CN109205558B - Conversion device and conversion method for coal-based natural gas - Google Patents
Conversion device and conversion method for coal-based natural gas Download PDFInfo
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- CN109205558B CN109205558B CN201710548350.5A CN201710548350A CN109205558B CN 109205558 B CN109205558 B CN 109205558B CN 201710548350 A CN201710548350 A CN 201710548350A CN 109205558 B CN109205558 B CN 109205558B
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
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- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
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Abstract
The invention discloses a conversion device and a conversion method for coal-based natural gas, wherein the device comprises the following components: the system comprises a raw material filter, a combined type shift reactor, a boiler feed water preheater, a desalted water preheater, a water cooler and a gas-liquid separator which are connected in sequence; the composite shift reactor is characterized in that the upper part in the composite shift reactor is an isothermal catalyst bed layer, the lower part of the composite shift reactor is an adiabatic fixed catalyst bed layer, the middle part of the composite shift reactor is a wound heat exchange tube, the outlet of the raw material filter is connected with the inlet of the wound heat exchange tube, the outlet of the wound heat exchange tube is connected with the inlet of the isothermal catalyst bed layer, and the outlet of the adiabatic fixed catalyst bed layer is connected with a boiler feed water preheater. The scheme of the invention reduces the arrangement of the shift reactor, reduces the pressure drop, and effectively simplifies the heat exchange process and the equipment floor area.
Description
Technical Field
The invention relates to the technical field of coal chemical industry, in particular to a conversion device and a conversion method for coal-based natural gas.
Background
The conversion device is an important link in the process flow of the coal-to-natural gas, and mainly has the function of adjusting the hydrogen-carbon ratio according to the requirements of downstream devices. The most existing conversion devices adopt multi-section heat-insulating fixed bed reactors, a plurality of heat exchangers are arranged to recover reaction heat, the process is complicated, the pressure drop of the device is increased, and the energy consumption and the cost of a downstream purification device and natural gas compression are increased.
Therefore, there is a need for a shift device and a shift method for coal-based natural gas, which can overcome the disadvantages of the prior art, simplify the process, and reduce the number of shift reactors and heat exchangers.
Disclosure of Invention
The invention aims to solve the problems of the current conversion device and process, and simplifies the flow, deepens the reaction balance and reduces the arrangement of a conversion reactor and a heat exchanger by combining the characteristics and the advantages of an adiabatic fixed bed reactor, an isothermal reactor and a wound heat exchange tube.
In order to achieve the above object, there is provided a shift converter for coal-based natural gas according to an aspect of the present invention, the shift converter comprising:
the system comprises a raw material filter, a combined type shift reactor, a boiler feed water preheater, a desalted water preheater, a water cooler and a gas-liquid separator which are connected in sequence;
the upper part in the composite shift reactor is an isothermal catalyst bed layer, the lower part is an adiabatic fixed catalyst bed layer, the middle part is a winding heat exchange tube,
the outlet of the raw material filter is connected with the inlet of the wound heat exchange tube, the outlet of the wound heat exchange tube is connected with the inlet of the isothermal catalyst bed layer, and the outlet of the adiabatic fixed catalyst bed layer is connected with the boiler feed water preheater.
According to another aspect of the present invention, there is provided a transformation method using the transformation apparatus of the present invention, the transformation method comprising the steps of:
raw material gas filtration: the raw material gas is filtered by a raw material filter and then is divided into a first part of raw material gas and a second part of raw material gas;
a first shift reaction: the first part of feed gas enters the isothermal catalyst bed layer to carry out a first shift reaction after being subjected to heat exchange and temperature rise through the wound heat exchange tubes, so that high-temperature gas is formed and medium-pressure steam is generated;
second transformation reaction: the high-temperature gas enters the heat-insulating fixed catalyst bed layer to perform a second shift reaction after being subjected to heat exchange and temperature reduction through the wound heat exchange tube;
generating product gas: and the high-temperature gas subjected to the second shift reaction is subjected to heat release through the boiler feed water preheater, then is mixed with a second part of feed gas, and then sequentially passes through the desalted water preheater, the water cooler and the gas-liquid separator to obtain a product gas.
