EA024400B1 - Method for producing gaseous compressed oxygen product by low-temperature air separation - Google Patents
Method for producing gaseous compressed oxygen product by low-temperature air separation Download PDFInfo
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- EA024400B1 EA024400B1 EA201201485A EA201201485A EA024400B1 EA 024400 B1 EA024400 B1 EA 024400B1 EA 201201485 A EA201201485 A EA 201201485A EA 201201485 A EA201201485 A EA 201201485A EA 024400 B1 EA024400 B1 EA 024400B1
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- compressed
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- stream
- cooled
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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
- 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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
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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
- 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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
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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
- 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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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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
- 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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04096—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of argon or argon enriched stream
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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
- 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
- F25J3/04—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 for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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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
- 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
- F25J3/04—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 for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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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
- 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
- F25J3/04—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 for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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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
- 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
- F25J3/04—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 for air
- F25J3/04406—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 for air using a dual pressure main column system
- F25J3/04412—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 for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
Настоящее изобретение относится к способу согласно ограничительной части в п.1 формулы изобретения.The present invention relates to a method according to the restrictive part in claim 1 of the claims.
Способы и устройства для низкотемпературного разделения воздуха известны, например, из книги Низкотемпературная технология, 2 издание 1985 г., глава 4, с. 281-337.Methods and devices for low-temperature air separation are known, for example, from the book Low-Temperature Technology, 2nd edition, 1985, chapter 4, p. 281-337.
Дистилляционная колонная система согласно настоящему изобретению может иметь конструкцию двухколонной системы (например, как классическая двухколонная система Ьшбе), или, в качестве альтернативы, это может быть трехколонная или многоколонная система. Она может помимо колонн для разделения азота и кислорода включать дополнительные устройства для изготовления высокочистых продуктов и/или других компонентов воздуха, в частности, благородных газов, например, для производства аргона и/или для производства криптона и ксенона.The distillation column system of the present invention may be a two-column system (for example, as a classic two-column system), or, alternatively, it may be a three-column or multi-column system. In addition to columns for the separation of nitrogen and oxygen, it may include additional devices for the manufacture of high-purity products and / or other air components, in particular, noble gases, for example, for the production of argon and / or for the production of krypton and xenon.
В этом процессе жидкий поток сжатого кислородного продукта испаряется теплоносителем, и в итоге его получают как газообразный сжатый продукт. Этот способ также называется термином внутреннее сжатие и служит для производства сжатого кислорода. В случае сверхкритического давления фазовый переход фактически не происходит и поток продукта затем псевдоиспаряется.In this process, the liquid stream of compressed oxygen product is evaporated by the coolant, and as a result, it is obtained as gaseous compressed product. This method is also called the term internal compression and serves to produce compressed oxygen. In the case of supercritical pressure, the phase transition actually does not occur and the product flow is then pseudo-evaporating.
Теплоноситель при высоком давлении сжижают (или псевдосжижают, если он находится при сверхкритическом давлении) (псевдо)испарившимся потоком продукта. В качестве теплоносителя часто используют некоторое количество воздуха, в данном случае это третий воздушный поток и четвертый воздушный поток, которые оба ответвляются от исходного подаваемого сжатого воздуха.The high pressure coolant is liquefied (or pseudo-liquefied if it is at supercritical pressure) (pseudo) by evaporated product flow. Some amount of air is often used as a heat carrier, in this case it is the third air flow and the fourth air flow, both of which branch off from the original supplied compressed air.
