CN102453564A - Carbon emission-free one-step method and equipment for synthesizing artificial natural gas - Google Patents
Carbon emission-free one-step method and equipment for synthesizing artificial natural gas Download PDFInfo
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- CN102453564A CN102453564A CN2010105197639A CN201010519763A CN102453564A CN 102453564 A CN102453564 A CN 102453564A CN 2010105197639 A CN2010105197639 A CN 2010105197639A CN 201010519763 A CN201010519763 A CN 201010519763A CN 102453564 A CN102453564 A CN 102453564A
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- gas
- natural gas
- sweet natural
- carbon
- methanation
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Abstract
The invention discloses a method for preparing synthetic natural gas from coal-formed gas, coke-oven gas and the like through methanation one-step reaction. The method is characterized in that: in the production of the synthetic artificial natural gas, CO2 emission is avoided, namely the artificial natural gas is synthesized at zero carbon emission, the flow is simple, a few pieces of equipment is arranged, the temperature resistance requirement of a methanation catalyst is low, no recycle or a low recycle ratio is achieved, and electricity is saved.
Description
Technical field
The present invention relates to the method and apparatus of the synthetic artificial Sweet natural gas of a kind of non-carbon-emitting single stage method, belong to field of chemical engineering.
Background technology
Make synthetic gas by gasification, with H wherein
2, CO, CO
2Carry out methanation reaction and can produce various artificial Sweet natural gases, reaction formula is following:
CO+3H
2＝CH
4+H
2O +206KJ/mol (1)
CO
2+4H
2＝CH
4+2H
2O +165KJ/mol (2)
Because methanation reaction (1) and (2) they are strong exothermal reaction, thus must control the temperature in the methanator in the synthetic gas methanation, to prevent the overheated of catalyst reactor.And, owing to help the formation of methane under the low temperature, see that from the equilibrated viewpoint high temperature is disadvantageous, high temperature has reduced synthetic gas and has changed into methane.The ordinary method of prior art controlled temperature in the methanation reaction process need be used the complex appts that comprises a plurality of heat exchangers and gas circulator; To cool off elute gas and to prevent the overheated of methanator; Chinese patent CN101560423A like the application of nearest disclosed Casale company; Application number 200910135203 (seeing accompanying drawing 1) with the synthetic parallel adiabatic reactor that feeds of virgin gas, adopts adiabatic reactor and tower external heat exchanger simultaneously; Methanation reaction is carried out in many series connection, because CO or CO
2Add H
2Methanation reaction heat very big, therefore one is the way that adopts reaction-heat exchange cooling-reaction to hocket, this just increases the table of equipment number, even like this, the exhaust gas temperature is also up to 600 ℃; The 2nd, adopt circulation gas to reduce into the CO content of methanation reaction gas and control reaction heat, this has just increased power consumption.
At publication CN101508922A, in the application number 200910058611, with in the applying for a patent of preparing synthesis gas from coke oven gas, through CO+CO in the dilution inlet gas
2＜3.5%, Outlet Gas Temperature is dropped to＜450 ℃.
The existing coal that uses is as in the artificial natural gas method of raw material system, no matter use which kind of gasification process, oxycarbide compares H in the synthetic gas of gained
2Many, and in the synthesizing methane preparing natural gas, H
2With oxycarbide be by (H
2-CO
2)/(CO+CO
2)=3 consume, and O is arranged in synthetic gas
2The time H that also can react
2+ 1/2O
2=H
2Therefore O has a large amount of CO in making artificial Sweet natural gas
2Discharging, for example big plain in u.s.a preparing methane from coal factory daily output 3890km
3Need discharge 5660km during (2064 tons) synthesizing methane gas
3/ day (11118 tons) CO
2(see blue or green favorable to the people engineering---the preparing methane from coal of Tang Hong; " nitrogenous fertilizer and methyl alcohol ", November in 2009 the 6th phase P120), and China has the discharging of a large amount of coke(oven)gas to utilize in coal coking; And coke(oven)gas is a hydrogen rich gas; When with the artificial Sweet natural gas of coke(oven)gas synthesizing methane system, then there are a large amount of hydrogen superfluous, synthetic each composition such as table 1 of methanation under the 1MPa pressure for example, i.e. CH in the methane synthetic gas in the 100mol exhaust gas
4Be 52%, excessive H in working off one's feeling vent one's spleen
243% (Chinese publication, publication number CN1919985A, application number 200610021836) nearly, this does not meet the national standard of China's natural gas and compressed natural gas, also need be through transformation fractionation by adsorption H
2And methane.
