하는 방법 및 장치가 개시된다. 스트림은 냉각되고 저압으로 팽창되며 중간 칼럼 공급 위치에서 제1 분류탑에 공급된다. 증류 액체 스트림은 팽창된 스트림의 공급 위치 아래의 제1 분류탑으로부터 취출되어 가열되며, 제2 분류탑으로 유도되어 공중 증기 스트림과 바닥 액체 스트림을 생성한다. 공중 증기 스트림은 냉각되어 응축되며, 응축된 스트림의 일부는 상부 공급원으로서 제2 분류탑으로 유도되며 나머지는 하측 칼럼 공급 위치에서 제1 분류탑으로 유도된다. 제2 분류탑으로부터의 바닥 액체 스트림은 냉각되어 상부 공급원으로서 제1 분류탑으로 유도된다.

带有混合塔和氪-氙回收装置的空气分馏工艺及设备

本发明所涉及的工艺和设备用于氮－氧分离用分馏塔系统(5，6)中的空气低温分馏。第一加压空气流(4)被导入到氮－氧分离用分馏塔系统。来自氮－氧分离用分馏塔系统的富氧馏分(22)以液态形式被加压(23)并被加入(25)到混合塔(26)中。热交换介质流，特别是第二加压空气流(43，343)，被导入混合塔(26)的下方区域并与富氧馏分(22，25)逆流接触。气态顶部产品(260)在混合塔(26)的上方区域获得。来自混合塔(26)下方或中部区域的液体(38，39，40，41)被导入氮－氧分离用分馏塔系统。来自氮－氧分离用分馏塔系统的含氪和氙的氧气流被导入氪－氙浓缩塔(36)。富氪和氙的馏分(51)在氪－氙浓缩塔(36)中获得。混合塔(26)中的气态顶部产品(260)被导入辅助塔(27)，并在其上方区域获得除去氪和氙的顶部馏分(28)。

联合生产氨合成混合物和一氧化碳的方法和设备

本发明涉及一种生产氨合成混合物和一氧化碳的方法。在氮清洗塔(61)中提纯氢。在中压汽提塔(62)中，然后在低压蒸馏塔(63)中，从在所述氮清洗塔(61)底部收集的第一种液体馏分(51)中低温回收一氧化碳。从洗涤塔(61)的顶部和底部之间的中间位置排出第二种液体馏分(52)。

질소 생성 극저온 공기 분리 유닛으로부터의 아르곤 및 산소의 향상된 회수율을 위한 시스템 및 방법

아르곤의 최대 약 96% 회수율, 98 퍼센트 이상의 전체 질소 회수율 및 제한된 기체 산소 생성을 제공하는 중압 공기 분리 유닛 및 공기 분리 사이클이 개시된다. 공기 분리는 저압 칼럼으로부터 제1 고 순도 산소 부화 스트림 및 제2 보다 낮은 순도의 산소 부화 스트림을 생성하도록 구성되고, 그 중 하나가 아르곤 응축기 내에서 아르곤을 응축시키기 위한 냉매로서 사용되며, 이때 생성되는 기화된 산소 스트림은 온도 스윙 흡착 사전-정화기 유닛을 재생하는 데 사용된다. 제1 고 순도 산소 부화 스트림의 전부 또는 일부분이 기체 산소 생성물을 생성하도록 주 열 교환기 내에서 기화된다.

空气的分离方法和装置

一种分离空气的方法和装置,其中,一含气相的氧气流从一单塔氮发生器中去出,然后被分成两个分流。这两个分流被冷凝,然后再相混合而在一汽提塔内进行汽提,以在塔底产生超高纯液氧。两个分流中的一个在一再沸器内和汽提塔的底部区域冷凝。两个分流中的另一个在一与氮汽提塔共同使用的塔顶冷凝器中冷凝。

整合的烯烃回收过程

用于将分馏过程和烯烃制冷系统整合的方法和设备能够省去典型地存在的分馏过程冷凝器和回流罐，其中将分馏过程烯烃流出物供给到制冷系统。能够从分馏过程收集多个底部流。烯烃制冷剂能够如希望地供给到可替代的烯烃制冷剂消耗器。分馏过程中来自制冷系统的烯烃流能够回流到柱，且烯烃产品能够通过管线收集或输出。

减少进入低温蒸馏过程的进料物流的冷冻和脱水负荷

调节低温蒸馏塔用酸性气体进料物流的系统，包含脱水单元，设置其以将酸性气体进料物流分离成包含水的第一物流以及进料物流；以及与该脱水单元以及该低温蒸馏塔二者连接的顺序冷却组合体，其中该顺序冷却组合体包含第一级，设置其以将进料物流分离成部分冷却的进料物流以及包含酸性气体的第二物流，第二级，设置其以将部分冷却的进料物流冷却成为冷却的进料物流以及包含酸性气体的第三物流，以及冷却的进料物流集管，其与低温蒸馏塔进料口连接，其中设置第一级、第二级、或者二者以输送第二以及第三物流至少之一至低温蒸馏塔的底部区域。

