CN103937572A - Methanation process for gasification by entrained-flow bed - Google Patents
Methanation process for gasification by entrained-flow bed Download PDFInfo
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Abstract
The invention relates to a methanation process for gasification by an entrained-flow bed and aims at the problem that the existing methanation process is complicated in process, difficult to adjust, high in equipment manufacturing difficulty and high in operation cost when the amount of a circulating gas volume is large. According to the technical scheme, the process comprises the following steps of dividing a raw material gas from an upstream into two strands A and B which respectively enter two high-temperature reaction sections connected in parallel to be subjected to high-temperature reaction and heat recovery; dividing each strand of synthesis gas after heat recovery into two strands, namely strand A1 and strand A2, strand B1 and strand B2; cooling the strand A1 and the strand B1 separately by a boiler feed water water-preheater, then mixing and supercharging to 3.06-3.12Mpa through a compressor, and then equally dividing the mixed gas into two strands which respectively return to the high-temperature reaction sections connected in parallel to supply gas as the circulating gas; mixing the strands A2 and B2 of synthesis gas and directly feeding the mixed gas to a low-temperature reaction section to have a reaction to obtain qualified natural gas. The methanation process is simple, simple in temperature control and system regulation, and good in reliability, and meets the large-capacity circulating requirement.
Description
Technical field
The present invention relates to a kind of methanation process, specifically a kind of methanation process of entrained flow gasification.
Background technology
Sweet natural gas is a kind of clean, efficient energy product.China's fast economic growth has pulled Natural Gas Demand, in addition along with the domestic strategy of sustainable development with strengthen the enforcement of the policy such as environmental protection, domesticly will grow with each passing day to the demand of Sweet natural gas.
Coal preparing natural gas technology is that the raw gas of producing by gasification is adjusted to suitable H/CO through CO conversion respectively, remove after sour gas and all the other impurity through purifying, qualified purified gas generates and meets the synthetic natural gas that national Natural gas standard requires through methanation reaction again.Wherein the selection of Coal Gasification Technology has material impact to Technological Economy and the environmental protection etc. of full factory.
At present domesticly all adopt fixed bed gasification in the coal preparing natural gas project of building, its three waste discharge problem is serious.In view of the domestic raising day by day to environmental requirement, adopting cleaner Coal Gasification Technology (as coal gasification) to produce SNG will be a later trend, due to the variation of gasification mode, under same size, for the methanation process (hereinafter to be referred as option A) of entrained flow gasification than greatly increasing for methanation process (hereinafter to be referred as the option b) difficulty of fixed bed gasification, be mainly reflected in following some:
1. methanation is the reaction of volume-diminished, contains hardly CH in option A unstripped gas
4, and CH in option b unstripped gas
4content reaches 20%mol, and in the situation of equal production capacity, option A material gas quantity, much larger than option b, is about 1.6 times of option b, reaches 1,000,000,000 Nm for output
3heavy construction more than/aSNG, is difficult to design the equipment that meets tolerance processing requirements.
2. methanation is a strong exothermic process, the CH of option b unstripped gas middle and high concentration
4can react by active balance, be easy to control and regulate temperature of reaction, the high CO concentration of feature of option A unstripped gas, low CH
4concentration, regulates difficulty to increase;
3. methanation is a strong exothermic process, if temperature of reaction can not be effectively controlled, can exist reaction overtemperature to damage the problem of catalyzer and equipment.For meeting reaction requirement, need to adopt the mode control temperature of synthetic gas circulation, for reaching same reaction effect, three times of left and right that the circulating flow rate of option A is option b;
4. because A scheme exists circulating flow rate large, temperature of reaction control and the large problem of adjusting difficulty cause manufacture and the design difficulty of the materials such as this scheme equipment, pipeline, instrument valve large, system operation reliability is poor, and A scheme is difficult to realize through engineering approaches in actual process of construction.