The technical scheme of the invention has the following beneficial effects:
(1) the shift reactor for coal-based natural gas integrates an adiabatic fixed catalyst bed layer, a wound heat exchange tube and an isothermal shift catalyst bed layer, thereby effectively simplifying the heat exchange process and the equipment occupation;
(2) because a tubular isothermal shift catalyst bed layer is adopted, the shift reaction equilibrium depth is favorably increased, the arrangement of a shift reactor is further reduced, and the pressure drop is reduced;
all the advantages mentioned above make the invention have higher economic benefit, lower comprehensive energy consumption and smaller equipment size compared with the traditional technical method. The invention is particularly suitable for the conversion device for preparing the substitute natural gas from the coal gasification synthesis gas.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in more detail exemplary embodiments thereof with reference to the attached drawings, in which like reference numerals generally represent like parts throughout.
Fig. 1 shows a transformation process flow diagram of the transformation method according to the invention.
Description of the reference numerals
1. The system comprises a raw material filter 2, a combined type shift reactor 3, a boiler feed water preheater 4, a desalted water heat exchanger 5, a water cooler 6, a gas-liquid separator 7, a raw material gas 8, a first part of raw material gas 9, a second part of raw material gas 10, a flow control valve 11, a hydrogen-carbon ratio control signal 12, boiler feed water 13, medium-pressure steam 14, an isothermal catalyst bed layer 15, a wound heat exchange tube 16, an adiabatic fixed catalyst bed layer 17, a product gas
Detailed Description
Preferred embodiments of the present invention will be described in more detail below with reference to the accompanying drawings. While the preferred embodiments of the present invention are shown in the drawings, it should be understood that the present invention may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.
Fig. 1 shows a transformation process flow diagram of the transformation method according to the invention.
As shown in fig. 1, there is provided a shift converter for coal-based natural gas according to an aspect of the present invention, the shift converter comprising:
the system comprises a raw material filter 1, a combined type shift reactor 2, a boiler feed water preheater 3, a desalted water preheater 4, a water cooler 5 and a gas-liquid separator 6 which are connected in sequence;
the upper part in the combined type shift reactor 2 is an isothermal catalyst bed layer 14, the lower part is an adiabatic fixed catalyst bed layer 16, the middle part is a winding type heat exchange tube 15,
the outlet of the raw material filter 1 is connected with the inlet of the wound heat exchange tube 15, the outlet of the wound heat exchange tube 15 is connected with the inlet of the isothermal catalyst bed layer 14, and the outlet of the adiabatic fixed catalyst bed layer 16 is connected with the boiler feed water preheater 3.
According to the present invention, it is preferred that the diameter of both the coiled heat exchange tubes 15 and the adiabatic fixed catalyst bed 16 be greater than the diameter of the isothermal catalyst bed 14.
Since the outlet temperature of the isothermal catalyst bed 14 is relatively low, a large heat exchange area is required for preheating to the required inlet temperature in the coiled heat exchange tube 15, and therefore, the diameter of the coiled heat exchange tube 15 is selected to be increased, which is beneficial to reducing the pressure drop of the system.
According to the present invention, preferably, the isothermal catalyst bed 14 is a fixed bed of tubes, wherein the tubes are boiler feed water 12 and the tubes are catalyst beds.
According to the invention, boiler feed water 12 in the tubes can be used to generate medium pressure steam 13 by means of the heat generated by the first shift reaction, and thus to control the final temperature of the first shift reaction.
Because of the adoption of the tubular isothermal shift catalyst bed, the shift reaction equilibrium depth is increased, the arrangement of a shift reactor is further reduced, and the pressure drop is reduced.
According to the present invention, preferably, the outlet of the raw material filter 1 is also connected to the inlet of the desalted water preheater 4 through a line. Through which a second portion of feed gas 9 is passed directly into the desalted water preheater 4.
According to the present invention, a flow control valve 10 is preferably provided on the pipeline. The flow control valve 10 is used for controlling the flow of the second part of the raw gas 9.
According to another aspect of the present invention, there is provided a transformation method using the transformation apparatus of the present invention, the transformation method including the steps of:
raw material gas filtration: the raw material gas 7 is filtered by the raw material filter 1 and then is divided into a first part of raw material gas 8 and a second part of raw material gas 9;
the feed filter 1 is used for removing solid particle impurities carried in the feed gas 7, so that downstream equipment is prevented from being blocked, the activity of the catalyst is reduced, and the service life of the catalyst is prolonged.