Patent RU2016147701A3

`7ВУ’” 2016147701`” АЗ Дата публикации: 14.04.2020 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 201614'7701/12(076628) 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. 15003483.3 07.12.2015 ЕР* Название изобретения (полезной модели): [Х] - как заявлено; [ ] - уточненное (см. Примечания) СПОСОБ ПОЛУЧЕНИЯ ЖИДКОГО И ГАЗООБРАЗНОГО, ОБОГАЩЕННОГО КИСЛОРОДОМ ПРОДУКТА РАЗДЕЛЕНИЯ ВОЗДУХА В УСТАНОВКЕ РАЗДЕЛЕНИЯ ВОЗДУХА И УСТАНОВКА РАЗДЕЛЕНИЯ ВОЗДУХА Заявитель: ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ, 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.] 3/04 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) 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, РАТЕМТСОРЕ, Рабеагсв, КОРТО 6. ДОКУМЕНТЫ, ОТНОСЯЩИЕСЯ К ПРЕДМЕТУ ПОИСКА Кате- Наименование документа с указанием (где необходимо) частей, Относится к гория* относящихся к ...

冷供应至烯烃装置的低温分离阶段的方法

本发明描述了在从含有烃类的进料制造烯烃的装置(烯烃装置)中的低温分离阶段的制冷供应的方法。在分离顺序中，首先分离成具有最多两个碳原子的馏份及具有至少三个碳原子的馏份。将具有至少三个碳原子的馏份送至长链烯烃的其他分离顺序(4)。将具有最多两个碳原子的馏份经过催化氢化阶段(5)送至包括在－50℃至－100℃的温度范围内的三个冷凝阶段的低温分离阶段(6)。从低温分离阶段抽取气态的氢(9)及甲烷(10)，同时将具有最多两个碳原子的烯烃送至其他的分馏阶段(7)。通过一部分来自前端乙烷馏除塔(3)的液体乙烯馏份(8)的蒸发经过热交换器提供低温分离阶段的制冷功率。将蒸发的乙烯馏份再循环至原料气体压缩机。

处理合成气和相关气体的方法和装置

公开了一种改进的甲烷洗涤循环,其中需要少量的甲烷洗涤,由此节省了该循环操作的能量成本和建设该循环的投资成本。另外的实施方式可回收能量,并且提高一氧化碳和/或氢气产品的分离。

Method and device for inert gas and oxygen production by cryogenic air distillation

Изобретение относится к способу и установке для производства инертных газов и кислорода посредством криогенной перегонки воздуха. Способ производства инертных газов и кислорода посредством перегонки в системе колонн, содержащей, по меньшей мере, одну колонну среднего давления, одну колонну низкого давления и одну вспомогательную колонну, состоит из следующих стадий: отводят выпуск промежуточного потока с промежуточного уровня колонны среднего давления и перемещают его в колонну низкого давления; отводят выпуск потока из колонны среднего давления, который обогащен кислородом по отношению к выпуску промежуточного потока, и перемещают его в резервуар вспомогательной колонны; отводят выпуск богатого азотом потока из верхней части колонны низкого давления; отводят выпуск потока жидкости, богатого кислородом, из резервуара колонны низкого давления как продукт, чтобы образовать газообразный продукт; и отводят выпуск потока жидкости, обогащенного кислородом, из вспомогательной колонны, который также обогащен криптоном и ксеноном по отношению к выпуску второго обогащенного кислородом потока, и перемещают выпуск потока жидкости, содержащий, по меньшей мере, 78 мол.% азота, в виде флегмы во вспомогательную колонну. Использование изобретения позволит повысить выход криптона и ксенона. 2 н. и 10 з.п. ф-лы, 9 ил. ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß RU (19) (11) 2 319 084 (13) C2 (51) ÌÏÊ F25J 3/04 (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÎÏÈÑÀÍÈÅ ÈÇÎÁÐÅÒÅÍÈß Ê ÏÀÒÅÍÒÓ (21), (22) Çà âêà: 2005109412/06, 30.07.2003 (72) Àâòîð(û): ÆÀÓÀÍÈ Ëàçàä (FR), ÆÞÄÀ Ôðåäåðèê (FR), ÑÎËÍÜÅ Áåðíàð (FR) (24) Äàòà íà÷àëà îòñ÷åòà ñðîêà äåéñòâè ïàòåíòà: 30.07.2003 (73) Ïàòåíòîîáëàäàòåëü(è): Ë`ÝÐ ËÈÊÈÄ, ÑÎÑÜÅÒÅ ÀÍÎÍÈÌ À ÄÈÐÅÊÒÓÀÐ Ý ÊÎÍÑÅÉ ÄÅ ÑÞÐÂÅÉßÍÑ ÏÓÐ Ë`ÝÒÞÄ Ý Ë`ÝÊÑÏËÓÀÒÀÑÜÎÍ ÄÅ ÏÐÎÑÅÄÅ ÆÎÐÆ ÊËÎÄ (FR) (43) Äàòà ïóáëèêàöèè çà âêè: 10.10.2005 (45) Îïóáëèêîâàíî: 10.03.2008 Áþë. ¹ 7 2 3 1 9 0 8 4 (56) Ñïèñîê äîêóìåíòîâ, öèòèðîâàííûõ â îò÷åòå î ïîèñêå: DE 2605305 ...

