• 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:
    The invention relates to petrochemistry, in particular the catalytic methanization of synthesis gas containing carbon monoxide, carbon dioxide and hydrogen. The goal is to simplify the process. It is brought into contact with the synthesis gas with a catalyst bed of solids with the gas passing successively through the injection area, through the high temperature synthesis gas (HOT-SPOT) area and the output area from the catalyst bed with a decreasing synthesis gas temperature with cooling catalyst refrigerant. The latter is evaporated due to the heat of methanization in the output area and the HOT-SPOT area and the resulting steam is overheated in the HOT-SPOT area (this makes it easier to control the desired process flow). The resulting exhaust gas contains,%: 58.66 H 2O 39,13 CH 4 1.89 H 2 (carbon oxides are absent), has a temperature of 315 ° C at a pressure of 47 bar and a speed of 1.67 kg / s. 3 il.
    公开号:SU1597094A3
    申请号:SU874202375
    申请日:1987-04-14
    公开日:1990-09-30
    发明作者:Ранге Йохен；Хелайн Бернд；Ниссен Ханс；Фау Фолькер；Х.И.Р.Шибан；Хоффманн Хорст；Форверк Манфред
    申请人:Кернфоршунгсанлаге Юлих Гмбх (Фирма)；
    IPC主号:
    专利说明:

    Synthesis gas is reduced. The refrigerant, which removes heat from the solid in the catalyst bed, is evaporated in the outlet area and in the Hot-spot area, and the resulting vapor is superheated in the Hot-Spot area. Thus, the heat release from the hot-spot area is not only used to produce superheated steam, but part of the heat is also given off to evaporate the refrigerant, which facilitates the controllability of the desired process flow.
    FIG. I shows the diagrams of the installation for carrying out the proposed method (Sb-synthesis gas, W - water, SW- - Boiling water, W superheated steam, PG - product-gas).
    The methanization reactor 1 contains a catalyst bed 2, permeated by a cooling system consisting of evaporator 3 and superheater 4. Between evaporator 3 and superheater 4, a steam chamber 5 is turned on, in which vapor coming out of evaporator 3 is collected through connecting pipe 6 with him still non-evaporated liquid. Pipe 7 is connected to the top of the steam chamber 5, which leads dried steam accumulated here to the superheater 4. Water is used as a refrigerant, which before entering the methanization reactor through pipeline 8 is passed through preheaters 9 and 10, in which water entering through inlet 11 at room temperature, is heated to the required inlet temperature at the inlet of refrigerant 12 during heat exchange with the product gas leaving the methanization reactor 1 through the pipeline 13 for the product gas Steam, superheated in the superheater 4, goes from above Coolant water from the methanisation reactor 14 to the steam line 15 and from there can flow as a working fluid, for example, into a steam
    turbine .. 1.
    The methanization reactor 1 in the course of the movement of synthesis gas 16 has three 8OH with characteristic M progress in the catalyst bed. According to this, the temporal profile in the catalyst bed, the methanization reactor with a stable operating mode is divided into regions
    input A with a steeply rising temperature, to the Hot-Spot region B with a temperature maximum in the catalyst bed and output area C with a constantly falling temperature.
    FIG. Figure 2 shows the design of the methanization reactor and cooling system. The evaporator 3 of the cooling system passes through the entire length of the catalyst bed from exit area C through Hot-Spot area B up to input area A of reactor 1. Superheater 4 is located in Hot-Spot-area, it also enters output area C, so superheater and evaporator are superimposed on each other. The heat transfer required simultaneously to the superheater 4 and the evaporator 3 can be achieved by the fact that the steam superheating pipelines go inside the catalyst tube containing catalyst particles, so that the reaction heat is absorbed by both the evaporating refrigerant that surrounds the catalyst tube and the superheated .ferry.
    Example 1. 1.27 kg / s of synthesis gas is introduced into the methanisation unit via pipeline 17, which contains the following gas fractions,% by volume: 1, SI 13.51, CO 8.93, CO 10.07, H j67.48. The synthesis gas in the preheater 18 is heated to approximately 180 ° C and in part 17 of the synthesis gas pipeline 17 is mixed with saturated steam 19 entering the displacement point via tee 20 with a temperature under pressure of 50 bar with the bypass closed at 17 s all synthesis gas passes through a conversion reactor 21, in which it is heated by the reaction of partial conversion of carbon monoxide to carbon dioxide. It is then introduced at a temperature of 280 ° C through nozzle 22 for synthesis gas into the methanization reactor 1.