Summary of the invention
The object of the invention is in order to solve the problems of the technologies described above, provide a kind of technique simple, can temperature control tune and system regulate simple, good reliability, meet the methanation process of the coal preparing natural gas for coal dust gasification that atm number circulation requires.
Technique of the present invention is: be divided into two strands of A, B from the unstripped gas of upstream, enter respectively two pyroreaction sections in parallel and carry out pyroreaction and heat recuperation, per share synthetic gas after heat recuperation is divided into two strands again, be A1 thigh and A2 thigh, B1 thigh and B2 thigh, A1 thigh and B1 thigh thigh are respectively hung oneself after feedwater preheater preheating and are merged, then after compressor is pressurized to 3.06-3.12MPag, are divided into two stocks again and are not recycled to pyroreaction section in parallel and fill into as circulation gas; A2 and B2 thigh synthetic gas obtain qualified Sweet natural gas after directly sending into the reaction of low-temp reaction section after merging.
In described any pyroreaction section, described A-share or B thigh unstripped gas are first preheated to after 60-250 DEG C in separator separates liquid wherein through feed gas heater again, unstripped gas after separator separates is divided into two strands, also be divided into two strands from the circulation gas of compressor, from first strand of unstripped gas of separator be mixed to 260-340 DEG C from first strand of circulation gas of compressor and enter 1# high-temperature reactor and carry out methanation reaction for the first time; The synthetic gas that goes out 1# high-temperature reactor is cooled to 320-410 DEG C through the useless pot of 1#.Afterwards with second strand of unstripped gas from separator, enter 2# high-temperature reactor after being mixed to 260-350 DEG C from second strand of circulation gas of compressor and carry out methanation reaction for the second time, go out the synthetic gas of 2# high-temperature reactor after the preliminary lowered temperature reclamation heat of vapor superheater, then enter the useless pot of 2# and further lower the temperature and reclaim heat to the synthetic gas after 350-250 DEG C and be divided into two strands (being A1 thigh, A2 thigh).
In the time of arbitrary high-temperature reactor overtemperature, to be interrupted in the described A-share before incoming stock air preheater or B thigh unstripped gas fill in methane, nitrogen and oiler feed at least one with regulation system high-temperature methanation temperature of reactor.
In described low-temp reaction section, A2 and B2 thigh synthetic gas are introduced into 1# low-temp reaction device after merging and carry out methanation reaction for the third time, then the feed gas heater in two pyroreaction sections of parallel connection and unstripped gas do not carry out indirect heat exchange and are cooled to 220-300 DEG C to be divided into two stocks, then two strands of synthetic gas merge and send into 2# low-temp reaction device and carry out methanation reaction the 4th time, the synthetic gas that goes out 2# low temperature methanator again after reactor product cooler cooling in product separator separatory, obtain qualified synthetic natural gas.
The inlet temperature of controlling described 1# high-temperature reactor is 260-340 DEG C, and temperature out is 580-700 DEG C; The inlet temperature of controlling 2# high-temperature reactor is that 260-350 DEG C, temperature out are 580-700 DEG C;
The inlet temperature of controlling 1# low-temp reaction device is that 250-300 DEG C, temperature out are 400-480 DEG C; The inlet temperature of controlling 2# low-temp reaction device is that 220-300 DEG C, temperature out are 250-380 DEG C.
The amount of filling into of described methane is 1-15%mol for making methane content in feeding gas; The amount of filling into of nitrogen is 1-3%mol for making a nitrogen content in feeding gas; The amount of filling into of oiler feed is 1-10%mol for making water-content in feeding gas.
Unstripped gas after separator separates is divided into two stocks and does not enter 1# high-temperature reactor and 2# high-temperature reactor, and the first burst of total tolerance of unstripped gas that wherein enters 1# high-temperature reactor accounts for the 35-65%mol of total tolerance.