Subordinate list 1
| Title | H 2 | CO | CO 2 | O 2 | CH 4 | N 2 | H 2O |
| Raw coke oven gas | 56.8 | 7 | 2 | 0.4 | 28 | 4 | 2 |
| The methanation inlet gas | 50.4 | 3.5 | 1 | 0.2 | 40 | 4.8 | 2.46 |
| Methanation is worked off one's feeling vent one's spleen | 42.76 | 0.16 | 0.12 | 0.12 | 51.76 | 5.2 |
Summary of the invention
The present invention is the deficiency that overcomes prior art, provides a kind of energy-conserving and environment-protective not have CO
2Discharging, flow process is simple, and equipment is few, and the methanation catalyst heatproof requires the method for the synthetic artificial Sweet natural gas of low methanation.
The present invention adopts coke(oven)gas and the producing synthesis gas from coal ratio allotment of synthesizing methane on demand, realizes no CO
2The artificial Sweet natural gas synthetic technology of discharging.
Existing mol with each composition in the coke(oven)gas divides rate than using
Y
CO,
Expression, each forms usefulness producing synthesis gas from coal
, Y
CO',
Expression is for realizing no CO
2The artificial Sweet natural gas compound method of discharging supposes that the 1000mol coke(oven)gas need be equipped with the Xmol producing synthesis gas from coal, reaction below main generation the in the methanation of mixing raw material gas:
3H
2+CO=CH
4+H
2O
4H
2+CO
2=CH
4+2H
2O
2H
2+O
2=2H
2O
The hydrogen-carbon ratio that obtains methanation reaction process in the gas mixture thus is by (H
2-CO
2-2O
2)/(CO+CO
2)=3 consume.
Can get by above-mentioned chemical equilibrium relational expression:
It is a kind of by raw materials such as producing synthesis gas from coal and coke(oven)gas that the present invention provides, and through the method for methanation single stage method reaction system synthetic natural gas, mainly is not have CO in the production of synthetic artificial Sweet natural gas
2Discharging realizes that promptly artificial Sweet natural gas is synthesized in the zero release of carbon.
The present invention provides the method for the synthetic artificial Sweet natural gas of a kind of non-carbon-emitting single stage method, mainly is to adopt coke(oven)gas and producing synthesis gas from coal usage ratio according to hydrogen-carbon ratio (H in the gas mixture
2-CO
2-2O
2)/(CO+CO
2) mol molecule number ratio be 3 to be made into.
The present invention provides the method for the synthetic artificial Sweet natural gas of a kind of non-carbon-emitting single stage method, mainly is that gas mixture can be counted ratio in the tolerance mol number of producing synthesis gas from coal and the mol of coke(oven)gas
Calculate, in the formula
Y
CO,
For distribution divides rate with each mol that forms in the coke(oven)gas,
, Y
CO',
For distribution divides rate with each mol that forms in the producing synthesis gas from coal.
The present invention provides the method for the synthetic artificial Sweet natural gas of a kind of non-carbon-emitting single stage method, mainly is the gas mixture process gas sweetening that is used to be made into, and removes H
2S etc. to the deleterious gas of catalyzer after; After heating up, the exhaust gas heat exchange do not carry out the CO conversion through advancing separately; The synthetic artificial Sweet natural gas of next footwork of methanation catalyst effect such as nickel system in water-cooled reactor 105; Exhaust gas with advance tower gas heat exchange cooling after, again through air-cooler or watercooler 107 to about 30 ℃ of condensation separation liquid phase moisture, obtain artificial Sweet natural gas.
The present invention provides the method for the synthetic artificial Sweet natural gas of a kind of non-carbon-emitting single stage method; Mainly be the reaction heat vaporization generation HP steam that methanator uses water as the methanation of heat-eliminating medium absorbing catalyst bed, with the drum pressure control vaporization temperature and the methanation reaction temperature that are communicated with.
The present invention provides the method for the synthetic artificial Sweet natural gas of a kind of non-carbon-emitting single stage method; Mainly be the reaction heat vaporization generation HP steam that methanator uses water as the outer beds methanation of cooling medium flowing water absorption tube in the pipe, with the drum pressure control vaporization temperature and the methanation reaction temperature that are communicated with.
