CN109205558A - A kind of converting means and transform method for natural gas from coal - Google Patents
A kind of converting means and transform method for natural gas from coal Download PDFInfo
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- CN109205558A CN109205558A CN201710548350.5A CN201710548350A CN109205558A CN 109205558 A CN109205558 A CN 109205558A CN 201710548350 A CN201710548350 A CN 201710548350A CN 109205558 A CN109205558 A CN 109205558A
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- gas
- catalyst bed
- heat exchanger
- winding type
- converting means
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- 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
- C01B3/32—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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
Abstract
The invention discloses a kind of converting means and transform method for natural gas from coal, which includes: sequentially connected raw material filter, combined type shift-converter, feedwater preheater, demineralized-water preheater, water cooler and gas-liquid separator；Top in the combined type shift-converter is Isothermal Catalyst bed, lower part is insulation fixed catalyst bed, middle part is winding type heat exchanger pipe, the outlet of the raw material filter is connected with the entrance of the winding type heat exchanger pipe, the outlet of the winding type heat exchanger pipe is connected with the entrance of the Isothermal Catalyst bed, and the outlet of the insulation fixed catalyst bed is connect with feedwater preheater.The solution of the present invention reduces the setting of shift-converter, reduces pressure drop, is effectively simplified heat exchange process and equipment land occupation.
Description
Technical field
The present invention relates to technical field of coal chemical industry, more particularly, to a kind of converting means for natural gas from coal and
Transform method.
Background technique
Converting means is link important in natural gas from coal process flow, and main function is the needs according to downstream unit
Adjust hydrogen-carbon ratio.The existing converting means overwhelming majority uses multistage insulation fixed bed reactor, and more heat exchangers are arranged and return
Receive heat of reaction, process is cumbersome, device pressure drop increase, increase downstream purification device and natural gas compressing energy consumption and at
This.
Therefore, it is necessary to provide a kind of converting means and transform method for natural gas from coal, the prior art can be overcome
In disadvantage, simple flow, reduce shift-converter and heat exchanger setting.
Summary of the invention
Present invention aim to address Current Transform device and technique there are the problem of, pass through and combine insulation fix bed reaction
The characteristics of device, isothermal reactor, winding type heat exchanger pipe and advantage simplify process, deepen reaction balance, reduce conversion reaction
The setting of device, heat exchanger.
To achieve the goals above, a kind of converting means for natural gas from coal is provided according to an aspect of the present invention,
The device includes:
Sequentially connected raw material filter, combined type shift-converter, feedwater preheater, demineralized-water preheater, water
Cooler and gas-liquid separator；
Top in the combined type shift-converter is Isothermal Catalyst bed, and lower part is insulation stationary catalyst bed
Layer, middle part are winding type heat exchanger pipe,
The outlet of the raw material filter is connected with the entrance of the winding type heat exchanger pipe, the winding type heat exchanger pipe
Outlet is connected with the entrance of the Isothermal Catalyst bed, and the outlet and boiler feedwater of the insulation fixed catalyst bed preheat
Device connection.
A kind of transform method using converting means of the invention, the transform method are provided according to another aspect of the present invention
Include the following steps:
Unstripped gas filtering: unstripped gas is divided into first part's unstripped gas and second part raw material after the filtering of raw material filter
Gas；
First conversion reaction: first part's unstripped gas is described by entering after winding type heat exchanger pipe heat exchange heating
First conversion reaction occurs for Isothermal Catalyst bed, forms High Temperature Gas and middle pressure steam occurs；
Second conversion reaction: the High Temperature Gas is fixed by entering the insulation after winding type heat exchanger pipe heat exchange cooling
Second conversion reaction occurs for catalyst bed；
Generate product gas: after the High Temperature Gas of second conversion reaction is by the feedwater preheater heat release and
The mixing of second part unstripped gas, then passes sequentially through the demineralized-water preheater, water cooler and gas-liquid separator, obtains product
Gas.
