RU2014128650A - METHOD AND DEVICE FOR REMOVING NITROGEN FROM CRYOGENIC HYDROCARBON COMPOSITION - Google Patents

METHOD AND DEVICE FOR REMOVING NITROGEN FROM CRYOGENIC HYDROCARBON COMPOSITION Download PDF

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RU2014128650A
RU2014128650A RU2014128650A RU2014128650A RU2014128650A RU 2014128650 A RU2014128650 A RU 2014128650A RU 2014128650 A RU2014128650 A RU 2014128650A RU 2014128650 A RU2014128650 A RU 2014128650A RU 2014128650 A RU2014128650 A RU 2014128650A
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nitrogen
stream
steam
desorption
stripping
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RU2014128650A
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Russian (ru)
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RU2622212C2 (en
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Александр М.К.Р. САНТОС
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Шелл Интернэшнл Рисерч Маатсхаппий Б.В.
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    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream

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Abstract

1. Способ удаления азота из криогенной углеводородной композиции, содержащей азот- и метансодержащую жидкую фазу, который включает:- обеспечение криогенной углеводородной композиции, содержащей азот- и метансодержащую жидкую фазу;- подачу первого потока сырья десорбера азота при давлении десорбции в колонну десорбции азота, содержащую по меньшей мере одну внутреннюю десорбционную секцию, расположенную внутри колонны десорбции азота, причем указанный первый поток сырья десорбера азота содержит первую часть указанной криогенной углеводородной композиции;- отведение обедненной азотом жидкости из области сборника колонны десорбции азота, расположенной под десорбционной секцией;- 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, которое ниже, чем давление десорбции;- сжатие указанного технологического пара до по меньшей мере давления десорбции, тем самым получая сжатый пар;- пропускание потока десорбирующего пара в колонну десорбции азота на уровне, находящемся ниже по вертикали от указанной десорбционной секции, причем указанный поток десорбирующего пара содержит по меньшей мере десорбирующую часть указанного сжатого пара;- отведение паровой фракции, содержащей отводимую фракцию пара головного погона, полученную из головной части колонны десорбции азота, в виде отходящего газа;- деление потока криогенной углеводородной композиции на указанную первую часть и вторую часть, имеющую тот же самый состав и фазу, что и первая часть;- сброс да1. A method for removing nitrogen from a cryogenic hydrocarbon composition containing a nitrogen and methane-containing liquid phase, which includes: providing a cryogenic hydrocarbon composition containing a nitrogen and methane-containing liquid phase; supplying a first stream of nitrogen stripper feed at a desorption pressure to a nitrogen desorption column, containing at least one internal desorption section located inside the nitrogen desorption column, wherein said first stream of nitrogen stripper feed contains the first part of said cryogenic carbohydrate a native composition; - discharge of nitrogen-depleted liquid from the region of the nitrogen desorption column collector located under the desorption section; - obtaining at least a stream of liquid hydrocarbon product and process steam from a nitrogen-depleted liquid, including at least a step of depressurizing the nitrogen-depleted liquid to instantaneous pressure evaporation, which is lower than the desorption pressure; - compression of the specified process steam to at least the desorption pressure, thereby obtaining compressed steam; - transmission the outflow of stripping steam to the nitrogen stripping column at a level lower vertically from said stripping section, wherein said stripping steam stream contains at least a stripping portion of said compressed steam; - a vapor fraction containing a withdrawn overhead vapor fraction obtained from a head portion nitrogen desorption columns, in the form of exhaust gas; - dividing the cryogenic hydrocarbon composition stream into said first part and second part having the same composition and phase as the first I am part; - reset yes

Claims (20)

1. Способ удаления азота из криогенной углеводородной композиции, содержащей азот- и метансодержащую жидкую фазу, который включает:1. The method of removing nitrogen from a cryogenic hydrocarbon composition containing a nitrogen and methane-containing liquid phase, which includes: - обеспечение криогенной углеводородной композиции, содержащей азот- и метансодержащую жидкую фазу;- providing a cryogenic hydrocarbon composition containing a nitrogen and methane-containing liquid phase; - подачу первого потока сырья десорбера азота при давлении десорбции в колонну десорбции азота, содержащую по меньшей мере одну внутреннюю десорбционную секцию, расположенную внутри колонны десорбции азота, причем указанный первый поток сырья десорбера азота содержит первую часть указанной криогенной углеводородной