Способы внутреннего сжатия известны, например, из следующих патентных документов:Methods of internal compression are known, for example, from the following patent documents:
БЕ 830805, БЕ 901542 (= ϋ3BU 830805, BU 901542 (= ϋ3
2712738/05 2784572), БЕ 952908, БЕ 1103363 (= УЗ 3033544), БЕ 1112997 (= из 3214925), БЕ 1124529, БЕ 1117616 (= ОЗ 3280574),2712738/05 2784572), BU 952908, BU 1103363 (= UZ 3033544), BU 1112997 (= of 3214925), BU 1124529, BU 1117616 (= OZ 3280574),
БЕ 1226616 (= из 3216206), БЕ 1229561 (= иЗ 3222878), БЕ 1199293, БЕ 1187248 (= 03 3371496), БЕ 1235347, БЕ 1258882 (=BU 1226616 (= of 3216206), BU 1229561 (= iZ 3222878), BU 1199293, BU 1187248 (= 03 3371496), BU 1235347, BU 1258882 (=
3426543), БЕ 1263037 (= 05 3401531), БЕ 1501722 ( = 03 3416323), БЕ 1501723 (= 03 3500651), БЕ 253132 {= 05 4279631),3426543), BU 1263037 (= 05 3401531), BU 1501722 (= 03 3416323), BU 1501723 (= 03 3500651), BU 253132 {= 05 4279631),
1031804 А1 (= ОЗ 6314755), БЕ 19909744 А1, ЕР 1067345 А1 (= из 6336345), ЕР 1074805 А1 (= 03 6332337), БЕ 19954593 А1, ЕР1031804 A1 (= OZ 6314755), BU 19909744 A1, EP 1067345 A1 (= of 6336345), EP 1074805 A1 (= 03 6332337), BU 19954593 A1, EP
1134525 А1 (= 05 6477860), БЕ 10013073 А1, ЕР 1139046 А1, ЕР 1146301 А1, ЕР 1150082 А1, ЕР 1213552 А1, БЕ 10115258 А1, ЕР 1284404 А1 (= 03 2003051504 А1) , ЕР 1308680 А1 (= ОЗ 6612129 В2), БЕ 10213212 А1, БЕ 10213211 А1, ЕР 1357342 А1 или БЕ 10238282 А1, БЕ 10302389 А1, БЕ 10334559 А1, БЕ 10334560 А1, БЕ 10332863 А1, ЕР 1544559А1, ЕР 1585926 А1, БЕ 102005029274 А1,1134525 A1 (= 05 6477860), BU 10013073 A1, EP 1139046 A1, EP 1146301 A1, EP 1150082 A1, EP 1213552 A1, BU 10115258 A1, EP 1284404 A1 (= 03 2003051504 A1), EP 1308680 A1 (= OS 6621) ), BU 10213212 A1, BU 10213211 A1, EP 1357342 A1 or BU 10238282 A1, BU 10302389 A1, BU 10334559 A1, BU 10334560 A1, BU 10332863 A1, EP 1544559A1, EP 1585926 A1, BU 102005029274 A1,
ЕР 1666824 А1, ЕР 1672301 А1, БЕ 102005028012 А1, МО 2007033838 А1, ИО 2007104449 А1, ЕР 1845324 А1, БЕ 102006032731 А1, ЕР 1892490 А1, ВЕ 102007014643 А1, ЕР 2015012 А2, ЕР 2015013 А2,EP 1666824 A1, EP 1672301 A1, BE 102 005 028 012 A1, MO 2007033838 A1 IO 2007104449 A1, EP 1845324 A1, BE 102 006 032 731 A1, EP 1892490 A1, BE 102 007 014 643 A1, EP 2015012 A2, EP 2015013 A2,
ЕР 2026024 А1 , ИО 2009095188 А2 или БЕ 102008016355А1.EP 2026024 A1, IO 2009095188 A2 or BU 102008016355A1.
Основная теплообменная система служит для охлаждения исходного подаваемого воздуха путем косвенного теплообмена с возвратными потоками из дистилляционной колонной системы. Она может состоять из одной или более параллельно или последовательно соединенных теплообменных секций, например, из одного или более пластинчатых теплообменных блоков.The main heat exchange system serves to cool the source air by indirect heat exchange with return flows from the distillation column system. It may consist of one or more parallel or serially connected heat exchange sections, for example, one or more plate heat exchange units.
Способ описанного выше типа известен из патента США № 5329776.A method of the type described above is known from US Pat. No. 5,329,776.
Задача настоящего изобретения заключается в том, чтобы предложить способ описанного выше типа, использование которого является особенно выгодным в экономическом отношении вследствие повышения производительности, повышения чистоты продукта, снижения эксплуатационных расходовThe present invention is to propose a method of the type described above, the use of which is particularly advantageous economically due to increased productivity, improved product purity, reduced operating costs
- 1 024400 и/или снижения капитальных расходов.- 1,04400 and / or lower capital costs.
