• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    1. A method of producing superheated steam by heat exchange with catalytically methanized synthesis gas, including CO, COj and Hj, a part of the flow of which is passed through a reactor with a built-in water evaporator and then mixed with the rest of the synthesis gas, the mixture is sequentially passed through an adiabatic a reactor, a steam booster and a reactor with an integrated heat exchange surface, to which feed water is supplied, characterized in that, in order to reduce costs, the water in the heat exchange surface is heated to perature saturation and then fed to the evaporator. 2. An apparatus for producing superheated steam in the methanisation of synthesis gas including CO, CO and H, containing a main line in which a reactor with a built-in cooling water evaporator, an adiabatic reactor, a superheater and built-in heat exchange surface for cooling water, all reactors are filled with a catalyst, a reactor with a built-in evaporator has a bypass duct, and the heat exchange surface of the latter is connected to the inlet along the synthesis gas of the reactor To a water supply pipe, characterized in that, in order to reduce costs, the heat exchange surface at the outlet is connected to the evaporator inlet by means of a bypass pipe. 3. The device according to claim 2, about tl and is so that it additionally contains a steam drum connected to the bypass pipeline and additionally connected to an evaporator and an inlet of a superheater. 4. The device according to PP. 2 and 3, about t - l and that the highway on the site located behind U N9 GO with
    公开号:SU1212331A3
    申请号:SU823444647
    申请日:1982-05-26
    公开日:1986-02-15
    发明作者:Хеляйн Бернд；Форверк Манфред；Больтендаль Удо
    申请人:Кернфоршунгсанлаге Юлих Гмбх (Фирма)；Райнише Браунколенверке Аг (Фирма)；
    IPC主号:
    专利说明:

    the latter, along the course of the synthesis gas reactor, is equipped with a gas-water circuit 1 of 1 ng NIKOM included in the water supply pipeline.
    5 The device according to claims 2, 3 and 4, t - characterized by the fact that it additionally contains a gas-gas heat exchanger connected to the main by the heating side after the last along the synthesis gas of the reactor and parallel to the gas-water heat exchange. The invention relates to energy and can be used to produce superheated steam in methanization of synthesis gas.
    The aim of the invention is to reduce the cost of producing superheated steam in the methane synthesis gas by operating the device without compressors for recirculating gas in the line, without supplying heat from the outside to preheat water and synthesis gas and without supplying steam to synthesis gas .
    Fig. 1 schematically shows a device for producing superheated steam; figure 2 - table with the compositions of synthesis gas in certain sections of the highway.
    A device for producing superheated steam at gasification of gas, including CO, GOj and Hj, contains line 1, in which, successively along the synthesis gas, a reactor 2 with an integrated cooling water evaporator 3, an adiabatic reactor 4, a superheater 5 and a reactor are installed 6 with built-in heat exchange surface. 7 For cooling water. Reactors 2, 4 and 6 are filled with catalyst 8, Reactor 2 with a built-in evaporator 3 has a bypass gas reactor 9 with fittings 10. The heat exchange surface 7 of the latter along the synthesis gas of reactor 6 is connected at the inlet to the feed line 11 and is connected to the outlet with the inlet of the reactor 6 -
    12331
    Nick, and the heating one, before the first reactor along the synthesis gas.
    6. The device according to PP.2 - 5, about t - is characterized in that it additionally contains a second gas-gas heat exchanger, connected to the main line by the heating side next to the first gas-gas heat exchanger and the first along the synthesis gas reactor, and the heated one between the superheater and the last in the course of the synthesis gas reactor.
    3 bypass pipe 12.
    Steam drum 13 connected to outlet of evaporator 3 and steam superheater inlet 5 is connected to bypass pipeline 12, and line 1 is equipped with gaseous tag exchanger 14 connected to water supply pipe 11 in the section located downstream of the synthesis gas to the reactor 6. Line 1 by the heating side after the latter along the synthesis gas of the reactor 6 and parallel to the gas-water heat exchanger 14 is inserted a gas-gas heat exchanger 15, which is connected by the heated side to the line 1 before the first along the synthesis gas reaction torus 2.
    The device for producing superheated steam contains a second gas-gas heat exchanger 16 connected in line 1 by the heating side between the first gas-gas heat exchanger 15 and the first reactor 2 along the synthesis gas, and the heated side between the superheater 5 and the last one gas reactor 6.