композиции;- supplying a first stream of nitrogen stripper feed at a stripping pressure to a nitrogen stripping column containing at least one internal stripping section located inside the nitrogen stripping column, said first nitrogen stripping feed stream comprising a first portion of said cryogenic hydrocarbon composition; - отведение обедненной азотом жидкости из области сборника колонны десорбции азота, расположенной под десорбционной секцией;- removal of nitrogen-depleted liquid from the region of the collector of the nitrogen desorption column located under the desorption section; - 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, которое ниже, чем давление десорбции;- obtaining at least a stream of liquid hydrocarbon product and process steam from a nitrogen-depleted liquid, comprising at least a step of depressurizing the nitrogen-depleted liquid to an instantaneous vapor pressure that is lower than the desorption pressure; - сжатие указанного технологического пара до по меньшей мере давления десорбции, тем самым получая сжатый пар;- compressing said process steam to at least a desorption pressure, thereby obtaining compressed steam; - пропускание потока десорбирующего пара в колонну десорбции азота на уровне, находящемся ниже по вертикали от указанной десорбционной секции, причем указанный поток десорбирующего пара содержит по меньшей мере десорбирующую часть указанного сжатого пара;- passing a stream of stripping steam into the nitrogen stripping column at a level lower vertically from said stripping section, wherein said stripping steam stream contains at least a stripping portion of said compressed steam; - отведение паровой фракции, содержащей отводимую фракцию пара головного погона, полученную из головной части колонны десорбции азота, в виде отходящего газа;- abstraction of the vapor fraction containing the withdrawn fraction of the overhead vapor obtained from the head of the nitrogen desorption column in the form of exhaust gas; - деление потока криогенной углеводородной композиции на указанную первую часть и вторую часть, имеющую тот же самый состав и фазу, что и первая часть;- dividing the cryogenic hydrocarbon composition stream into said first part and second part having the same composition and phase as the first part; - сброс давления второй части до указанного давления мгновенного испарения;- pressure relief of the second part to the specified pressure instantaneous evaporation; - подачу второй части в по меньшей мере один поток из группы, состоящей из: обедненной азотом жидкости, жидкого углеводородного продукта и технологического пара; причем от указанного деления потока до указанной подачи второй части вторая часть обходит колонну десорбции азота.- supplying the second part to at least one stream from the group consisting of: a nitrogen-depleted liquid, a liquid hydrocarbon product, and process steam; moreover, from the specified division of the flow to the specified feed of the second part, the second part bypasses the nitrogen desorption column. 2. Способ по п. 1, дополнительно включающий стадию:2. The method according to p. 1, further comprising a stage: - регулирования отношения деления криогенной углеводородной композиции на указанную первую часть и указанную вторую часть, определенного как расход указанной первой части по отношению к общему расходу первой и второй частей вместе, тем самым поддерживая расход указанной первой части на заданном целевом уровне расхода.- regulating the ratio of the division of the cryogenic hydrocarbon composition into the specified first part and the specified second part, defined as the flow rate of the specified first part relative to the total flow rate of the first and second parts together, thereby maintaining the flow rate of the specified first part at a given target flow rate. 3. Способ по п. 1, в котором давление десорбции находится в диапазоне от 2 до 15 бар абс., и/или в котором давление мгновенного испарения составляет от 1 до 2 бар абс.3. The method according to p. 1, in which the desorption pressure is in the range from 2 to 15 bar abs. And / or in which the flash pressure is from 1 to 2 bar abs. 4. Способ по п. 1, дополнительно включающий пропускание по меньшей мере топливной части паровой фракции в устройство сжигания при давлении топливного газа, не превышающем давления десорбции.4. The method according to claim 1, further comprising transmitting at least the fuel portion of the vapor fraction to the combustion device at a fuel gas pressure not exceeding the desorption pressure. 5. Способ по п. 1, в котором технологический пар содержит отпарной газ, полученный путем добавления тепла в поток жидкого углеводородного продукта, в результате чего часть потока жидкого углеводородного продукта испаряется с образованием указанного отпарного газа.5. The method according to claim 1, wherein the process steam contains stripping gas obtained by adding heat to the liquid hydrocarbon product stream, as a result of which a portion of the liquid hydrocarbon product stream evaporates to form the specified stripping gas. 6. Способ по п. 1, в котором во время указанного сброса давления указанной обедненной азотом жидкости до указанного давления мгновенного испарения образуется пар мгновенного испарения, при этом указанный технологический пар содержит указанный пар мгновенного испарения.6. The method according to claim 1, wherein during said depressurization of said nitrogen-depleted liquid to said flash pressure, flash steam is generated, said process steam containing said flash vapor. 