Process and plant for production of carbon monoxide and hydrogen

在本发明的方法中，通过在热交换器(310)中部分冷凝从分离罐(320)底部回收的冷凝馏分(322)生产一氧化碳，不纯氢(321)在罐(320)顶部产生并通过在塔(350)内用氮清洗而提纯。由在上述塔顶收集的氢气流(353)生产氨合成混合物。从在氮清洗塔(350)底部收集的馏分(351)中进一步生产一氧化碳。所有塔和交换器均在一个单一的冷却箱(400)内。

Hydrocarbon gas processing

公开了从烃气流中回收乙烷、乙烯和重烃组分的工艺和设备。所述流被冷却、膨胀至较低压力，并且被供应至第一分馏塔的塔中部进料位置。从所述第一分馏塔的低于所述膨胀流的进料位置抽取蒸馏液体流，加热并且引导进入产生顶部蒸气流和底部液体流的第二分馏塔。冷却所述顶部蒸气流以使它冷凝，其中冷凝流的一部分被引导至第二分馏塔以作为其顶部进料，而剩余部分被引导至第一分馏塔的塔下部进料位置。来自第二分馏塔的底部液体流被冷却并引导至第一分馏塔以作为其顶部进料。

Hydrocarbon gas processing

公开了从烃气流中回收乙烷、乙烯和重烃组分的工艺和设备。所述流被冷却、膨胀至较低压力，并且被供应至第一分馏塔的塔中部进料位置。从所述第一分馏塔的低于所述膨胀流的进料位置抽取蒸馏液体流，加热并且引导进入产生顶部蒸气流和底部液体流的第二分馏塔。冷却所述顶部蒸气流以使它冷凝，其中冷凝流的一部分被引导至第二分馏塔以作为其顶部进料，而剩余部分被引导至第一分馏塔的塔下部进料位置。来自第二分馏塔的底部液体流被冷却并引导至第一分馏塔以作为其顶部进料。

METHOD AND INSTALLATION FOR OBTAINING CARBON MONOXIDE BY PARTIAL CONDENSATION

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2020 127 582 A (51) МПК F25J 3/02 (2006.01) C01B 3/02 (2006.01) C01B 32/40 (2017.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2020127582, 19.08.2020 (71) Заявитель(и): Л'ЭР ЛИКИД СОСЬЕТЕ АНОНИМ ПУР Л'ЭТЮД Э Л'ЭКСПЛУАТАСЬОН ДЕ ПРОСЕДЕ ЖОРЖ КЛОД (FR) Приоритет(ы): (30) Конвенционный приоритет: 20.08.2019 FR 19 09300 (72) Автор(ы): ЭРНАНДЕС, Антуан (FR) Адрес для переписки: 129090, Москва, ул. Большая Спасская, д. 25, строение 3, ООО "Юридическая фирма Городисский и Партнеры" Стр.: 1 A 2 0 2 0 1 2 7 5 8 2 R U A (57) Формула изобретения 1. Способ разделения смеси водорода, метана и моноксида углерода (1, 5, 7) криогенной дистилляцией в системе колонн, содержащей первую колонну и вторую колонну, при этом в указанном способе: i. смесь охлаждают в первом теплообменнике (3, 9), и по меньшей мере одну ее часть подвергают частичной конденсации в по меньшей мере одном втором теплообменнике (11, 13), который представляет собой кубовый ребойлер второй колонны (К1, К2) из системы колонн, и по меньшей мере одну часть жидкости (17, 67), полученной частичной конденсацией, или жидкость (23, 75), полученную из данной жидкости (67) посредством по меньшей мере одного этапа частичной конденсации, направляют к промежуточному уровню первой колонны (К1), при этом только данную по меньшей мере одну часть смеси и кубовую жидкость (21) из второй колонны подвергают теплообмену во втором теплообменнике, при этом испарившуюся кубовую жидкость направляют обратно в колонну, в которой она образуется; ii. обогащенный водородом, верхний газ (39) отводят из первой колонны и подогревают в первом теплообменнике; iii. жидкость (25, 27, 29), обогащенную моноксидом углерода и метаном, отводят из нижней части первой колонны (К1), и ее направляют к по меньшей мере одному промежуточному уровню второй колонны (К2); iv. жидкость (23), обогащенную метаном, отводят из нижней части второй колонны, и текучую среду, ...