    A pump 17 is installed on the supply line 11, and a pump 18 is located on the section of the overflow pipe 12 located between the drum 13 and the evaporator 3. A gas cleaner 19 filled with oxide is included in the section of the pipeline 1 located between the gas-gas heat exchanger 16 and the reactor 2 zinc.
    The method is carried out as follows.
    Along the line 1, synthesis gas is passed, the composition of which varies as it passes through individual sections of this line I and interacts with catalyst 8 of reactors 2, 4 and 6 as shown in Figure 2, where q is the initial composition of the gas ; S is the gas composition after reactor 2 and bypass bypass duct 9; L is the composition of the gas after the gas flue 9 and before the adiabatic reactor 4; - the composition of the gas after the adiabatic reactor 4 and before the reactor 6; 3 — gas composition after reactor 6 and before heat exchangers 14 and 15; in - the final composition of the gas.
    The synthesis gas enters the device at a temperature of 10 ° C at a pressure of 41 bar. In the gas-gas heat exchanger 15, the gas is heated to 230 ° C, and in the gas-gas heat exchanger 16 - to. With a temperature of CJSC C, synthesis gas is passed through a scrubber 19 to desulfurize it. After the scrubber 19, the synthesis gas is divided into two streams, the required cost ratio of which is set by the fitting 10. One gas stream with a temperature of 330 ° C at pressure. 40 bar is passed through reactor 2, where it is cooled, returning heat to the evaporator 3, and another stream
    The gas passes through the bypass duct 9 and then mixes with the gas flow passing through the reactor 2. Before the adiabatic reactor 4 the gas has a retf
    The temperature is 325 C and pressure is 39 bar, and after reactor 4, where it is heated as a result of contact with catalyst 8, the temperature is 675 seconds and the pressure is 38.5 bar. After the adiabatic reactor 4, the gas is passed through a superheater 5 and a gas-gas heat exchanger 16, where it is cooled to 300 ° C. at a pressure of 37.5 bar, and then sent to reactor 6,
    where gives heat to the surface 7 of the heat exchanger. After the reactor 6, the gas passes heat exchangers 14 and 15, where it is cooled to the final temperature.
    The initial heated water, which is fed to the line 1, has a temperature of 50 s and a pressure of 3 bar. After the pump 17, the water pressure rises to the PO bar, and after the gas flue -
    heat exchanger 14 water acquires a temperature. In the heat-transfer surface 7 of the reactor 6, it is heated to a temperature of Naziocene equal to 318 C. Next, the heated
    It is fed to the drum 13, from which water is fed through the pump 18 to the evaporator 3 of the reactor 2. In the evaporator 3, the water is converted into saturated steam, which is fed through the drum 13 to the superheater 5, where the steam is heated to a predetermined temperature.
    (picture 1
    FIG. 2
    Soytavitel L. Andreev Editor I. Rybchenko Tehred.Gergel
    Order 653/62 Circulation 399 Subscription
    VNIIPI USSR State Committee
    for inventions and discoveries 113035, Moscow, F - 35, Raushsk nab., 4/5
    Branch GShP Patent, Uzhgorod, Proektna St., 4
    Proofreader A. Obruchar
    权利要求:
    Claims (6)
    [1]
    1. A method of producing superheated steam by heat exchange with a catalytically methanizing synthesis gas, including CO, C0 2 and H 2 , part of the stream of which is passed through a reactor with an integrated water evaporator and then mixed with the rest of the synthesis gas, the resulting mixture is sequentially passed through adiabatic reactor, superheater, reactor with a built-in heat exchange surface, into which feed water is supplied, characterized in that, in order to reduce costs, the water in the heat exchange surface is heated to a temperature Saturation and then fed to the evaporator.
    [2]
    2. The apparatus for producing superheated steam at methanation syngas comprising CO, C0 2 and H 2 comprising a backbone, wherein successively during the syngas reactor fitted with an integrated cooling-water evaporator, an adiabatic reactor, a steam superheater and reproductive actor with embedded a heat exchange surface for cooling water, with all reactors filled with a catalyst, a reactor with a built-in evaporator has a bypass gas duct, and the heat exchange surface of the latter along the synthesis gas of the reactor is connected at the inlet to doprovodyaschemu conduit, characterized in that, to reduce costs, the heat exchange surface at the outlet connected to the inlet of the evaporator through the bypass duct.
    [3]
    3. The device according to claim 2, characterized in that it further comprises a steam drum included in the bypass pipe and further connected to the outlet of the evaporator and the inlet of the superheater.