Данная задача достигается за счет отличительных признаков, приведенных в п.1 формулы изобретения.This task is achieved due to the distinctive features given in claim 1 of the claims.
В принципе, в поджимающем компрессоре также или только дросселированный воздух (третий воздушный поток), или весь турбинный воздух (в частности, первый, второй и третий воздушные потоки в совокупности) можно повторно сжимать до давления, превышающего выходное давление основного воздушного компрессора (первое давление). В контексте настоящего изобретения, однако, показано, что сочетание следующих мер приводит к особенно благоприятному количественному соотношению между турбинным потоком (первым или вторым воздушным потоком, в зависимости от того, какая турбина приводит в действие поджимающий компрессор) и нагнетаемым потоком (третий воздушный поток), составляющему приблизительно 1:1,1:In principle, in the compressing compressor also either only throttled air (third air flow), or all turbine air (in particular, the first, second and third air flows in total) can be re-compressed to a pressure exceeding the outlet pressure of the main air compressor (first pressure ). In the context of the present invention, however, it is shown that a combination of the following measures results in a particularly favorable quantitative ratio between the turbine flow (first or second air flow, depending on which turbine drives the biasing compressor) and the discharge flow (third air flow) approximately 1: 1,1:
повторное сжатие только первого и третьего воздушных потоков;recompressing only the first and third air streams;
отсутствие повторного сжатия второго и четвертого воздушных потоков;no re-compression of the second and fourth air streams;
расширение первого турбинного потока (первого воздушного потока) от второго давления;expansion of the first turbine flow (first air flow) from the second pressure;
расширение второго турбинного потока (второго воздушного потока) от первого давления.expansion of the second turbine flow (second air flow) from the first pressure.
Благоприятное количественное соотношение при сочетании турбины и нагнетания повышает технологичность изготовления соответствующего устройства и обеспечивает особенно высокую эффективность поджимающего компрессора.Favorable quantitative ratio with a combination of turbine and injection improves the manufacturability of the corresponding device and ensures a particularly high efficiency of the compressing compressor.
В величинах давления, приведенных в формуле изобретения, естественные перепады давления не включены. Здесь величины давления считаются равными, если разность давления между соответствующими положениями не превышает естественных потерь давления в трубопроводе, которые вызваны перепадами давления в трубах, теплообменниках, холодильниках, адсорберах и т.д. Аналогичным образом, два потока тогда также считаются имеющими одинаковую температуру, если их температуры различаются на величину, которая соответствует разности температур, вызванной естественными колебаниями или обычными потерями в изоляции вдоль линии.In the pressure values given in the claims, the natural pressure drops are not included. Here, pressure values are considered equal if the pressure difference between the respective positions does not exceed the natural pressure losses in the pipeline, which are caused by pressure drops in pipes, heat exchangers, refrigerators, adsorbers, etc. Similarly, the two streams are then also considered to have the same temperature if their temperatures differ by an amount that corresponds to the temperature difference caused by natural fluctuations or normal insulation losses along the line.
Каждая из турбин механически присоединена непосредственно к поджимающему компрессору или к генератору для производства электроэнергии. Здесь термин непосредственное механическое соединение означает непосредственное соединение расширительным устройством и поджимающим компрессором или генератором, например, через общий вал, а не через коробку передач. Соединенные устройства, таким образом, имеют одинаковую скорость вращения. Считается особенно благоприятным, когда первая турбина присоединена к поджимающему компрессору, и вторая турбина сконструирована в качестве генераторной турбины.Each turbine is mechanically connected directly to a biasing compressor or to a generator for generating electricity. Here, the term direct mechanical connection means direct connection by an expansion device and a biasing compressor or generator, for example, through a common shaft, and not through a gearbox. Connected devices thus have the same rotational speed. It is considered particularly favorable when the first turbine is connected to a biasing compressor, and the second turbine is designed as a generating turbine.