Method and system for cold air separation

본 발명은 제1 컬럼(11), 제2 컬럼(12), 제3 컬럼(13) 및 제4 컬럼(14)을 갖는 컬럼 시스템(10)을 가진 공기 분리 시스템(100 내지 500)이 사용되는, 저온 공기 분리를 위한 방법으로서, 제1 컬럼(11)으로부터의 유체가 적어도 제2 컬럼(12) 내로 공급되고, 제2 컬럼(12)으로부터의 유체가 적어도 제3 컬럼(13) 내로 공급되고, 제3 컬럼(13)으로부터의 유체가 적어도 제4 컬럼(14) 내로 공급되고, 제4 컬럼(14)으로부터의 유체가 적어도 제3 컬럼(13) 내로 공급되고, 제3 컬럼(13)으로부터 제4 컬럼(14) 내로 공급되는 유체는, 제3 컬럼(13)으로부터 인출되고 제3 섬프 액체보다 더 낮은 산소 함량 및 더 높은 아르곤 함량을 갖는 사이드 유동의 적어도 일부를 포함하는, 저온 공기 분리를 위한 방법에 관한 것이다. 본 발명에 따르면, 귀환 액체가 제1 컬럼(11)으로부터의 헤드 가스를 응축시킴으로써 형성되고, 다시 제1 컬럼(11)으로 유동 공급된다. 제1 컬럼(11)으로부터의 헤드 가스를 응축시키기 위해, 액체 냉각 유동이 제공되고, 헤드 가스와의 간접 열교환에서 증발되거나 부분적으로 증발되고, 냉각 스트림의 증발 또는 부분 증발 동안 형성된 기체는 제2 압력 범위 내의 압력으로 팽창되어 일이 수행되고, 제2 컬럼(12) 내로 공급된다. 본 발명은 또한 대응하는 시스템(100 내지 500)에 관한 것이다.

Ultra high purity nitrogen and oxygen production equipment

METHOD AND INSTALLATION FOR THE PRODUCTION OF INERT GASES AND OXYGEN BY MEANS OF CRYOGENIC AIR DISTRIBUTION

ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß (19) RU (51) ÌÏÊ 7 (11) 2005 109 412 (13) A F 25 J 3/04 ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÇÀßÂÊÀ ÍÀ ÈÇÎÁÐÅÒÅÍÈÅ (21), (22) Çà âêà: 2005109412/06, 30.07.2003 (30) Ïðèîðèòåò: 04.09.2002 FR 02 10922 (43) Äàòà ïóáëèêàöèè çà âêè: 10.10.2005 Áþë. ¹ 28 (86) Çà âêà PCT: FR 03/02420 (30.07.2003) (72) Àâòîð(û): ÆÀÓÀÍÈ Ëàçàä (FR), ÆÞÄÀ Ôðåäåðèê (FR), ÑÎËÍÜÅ Áåðíàð (FR) R U (87) Ïóáëèêàöè PCT: WO 2004/023054 (18.03.2004) (74) Ïàòåíòíûé ïîâåðåííûé: Åãîðîâà Ãàëèíà Áîðèñîâíà 2 0 0 5 1 0 9 4 1 2 (85) Äàòà ïåðåâîäà çà âêè PCT íà íàöèîíàëüíóþ ôàçó: 04.04.2005 (71) Çà âèòåëü(è): Ë`ÝÐ ËÈÊÈÄ, ÑÎÑÒÜÅÒÅ ÀÍÎÍÈÌ À ÄÈÐÅÊÒÓÀÐ Ý ÊÎÍÑÅÉ ÄÅ ÑÞÐÂÅÉßÍÑ ÏÓÐ Ë`ÝÒÞÄ Ý Ë`ÝÊÑÏËÓÀÒÀÑÜÎÍ ÄÅ ÏÐÎÑÅÄÅ ÆÎÐÆ ÊËÎÄ (FR) Àäðåñ äë ïåðåïèñêè: 129010, Ìîñêâà, óë. Á.Ñïàññêà , 25, ñòð.3, ÎÎÎ "Þðèäè÷åñêà ôèðìà Ãîðîäèññêèé è Ïàðòíåðû", ïàò.ïîâ. Ã.Á. Åãîðîâîé R U Ôîðìóëà èçîáðåòåíè 1. Ñïîñîá ïðîèçâîäñòâà êèñëîðîäà è èíåðòíûõ ãàçîâ ïîñðåäñòâîì ïåðåãîíêè â ñèñòåìå êîëîíí, ñîäåðæàùåé, ïî ìåíüøåé ìåðå, îäíó êîëîííó (Ê01) ñðåäíåãî äàâëåíè , îäíó êîëîííó (Ê02) íèçêîãî äàâëåíè è, ïî ìåíüøåé ìåðå, îäíó âñïîìîãàòåëüíóþ êîëîííó (Ê05), ïðè÷åì â ýòîì ñïîñîáå i) ïî ìåíüøåé ìåðå, îäèí ïîòîê îõëàæäåííîãî è î÷èùåííîãî âîçäóõà (1) íàïðàâë þò â êîëîííó ñðåäíåãî äàâëåíè , â êîòîðîé åãî ðàçäåë þò; ii) ïî ìåíüøåé ìåðå, ïåðâûé îáîãàùåííûé àçîòîì ïîòîê (11) îòâîä ò èç êîëîííû ñðåäíåãî äàâëåíè , è, ïî ìåíüøåé ìåðå, îäíó ÷àñòü ýòîãî ïîòîêà íàïðàâë þò, íàïð ìóþ èëè íå íàïð ìóþ, â êîëîííó íèçêîãî äàâëåíè ; iii) ïðîìåæóòî÷íûé ïîòîê (ÁÆ1) îòâîä ò ñ ïðîìåæóòî÷íîãî óðîâí êîëîííû ñðåäíåãî äàâëåíè ; iv) ïîòîê (ÁÆ2), îáîãàùåííûé êèñëîðîäîì ïî îòíîøåíèþ ê ïðîìåæóòî÷íîìó ïîòîêó, îòâîä ò èç íèæíåé ÷àñòè êîëîííû ñðåäíåãî äàâëåíè è íàïðàâë þò â íèæíþþ ÷àñòü âñïîìîãàòåëüíîé êîëîííû; v) áîãàòûé àçîòîì ïîòîê (ÎÀ2) îòâîä ò èç âåðõíåé ÷àñòè êîëîííû íèçêîãî äàâëåíè ; vi) áîãàòûé êèñëîðîäîì ïîòîê æèäêîñòè (ÆÊ) îòâîä ò èç êîëîííû íèçêîãî äàâëåíè â âèäå ïðîäóêòà, íåîá çàòåëüíî ïîñëå ñòàäèè ...