Per share synthetic gas after heat recuperation is divided into two strands again, sends into compressor compresses and account for as the tolerance of circulation gas the 55-80%mol of the total tolerance of per share synthetic gas after heat recuperation.
Described in any in pyroreaction section, described in send into 1# high-temperature reactor circulation gas account for the 80-95%mol of total tolerance of the circulation gas of sending into this pyroreaction section.
Unstripped gas in the present invention is the high CO concentration purification gas based on entrained flow bed gasification technology, more than CO concentration can reach 24%mol in this unstripped gas, and contains hardly CH
4, circulating flow rate large (accounting for the 55-80%mol of high-temperature reactor outlet tolerance)
Contriver is for the problem existing in background technology, the existing methanation process based on entrained flow bed gasification technology is furtherd investigate, for the large problem of circulating flow rate, contriver finds, intractability mainly concentrates on the pyroreaction stage, due to the restriction of high-temperature methanation reactor manufacturing technology at present, its size is limited, in unit time, be difficult to process a large amount of unstripped gass, therefore pyroreaction section is designed to two sections in parallel, unstripped gas (claiming again to purify) can be divided equally two strands, carry out respectively pyroreaction and heat recuperation, then for the synthetic gas that reclaims heat after pyroreaction, because temperature reduces, the volume of gas reduces, therefore can share a compressor and low-temp reaction section and carry out respectively circularly-supercharged and low-temp reaction, thereby solve the equipment existing in the past, pipeline, manufacture and the design difficulty of the materials such as instrument valve are large, be difficult to realize the problem of through engineering approaches,
For the problem of the control of resolution system temperature and adjusting, contriver has carried out the improvement of two aspects, the one, by filling into a large amount of circulation gas to regulate the temperature in of high-temperature reactor in pyroreaction section, preferably send into compressor compresses accounts for the total tolerance of synthetic gas after pyroreaction and heat recuperation (i.e. total tolerance of synthetic gas after two pyroreaction section reactions in parallel) 55-80%mol as the tolerance of circulation gas, be that major part circulates, can effectively control like this temperature of reaction, for any one pyroreaction Duan Eryan, the circulation gas of sending into 1# high-temperature reactor preferably accounts for the 80-95%%mol of total tolerance of the circulation gas of sending into this pyroreaction section, surplus fills into 2# high-temperature reactor, fill into the adjusting of ratio by circulating flow rate, can control preferably the temperature in of two high-temperature reactors, ensure normally carrying out of methanation reaction.The 2nd, in any one pyroreaction section, unstripped gas enters at least one having filled into before preheater in methane, nitrogen and oiler feed (can injector spray into mode), and it is in order to increase temperature control means that contriver adds three's object especially herein.Three can select one or be together interrupted add, the add-on of methane is controlled at and makes the content of methane in unstripped gas at 1-15%mol; The add-on of nitrogen is controlled at and makes the content of nitrogen in unstripped gas at 1-3%mol; The addition of oiler feed is controlled at and makes in unstripped gas water-content between 1-10%mol; Concrete add-on is so that be down to and require in temperature in the high-temperature reactor of overtemperature state, but addition had better not exceed in above-mentioned scope, in the time adding any temperature that still cannot make high-temperature reactor to be down in claimed range, can consider that merging adds other one or both, to realize flexibly the object of temperature control fast.Here, it is methanation and the water resultant as methanation reaction that contriver has selected the principle of methane, nitrogen and oiler feed, can effectively regulate the balance of reaction, and nitrogen interpolation principle be not for explosion-proof object, but because nitrogen adds the effect in unstripped gas with diluting reaction thing, thereby realize the object of temperature control, never in methanation process, add so far nitrogen and the methane report with regulation system temperature.
Contriver is by twice high-temperature methanation, the design of twice low temperature methanation, and strictly control the out temperature of reactor, thereby ensure normally carrying out of methanation reaction, the safe and stable operation of guarantee system, can be good at reclaiming for the heat of methanation reaction, except by-product superheated vapour, can also be used for the preheating to unstripped gas, have advantages of energy-saving and cost-reducing.