7. Способ по п. 6, в котором указанное образование указанного по меньшей мере потока жидкого углеводородного продукта и технологического пара из обедненной азотом жидкости дополнительно включает стадию фазового разделения обедненной азотом жидкости в конечном сепараторе мгновенного испарения при давлении мгновенного разделения, которое равно или меньше, чем давление мгновенного испарения, на поток жидкого углеводородного продукта и указанный пар мгновенного испарения.7. The method of claim 6, wherein said formation of said at least liquid hydrocarbon product stream and process steam from a nitrogen-depleted liquid further comprises the step of phase separating the nitrogen-depleted liquid in a flash flash separator at a flash point that is equal to or less, than flash pressure, on the liquid hydrocarbon product stream and said flash vapor. 8. Способ по п. 7, в котором указанная подача второй части в указанный по меньшей мере один поток из группы, состоящей из: обедненной азотом жидкости, жидкого углеводородного продукта и технологического пара, включает в себя: подачу второй части в конечный сепаратор мгновенного испарения после указанного сброса давления указанной второй части до указанного давления мгновенного испарения.8. The method according to p. 7, in which the specified supply of the second part to the specified at least one stream from the group consisting of: nitrogen-depleted liquid, liquid hydrocarbon product and process steam, includes: supplying the second part to the final flash evaporator after said depressurization of said second part to said instant flash pressure. 9. Способ по п. 1, в котором колонна десорбции азота дополнительно содержит по меньшей мере одну внутреннюю ректификационную секцию, расположенную выше по вертикали, чем указанная десорбционная секция в указанной колонне десорбции азота; причем указанный способ дополнительно включает в себя:9. The method according to claim 1, wherein the nitrogen desorption column further comprises at least one internal distillation section located vertically higher than said desorption section in said nitrogen desorption column; moreover, the specified method further includes: - образование частично сконденсированного промежуточного потока из пара головного погона, полученного из головной части колонны десорбции азота над ректификационной секцией, причем указанный частично сконденсированный промежуточный поток содержит сконденсированную фракцию и паровую фракцию, причем указанное образование включает частичную конденсацию пара головного погона за счет теплообмена пара головного погона с потоком вспомогательного хладагента и, тем самым, поступление тепла от пара головного погона к потоку вспомогательного хладагента в количестве производительности по холоду;- the formation of a partially condensed intermediate stream from the overhead steam obtained from the head of the nitrogen desorption column above the distillation section, said partially condensed intermediate stream containing a condensed fraction and a vapor fraction, said formation comprising partial condensation of the overhead steam due to heat exchange of the overhead steam with a stream of auxiliary refrigerant and, thus, heat from the overhead steam to the auxiliary stream th refrigerant in the amount of performance in the cold; - отделение сконденсированной фракции от паровой фракции при давлении разделения;- separation of the condensed fraction from the vapor fraction at a separation pressure; - позволяют по меньшей мере части обратного орошения из сконденсированной фракции входить в ректификационную секцию в колонне десорбции азота на уровне над ректификационной секцией.- allow at least part of the reverse irrigation from the condensed fraction to enter the distillation section in the nitrogen desorption column at a level above the distillation section. 10. Способ по п. 1, в котором указанное обеспечение указанной криогенной углеводородной композиции включает:10. The method of claim 1, wherein said providing said cryogenic hydrocarbon composition comprises: - теплообмен потока сырья, содержащего углеводородсодержащее парообразное сырье, в криогенном теплообменнике с потоком основного хладагента, приводящий к сжижению парообразного сырья из потока сырья с получением сжиженного потока; и- heat transfer of a feed stream containing a hydrocarbon-containing vaporous feedstock in a cryogenic heat exchanger with a main refrigerant stream leading to liquefaction of the vaporous feedstock from the feedstream to produce a liquefied stream; and - получение криогенной углеводородной композиции из сжиженного потока.- obtaining a cryogenic hydrocarbon composition from a liquefied stream. 