Первое давление (выходное давление из основного воздушного компрессора) в настоящем изобретении составляет, например, от 6 до 30 бар (0,6-3 МПа), предпочтительно от 10 до 25 бар (1-2,5 МПа); второе давление (выходное давление из поджимающего компрессора) составляет, например, от 8 до 50 бар (0,8-5 МПа), предпочтительно от 12 до 40 бар (1,2-4 МПа).The first pressure (output pressure from the main air compressor) in the present invention is, for example, from 6 to 30 bar (0.6-3 MPa), preferably from 10 to 25 bar (1-2.5 MPa); the second pressure (the outlet pressure from the compressing compressor) is, for example, from 8 to 50 bar (0.8-5 MPa), preferably from 12 to 40 bar (1.2-4 MPa).
Предпочтительно вторая промежуточная температура (Т2) составляет по меньшей мере на 2 К меньше, чем первая промежуточная температура (Т1). Например, первая промежуточная температура (входная температура первой турбины) составляет от 115 до 135 К, и вторая промежуточная температура (входная температура второй турбины) составляет от 110 до 130 К.Preferably, the second intermediate temperature (T2) is at least 2 K lower than the first intermediate temperature (T1). For example, the first intermediate temperature (the input temperature of the first turbine) is 115 to 135 K, and the second intermediate temperature (the input temperature of the second turbine) ranges from 110 to 130 K.
Помимо потока сжатого кислородного продукта можно также получать азот в качестве газообразного сжатого продукта, где поток жидкого азотного продукта выводят из дистилляционной колонной системы, доводят в жидком состоянии до повышенного давления, испаряют или псевдоиспаряют при этом повышенном давлении в основной теплообменной системе, нагревают приблизительно до температуры окружающей среды и, наконец, выводят в виде потока газообразного сжатого азотного продукта.In addition to the compressed oxygen product stream, it is also possible to produce nitrogen as a gaseous compressed product, where the liquid nitrogen product stream is removed from the distillation column system, brought to an elevated pressure in a liquid state, evaporated or pseudo-evaporated at this increased pressure in the main heat exchange system, heated to approximately environment, and finally output as a stream of gaseous compressed nitrogen product.
В контексте настоящего изобретения считается целесообразным, чтобы поджимающий компрессор был сконструирован как холодный компрессор, другими словами, чтобы его входная температура составляла ниже 210 К, в частности ниже 170 К, например ниже 160 К. Однако она часто оказывается выше, чем первая промежуточная температура (входная температура первой турбина). Например, входная температура поджимающего компрессора составляет от 125 до 160 К.In the context of the present invention, it is considered expedient that the biasing compressor is designed as a cold compressor, in other words, its inlet temperature is lower than 210 K, in particular lower than 170 K, for example lower than 160 K. However, it often turns out to be higher than the first intermediate temperature ( first turbine inlet temperature). For example, the inlet temperature of the compressing compressor ranges from 125 to 160 K.
Далее настоящее изобретение и дополнительные характеристики настоящего изобретения будут разъяснены более подробно со ссылкой на примерный вариант осуществления, схематически представленный на чертеже. Дистилляционная колонная система согласно примерному варианту осуществления в первом варианте содержит колонну 50 высокого давления и колонну 51 низкого давления как единственные дистилляционные колонны, а также главный конденсатор, который не представлен на чертеже и через который верхняя часть колонны высокого давления и нижняя часть колонны низкого давления находятся в теплообменном соединении. Рабочие давления (в каждом случае в верхней части) составляют 5,4 бар (0,54 МПа) в колонне высокого давления и 1,3 бар (0,13 МПа) в колонне низкого давления.Further, the present invention and additional features of the present invention will be explained in more detail with reference to the exemplary embodiment shown schematically in the drawing. The distillation column system according to the exemplary embodiment in the first embodiment comprises a high pressure column 50 and a low pressure column 51 as the only distillation columns, as well as a main condenser that is not shown in the drawing and through which the upper part of the high pressure column and the lower part of the low pressure column are in the heat exchange connection. The working pressures (in each case in the upper part) are 5.4 bar (0.54 MPa) in the high-pressure column and 1.3 bar (0.13 MPa) in the low-pressure column.