Technical solution of the present invention has the following beneficial effects:
(1) for natural gas from coal shift-converter be integrated with insulation fixed catalyst bed, winding type heat exchanger pipe and
Equal intermediate temp conversion catalysts bed is effectively simplified heat exchange process and equipment land occupation；
(2) because using the intermediate temp conversion catalysts beds such as shell and tube, it is conducive to increase conversion reaction equilibrium depth, further
The setting for reducing shift-converter, reduces pressure drop；
Above-mentioned all advantages make the present invention compared with traditional technology method, have higher economic benefit, lower
Comprehensive energy consumption, smaller equipment size.Present invention is particularly suitable for the converting means that synthesis gas from coal gasification produces substitution natural gas.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
Exemplary embodiment of the invention is described in more detail in conjunction with the accompanying drawings, it is of the invention above-mentioned and its
Its purpose, feature and advantage will be apparent, wherein in exemplary embodiment of the invention, identical reference label
Typically represent same parts.
Fig. 1 shows the conversion process flow chart of transform method according to the present invention.
Description of symbols
1, raw material filter 2, combined type shift-converter 3, feedwater preheater 4, desalination water- to-water heat exchanger 5, water
Cooler 6, gas-liquid separator 7, unstripped gas 8, first part's unstripped gas 9, second part unstripped gas 10, flow control valve
11, hydrogen-carbon ratio controls signal 12, boiler feedwater 13, middle pressure steam 14, Isothermal Catalyst bed 15, winding type heat exchanger pipe
16, fixed catalyst bed 17, product gas are insulated
Specific embodiment
The preferred embodiment that the present invention will be described in more detail below with reference to accompanying drawings.Although showing the present invention in attached drawing
Preferred embodiment, however, it is to be appreciated that may be realized in various forms the present invention without the embodiment party that should be illustrated here
Formula is limited.On the contrary, thesing embodiments are provided so that the present invention is more thorough and complete, and can will be of the invention
Range is completely communicated to those skilled in the art.
Fig. 1 shows the conversion process flow chart of transform method according to the present invention.
As shown in Figure 1, providing a kind of converting means for natural gas from coal, the device according to an aspect of the present invention
Include:
Sequentially connected raw material filter 1, combined type shift-converter 2, feedwater preheater 3, demineralized-water preheater
4, water cooler 5 and gas-liquid separator 6；
Top in the combined type shift-converter 2 is Isothermal Catalyst bed 14, and lower part is insulation fixed catalyst
Bed 16, middle part are winding type heat exchanger pipe 15,
The outlet of the raw material filter 1 is connected with the entrance of the winding type heat exchanger pipe 15, the winding type heat exchanger
The outlet of pipe 15 is connected with the entrance of the Isothermal Catalyst bed 14, the outlet of the insulation fixed catalyst bed 16 and pot
Furnace feed water preheater 3 connects.
In accordance with the present invention it is preferred that the diameter of the winding type heat exchanger pipe 15 and the insulation fixed catalyst bed 16
It is all larger than the diameter of the Isothermal Catalyst bed 14.
Since the outlet temperature of the Isothermal Catalyst bed 14 is relatively low, in order to be preheated in winding type heat exchanger pipe 15
To the inlet temperature of requirement, biggish heat exchange area is needed, therefore selects to increase the diameter of winding type heat exchanger pipe 15, it is advantageous in this way
In reduction system pressure drop.
In accordance with the present invention it is preferred that, wherein the Isothermal Catalyst bed 14 be it is calandria type fixed bed, be in tubulation
Boiler feedwater 12, tubulation are outside catalyst bed.
According to the present invention, it can be steamed by being pressed in the heat generation of the first conversion reaction generation in tubulation for boiler feedwater 12
Vapour 13, and then control the final temperature of the first conversion reaction.
Because using the intermediate temp conversion catalysts beds such as shell and tube, it is conducive to increase conversion reaction equilibrium depth, further subtracts
The setting of few shift-converter, reduces pressure drop.
In accordance with the present invention it is preferred that the outlet of the raw material filter 1 also passes through pipeline and the demineralized-water preheater 4
Entrance connection.Second part unstripped gas 9 is directly entered the demineralized-water preheater 4 by this pipeline.