Method to separate air into components by cryogenic distillation

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 ...

The method and apparatus of High Purity Nitrogen, oxygen and liquid oxygen is produced from air by cryogenic rectification

本发明公开了一种通过低温精馏从空气中生产高纯氮、氧气和液氧的方法及设备，可以同时满足市场对氮和氧的需求，在保证产量的同时，又能实现对氮氧纯度的要求。本发明充分考虑了各方面因素以实现生产高纯氮、氧气和液氧设备的平稳、高效、低能耗的运行。

The method for separating hydrocarbonaceous gaseous mixture

本发明涉及用于处理含烃气态混合物的技术，并且特别是涉及气体组分的低温分离，并且本发明可以被用于处理油井气体或天然气。该方法包括以下阶段：a)将混合物脱水，b)将所述混合物冷却，c)使所述混合物穿过第一精馏塔(7)，用于产生富含烃类的第一料流(105)和包括溶解在CO 2 中的烃类的第二料流(106)，d)供应第一料流(105)的组分用于在喷嘴中旋转的气态流中的分离，以用于将所述组分分离成贫化比甲烷重的组分的第三料流(107)和富含所述组分的第四料流(108)，e)加热所述第三料流(107)，f)使用所述第三料流(107)的一部分作为排放气体(114)，g)将所述第三料流(107)的另一部分(115)冷却，并且将所述部分与所述第一料流(105)混合，并将产生的混合物(117)供应至阶段(d)，h)将所述第二料流(106)和所述第四料流(108)供应至第二精馏塔(12)，用于分离富含C3+烃类的第五料流(109)、富含CO 2 的第六料流(110)和富含甲烷的第七料流(111)，i)将所述第七料流(111)与初始气态混合物(101)混合，并将组分引导至阶段(a)。技术结果包括减少目标组分的损失和增加方法的效率。

Method for obtaining liquid and gaseous oxygen-enriched air products in air separation plant and air separation plant

本申请建议了低温分离空气的方法，其中使用具有主热交换器(3)和蒸馏塔系统(6，7)的空气分离设备(100)，该蒸馏塔系统包括在第一压力水平运行的高压塔(61)、在更低的第二压力水平运行的低压塔(62)以及混合塔(7)。本发明还涉及相应的空气分离设备(100)。

METHOD FOR PRODUCING LIQUID AND GAS-OXYGEN ENRICHED AIR SEPARATION PRODUCT IN INSTALLATION OF AIR SEPARATION AND INSTALLATION OF AIR SEPARATION

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2016 147 701 A (51) МПК F25J 3/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2016147701, 06.12.2016 (71) Заявитель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ (DE) Приоритет(ы): (30) Конвенционный приоритет: (72) Автор(ы): ЛАУТЕНШЛАГЕР Тобиас (DE) 07.12.2015 EP 15003483.3 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 1 R U A (57) Формула изобретения 1. Способ низкотемпературного разделения воздуха, при котором применяют установку (100) разделения воздуха с главным теплообменником (3) и системой дистилляционных колонн (6, 7), которая включает одну действующую на первом уровне давления колонну (61) высокого давления, одну действующую на втором, более низком уровне давления колонну (62) низкого давления, и смесительную колонну (7), и при котором - из колонны (62) низкого давления отводят в жидком состоянии обогащенный кислородом поток (n) с первым содержанием кислорода, и с этим первым содержанием кислорода в жидком состоянии подают в смесительную колонну (7), - кроме того, в смесительную колонну (7) подают первый поток (h) сжатого воздуха в газообразном состоянии, и пропускают в смесительной колонне (7) в противоточном режиме навстречу обогащенному кислородом потоку (n) с первым содержанием кислорода, - из головной части смесительной колонны (7) отбирают обогащенный кислородом поток (о) со вторым содержанием кислорода ниже первого содержания кислорода, и выводят из установки (100) разделения воздуха, - формируют первый поток (h) сжатого воздуха с использованием воздуха, который сжимают до исходного уровня давления свыше первого уровня давления, и после этого охлаждают до первого уровня температуры, на первом уровне температуры подводят в первую турбину (4) и расширяют в первой турбине (4), и - из установки (100) разделения воздуха, по меньшей мере частично, выводят жидкий обогащенный ...