The present invention provides the method for the synthetic artificial Sweet natural gas of a kind of non-carbon-emitting single stage method; Mainly be the reaction heat vaporization generation HP steam that methanator uses water as cooling medium flowing water absorption tube inner catalyst bed methanation between pipe, with the drum pressure control vaporization temperature and the methanation reaction temperature that are communicated with.
The present invention provides the method for the synthetic artificial Sweet natural gas of a kind of non-carbon-emitting single stage method, mainly is gas temperature＜430 ℃ that methanator, and more excellent is＜350 ℃.
The present invention provides the method for the synthetic artificial Sweet natural gas of a kind of non-carbon-emitting single stage method, mainly is not circulate after exhaust gas goes out the methanator heat exchange, further goes refrigerated separation water to obtain product gas.
The present invention provides the method for the synthetic artificial Sweet natural gas of a kind of non-carbon-emitting single stage method, mainly is ratio＜1 of small portion gas and virgin gas, after circulator boosts and material mixed gas converge the demethanization tower and react.
Description of drawings
Fig. 1 is many adiabatic reactor series system substitute natural gas schematic flow sheets (documents: Chinese patent CN101560423A, application number 200910135203).
Fig. 2 is the artificial Sweet natural gas synthesis flow of a non-carbon-emitting single stage method synoptic diagram.
Fig. 3 is the artificial Sweet natural gas synthesis flow of a non-carbon-emitting band circulator single stage method synoptic diagram.
Fig. 4 is the artificial Sweet natural gas synthesis flow of the single stage method synoptic diagram that non-carbon-emitting has two drums.
Embodiment
Below in conjunction with accompanying drawing technical scheme of the present invention is at length explained.
Fig. 1 is the artificial Sweet natural gas synthesis flow of a non-carbon-emitting single stage method synoptic diagram; Be generally non-pressurized coke(oven)gas boosts to 0.5～7MPa through compressor 101 methanation synthesis pressure; Generally reached the synthesis pressure of methanation with the next water-gas of vapourizing furnaces such as Texco, Shell, GSP or Lurgi; Above-mentioned two kinds of gases are sent into distribution cylinder 102, and tolerance is pressed CO in the gas mixture, CO
2All the needed hydrogen-carbon ratio of hydrogenation generation methane is sent into, and the gas mixture of configuration is sloughed H in scavenging tower 103
2S etc. satisfy the methanation requirement to the active prejudicial harmful gas of methanation catalyst, are heated to the isothermal methanation of water inlet pipe heat exchange more than 260 ℃ reactor drum 105 through the gas mixture that purifies through methanator turnover gas-gas heat exchanger 104 and carry out methanation reaction; Methanator internal cooling WATER AS FLOW MEDIUM absorption reaction heat; Drum 106 byproduct steams that are communicated with water-cooled reactor are removed in portion water vaporization, and the methanator temperature of reaction is controlled pressure for vaporization and temperature of reaction through the variable valve on the drum 106 110, behind the virgin gas synthesizing methane; Temperature is 296 ℃; Exhaust gas through gas-gas heat exchanger cool to＜100 ℃, further be cooled to low temperature about in the of 30 ℃ through air-cooler or water cooler 107 again, moisture content is condensed in the gas; Through water separator 108 separating and condensing water, obtain CH then
4＞80% synthetic Sweet natural gas.When the milder methanation reaction temperature of needs control, the gas of the exhaust gas circulation of equipment circulator 109 after will the part cooling and scavenging tower 103 converges through the interchanger 104 heat exchange into methanator reaction that heats up again.
Fig. 3 is the artificial Sweet natural gas synthesis flow of a non-carbon-emitting band circulator single stage method synoptic diagram.Fig. 3 is different with Fig. 2 be that the small portion exhaust gas gets into circulator 109 and boosts after, converge demethanization reactor reaction again after heat exchange heats up with virgin gas.
Fig. 4 is the artificial Sweet natural gas synthesis flow of the single stage method synoptic diagram that non-carbon-emitting has two drums.Fig. 4 also is the reactor drum that adopts water-cooled in the horizontal pipe, differently with Fig. 3 is that two drums are connected with the water cooling tube of bottom with the water cooling tube on methanator top respectively, regulate the temperature of controlling upper strata and lower floor through the pressure of two drums.