    [4]
    4. ’The device according to PP. 2 and 3, due to the fact that the main in the section located behind the last along the synthesis gas reactor is equipped with gas-water heat exchange nickname included in the water supply pipe.
    [5]
    5 ”The device according to paragraphs 2,3 and 4, characterized in that it additionally contains a gas-gas heat exchanger connected to the mains by the heating side after the last in the synthesis gas reactor and parallel to the gas-water heat exchanger, and heated before the first along the synthesis gas reactor.
    [6]
    6. The device according to claims 2 to 5, characterized in that it further comprises a second gas-gas heat exchanger included in the mains by the heating side between the first gas-gas heat exchanger and the first reactor along the synthesis gas, and the heated one between the superheater and the last along the synthesis gas reactor.
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    同族专利:
    公开号 | 公开日
    DE3121991C2|1985-11-28|
    JPS586303A|1983-01-13|
    EP0066258A1|1982-12-08|
    CA1192403A|1985-08-27|
    EP0066258B1|1986-01-29|
    AU547028B2|1985-10-03|
    ZA823845B|1983-04-27|
    US4431751A|1984-02-14|
    DE3121991A1|1983-01-05|
    AU8357582A|1982-12-09|
    DK248882A|1982-12-04|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    JPS5320481B2|1972-01-24|1978-06-27|
    DE2440456C3|1974-08-23|1978-06-08|Linde Ag, 6200 Wiesbaden|Process for the purification of a methane-rich gas contaminated with carbon dioxide|
    DE2705151A1|1977-02-08|1978-08-10|Josef Gail|MOLDED PLASTER PIECE AND METHOD OF MANUFACTURING THESE|
    DE2705141C2|1977-02-08|1984-09-13|Linde Ag, 6200 Wiesbaden|Process for the production of methane or methanol|
    DE2729921C3|1977-07-02|1985-01-03|Metallgesellschaft Ag, 6000 Frankfurt|Process for generating a gas that is exchangeable with natural gas|
    DK143162C|1978-12-12|1981-12-14|Topsoee H A S|PROCEDURE AND PLANT FOR THE MANUFACTURING OF A METAN rich gas|DE3511191A1|1985-03-25|1986-09-25|Josef Hubert 5203 Much Schick|Process for producing thermal energy and recovering hydrocarbon compounds|
    JPS62190307A|1986-02-18|1987-08-20|Toyo Engineering Corp|Method of recovering heat of reaction|
    DE3612734C1|1986-04-16|1987-12-17|Kernforschungsanlage Juelich|Process for the catalytic methanation of a synthesis gas containing carbon monoxide, carbon dioxide and hydrogen and reactor for methanation|
    WO1997048639A1|1996-06-21|1997-12-24|Syntroleum Corporation|Synthesis gas production system and method|
    PE17599A1|1996-07-09|1999-02-22|Syntroleum Corp|PROCEDURE TO CONVERT GASES TO LIQUIDS|
    US6011073A|1997-10-10|2000-01-04|Syntroleum Corporation|System and method for converting light hydrocarbons to heavier hydrocarbons with separation of water into oxygen and hydrogen|
    US6794417B2|2002-06-19|2004-09-21|Syntroleum Corporation|System and method for treatment of water and disposal of contaminants produced by converting lighter hydrocarbons into heavier hydrocarbon|
    AU2003279683A1|2002-06-26|2004-01-19|Shell Internationale Research Maatschappij B.V.|Process for the preparation of hydrocarbons|
    US7053128B2|2003-02-28|2006-05-30|Exxonmobil Research And Engineering Company|Hydrocarbon synthesis process using pressure swing reforming|
    US20070245736A1|2006-04-25|2007-10-25|Eastman Chemical Company|Process for superheated steam|
    WO2010078256A1|2008-12-31|2010-07-08|Shell Oil Company|Process for producing a methane-rich gas|
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    AU2010279667B2|2009-08-03|2014-01-23|Shell Internationale Research Maatschappij B.V.|Process for the co-production of superheated steam and methane|
    DE102009059310A1|2009-12-23|2011-06-30|Solar Fuel GmbH, 70565|Highly efficient process for the catalytic methanation of gas mixtures containing carbon dioxide and hydrogen|
    CN103571554A|2012-08-10|2014-02-12|赫多特普索化工设备公司|Process for production of methane rich gas|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3121991A|DE3121991C2|1981-06-03|1981-06-03|Process for generating superheated steam in heat exchange with a synthesis gas to be catalytically methanized and containing carbon monoxide, carbon dioxide and hydrogen, as well as device for carrying out the process|
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