Cryogenic system for removing acid gases from a hydrocarbon gas stream

A system for removing acid gases from a raw gas stream is provided. The system includes a cryogenic distillation tower. The cryogenic distillation tower has a controlled freezing zone that receives a cold liquid spray comprised primarily of methane. The tower receives and then separates the raw gas stream into an overhead methane gas stream and a substantially solid material comprised on carbon dioxide. The system includes a collector tray below the controlled freezing zone. The collector tray receives the substantially solid material as it is precipitated in the controlled freezing zone. The system also has a filter. The filter receives the substantially solid material and then separates it into a solid material comprised primarily of carbon dioxide, and a liquid material comprising methane. The solid material may be warmed as a liquid and sold, while the liquid material is returned to the cryogenic distillation tower.

Mixing and heat integration of melt tray liquids in a cryogenic distillation tower

A cryogenic distillation tower for separating a feed stream. The tower includes a distillation section. A controlled freeze zone section is situated above the distillation section and forms a solid from the feed stream. The controlled freeze zone section includes a spray assembly in an upper section and a melt tray assembly in a lower section. The melt tray assembly includes at least one vapor stream riser that directs the vapor from the distillation section into liquid retained by the melt tray assembly, and one or more draw-off openings positioned to permit a portion of the liquid to exit the controlled freeze zone section. The portion of the liquid indirectly exchanges heat with a heating fluid. One or more return inlets return the portion of the liquid to the melt tray assembly after it has been heated in the heat exchanger.

Process for generating and separating hydrogen-carbon monoxide mixture by cryogenic distillation

本发明涉及一种产生和分离合成气的方法，在该方法中，由给料气体产生含有低于2.3％的甲烷的合成气(15)，含有氢和一氧化碳的合成气通过至少一个处理工序净化以便产生净化的合成气，且该合成气在包括至少一个甲烷洗涤塔(29)的装置(25)中通过低温蒸馏分离以便产生富氢气体和/或富含一氧化碳的气体，该合成气在低温蒸馏分离的上游被增浓以便通过将一部分给料气体(11)不经过合成气产生单元地输送到位于合成气产生步骤下游的处理工序而获得包含超过2.3％的甲烷的合成气。

Process and apparatus for producing pressurized oxygen and krypton/xenon by low-temperature fractionation of air

본 발명은 공기의 저온 증류에 의해 가압된 산소 및 크립톤-크세논을 생성시키기 위한 방법 및 장치에 관한 것이다. 정류 시스템은 질소-산소 분리용 저압 칼럼(3) 및 크립톤-크세논 풍부 칼럼(15)을 갖는다. 압축되고 정제된 공급 공기(4)는 정류 시스템내로 도입된다. 제 1 산소 분획(11)은 저압 칼럼(3)으로부터 제거되고, 액체 상태로 압력 상승되고(12), 증발되고 기체 상태의 가압된 산소 생성물(24)로서 제거된다. 또한, 제 2 산소 분획(16)은 저압 칼럼(3)으로부터 제거되고 크립톤-크세논 풍부 칼럼(15)의 하부 또는 중심 영역내로 통과된다(18). 제 1 산소 분획(11)은 저압 칼럼(3) 바닥 위의 하나 이상의 실제단 또는 이론단에서 제거되고, 압력 상승(12) 후, 크립톤-크세논 풍부 칼럼(15)의 상부 영역내로 액체 상태로 도입된다. 크립톤 풍부 및/또는 크세논 풍부 분획(19)은 크립톤-크세논 풍부 칼럼(15)의 하부 영역으로부터 제거된다. 가압된 산소 생성물(24)은 크립톤-크세논 풍부 칼럼(15)의 상부 영역으로부터 기체 상태로 회수된다. The present invention relates to a method and apparatus for producing pressurized oxygen and krypton-xenon by cold distillation of air. The rectification system has a low pressure column 3 for nitrogen-oxygen separation and a krypton-xenon rich column 15. Compressed and purified feed air 4 is introduced into the rectification system. The first oxygen fraction 11 is removed from the low pressure column 3, pressure raised 12 in the liquid state, and removed as a pressurized oxygen product 24 in the evaporated and gaseous state. In addition, the second oxygen fraction 16 is removed from the low pressure column 3 and passed 18 into the lower or central region of the krypton-xenon rich column 15. The first oxygen fraction 11 is removed at one or more actual or theoretical stages on the bottom of the low pressure column 3 and, after the pressure rise 12, is introduced in the liquid state into the upper region of the krypton-xenon rich column 15. do. The krypton rich and / or xenon rich fraction 19 is removed from the lower region of the krypton-xenon rich column 15. Pressurized oxygen product 24 is recovered in gaseous form from the upper region of krypton-xenon rich column 15.

