CN102010767A - Natural gas synthesizing process - Google Patents
Natural gas synthesizing process Download PDFInfo
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- CN102010767A CN102010767A CN2010105676366A CN201010567636A CN102010767A CN 102010767 A CN102010767 A CN 102010767A CN 2010105676366 A CN2010105676366 A CN 2010105676366A CN 201010567636 A CN201010567636 A CN 201010567636A CN 102010767 A CN102010767 A CN 102010767A
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Abstract
The invention provides a natural gas synthesizing process. Circulating gas, inert gas or fresh gas is mixed with gas after reaction at the bottom of a methane synthesis reactor, and the temperatures of reaction gases at the outlet of the reactor are controlled, so that the temperatures of various paths of gas requiring to enter a waste heat boiler are ensured to be basically consistent; aiming at a natural gas synthesizing flow employing a plurality of methane synthesis reactors, a central waste heat boiler is adopted to facilitate the collection of saturated steam and overheating operation control; meanwhile, the temperatures of the reaction gases out of the waste heat boiler are basically same so as to facilitate the control and operation of multi-stage methane synthesis reactors; and the temperatures of the reaction gases at the outlet of the reactor are low, so the requirement on the material of a connecting pipeline between the reactor and the waste heat boiler can be reduced. The natural gas synthesizing process energy-saving technology can reduce the investment on the waste heat boiler and the pipeline, improve heat recovery efficiency, make process operation and control easier, and finally increase the economic benefit of synthetic gas-prepared natural gas.
Description
Technical field
The present invention relates to synthetic gas preparing natural gas field, particularly the novel process of energy recovery utilization and minimizing facility investment in the methane synthesis system.
Background technology
Methanation technology is applied in the ammonia synthesis process the earliest to remove CO and the CO in the unstripped gas
2, the forties, abroad just attaching great importance to methanation produces qualified Sweet natural gas and town gas Study on Technology, makes most of CO and H in the coal gas by some or all of methanation
2Reaction is converted into the methane of high heating value, thereby generates SNG (instead of natural gas), and the methane building-up reactions is a strong exothermal reaction, and the numerical value of thermal insulation warming is roughly:
CO+3H
2→CH
4+H
2O，
CO
2+4H
2→CH
4+2H
2O，
The a large amount of heat energy how high efficiente callback utilizes strong exothermal reaction to emit are the key issues that influence synthetic gas preparing natural gas economy.
At present, the heat that produces for the methane building-up reactions adopts dual mode to reclaim, a kind of mode utilizes the interchanger between a plurality of tandem reactors to reclaim the heat of reaction gas, this mode device structure is simple, not only can the heat hot water generates steam, steam heating can also be converted into superheated vapour or high pressure steam, but there is certain shortcoming, the material of useless pot and transport pipe requires high, cost an arm and a leg, adopt interchanger between reactor to reclaim the heat of reaction gas among the US4205961 as the US4130575 of Denmark TOPSOE company and German Metallgasellschaft company; A kind of mode utilizes the interchanger in the reactor to reclaim the heat of reaction gas, comprise interchanger in catalyst bed interlayer interchanger and the beds, its shortcoming is the equipment complexity, reactor needs big heat interchanging area, cost is too high, for example: reactor is the tubulation water-cooled reactor in the CN87102871A patent of Kernforschungsanlage Julich GmbH, synthetic gas in the catalyst bed input field of flowing through in succession, high-temperature zone (local superheating district) and the significantly reduced output section of gas temperature, water coolant is converted to the heat that produces when superheated vapour reclaims methanation, this processing unit relative complex, very high to the material requirement, thermal expansion is inhomogeneous, does not realize industrialization.
In the patent US3967936 of american energy research centre application, adopt the single reactor methanation process, comprise two conversion zones in the methanator at least, separate by a non-reactive zone between the reaction zone.Be filled with catalyzer at reaction zone, and non-reaction zone loading catalyst not; The reactor outlet gas cooling enters reactor from the non-reaction zone side line, and then regulates the concentration of next reaction zone import reaction mass and the temperature of reaction after the compression of overdraft machine mixes with part fresh feed gas.In order to guarantee that the content of methane in the reacting rear material reaches the standard of methane content in the Sweet natural gas, temperature of reaction is lower, or the part in the reactor is carried out methanation reaction under lower service temperature at least.The temperature of the lower or middle temperature medium of the temperature of reactor outlet is lower like this, is unfavorable for discharging in the methanation recovery of chemical energy.