In accordance with the present invention it is preferred that being provided with flow control valve 10 on the pipeline.The flow control valve 10 is for controlling
The flow of second part unstripped gas 9 processed.
A kind of transform method using converting means of the invention, the transformation side are provided according to another aspect of the present invention
Method includes the following steps:
Unstripped gas filtering: unstripped gas 7 is divided into first part's unstripped gas 8 and second part after the filtering of raw material filter 1
Unstripped gas 9；
The raw material filter 1 for removing entrained solid granule foreign in unstripped gas 7, avoid clog downstream equipment,
Reduce catalyst activity and service life.
First conversion reaction: first part's unstripped gas 8 after the winding type heat exchanger pipe 15 heat exchange heating by entering
First conversion reaction occurs for the Isothermal Catalyst bed 14, forms High Temperature Gas and middle pressure steam 13 occurs；
Preferably, first part's unstripped gas 8 passes through the winding type heat exchanger pipe 15 and the first conversion reaction
The High Temperature Gas of formation carries out heat exchange heating.
The present invention controls the final temperature of first conversion reaction by the way that middle pressure steam 13 occurs.
Second conversion reaction: the High Temperature Gas is solid by entering the insulation after the winding type heat exchanger pipe 15 heat exchange cooling
Determine catalyst bed 16 and the second conversion reaction occurs；
Preferably, the High Temperature Gas is changed by the winding type heat exchanger pipe 15 and first part unstripped gas 8
Heat drop temperature.
Generate product gas: after the High Temperature Gas of second conversion reaction is by 3 heat release of feedwater preheater
It is mixed with second part unstripped gas 9, then passes sequentially through the demineralized-water preheater 4, water cooler 5 and gas-liquid separator 6, obtained
Product gas 17.
Gas-liquid separator 6 of the invention is used to isolate the product gas 17 of gas phase.
In accordance with the present invention it is preferred that the inlet temperature of the Isothermal Catalyst bed 14 is 220-320 DEG C, outlet temperature
It is 300-400 DEG C.
In accordance with the present invention it is preferred that the inlet temperature of the insulation fixed catalyst bed 16 is 200-300 DEG C.
In accordance with the present invention it is preferred that hydrogen-carbon ratio signal 11 of the flow of the second part unstripped gas 9 according to downstream units
It is controlled.Specifically, the hydrogen-carbon ratio signal 11 controls the flow of the second part unstripped gas 9 by flow control valve.
Preferably, the flow of the second part unstripped gas 9 accounts for the 5%-40% of 7 total amount of unstripped gas.
Embodiment 1
Fresh feed gas from upstream gasification member, feature composition are as follows: H2, 24.2mol%, CO, 31.1mol%, CO2,
15.1mol%, CH4, 2.09mol%, N2, 0.23mol%, H2O, 27.28mol%.186 DEG C of temperature.
As shown in Figure 1, the present invention has passed through a kind of transform method using converting means of the invention, the transform method packet
Include following steps:
Unstripped gas filtering: unstripped gas 7 is divided into first part's unstripped gas 8 and second part after the filtering of raw material filter 1
Unstripped gas 9；First part's unstripped gas 8 accounts for the 75% of 7 total amount of unstripped gas；
First conversion reaction: first part's unstripped gas 8 is risen by the winding type heat exchanger pipe 15 and High Temperature Gas heat exchange
Wen Hou, temperature reach 250 DEG C, and the first conversion reaction occurs subsequently into the Isothermal Catalyst bed 14, forms High Temperature Gas simultaneously
Middle pressure steam 13 occurs, controls the first conversion reaction final temperature at 300 DEG C by the way that 4.0MPa middle pressure steam 13 occurs；
Second conversion reaction: the High Temperature Gas is dropped by the winding type heat exchanger pipe 15 and the heat exchange of first part's unstripped gas 8
Temperature, temperature enter the insulation fixed catalyst bed 16 after being down to 240 DEG C and the second conversion reaction occur；
Product gas: the High Temperature Gas Jing Guo second conversion reaction is generated, temperature is 260 DEG C, passes through the boiler feedwater
It is mixed after 3 heat release of preheater with second part unstripped gas 9, it is gentle then to pass sequentially through the demineralized-water preheater 4, water cooler 5
Liquid/gas separator 6 obtains product gas 17.