Method and equipment for producing air product based on cryogenic rectification

本发明公开了一种基于深冷精馏生产空气产品的方法及设备，通过压缩机压缩后的原料空气及氮气经过主换热器降温后，送入到精馏系统进行低温分离。在精馏系统中，通过低温分离，得到氧氮等产品，同时也将在精馏塔底部或附近得到富氧液空。将精馏系统中的富氧液空或液态空气通过低温液空泵提升到目标压力后送出，然后在气相与循环氮气混合生产各种压力的空气产品。采用这种方法，可以避免现有技术中在液相将液氮与富氧液空或液态空气混合，而在汽化之后不能确定所得到的空气产品正好是所需的比例的问题；同时还能够在使用氮气循环内压缩流程的前提下，以更精确和安全的方式获得空气产品。

Method of liquefying and separating air

(57)【要約】本公報は電子出願前の出願データであるた め要約のデータは記録されません。

Method of liquefying natural gas

Integrated nitrogen liquefier for nitrogen and argon generating cryogenic air separation units

아르곤 및 질소 생성 극저온 공기 분리 유닛과 통합되도록 구성된 질소 액화기 및 질소 액화 방법이 제공된다. 통합형 질소 액화기 및 이와 연관된 방법은 (i) 제로 액체 질소 모드; (ii) 저 액체 질소 모드; 및 (iii) 고 액체 질소 모드를 포함한 적어도 세 가지 별개 모드에서 작동될 수 있다. 본 시스템 및 방법은, 공기 분리 유닛의 저압 칼럼으로부터의 산소 풍부 스트림이 아르곤 응축기에 사용되는 산소 풍부 응축 매질인 것을 추가적인 특징으로 한다.

PROCESS AND PLANT FOR PRODUCING OXYGEN AND RARE GASES BY CRYOGENIC AIR DISTILLATION

Hydrocarbon gas processing

탄화수소 가스 스트림으로부터 에탄, 에틸렌 및 그보다 무거운 탄화수소 성분을 회수하는 방법 및 장치가 개시된다. 스트림은 냉각되고 저압으로 팽창되며 중간 칼럼 공급 위치에서 제1 분류탑에 공급된다. 증류 액체 스트림은 팽창된 스트림의 공급 위치 아래의 제1 분류탑으로부터 취출되어 가열되며, 제2 분류탑으로 유도되어 공중 증기 스트림과 바닥 액체 스트림을 생성한다. 공중 증기 스트림은 냉각되어 응축되며, 응축된 스트림의 일부는 상부 공급원으로서 제2 분류탑으로 유도되며 나머지는 하측 칼럼 공급 위치에서 제1 분류탑으로 유도된다. 제2 분류탑으로부터의 바닥 액체 스트림은 냉각되어 상부 공급원으로서 제1 분류탑으로 유도된다. A method and apparatus are disclosed for recovering ethane, ethylene, and heavier hydrocarbon components from a hydrocarbon gas stream. The stream is cooled and expanded at low pressure and fed to the first fractionation column at the intermediate column feed position. The distillation liquid stream is withdrawn from the first distillation column below the feed location of the expanded stream and heated and is directed to a second distillation column to produce a vapor stream and bottom liquid stream. The vapor stream is cooled and condensed and a portion of the condensed stream is directed to the second column as an upper source and the remainder is directed to the first column at the lower column feed location. The bottom liquid stream from the second fractionation column is cooled and directed to the first fractionation column as an upper source.

Nitrogen production method and nitrogen production apparatus

액체 질소를 제조하기 위한, 질소 회수율이 높고, 에너지 효율이 높은 질소 제조 방법 및 질소 제조 장치를 제공한다. 원료 공기의 일부를, 주 열교환기(1)의 전단에서 팽창시켜서 냉각하고, 팽창되지 않은 나머지 원료 공기를 주 열교환기(1) 내부에서 예랭하기 위한 한랭으로서 이용한다. 또한, 주 열교환기(1) 내부에서 예랭된 원료 공기의 일부를 주 열교환기(1) 외부로 취출하여 팽창시켜서 냉각하고, 팽창되지 않은 나머지 예랭된 원료 공기를 주 열교환기(1) 내부에서 냉각하기 위한 한랭으로서 이용한다.

Process and plant for production of carbon monoxide and hydrogen

본 발명은 열 교환기(310)에서 부분 응축 반응에 의해 분리 용기(320)의 기저에서 회수된 응축된 분획(322)으로부터 일산화탄소를 제조하는 방법에 관한 것이다. 불순한 수소(321)는 용기(320)의 상부에서 생성되고, 칼럼(350)에서 질소로 세척됨으로써 정제된다. 암모니아 합성 혼합물은 상기 칼럼의 상부에서 수집된 수소 흐름(353)으로부터 생성된다. 일산화탄소는 질소 세척 칼럼(350)의 기저에서 수집된 분획(351)으로부터 추가로 생성된다. 칼럼들 전부와 교환기는 하나의 냉각 박스(400)에 내장된다.