It is low to the invention is intended to develop a kind of energy consumption, easy to operate, reclaims the novel process that heat energy efficiency synthetic gas high and the pipe-line equipment less investment is produced Sweet natural gas.
Summary of the invention
At present, the technology of producing firedamp by syngas is comparative maturity, but they all more or less the energy recovery efficiency that exists be not very high, facility investment is big, material requires high, problems such as complicated operation make that the economy of synthetic natural gas is relatively poor.
The invention provides a kind of synthetic natural gas technology, utilize circulation gas, rare gas element or virgin gas etc. to mix in the methane synthesis reactor bottom with reaction back gas, the temperature of controlling reactor outlet reaction gas, thereby guarantee that each strand needs enter the gas temperature basically identical of useless pot, at the synthetic natural gas flow process of using a plurality of methane synthesis reactors, the present invention adopts the useless pot of central authorities, make and the saturation steam specification stable and consistent that produces help the collection of saturation steam and the operation control of superheat; Basic identical from useless pot of reaction gas temperature of coming out simultaneously, help the control and the operation of multistage methane synthesis reactor, can better avoid the too high generation that causes sintering of catalyst and heat inactivation of reactor temperature, reduce because the unstripped gas temperature not reaching the catalyzer light-off temperature, even nickel-base catalyst active ingredient Ni and carbon monoxide react and form the possibility of nickle carbonoxide.Because each reactor outlet is mixed back gas control lesser temps (less than 550 ℃), can reduce requirement to connecting tube material between reactor and useless pot, reduce the investment of useless pot and pipeline.
The unstripped gas of described synthetic natural gas is the synthetic gas that obtains of coal, heavy oil or gasifying biomass, coke(oven)gas etc.
The a plurality of methane synthesis reactors of described synthetic natural gas process using are generally 2～4, preferred 3～4.Methane synthesis reactor is one or both in adiabatic reactor or the heat exchange type reactor, and reactor is preferable to be chosen as in cold shock formula reactor, the cooling pipe type reactor one or both.
Described rare gas element is selected from water vapour or nitrogen etc., more preferably water vapour.
Described synthetic natural gas technology can have circulation gas, also can not have circulation gas.
The gas temperature that described each strand needs enter useless pot is generally 400～600 ℃, is preferably 450～550 ℃.
Described reaction gas temperature of coming out from the useless pot of central authorities is generally 200～300 ℃, is preferably 240～280 ℃.
In a word, synthetic gas of the present invention is produced the useless pot of novel process minimizing of Sweet natural gas and the investment of pipeline, can improve heat recovery efficiency simultaneously, makes that technological operation control is easier, finally increases the economic benefit of synthetic gas preparing natural gas.
Description of drawings
Fig. 1 is embodiment 1 process flow sheet.
Fig. 2 is embodiment 2 process flow sheets.
Fig. 3 is embodiment 3 process flow sheets.
Fig. 4 is embodiment 4 process flow sheets.
Among the figure: E1, E2---interchanger; R1, R2, R3, R4---reactor; C---circulator.
Fig. 1 is a Figure of abstract.
Embodiment
The present invention will be further described below in conjunction with Figure of description, below only is preferred embodiment of the present invention, can not limit scope of the present invention with this.Be every variation and modification of being done according to the present patent application claim, all should still belong in the scope that patent of the present invention contains.
Embodiment 1
Consist of example with lurgi gasifier typical case gasification, it is as follows to form volumn concentration:
| Form | CH 4 | H 2 | CO | CO 2 | N 2+Ar | Other |
| Gasification back/% | 9.8 | 38.1 | 22 | 27.4 | 2 | 0.7 |
| Conversion decarburization/% | 13.6 | 62.7 | 20.7 | 0.2 | 2.8 | - |
Technology is used 4 reactors, and wherein R1, R2 and R3 are for having circulation gas, rare gas element or a virgin gas etc. and the adiabatic reactor that reacts back gas blended cushion chamber at reactor bottom, and the R4 reactor is the heat exchange type reactor.Loading body in R1, R2 and the R3 reactor is pottery, consists of: Al
2O
3: 53～61%; MgO:20～23%; NiO:12～20%; La:0.5～5%; Ce:0.1～5%; The catalyzer of Ba:0.01～1%.Dress consists of in the R4 reactor: Al
2O
3: 70～80%; NiO:12～20%; La:0.5～5%; Ce:0.1～5%; Ca:0.1～3%; Na:0.1～1%; The catalyzer of Ba:0.01～1%.Adopting a certain amount of circulation, is quench gas with virgin gas, sees Fig. 1.Scale 1.7 hundred million sides Sweet natural gas/year.