11. Способ по п. 1, в котором указанная вторая часть не подвергается какому-либо функциональному косвенному теплообмену по пути к указанной последующей подаче в по меньшей мере один поток из группы, состоящей из: обедненной азотом жидкости, жидкого углеводородного продукта и технологического пара; причем от указанного деления потока до указанной подачи второй части вторая часть обходит колонну десорбции азота.11. The method according to claim 1, wherein said second part does not undergo any functional indirect heat transfer along the path to said subsequent supply to at least one stream from the group consisting of: a nitrogen-depleted liquid, a liquid hydrocarbon product, and process steam; moreover, from the specified division of the flow to the specified feed of the second part, the second part bypasses the nitrogen desorption column. 12. Способ по п. 1, дополнительно включающий:12. The method according to p. 1, further comprising: - отведение парообразной рециркулирующей части от указанной паровой фракции;- the removal of the vapor recycle portion from the specified vapor fraction; - сброс давления указанной парообразной рециркулирующей части до давления мгновенного испарения;- depressurization of said vaporous recycle portion to flash pressure; - ввод парообразной рециркулирующей части в по меньшей мере один поток из группы, состоящей из: обедненной азотом жидкости, жидкого углеводородного продукта и технологического пара.- introducing a vaporous recycle portion into at least one stream from the group consisting of: a nitrogen-depleted liquid, a liquid hydrocarbon product, and process steam. 13. Способ по п. 1, в котором паровая фракция содержит от 50 мол.% до 95 мол.% азота.13. The method according to p. 1, in which the vapor fraction contains from 50 mol.% To 95 mol.% Nitrogen. 14. Способ по п. 1, в котором сконденсированная фракция содержит менее 35 мол.% азота.14. The method according to p. 1, in which the condensed fraction contains less than 35 mol.% Nitrogen. 15. Способ по любому из пп. 1-14, дополнительно включающий селективный ввод перепускаемой части указанного сжатого пара, которая не содержит указанной десорбирующей части, в пар головного погона, при этом обходя по меньшей мере десорбционную секцию колонны десорбции азота.15. The method according to any one of paragraphs. 1-14, further comprising selectively introducing a bypass portion of said compressed steam, which does not contain said stripping portion, into the overhead steam, while bypassing at least the desorption section of the nitrogen desorption column. 16. Устройство для удаления азота из криогенной углеводородной композиции, содержащей азот- и метансодержащую жидкую фазу, которое содержит:16. A device for removing nitrogen from a cryogenic hydrocarbon composition containing a nitrogen and methane-containing liquid phase, which contains: - линию подачи криогенного сырья, соединенную с источником криогенной углеводородной композиции, содержащей азот- и метансодержащую жидкую фазу;- a cryogenic feed line connected to a source of a cryogenic hydrocarbon composition containing a nitrogen and methane-containing liquid phase; - колонну десорбции азота, находящуюся в сообщении по текучей среде с линией подачи криогенного сырья, причем указанная колонна десорбции азота содержит по меньшей мере одну внутреннюю десорбционную секцию, расположенную внутри колонны десорбции азота;- a nitrogen desorption column in fluid communication with the cryogenic feed line, said nitrogen desorption column comprising at least one internal desorption section located inside the nitrogen desorption column; - линию отведения пара головного погона, сообщающуюся с колонной десорбции азота через головную область внутри колонны десорбции азота;- a steam discharge line of the overhead steam, communicating with the nitrogen desorption column through the head region inside the nitrogen desorption column; - линию отведения обедненной азотом жидкости, сообщающуюся с областью сборника внутри колонны десорбции азота, расположенной ниже по вертикали от десорбционной секции;- the discharge line of a nitrogen-depleted liquid in communication with the collection area inside the nitrogen desorption column located downright from the desorption section; - промежуточное устройство сброса давления в линии отведения обедненной азотом жидкости, находящееся в сообщении по текучей среде с колонной десорбции азота, выполненное с возможностью принимать обедненную азотом жидкость из области сборника колонны десорбции азота и сбрасывать давление обедненной азотом жидкости, причем указанное промежуточное устройство сброса давления находится на границе раздела между стороной давления десорбции, включающей колонну десорбции азота, и стороной давления мгновенного испарения;- an intermediate pressure relief device in the discharge line of a nitrogen-depleted liquid in fluid communication with a nitrogen desorption column, configured to receive a nitrogen-depleted liquid from an area of the collector of a nitrogen desorption column and relieve pressure of a