A first shift reaction: the first part of feed gas 8 enters the isothermal catalyst bed layer 14 to perform a first shift reaction after being subjected to heat exchange and temperature rise through the wound heat exchange tube 15, so as to form high-temperature gas and generate medium-pressure steam 13;
preferably, the first part of raw material gas 8 exchanges heat with high-temperature gas formed by the first shift reaction through the wound heat exchange tube 15 to increase the temperature.
The present invention controls the final temperature of the first shift reaction by generating medium pressure steam 13.
Second transformation reaction: the high-temperature gas enters the heat insulation fixed catalyst bed layer 16 to perform a second shift reaction after being subjected to heat exchange and temperature reduction through the wound heat exchange tube 15;
preferably, the high-temperature gas and the first part of raw material gas 8 are subjected to heat exchange and temperature reduction through the wound heat exchange tube 15.
Generating product gas: the high-temperature gas subjected to the second shift reaction is subjected to heat release through the boiler feed water preheater 3, then mixed with a second part of feed gas 9, and then sequentially passes through the desalted water preheater 4, the water cooler 5 and the gas-liquid separator 6 to obtain a product gas 17.
The gas-liquid separator 6 of the present invention is for separating a product gas 17 in a gas phase.
According to the present invention, preferably, the inlet temperature of the isothermal catalyst bed 14 is 220-320 ℃ and the outlet temperature is 300-400 ℃.
According to the present invention, it is preferred that the inlet temperature of the adiabatic fixed catalyst bed 16 is 200-300 ℃.
According to the present invention, it is preferable that the flow rate of the second portion of the raw material gas 9 is controlled according to a hydrogen-carbon ratio signal 11 of a downstream unit. Specifically, the hydrogen-carbon ratio signal 11 controls the flow rate of the second portion of the feed gas 9 through a flow control valve.
Preferably, the flow rate of the second part of the raw gas 9 accounts for 5-40% of the total amount of the raw gas 7.
Example 1
Fresh feed gas from an upstream gasification unit, characterized by the composition: h2，24.2mol％，CO，31.1mol％，CO2，15.1mol％，CH4，2.09mol％，N20.23 mol%, H2O, 27.28 mol%. The temperature was 186 ℃.
As shown in fig. 1, the present invention is a transformation method using the transformation apparatus of the present invention, the transformation method comprising the steps of:
raw material gas filtration: the raw material gas 7 is filtered by the raw material filter 1 and then is divided into a first part of raw material gas 8 and a second part of raw material gas 9; the first part of raw material gas 8 accounts for 75% of the total amount of the raw material gas 7;
a first shift reaction: after the first part of feed gas 8 exchanges heat with high-temperature gas through the wound heat exchange tubes 15 and is heated to 250 ℃, the temperature of the first part of feed gas enters the isothermal catalyst bed layer 14 to perform a first shift reaction, high-temperature gas is formed, medium-pressure steam 13 is generated, and the final temperature of the first shift reaction is controlled to be 300 ℃ by generating the medium-pressure steam 13 with 4.0 MPa;
second transformation reaction: the high-temperature gas exchanges heat with a first part of feed gas 8 through the wound heat exchange tube 15 to reduce the temperature, and enters the heat insulation fixed catalyst bed layer 16 to perform a second shift reaction after the temperature is reduced to 240 ℃;
generating product gas: the high-temperature gas subjected to the second shift reaction is heated to 260 ℃, is mixed with a second part of feed gas 9 after being released by the boiler feed water preheater 3, and then sequentially passes through the desalted water preheater 4, the water cooler 5 and the gas-liquid separator 6 to obtain a product gas 17.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the disclosed embodiments. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the illustrated embodiments.
Claims (9)
1. A shift device for coal-to-natural gas, the device comprising:
the system comprises a raw material filter (1), a combined type shift reactor (2), a boiler feed water preheater (3), a desalted water preheater (4), a water cooler (5) and a gas-liquid separator (6) which are connected in sequence;
the upper part in the combined type shift reactor (2) is an isothermal catalyst bed layer (14), the lower part is an adiabatic fixed catalyst bed layer (16), the middle part is a winding type heat exchange tube (15),
the outlet of the raw material filter (1) is connected with the inlet of the wound heat exchange tube (15), the outlet of the wound heat exchange tube (15) is connected with the inlet of the isothermal catalyst bed layer (14), and the outlet of the adiabatic fixed catalyst bed layer (16) is connected with a boiler feed water preheater (3);
wherein the diameters of the coiled heat exchange tubes (15) and the adiabatic fixed catalyst bed (16) are both greater than the diameter of the isothermal catalyst bed (14).