Fresh feed gas is 2785kmol/h through the total tolerance behind the conversion decarburization, wherein 1000kmol/h gas mixes with the product gas 1000kmol/h that loops back after interchanger E1 heat exchange to 260 ℃ and enters first methane synthesis reactor R1, mix with the unstripped gas of 840kmol/h at reactor bottom, make temperature reduce to 500 ℃, go to the useless pot of central authorities and be cooled to 260 ℃, go to second methane synthesis reactor R2, it is CH that methane synthesis reactor R2 inlet is formed volumn concentration
451.1%, H
229.9%, CO 8.7%, CO
21.4%, N
24.9%, H
2O 4.0%, ℃ gone to the useless pot of central authorities in the exit by the virgin gas cold shock to 500 of 719kmol/h simultaneously through the reaction of second methane synthesis reactor and be cooled to 260 ℃, go to the 3rd methane synthesis reactor R3, it is CH that methane synthesis reactor R3 inlet is formed volumn concentration
453.5%, H
224.8%, CO5.8%, CO
21.9%, N
24.9%, H
2O 9.1%, ℃ gone to the useless pot of central authorities in the exit by the virgin gas cold shock to 500 of 226kmol/h simultaneously through the reaction of the 3rd methane synthesis reactor and is cooled to 260 ℃, and going out the useless pan gas body of central authorities this moment, to form volumn concentration be CH
461.5%, H
214.2%, CO 2.2%, CO
21.9%, N
25.2%, H
2O15.0%, the 4th reactor adopts the heat exchange type reactor by interchanger E2 temperature in to be reduced to 150 ℃ more earlier, and obtaining product gas composition volumn concentration after 320 ℃ of the reactor outlet temperature, refrigerated separation is CH
490.3%, H
21.9%, CO
20.5%, N
27.3%.
Central authorities' useless pot inlet gas temperature is 500 ℃, 260 ℃ of exit gass, the steam of 220 ℃ of about 2.3MPa of product.
Embodiment 2
Consist of example with Texaco's stove typical case gasification, it is as follows to form volumn concentration:
| Form | ?CH 4 | H 2 | CO | CO 2 | N 2+Ar | Other |
| Gasification back/% | ?- | 37 | 38 | 23 | 2 | - |
| Conversion decarburization/% | ?- | 73.6 | 23.2 | 0.6 | 2.6 | - |
Technology is used 3 methane synthesis reactors, and wherein R1, R2 are for having circulation gas, rare gas element or a virgin gas etc. and the adiabatic reactor that reacts back gas blended cushion chamber at reactor bottom, and the R3 reactor is the heat exchange type reactor.Loading body in R1, the R2 reactor is pottery, consists of: Al
2O
3: 53～61%; MgO:20～23%; NiO:12～20%; La:0.5～5%; Ce:0.1～5%; The catalyzer of Ba:0.01～1%.Dress consists of in the R3 reactor: Al
2O
3: 70～80%; NiO:12～20%; La:0.5～5%; Ce:0.1～5%; Ca:0.1～3%; Na:0.1～1%; The catalyzer of Ba:0.01～1%.Adopting a certain amount of circulation, is quench gas with circulation gas, sees Fig. 2.Scale 4.5 hundred million sides Sweet natural gas/year.
Fresh feed gas is 4000kmol/h through the total tolerance behind the conversion decarburization, after interchanger E1 heat exchange to 260 ℃, enter first methane synthesis reactor R1, mix with the circulation gas of 4874kmol/h at reactor bottom, make temperature reduce to 550 ℃, go to the useless pot of central authorities and be cooled to 280 ℃, go to second methane synthesis reactor R2, it is CH that methane synthesis reactor R2 inlet is formed volumn concentration
440.0%, H
236.8%, CO 10.0%, CO
21.2%, N
25.6%, H
2O 6.4%, ℃ gone to the useless pot of central authorities in the exit by the circulation gas cold shock to 550 of 2447kmol/h simultaneously through the reaction of second methane synthesis reactor and is cooled to 280 ℃, and going out the useless pan gas body of central authorities this moment, to form volumn concentration be CH
460.6%, H
216.6%, CO 1.7%, CO
22.4%, N
27.1%, H
2O11.6%, the 3rd reactor R3 adopts the heat exchange type reactor by interchanger E2 temperature in to be reduced to 140 ℃ more earlier, and obtaining product gas composition volumn concentration after 319 ℃ of the reactor outlet temperature, refrigerated separation is CH
487.3%, H
23.1%, N
29.6%.