Beneficial effect
1. the methanation process for coal preparing natural gas of the high CO concentration purification gas that the present invention is entrained flow bed gasification technology provides solution, and technical process is simple and reliable, facility investment and running cost is low, Sweet natural gas that produce meets national standard (GB17820-2012) completely calorific value requirement.
2. the technique that has adopted two pyroreaction Duan Yuyi low-temp reaction section series connection in parallel, the manufacture and the design difficulty that effectively solve the materials such as equipment, pipeline, instrument valve are large, are difficult to realize the problem of through engineering approaches, are specially adapted to reach 1,000,000,000 Nm for output
3heavy construction more than/a SNG;
3. each pyroreaction section is equipped with the multistage efficient recovery heat of useless pot, and the flow process that simplifies the operation, avoids the interference between pyroreaction section, is convenient to system control;
4. adopt and supplement CH
4, nitrogen and oiler feed mode regulate methanation reaction temperature and balance, effectively control reaction, improved the operation stability of operation; The method of spraying oiler feed regulates methanation reaction temperature and balance.Control device and control method are increased, before oiler feed is arranged on feed gas heater, before entering 1# high-temperature reactor, unstripped gas is also provided with separator, can ensure the oiler feed that fills into before entering reactor the water vapour in synthetic gas in superheat state, prevent contacting of water of condensation and catalyzer, ensure technology reliability service;
5. adopt two pyroreaction sections in parallel, meet the circulation requirement of atm number circulation gas, circulation gas is circulated to respectively 1# high-temperature reactor and the 2# high-temperature reactor of two pyroreaction sections, further ensures normally carrying out of methanation reaction.
Brief description of the drawings
Fig. 1 is system diagram of the present invention and process flow sheet.
Wherein, E01A---feed gas heater, R01A---1# high-temperature reactor, R02A---2# high-temperature reactor, E01B---feed gas heater, R01B---1# high-temperature reactor, R02B---2# high-temperature reactor, the useless pot of E02A---1#, E03A---vapor superheater, the useless pot of E04A---2#, E05A---feedwater preheater, the useless pot of E02B---1#, E03B---vapor superheater, the useless pot of E04B---2#, E05B---feedwater preheater, K01---compressor, R03---1# low-temp reaction device, R04---2# low-temp reaction device, E06---reactor product cooler, S01-separator, S02---product separator, U01A---oiler feed injector, U02A---methane fills into mouth, U03A---nitrogen fills into mouth, U01B---oiler feed injector, U02B---methane fills into mouth, U03B---nitrogen fills into mouth, A---pyroreaction section, B---pyroreaction section.
Embodiment
System embodiment:
Pyroreaction section is two (pyroreaction section A and pyroreaction section B) in parallel, the outlet of described two pyroreaction section A, B is all connected with low-temp reaction section, and be connected with compressor K01 through each self-corresponding feedwater preheater E05A, E05B respectively, the outlet of described compressor K01 is connected with two pyroreaction section A, B respectively.
In described two pyroreaction section A, B, the annexation of each equipment room and processing tolerance are identical.Taking pyroreaction section A as example: described pyroreaction section A comprises feed gas heater E01A, the separator S01A, the useless pot of 1# high-temperature reactor R01A, 1# E02A, 2# high-temperature reactor R02A, vapor superheater E03A and the useless pot of the 2# E04A that connect successively; The outlet of described separator S01A is also connected with the pipeline before 2# high-temperature reactor R02A entrance; The outlet of described compressor K01 is also connected with the pipeline before 1# high-temperature reactor and 2# high-temperature reactor entrance respectively.On pipeline before feed gas heater U01A, be also provided with that methane fills into a mouthful U02A, nitrogen fills into mouthful U03A and oiler feed injector U01A.