The embodiment of the present invention is described above, above description is exemplary, and non-exclusive, and also not
It is limited to disclosed embodiment.Without departing from the scope and spirit of embodiment described, for the art
Those of ordinary skill for many modifications and changes are obvious.
Claims (10)
1. a kind of converting means for natural gas from coal, which is characterized in that the device includes:
Sequentially connected raw material filter (1), combined type shift-converter (2), feedwater preheater (3), demineralized water preheating
Device (4), water cooler (5) and gas-liquid separator (6)；
Top in the combined type shift-converter (2) is Isothermal Catalyst bed (14), and lower part is insulation fixed catalyst
Bed (16), middle part are winding type heat exchanger pipe (15),
The outlet of the raw material filter (1) is connected with the entrance of the winding type heat exchanger pipe (15), the winding type heat exchanger
The outlet of pipe (15) is connected with the entrance of the Isothermal Catalyst bed (14), and insulation fixed catalyst bed (16) goes out
Mouth is connect with feedwater preheater (3).
2. the converting means according to claim 1 for natural gas from coal, wherein the winding type heat exchanger pipe (15) and
The diameter of insulation fixed catalyst bed (16) is all larger than the diameter of the Isothermal Catalyst bed (14).
3. the converting means according to claim 1 for natural gas from coal, wherein the Isothermal Catalyst bed (14)
To be calandria type fixed bed, it is in tubulation boiler feedwater (12), is catalyst bed outside tubulation.
4. the converting means according to claim 1 for natural gas from coal, wherein the raw material filter (1) goes out
Mouth is also connect by pipeline with the entrance of the demineralized-water preheater (4).
5. the converting means according to claim 4 for natural gas from coal, wherein be provided with flow control on the pipeline
Valve (10) processed.
6. a kind of transform method using converting means of any of claims 1-5, which is characterized in that the transformation side
Method includes the following steps:
Unstripped gas filtering: unstripped gas (7) is divided into first part's unstripped gas (8) and second after raw material filter (1) is filtered
Divide unstripped gas (9)；
First conversion reaction: first part's unstripped gas (8) after the winding type heat exchanger pipe (15) heat exchange heating by entering
First conversion reaction occurs for the Isothermal Catalyst bed (14), forms High Temperature Gas and middle pressure steam (13) occur；
Second conversion reaction: the High Temperature Gas is fixed by entering the insulation after the winding type heat exchanger pipe (15) heat exchange cooling
Second conversion reaction occurs for catalyst bed (16)；
Generate product gas: by the High Temperature Gas of second conversion reaction is by the feedwater preheater (3) heat release after and
Second part unstripped gas (9) mixing, then passes sequentially through the demineralized-water preheater (4), water cooler (5) and gas-liquid separator
(6), product gas (17) are obtained.
7. transform method according to claim 6, wherein the inlet temperature of the Isothermal Catalyst bed (14) is 220-
320 DEG C, outlet temperature is 300-400 DEG C.
8. transform method according to claim 6, wherein it is described insulation fixed catalyst bed (16) inlet temperature be
200-300℃。
9. transform method according to claim 6, wherein the flow of the second part unstripped gas (9) accounts for unstripped gas (7)
The 5%-40% of total amount.
10. transform method according to claim 9, wherein the flow of the second part unstripped gas (9) is according to downstream list
The hydrogen-carbon ratio signal (11) of member is controlled.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710548350.5A CN109205558B (en) | 2017-07-06 | 2017-07-06 | Conversion device and conversion method for coal-based natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710548350.5A CN109205558B (en) | 2017-07-06 | 2017-07-06 | Conversion device and conversion method for coal-based natural gas |
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| Publication Number | Publication Date |
|---|---|
| CN109205558A true CN109205558A (en) | 2019-01-15 |
| CN109205558B CN109205558B (en) | 2020-08-04 |
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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 |
-
2017
- 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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