Central authorities' useless pot inlet gas temperature is 550 ℃, 280 ℃ of exit gass, the steam of 240 ℃ of about 3.3MPa of product.
Embodiment 3
Become example with the coke(oven)gas classical group, it is as follows to purify back composition volumn concentration:
| Form | CH 4 | H 2 | CO | CO 2 | N 2+Ar | Other |
| Purify back/% | 21.9 | 66.0 | 6.6 | 2.2 | 3.3 | - |
Technology is used 3 methane synthesis reactors, and wherein R1, R2 are for having circulation gas, rare gas element or a virgin gas etc. and the adiabatic reactor that reacts back gas blended cushion chamber at reactor bottom, and the R3 reactor is the heat exchange type reactor.Loading body in R1, the R2 reactor is pottery, consists of: Al
2O
3: 53～61%; MgO:20～23%; NiO:12～20%; La:0.5～5%; Ce:0.1～5%; The catalyzer of Ba:0.01～1%.Dress consists of in the R3 reactor: Al
2O
3: 70～80%; NiO:12～20%; La:0.5～5%; Ce:0.1～5%; Ca:0.1～3%; Na:0.1～1%; The catalyzer of Ba:0.01～1%.No circulation gas is quench gas with virgin gas, sees Fig. 3.Scale 4.3 hundred million sides Sweet natural gas/year.
Fresh feed gas is 4000kmol/h through purifying total tolerance, wherein 335kmol/h virgin gas enters first methane synthesis reactor R1 to 260 ℃ after interchanger E1 heat exchange, mix with the virgin gas of 2908kmol/h at reactor bottom, make temperature reduce to 450 ℃, go to the useless pot of central authorities and be cooled to 240 ℃, go to second methane synthesis reactor R2, it is CH that methane synthesis reactor R2 inlet is formed volumn concentration
429.3%, H
256.1%, CO 3.4%, CO
21.1%, N
23.6%, H
2O 6.5%, ℃ gone to the useless pot of central authorities in the exit by the virgin gas cold shock to 450 of 757kmol/h simultaneously through the reaction of second methane synthesis reactor and be cooled to 240 ℃, this moment methane synthesis reactor R3 inlet to form volumn concentration be CH
435.4%, H
247.9%, CO 0.7%, CO
20.3%, N
23.9%, H
2O 11.8%, reacts in heat exchange type reactor R3, and obtaining product gas composition volumn concentration after 296 ℃ of the temperature outs, refrigerated separation is CH
443.0%, H
252.5%, N
24.5%, obtain synthetic natural gas after the hydrogen to form volumn concentration be CH through carrying
488.7%, H
22.1%, N
29.2%.
Central authorities' useless pot inlet gas temperature is 450 ℃, 240 ℃ of exit gass, the steam of 190 ℃ of about 1.3MPa of product.
Embodiment 4
Consist of example with lurgi gasifier typical case gasification, carry out water vapour and replenish, it is as follows specifically to form volumn concentration:
| Form | CH 4 | H 2 | CO | CO 2 | N 2+Ar | Other |
| Gasification back/% | 9.8 | 38.1 | 22 | 27.4 | 2 | 0.7 |
| Conversion decarburization/% | 13.6 | 62.7 | 20.7 | 0.2 | 2.8 | - |
Technology is used 3 reactors, and wherein R1 and R2 are for having circulation gas, rare gas element or a virgin gas etc. and the adiabatic reactor that reacts back gas blended cushion chamber at reactor bottom, and the R3 reactor is the heat exchange type reactor.Loading body in R1 and the R2 reactor is pottery, consists of: Al
2O
3: 53～61%; MgO:20～23%; NiO:12～20%; La:0.5～5%; Ce:0.1～5%; The catalyzer of Ba:0.01～1%.Dress consists of in the R3 reactor: Al
2O
3: 70～80%; NiO:12～20%; La:0.5～5%; Ce:0.1～5%; Ca:0.1～3%; Na:0.1～1%; The catalyzer of Ba:0.01～1%.Adopt a certain amount of circulation, the saturated steam that adopts 200 ℃ is as rare gas element, and cold shock reactor bottom gas is seen Fig. 4.1.08 hundred million side's Sweet natural gas/years of scale.