Equipment connecting relation in pyroreaction section B, with pyroreaction section B, is not done to sew to state at this.
Described low-temp reaction section comprises 1# low-temp reaction device R03, the entrance of described 1# low-temp reaction device is connected with the 2# useless pot outlet of E04A and the useless pot of the 2# of the pyroreaction section B E04B of pyroreaction section A respectively, outlet is connected with 2# low-temp reaction device R04 through feed gas heater U01A, the U01B of two pyroreaction section A, B respectively, and described 2# low-temp reaction device R04 is connected with product separator S02 through reactor product cooler E06.
Process example:
The purified gas (hereinafter to be referred as purified gas) that upstream refining plant comes consists of: H
2: 74.7%mol; CH
4: 200ppm; N
2: 0.4%mol; CO:24.1%mol; CO
2: 0.8%mol; H2S+COS:<0.1ppm.Temperature: 30 DEG C, pressure: 3.12MPag, flow: 4272898Nm3/h.
The unstripped gas that enters battery limit (BL) is as A, two strands of unstripped gass of B, enters respectively two pyroreaction section A, B in parallel, and in two conversion zones, technological process and the processing condition of unstripped gas are identical, is below described as the flow process of one of them pyroreaction section A:
The oiler feed that first A-share unstripped gas is supplied with the interruption that sprayed into by injector U01 and methane fill into a mouthful U02A and fill into methane, nitrogen fills into a mouthful U03A and fills into nitrogen (methane in feeding gas, the ratio of nitrogen and water vapour is respectively 1-15%mol, 1-3%mol, 1-10%mol), its effect is mainly as regulating measure in the time of system overtemperature) evenly mix, the synthetic gas indirect heat exchange with the pot E04A that gives up from 2# through feed gas heater E01A again, unstripped gas is preheated to 60 DEG C-250 DEG C, then isolate the liquid in gas through separator S01A, to avoid the liquid in unstripped gas to be brought in high-temperature reactor, the unstripped gas that contains steam of being discharged by separator S01A top is divided into two strands.One unstripped gas (accounting for the 35-65%mol of unstripped gas total amount) with from first strand of circulation gas of recycle gas compressor K01 (described in send into 1# high-temperature reactor R01A circulation gas account for the 80-95%mol of total tolerance of the circulation gas of sending into pyroreaction section A, remainder is sent into 2# high-temperature reactor R02A) be mixed to 260-340 DEG C and enter 1# high-temperature reactor R01A and carry out methanation reaction, controlling reactor outlet temperature is 580-700 DEG C; Another strand of unstripped gas (accounting for the 65-35%mol of unstripped gas total amount) enters 2# high-temperature reactor R02A with the synthetic gas after the useless pot of 1# E02A heat exchange from 1# high-temperature reactor R01 and after being mixed to 260-350 DEG C from second strand of circulation gas of recycle gas compressor K01, reactor outlet temperature is 580-700 DEG C, and after first the synthetic gas that goes out 2# methane reactor R02 enters the useless pot of a 2# E04A again temperature is reduced to 350-250 DEG C after the preliminary cooling of vapor superheater E03A, synthetic gas is divided into A1, A2 thigh.In like manner be divided into B1, B2 thigh from the synthetic gas of pyroreaction section B.
A1 thigh synthetic gas through feedwater preheater E05A be cooled to 200-150 DEG C with from pyroreaction section B after feedwater preheater E05B is cooled to the B1 thigh synthetic gas of 200-150 DEG C and merges, (account for the 55-80%mol of the synthetic gas total amount that pyroreaction section A and pyroreaction section B generate) to be pressurized to 3.06-3.12Mpag by compressor K01 after be divided into again two strands and send into respectively pyroreaction section A as circulation gas, B, taking pyroreaction section A as example, the circulation gas of sending into pyroreaction section A is divided into two strands again, first gang of 1# methane reactor R01A sending in pyroreaction section A, send into 2# high-temperature reactor R02A for second strand.The circulation gas of sending into pyroreaction section B fills into mode with pyroreaction section A.