Атмосферный воздух сжимают до первого давление р1, составляющего 12 бар (1,2 МПа) в основном воздушном компрессоре, который не показан. Исходный подаваемый воздух (1), сжатый до первого давления, затем (после предварительного охлаждения и очистки, которые также не показаны) подразделяют на четыре воздушных потока, первый воздушный поток 10, второй воздушный поток 20, третийAtmospheric air is compressed to a first pressure p1 of 12 bar (1.2 MPa) in the main air compressor, which is not shown. The original feed air (1), compressed to the first pressure, then (after pre-cooling and cleaning, which are also not shown) is divided into four air streams, the first air stream 10, the second air stream 20, the third
- 2 024400 воздушный поток 30 и четвертый воздушный поток 40. Предпочтительно эти четыре подразделенных потока (помимо каких-либо возможных фракций, таких как, например, воздух, используемый в пневматических устройствах) образуют весь исходный воздух, и не существуют никакие другие части воздушного потока, которые поступают в разделительное устройство.- 2 024400 air stream 30 and fourth air stream 40. Preferably, these four subdivided streams (besides any possible fractions, such as, for example, air used in pneumatic devices) form all the original air, and no other parts of the air stream exist which enter the separation device.
Первый воздушный поток проходит через линию 2 в теплый конец основной теплообменной системы 3 и сначала охлаждается до промежуточной температуры 136 К. Он проходит при этой промежуточной температуре через линию 4 в поджимающий компрессор 5, который сконструирован как холодный компрессор, и в нем повторно сжимается до второго давления р2, составляющего 17 бар (1,7 МПа). Повторно сжатый первый подпоток проходит через линию 6 при температуре 156 К обратно в основную теплообменную систему 3. Первый подпоток 10 выходит из нее при первой промежуточной температуре, составляющей 119 К, и поступает на производящее работу расширение в первую турбину 11, которая приводит в действие поджимающий компрессор 5 через общий вал. Производящий работу при расширении первый подпоток 12, наконец, поступает при давлении 5,5 бар (0,55 МПа) в колонну 50 высокого давления.The first air flow passes through line 2 to the warm end of the main heat exchange system 3 and is first cooled to an intermediate temperature of 136 K. It passes at this intermediate temperature through line 4 to a biasing compressor 5, which is designed as a cold compressor, and re-compressed to a second pressure p2 of 17 bar (1.7 MPa). The recompressed first sub-stream passes through line 6 at a temperature of 156 K back to the main heat exchange system 3. The first sub-stream 10 leaves it at the first intermediate temperature of 119 K and enters the work-producing expansion into the first turbine 11, which actuates the clamped compressor 5 through a common shaft. The first substream 12, which performs the expansion work, finally arrives at a pressure of 5.5 bar (0.55 MPa) in the high-pressure column 50.
Второй воздушный поток охлаждается в основной теплообменной системе 3 до второй промежуточной температуры, составляющей 115 К. Охлажденный второй подпоток 21 поступает на производящее работу расширение во вторую турбину 22, которая приводит в действие электрический генератор 23. Производящий работу при расширении второй подпоток 24, наконец, проходит при давлении 5,5 бар (0,55 МПа) через линию 7 в колонну 50 высокого давления.The second air flow is cooled in the main heat exchange system 3 to a second intermediate temperature of 115 K. The cooled second sub-stream 21 enters the work-producing expansion into the second turbine 22, which drives the electric generator 23. The second sub-stream 24 that performs the work while expanding passes at a pressure of 5.5 bar (0.55 MPa) through line 7 into the high-pressure column 50.
Третий воздушный поток 30 проходит вместе с первым потоком через линии 2, 4 и 6 и 20в поджимающий компрессор 5, но затем проходит через основную теплообменную систему 3 в холодный конец. В ходе этого процесса он сжижается. После дросселирования 31 до давления колонны высокого давления дросселированный третий воздушный поток 32 поступает в колонну 50 высокого давления через линию 7.The third air flow 30 passes along with the first flow through lines 2, 4 and 6 and 20B of the compressing compressor 5, but then passes through the main heat exchange system 3 to the cold end. During this process, it liquefies. After throttling 31 to the pressure of the high pressure column, the throttled third air stream 32 enters the high pressure column 50 through line 7.