2. The shift converter for coal-to-natural gas of claim 1, wherein the isothermal catalyst bed (14) is a fixed tubular bed with boiler feed water (12) inside the tubular and a catalyst bed outside the tubular.
3. The shift arrangement for coal-to-natural gas according to claim 1, wherein the outlet of the feed filter (1) is further connected to the inlet of the demineralized water preheater (4) by means of a pipeline.
4. The shift device for coal-based natural gas according to claim 3, wherein a flow control valve (10) is provided on the pipeline.
5. A transformation method using the transformation device according to any one of claims 1 to 4, characterized in that the transformation method comprises the steps of:
raw material gas filtration: the feed gas (7) is filtered by the feed filter (1) and then is divided into a first part of feed gas (8) and a second part of feed gas (9);
a first shift reaction: the first part of feed gas (8) enters the isothermal catalyst bed layer (14) to perform a first shift reaction after being subjected to heat exchange and temperature rise through the wound heat exchange tube (15), so that high-temperature gas is formed and medium-pressure steam (13) is generated;
second transformation reaction: the high-temperature gas enters the heat insulation fixed catalyst bed layer (16) to perform a second shift reaction after being subjected to heat exchange and temperature reduction through the wound heat exchange tube (15);
generating product gas: and the high-temperature gas subjected to the second shift reaction is subjected to heat release through the boiler feed water preheater (3), then is mixed with a second part of feed gas (9), and then sequentially passes through the desalted water preheater (4), the water cooler (5) and the gas-liquid separator (6) to obtain a product gas (17).
6. The shift method as claimed in claim 5, wherein the inlet temperature of the isothermal catalyst bed (14) is 220-320 ℃ and the outlet temperature is 300-400 ℃.
7. The shift method as claimed in claim 5, wherein the inlet temperature of the adiabatic fixed catalyst bed (16) is 200-300 ℃.
8. The shift conversion process according to claim 5, wherein the flow rate of the second portion of feed gas (9) is 5-40% of the total amount of feed gas (7).
9. A shift conversion method according to claim 8, wherein the flow rate of the second portion of feed gas (9) is controlled in dependence of a hydrogen to carbon ratio signal (11) of a downstream unit.
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| CN201710548350.5A CN109205558B (en) | 2017-07-06 | 2017-07-06 | Conversion device and conversion method for coal-based natural gas |
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| CN201710548350.5A CN109205558B (en) | 2017-07-06 | 2017-07-06 | Conversion device and conversion method for coal-based natural gas |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20070293590A1 (en) * | 2004-05-28 | 2007-12-20 | Ammonia Casale S.A. | Method for Carrying Out Heterogeneous Catalytic Exothermic Gas Phase Reactions |
| CN104150439A (en) * | 2014-07-21 | 2014-11-19 | 中国五环工程有限公司 | Carbon monoxide shifting process |
| CN104774663A (en) * | 2015-04-27 | 2015-07-15 | 中国五环工程有限公司 | Synthetic natural gas prepared from one-step process coal and system thereof |
| CN205398571U (en) * | 2016-03-11 | 2016-07-27 | 山西高碳能源低碳化利用研究设计院有限公司 | Coke oven gas methanation reaction unit |
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- 2017-07-06 CN CN201710548350.5A patent/CN109205558B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20070293590A1 (en) * | 2004-05-28 | 2007-12-20 | Ammonia Casale S.A. | Method for Carrying Out Heterogeneous Catalytic Exothermic Gas Phase Reactions |
| US7683099B2 (en) * | 2004-05-28 | 2010-03-23 | Ammonia Casale S.A. | Method for carrying out heterogeneous catalytic exothermic gas phase reactions |
| CN104150439A (en) * | 2014-07-21 | 2014-11-19 | 中国五环工程有限公司 | Carbon monoxide shifting process |
| CN104774663A (en) * | 2015-04-27 | 2015-07-15 | 中国五环工程有限公司 | Synthetic natural gas prepared from one-step process coal and system thereof |
| CN205398571U (en) * | 2016-03-11 | 2016-07-27 | 山西高碳能源低碳化利用研究设计院有限公司 | Coke oven gas methanation reaction unit |
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