Methanator 105 among above-mentioned Fig. 2-Fig. 4 is to adopt horizontal water-cooled reactor, does not have water circulating pump among the figure, but also can add water circulating pump as required.Methanator also can adopt vertical water-cooled reactor among the figure.Can be to be heat-eliminating medium water in the pipe in the vertical reactor, also can be the pipe apparatus with catalyst inside, is heat-eliminating medium water between pipe.Heat-eliminating medium water can be natural circulation, does not need water circulating pump.
Embodiment 1: the gas composition with Texaco's coal water slurry system gas of the coke(oven)gas of sequence number 1 in the following table 2 and sequence number 2 makes is formed; Calculate to such an extent that 1000mol coke(oven)gas adapted Xmol water-gas makes the gas mixture of 1000mol+Xmol sequence number 3 by above-mentioned formula; The methanator that this patent is equipped with nickel catalyzator air speed 4000 under 1.5MPa advances tower for 260 ℃ at inlet temperature of stabilizer; 296 ℃ of methanation reactions of exhaust gas temperature get the artificial Sweet natural gas 470mol of sequence number 4 through refrigerated separation, obtain 1.62 tons/km simultaneously
3Byproduct steam.
Subordinate list 2
Product gas calorific value 31.4MJ/M
3, product gas specification is formed and is met China's natural gas and compressed natural gas standard GB 17820-1999 and GB18047-2000 requirement.
Beneficial effect
Compared with present technology the present invention has significant advantage, and the one, with CO in synthetic gas and the coke(oven)gas and CO
2All produce a large amount of CO of discharging in the methane process in the artificial Sweet natural gas technology of the not existing coal system of synthetic generation of methane
2, really realize CO
2Zero release is preserved the ecological environment; The 2nd, production process is simple, does not need CO conversion, CO in the synthesis gas preparation
2Remove, also do not need the methanation exhaust gas through methods such as transformation absorption, excessive separation H
2Etc. component, practice thrift the process energy consumption; The 3rd, realized not circulating or low recycle ratio, practiced thrift power consumption; The 4th, significantly reduce equipment and save facility investment; The 5th, reclaim reaction heat, pay producing steam.
Claims (10)
1. one kind by raw materials such as producing synthesis gas from coal and coke(oven)gas, through the method for methanation single stage method reaction system synthetic natural gas, it is characterized in that not having CO in the production of synthetic artificial Sweet natural gas
2Discharging realizes that promptly artificial Sweet natural gas is synthesized in the zero release of carbon.
2. according to the method for the synthetic artificial Sweet natural gas of the said non-carbon-emitting single stage method of claim 1, it is characterized in that adopting coke(oven)gas and producing synthesis gas from coal usage ratio according to hydrogen-carbon ratio (H in the gas mixture
2-CO
2-2O
2)/(CO+CO
2) mol molecule number ratio be 3 to be made into.
3. according to the method for the synthetic artificial Sweet natural gas of the said non-carbon-emitting single stage method of claim 1, it is characterized in that gas mixture can count ratio in the tolerance mol number of producing synthesis gas from coal and the mol of coke(oven)gas
Calculate, in the formula
Y
CO,
For distribution divides rate with each mol that forms in the coke(oven)gas,
, Y
CO',
For distribution divides rate with each mol that forms in the producing synthesis gas from coal.
4. according to the method for the synthetic artificial Sweet natural gas of the said non-carbon-emitting single stage method of claim 1, the gas mixture that it is characterized in that being used to be made into is removed H through gas sweetening
2S etc. to the deleterious gas of catalyzer after; After heating up, the exhaust gas heat exchange do not carry out the CO conversion through advancing separately; The synthetic artificial Sweet natural gas of next footwork of methanation catalyst effect such as nickel system in water-cooled reactor (105); Exhaust gas with advance tower gas heat exchange cooling after, again through air-cooler or watercooler (107) to about 30 ℃ of condensation separation liquid phase moisture, obtain artificial Sweet natural gas.
5. the method for synthesizing artificial Sweet natural gas according to the said non-carbon-emitting single stage method of claim 1; It is characterized in that methanator uses water as the reaction heat vaporization generation HP steam of heat-eliminating medium absorbing catalyst bed methanation, with the drum pressure control vaporization temperature and the methanation reaction temperature that are communicated with.