nitrogen-depleted liquid, wherein said intermediate pressure relief device is at the interface between the desorption pressure side including the nitrogen desorption column and the flash side; - линию жидкого углеводородного продукта, расположенную на стороне давления мгновенного испарения, для отведения потока жидкого углеводородного продукта, полученного из обедненной азотом жидкости;- a line of liquid hydrocarbon product, located on the pressure side of the flash, to divert the flow of liquid hydrocarbon product obtained from a nitrogen-depleted liquid; - линию технологического пара, расположенную на стороне давления мгновенного испарения, для приема технологического пара, полученного из обедненной азотом жидкости;- a process steam line located on the pressure side of flash flash to receive process steam obtained from a nitrogen-depleted liquid; - технологический компрессор, расположенный в линии технологического пара, выполненный с возможностью приема технологического пара и сжатия технологического пара для создания сжатого пара на выпускном отверстии технологического компрессора, причем указанный технологический компрессор находится на указанной границе раздела между стороной давления десорбции и стороной давления мгновенного испарения;- a process compressor located in the line of process steam configured to receive process steam and compress process steam to create compressed steam at the outlet of the process compressor, said process compressor being at a specified interface between the desorption pressure side and the flash side; - линию десорбирующего пара, находящуюся в сообщении по текучей среде с колонной десорбции азота на уровне, расположенном ниже по вертикали от десорбционной секции, и выполненную с возможностью приема по меньшей мере десорбирующей части указанного сжатого пара из технологического компрессора;- a line of stripping steam in fluid communication with the nitrogen stripping column at a level lower down from the stripping section and configured to receive at least the stripping portion of said compressed steam from the process compressor; - делитель исходного потока, расположенный в линии подачи криогенного сырья, выполненный с возможностью деления криогенной углеводородной композиции на первую часть и вторую часть, имеющую тот же самый состав и фазу, что и первая часть;- a feed stream divider located in the cryogenic feed line, configured to divide the cryogenic hydrocarbon composition into a first part and a second part having the same composition and phase as the first part; - первую линию подачи сырья для транспортировки первой части из делителя исходного потока в колонну десорбции азота;- a first feed line for transporting a first portion from a feed stream divider to a nitrogen desorption column; - вторую линию подачи сырья для транспортировки второй части из делителя исходного потока в по меньшей мере одну линию из группы, состоящей из: линии обедненной азотом жидкости, линии жидкого углеводородного продукта и линии технологического пара, причем указанная вторая линия подачи сырья обходит колонну десорбции азота.- a second feed line for transporting the second part from the feed stream divider to at least one line from the group consisting of: a line of nitrogen-depleted liquid, a line of liquid hydrocarbon product and a process steam line, said second feed line bypassing the nitrogen desorption column. 17. Устройство по п. 16, в котором во второй линии подачи сырья расположен регулирующий клапан обходящего потока.17. The device according to claim 16, wherein a bypass flow control valve is located in the second feed line. 18. Устройство по п. 17, в котором указанный регулирующий клапан обходящего потока функционально связан с регулятором FC потока, расположенном в первой линии подачи сырья.18. The device of claim 17, wherein said bypass flow control valve is operatively coupled to an FC flow regulator located in a first feed line. 19. Устройство по п. 18, в котором указанный регулятор FC потока выполнен с возможностью поддерживать расход указанной первой части через первую линию подачи сырья на заданном целевом уровне расхода, регулируя отношение деления криогенной углеводородной композиции, протекающей через линию подачи криогенного сырья, на указанные первую и вторую части.19. The device according to p. 18, in which the specified FC flow regulator is configured to maintain the flow rate of the first part through the first feed line at a predetermined target flow rate by adjusting the division ratio of the cryogenic hydrocarbon composition flowing through the cryogenic feed line to the first and the second part. 20. Устройство по любому из пп. 16-19, в котором указанная вторая линия подачи сырья не проходит через какой-либо косвенный теплообменник, функционирующий для косвенного обмена теплом с каким-либо технологическим потоком. 20. The device according to any one of paragraphs. 16-19, wherein said second feed line does not pass through any indirect heat exchanger that functions to indirectly exchange heat with any process stream.
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