Четвертый воздушный поток 40 проходит через основную теплообменную систему 3 от теплого конца до холодного конца при первом давлении р1. После дросселирования 41 до давления колонны высокого давления дросселированный четвертый воздушный поток 42 поступает в колонну 50 высокого давления через линию 7.The fourth air stream 40 passes through the main heat exchange system 3 from the warm end to the cold end at the first pressure p1. After throttling 41 to the pressure of the high pressure column, the throttled fourth air flow 42 enters the high pressure column 50 through line 7.
Поток 52 жидкого кислородного продукта выходит из колонны 51 низкого давления и в жидком состоянии доводится в кислородном насосе 53 до повышенного давления 28 бар (2,8 МПа). Имеющий высокое давление кислород 54 испаряется в основной теплообменной системе 3, нагревается приблизительно до температуры окружающей среды и, наконец, выходит через линию 55 в виде потока газообразного сжатого кислородного продукта (ООХ-1С).The flow 52 of the liquid oxygen product leaves the low pressure column 51 and, in the liquid state, is brought in the oxygen pump 53 to an increased pressure of 28 bar (2.8 MPa). High-pressure oxygen 54 evaporates in the main heat exchange system 3, is heated to approximately ambient temperature, and finally exits through line 55 as a stream of gaseous compressed oxygen product (OOX-1C).
Поток 56 жидкого азотного продукта выводят из колонны 50 высокого давления или из основного конденсатора и в азотном насосе 57 доводится в жидком состоянии до повышенного давления 28 бар (2,8 МПа). При этом повышенном давлении он испаряется в основной теплообменной системе 3, нагревается приблизительно до температуры окружающей среды и, наконец, выходит через линию 59 в виде потока газообразного сжатого азотного продукта (ΟΑΝ-ΙΟ).The stream 56 of the liquid nitrogen product is withdrawn from the high-pressure column 50 or from the main condenser and, in the nitrogen pump 57, is brought in a liquid state to an elevated pressure of 28 bar (2.8 MPa). At this increased pressure, it evaporates in the main heat exchange system 3, is heated to approximately ambient temperature and, finally, leaves through line 59 as a stream of gaseous compressed nitrogen product (ΟΑΝ-ΙΟ).
Далее поток 60 азотного продукта и поток 62 азота с примесями выходят в газообразном состоянии из колонны 51 низкого давления, нагреваются в основной теплообменной системе 3 приблизительно до температуры окружающей среды и используются как имеющий низкое давление азотный продукт (ΟΑΝ) через линию 61 или как регенерационный газ через линию 63.Next, the nitrogen product stream 60 and the nitrogen stream 62 with impurities exit in a gaseous state from the low pressure column 51, are heated in the main heat exchange system 3 to approximately ambient temperature and are used as a low pressure nitrogen product () through line 61 or as regeneration gas through line 63.
Во втором варианте дистилляционная колонная система согласно примерному варианту осуществления дополнительно включает производство аргона; в частности, она содержит колонну неочищенного аргона и колонну чистого аргона (обе они не представлены на чертеже). Жидкий чистый аргон 70 выходит из колонны чистого аргона и доводится в жидком состоянии в аргоновом насосе 71 до повышенного давления 31 бар (3,1 МПа). Имеющий высокое давление аргон 72 испаряется в основной теплообменной системе 3, нагревается приблизительно до температуры окружающей среды и, наконец, выходит через линию 73 в виде потока газообразного сжатого аргонового продукта (ОАК-1С).In the second embodiment, the distillation column system according to the exemplary embodiment further comprises producing argon; in particular, it contains a column of crude argon and a column of pure argon (both are not shown in the drawing). Liquid pure argon 70 leaves the column of pure argon and is brought in a liquid state in an argon pump 71 to an elevated pressure of 31 bar (3.1 MPa). The high pressure argon 72 evaporates in the main heat exchange system 3, is heated to approximately ambient temperature, and finally exits through line 73 as a stream of gaseous compressed argon product (OAK-1C).
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EA201201485A1 (en) | 2013-08-30 |
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