    权利要求:
    Claims (2)
    [1]
    After the synthesis gas is transformed into the methanation reactor, a product-gas product is obtained at the product gas outlet, containing, vol.%: 58.66, CH 4. 39.13, CO O, CO 0.35, and H 1.89. The product gas leaves the methanization reactor at a pressure of 47 bar with temperature. The product gas mass flow in the product gas pipeline is 1.67 kg / s. After passing through the preheaters 9, 10 and 18, and after separating from the water in the separators 23 and 24, liquid at the outlet of gas 25 produces a gas product with a share of 94.6% by volume of methane. For removal of heat, which is installed in the plant for methane emission, a 1.89 kg / s of cooling water with a temperature of about 20 ° C is fed through the refrigerant pipe at inlet 11. The cooling water is heated in preheaters 9 and 10 up to 260 ° C, with which it is introduced into the steam chamber .5. In the steam chamber, the cooling water is brought to a pressure of 100 bar and introduced into the evaporator 3, in which it evaporates at an evaporation temperature of 311 ° C. The resulting steam is returned to the steam chamber 5 and passes through the connecting pipe 6 to the superheater 4, where the steam is superheated to a pressure of 100 bar. 1.49 kg / s of superheated steam is removed from the methanization unit. Residual steam in the amount of 0.4 kg / s from the steam chamber 5 through the extraction line 19 and the tee 20 enters the synthesis gas. The maximum temperature of synthesis gas in the catalyst bed is 650–655 ° C. Example
    [2]
    2. The method is carried out analogously to Example 1, but in a methanization reactor, characterized by the location of the coolant system, in the catalyst bed. A diagram of the methanization reactor and cooling system as well as the course of the temperature of the synthesis gas in the catalyst bed are shown in. FIG. Figures 3 and 2 show the dependences of the change in the temperature of the refrigerant along the length of the catalyst bed (SD is vapor at the evaporation temperature). In this case, the superheater 4 is located exclusively in the Hot-Spot area - area B. When implementing the method, the quantity, composition and parameters of the material flows are the same as for example 1. The maximum temperature of the synthesis gas in the catalyst bed is 640-645 C. Claims catalytic methanization of synthesis gas containing carbon monoxide, carbon dioxide and hydrogen by contacting it with a catalyst layer of solids while passing synthesis gas in a catalyst layer successively through the synthesis gas inlet area a, a region with a high temperature of synthesis gas (Hot-spot region) and a region of withdrawal from a catalyst bed with a decreasing temperature of synthesis gas with a cooling of the catalyst layer with a refrigerant that is evaporated due to the heat of methanization, and the resulting vapor is superheated in the Hot Spot - area, characterized in that, in order to simplify the process technology, the refrigerant is evaporated in the output area and the Hot-Spot area.
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    类似技术:
    公开号 | 公开日 | 专利标题
    SU1597094A3|1990-09-30|Method of catalytic methanization of synthesis gas
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    SU1368455A1|1988-01-23|Steam-gas unit complex
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    同族专利:
    公开号 | 公开日
    EP0241902A1|1987-10-21|
    US4839391A|1989-06-13|
    DK148287A|1987-10-17|
    AU7158287A|1987-10-22|
    CN87102871A|1987-11-18|
    CN1011965B|1991-03-13|
    DK148287D0|1987-03-23|
    AU591267B2|1989-11-30|
    DE3612734C1|1987-12-17|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2662911A|1948-10-01|1953-12-15|Metallgesellschaft Ag|Temperature control in the catalytic hydrogenation of carbon monoxide|
    DE2705141C2|1977-02-08|1984-09-13|Linde Ag, 6200 Wiesbaden|Process for the production of methane or methanol|
    DE2834589C3|1978-08-07|1994-11-17|Didier Eng|Process for the catalytic conversion of a carbon dioxide and hydrogen-rich, low-sulfur feed gas mixture|
    DK143162C|1978-12-12|1981-12-14|Topsoee H A S|PROCEDURE AND PLANT FOR THE MANUFACTURING OF A METAN rich gas|
    DE3121991C2|1981-06-03|1985-11-28|Kernforschungsanlage Jülich GmbH, 5170 Jülich|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|DK169696B1|1992-12-07|1995-01-16|Topsoe Haldor As|Process for cooling synthesis gas in a catalytic reactor|
    US6419888B1|2000-06-02|2002-07-16|Softrock Geological Services, Inc.|In-situ removal of carbon dioxide from natural gas|
    EP1800739A1|2005-12-23|2007-06-27|Methanol Casale S.A.|Method for controlling the temperature of exothermic chemical reactions|
    WO2010078256A1|2008-12-31|2010-07-08|Shell Oil Company|Process for producing a methane-rich gas|
    CN101817716B|2009-02-27|2013-05-01|中国科学院过程工程研究所|Method and device for catalyzing methanation of synthesis gas|
    PL2462088T3|2009-08-03|2017-01-31|Shell Internationale Research Maatschappij B.V.|Process for the production of methane|
    AU2010279667B2|2009-08-03|2014-01-23|Shell Internationale Research Maatschappij B.V.|Process for the co-production of superheated steam and methane|
    CN102234213B|2010-04-20|2013-05-01|中国科学院过程工程研究所|Complete methanation reaction device for synthesis gas|
    FR3010915B1|2013-09-26|2017-08-11|Gdf Suez|A METHANATION REACTOR FOR REACTING HYDROGEN WITH AT LEAST ONE CARBON-BASED COMPOUND AND PRODUCING METHANE AND WATER|
    WO2015092006A2|2013-12-20|2015-06-25|Basf Se|Two-layer catalyst bed|
    DE102014010055A1|2014-07-07|2016-01-07|Etogas Gmbh|Method for operating a reactor|
    CN104353403B|2014-10-21|2016-08-17|浙江大学|A kind of realize the system that energy recovery couples with continuous coke cleaning|
    DE102016110498A1|2016-06-07|2017-12-21|Karlsruher Institut für Technologie|Microreactor and process control for methanation|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE19863612734|DE3612734C1|1986-04-16|1986-04-16|Process for the catalytic methanation of a synthesis gas containing carbon monoxide, carbon dioxide and hydrogen and reactor for methanation|
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