Method of producing liquid and gaseous oxygen-enriched air separation product in an air separation plant and an air separation plant

FIELD: water and air purification technology.SUBSTANCE: invention relates to an air separation plant. Air separation unit (100) includes high pressure column (61), low pressure column (62) and mixing column (7). First flow (h) of compressed air, which is cooled to the first temperature level and expanded in first turbine (4), is supplied to mixing column (7). High pressure column (62) is supplied with the second flow (g) of compressed cooled to the first level temperature and expanded in the first air turbine (4). At the same time, a third compressed air flow (f) is supplied to the low pressure column (62), which is then cooled to a second temperature level, expanded in second turbine (5) and further cooled in main heat exchanger (3). Air expelled in the first and second turbines (4, 5) is supplied to first turbine (4) at the first and second turbine (5) at the second temperature level. Liquid oxygen-enriched air separation product is discharged from unit (100).EFFECT: technical result is providing process flexibility at variable demand for liquid and gaseous oxygen-enriched air separation products.15 cl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 722 074 C2 (51) МПК F25J 3/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК F25J 3/04175 (2020.02); F25J 3/042 (2020.02); F25J 3/0429 (2020.02); F25J 3/04296 (2020.02); F25J 3/04303 (2020.02); F25J 3/04393 (2020.02); F25J 3/04412 (2020.02); F25J 3/04466 (2020.02); F25J 3/04787 (2020.02); F25J 3/04793 (2020.02); F25J 3/04812 (2020.02) (21)(22) Заявка: 2016147701, 06.12.2016 06.12.2016 (73) Патентообладатель(и): ЛИНДЕ АКЦИЕНГЕЗЕЛЛЬШАФТ (DE) Дата регистрации: (56) Список документов, цитированных в отчете о поиске: RU 2387934 C2, 27.04.2010. RU 2479806 C2, 20.04.2013. DE 102013002094 A1, 07.08.2014. US 5379598 A, 10.01.1995. EP 0698772 A1, 28.02.1996. Приоритет(ы): (30) Конвенционный приоритет: 07.12.2015 EP 15003483.3 (43) Дата публикации заявки: 07.06.2018 Бюл ...

Method of separating hydrocarbon mixture

Изобретение относитс  к холодильной технике. Цель изобретени  - уменьшение энергозатрат и упрощение технологической схемы. Смесь, содержаща  углекислый газ, охлаждаетс  и частично конденсируетс  в охладителе 2, откуда в виде смеси газ - жидкость поступает в сепаратор 3, где раздел етс . Из сепаратора газ и жидкость отдельньми потоками подаютс  в ректификационную колонну 6. С помощью подогревател  7 часть жидкости в нижней части колонны испар етс , газ поднимаетс  по колонне, обогащаетс  легкими углеводородами и отводитс  в виде продукта. Конденсат на орошение колонны охлаждают до т-ры -30... +30 С и подают из ее нижней части. Из средней части колонны ниже уровн  ввода газа и жидкости на разделение отвод т газообразную боковую фракцию и конденсируют ее под давлением. 3 з,п, ф-лы, 1 ил. to СО

Method and device for separating air

(57)【要約】 【課題】 液体の窒素流を加えることなく、重質成分の 濃度が薄い酸素を含む蒸気流が液化され、ストリップカ ラムに還流させるべく単一のカラム内でストリッピング 除去されるようにした、空気の分離方法及びその装置を 提供すること。 【解決手段】 酸素を含む蒸気流４６が単一カラムの窒 素発生器１２から除去され、次に、２つの補助流４８、 ５０に分割される、空気の分離方法及びその装置１であ る。該２つの補助流４８、５０は凝縮され、その後に混 合して、単一カラム内でストリッピングされ、カラムが 底になると、超高純度の液体酸素が製造される。この２ つの補助流４８、５０の一方はリボイラー５２内で及び ストリッピングカラム１４の底部領域５４内で凝縮され る。２つの補助流４８、５０のもう一方は、窒素ストリ ッピングカラム１４に接続して使用される頂部凝縮器２ ２内で凝縮される。

Patent FR2368435B1

Nitrogen production method and nitrogen production apparatus

提供一种用于制造液氮的、氮回收率高且能量效率高的氮制造方法和氮制造装置。将原料空气的一部分在主热交换器(1)的前段膨胀并冷却，将没有膨胀的剩余原料空气作为用于在主热交换器(1)内部预冷的寒冷利用。另外，将主热交换器(1)内部预冷了的原料空气的一部分向主热交换器(1)外部取出使其膨胀并冷却，将没有膨胀的剩余的预冷了的原料空气作为用于在主热交换器(1)内部冷却的寒冷利用。