6. the method for synthesizing artificial Sweet natural gas according to the said non-carbon-emitting single stage method of claim 1; It is characterized in that methanator uses water as the reaction heat vaporization generation HP steam of the outer beds methanation of cooling medium flowing water absorption tube in the pipe, with the drum pressure control vaporization temperature and the methanation reaction temperature that are communicated with.
7. the method for synthesizing artificial Sweet natural gas according to the said non-carbon-emitting single stage method of claim 1; It is characterized in that methanator uses water as the reaction heat vaporization generation HP steam of cooling medium flowing water absorption tube inner catalyst bed methanation between pipe, with the drum pressure control vaporization temperature and the methanation reaction temperature that are communicated with.
8. according to the method for the synthetic artificial Sweet natural gas of the said non-carbon-emitting single stage method of claim 1, it is characterized in that gas temperature＜430 ℃ of methanator, more excellent is＜350 ℃.
9. according to the method for the synthetic artificial Sweet natural gas of claim 1 non-carbon-emitting single stage method, it is characterized in that not circulating after exhaust gas goes out the methanator heat exchange, further go refrigerated separation water to obtain product gas.
10. according to the method for the synthetic artificial Sweet natural gas of claim 1 non-carbon-emitting single stage method, it is characterized in that ratio＜1 of small portion gas and virgin gas, after circulator boosts and material mixed gas converge the demethanization tower and react.
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| CN201010519763.9A CN102453564B (en) | 2010-10-17 | 2010-10-17 | Carbon emission-free one-step method and equipment for synthesizing artificial natural gas |
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| CN102453564B CN102453564B (en) | 2015-04-08 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102942972A (en) * | 2012-11-14 | 2013-02-27 | 中国电子工程设计院 | Method for producing liquefied natural gas by coke oven gas |
| CN104152200A (en) * | 2014-08-20 | 2014-11-19 | 北京创时能源技术有限公司 | Water-saving type compressed natural gas production system and production method thereof |
| CN109266413A (en) * | 2018-10-30 | 2019-01-25 | 青岛联信催化材料有限公司 | A method of synthetic natural gas is produced using hydrogen retrieval impermeable gas |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1033764A (en) * | 1963-09-23 | 1966-06-22 | Gas Council | Improvements in or relating to the production of methane gases |
| US5935544A (en) * | 1996-06-06 | 1999-08-10 | Brown & Root, Inc. | Moderate excess nitrogen Braun Purifier™ process and method for retrofitting non-Braun Purifier™ ammonia plants |
| CN101074397A (en) * | 2007-06-22 | 2007-11-21 | 清华大学 | Combined system and process for producing electric-substituted natural gas based on coal gasification and methanation |
-
2010
- 2010-10-17 CN CN201010519763.9A patent/CN102453564B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1033764A (en) * | 1963-09-23 | 1966-06-22 | Gas Council | Improvements in or relating to the production of methane gases |
| US5935544A (en) * | 1996-06-06 | 1999-08-10 | Brown & Root, Inc. | Moderate excess nitrogen Braun Purifier™ process and method for retrofitting non-Braun Purifier™ ammonia plants |
| CN101074397A (en) * | 2007-06-22 | 2007-11-21 | 清华大学 | Combined system and process for producing electric-substituted natural gas based on coal gasification and methanation |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102942972A (en) * | 2012-11-14 | 2013-02-27 | 中国电子工程设计院 | Method for producing liquefied natural gas by coke oven gas |
| CN102942972B (en) * | 2012-11-14 | 2014-10-15 | 中国电子工程设计院 | Method for producing liquefied natural gas by coke oven gas |
| CN104152200A (en) * | 2014-08-20 | 2014-11-19 | 北京创时能源技术有限公司 | Water-saving type compressed natural gas production system and production method thereof |
| CN109266413A (en) * | 2018-10-30 | 2019-01-25 | 青岛联信催化材料有限公司 | A method of synthetic natural gas is produced using hydrogen retrieval impermeable gas |
| CN109266413B (en) * | 2018-10-30 | 2021-09-07 | 青岛联信催化材料有限公司 | Method for producing synthetic natural gas by utilizing hydrogen to recover non-permeate gas |
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