Fresh feed gas is 1000kmol/h through the total tolerance behind the conversion decarburization, the product gas 300kmol/h that loops back mixes after interchanger E1 heat exchange to 260 ℃ and enters first methane synthesis reactor R1, mix with the water vapour of 329kmol/h at reactor bottom, make temperature reduce to 480 ℃, go to the useless pot of central authorities and be cooled to 260 ℃, go to second methane synthesis reactor R2, it is CH that methane synthesis reactor R2 inlet is formed volumn concentration
436.6%, H
222.8%, CO 5.2%, CO
21.8%, N
23.6%, H
2O 30%, ℃ gone to the useless pot of central authorities in the exit by the water vapour cold shock to 480 of 6kmol/h simultaneously through the reaction of second methane synthesis reactor and be cooled to 260 ℃, be cooled to 200 ℃ again and go to the 3rd methane synthesis reactor R3, it is CH that methane synthesis reactor R3 inlet is formed volumn concentration
444.2%, H
212.2%, CO 0.2%, CO
22.9%, N
23.8%, H
2O 36.7%, and through 306 ℃ of the 3rd methane synthesis reactor temperature outs, obtaining product gas composition volumn concentration after the refrigerated separation is CH
487.8%, H
24.0%, CO
21.0%, N
272%.
Central authorities' useless pot inlet gas temperature is 480 ℃, 260 ℃ of exit gass, the steam of 200 ℃ of about 1.57MPa of product.
Claims (10)
1. a synthetic natural gas technology is characterized in that, utilize circulation gas, rare gas element or virgin gas and reaction after gas mixes in the methane synthesis reactor bottom, controlling reactor exports the temperature of reaction gas.
2. according to the described technology of claim 1, it is characterized in that methane synthesis reactor is 2～4, preferred 3～4.
3. according to the described technology of claim 1, it is characterized in that synthetic natural gas technology has circulation gas or do not have circulation gas.
4. according to the described technology of claim 1, it is characterized in that rare gas element is selected from water vapour or nitrogen, more preferably water vapour.
5. according to described any one technology of claim 1～4, it is characterized in that each reactor outlet gas temperature is less than 550 ℃.
6. according to described any one technology of claim 1～5, it is characterized in that, in the synthetic natural gas flow process of a plurality of methane synthesis reactors, adopt the useless pot of central authorities.
7. according to the described technology of claim 6, it is characterized in that each methane synthesis reactor need enter the gas temperature basically identical of the useless pot of central authorities.
8. according to the described technology of claim 7, it is characterized in that the gas temperature that each methane synthesis reactor need enter the useless pot of central authorities is 400～600 ℃, is preferably 450～550 ℃.
9. according to claim 6 or 7 described technologies, it is characterized in that, basic identical from the reaction gas temperature that the useless pot of central authorities comes out.
10. according to the described technology of claim 9, it is characterized in that the reaction gas temperature of coming out from the useless pot of central authorities is 200～300 ℃, is preferably 240～280 ℃.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102585949A (en) * | 2012-02-03 | 2012-07-18 | 中国石油化工股份有限公司 | Process for preparing substitute natural gas from synthesis gas |
| CN103013598A (en) * | 2013-01-04 | 2013-04-03 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthesized natural gas |
| CN104419484A (en) * | 2013-08-20 | 2015-03-18 | 中国石油化工股份有限公司 | High-temperature-circulation methane synthetic technology |
| CN107087415A (en) * | 2015-03-03 | 2017-08-22 | 庄信万丰戴维科技有限公司 | The method that production substitutes natural gas |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101560423A (en) * | 2008-04-16 | 2009-10-21 | 卡萨尔甲醇公司 | Process and plant for substitute natural gas |
| CN101880559A (en) * | 2010-06-18 | 2010-11-10 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
-
2010
- 2010-11-30 CN CN2010105676366A patent/CN102010767A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101560423A (en) * | 2008-04-16 | 2009-10-21 | 卡萨尔甲醇公司 | Process and plant for substitute natural gas |
| CN101880559A (en) * | 2010-06-18 | 2010-11-10 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102585949A (en) * | 2012-02-03 | 2012-07-18 | 中国石油化工股份有限公司 | Process for preparing substitute natural gas from synthesis gas |
| CN103013598A (en) * | 2013-01-04 | 2013-04-03 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthesized natural gas |
| CN103013598B (en) * | 2013-01-04 | 2014-07-16 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthesized natural gas |
| CN104419484A (en) * | 2013-08-20 | 2015-03-18 | 中国石油化工股份有限公司 | High-temperature-circulation methane synthetic technology |
| CN107087415A (en) * | 2015-03-03 | 2017-08-22 | 庄信万丰戴维科技有限公司 | The method that production substitutes natural gas |
| CN107087415B (en) * | 2015-03-03 | 2020-06-30 | 庄信万丰戴维科技有限公司 | Process for producing substitute natural gas |
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Application publication date: 20110413 |
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