From pyroreaction section A, the A2 thigh of B and B2 thigh synthetic gas enter 1# low-temp reaction device R03 after merging and carry out methanation reaction for the third time, the inlet temperature of controlling 1# low-temp reaction device R03 is 250-300 DEG C, temperature out 400-480 DEG C, the synthetic gas that goes out 1# low-temp reaction device R03 is divided into two strands, enter respectively pyroreaction section A, after being cooled to 220-300 DEG C with unstripped gas heat exchange in the purified gas preheater E01A of B and E01B, two strands of synthetic gas merge and enter 2# low-temp reaction device R04 and carry out methanation reaction the 4th time, the inlet temperature of controlling 2# low-temp reaction device is 220-300 DEG C, temperature out is 250-380 DEG C, the synthetic gas that goes out 2# low temperature reactor R04 again after reactor product cooler E06 cooling in product separator S02 separatory, obtain qualified synthetic natural gas (SNG).
Sweet natural gas consists of: H
2: 1.8%mol; CH
4: 95.2%mol; N
2: 1.4%mol; CO:149ppm; CO
2: 1.3%mol; H2O:0.3%mol, temperature: 40 DEG C, pressure: 2.3MPag, flow: 126524Nm3/h.Indices meets the requirement of GB17820-2012 to Sweet natural gas.The overheated high pressure steam of by-product (9.8MPag, 535 DEG C): 357t/h.
Claims (10)
1. the methanation process of an entrained flow gasification, it is characterized in that, be divided into two strands of A, B from the unstripped gas of upstream, enter respectively two pyroreaction sections in parallel and carry out pyroreaction and heat recuperation, per share synthetic gas after heat recuperation is divided into two strands again, be A1 thigh and A2 thigh, B1 thigh and B2 thigh, A1 thigh and B1 thigh are respectively hung oneself, and feedwater preheater cooling is rear to be merged, again after compressor is pressurized to 3.06-3.12Mpag, then is divided into two stocks and is not recycled to pyroreaction section in parallel and fills into as circulation gas; A2 and B2 thigh synthetic gas obtain qualified Sweet natural gas after directly sending into the reaction of low-temp reaction section after merging.
2. the methanation process of entrained flow gasification as claimed in claim 1, it is characterized in that, in described any pyroreaction section, described A-share or B thigh unstripped gas are first preheated to after 60-250 DEG C in separator separates liquid wherein through feed gas heater again, unstripped gas after separator separates is divided into two strands, also be divided into two strands from the circulation gas of compressor, from first strand of unstripped gas of separator be mixed to 260-340 DEG C from first strand of circulation gas of compressor and enter 1# high-temperature reactor and carry out methanation reaction for the first time; The synthetic gas that goes out 1# high-temperature reactor enters 2# high-temperature reactor and carries out methanation reaction for the second time after the useless pot of 1# is cooled to after 320-410 DEG C and is mixed to 260-350 DEG C from second strand of unstripped gas of separator, from second strand of circulation gas of compressor, go out the synthetic gas of 2# high-temperature reactor after the preliminary lowered temperature reclamation heat of vapor superheater, then enter the useless pot of 2# and further lower the temperature and reclaim heat to the synthetic gas after 350-250 DEG C and be divided into two strands.
3. the methanation process of entrained flow gasification as claimed in claim 2, it is characterized in that, in the time of arbitrary high-temperature reactor overtemperature, to be interrupted in the described A-share before incoming stock air preheater or B thigh unstripped gas fill in methane, nitrogen and oiler feed at least one with regulation system high-temperature methanation temperature of reactor.
4. the methanation process of entrained flow gasification as claimed in claim 1, it is characterized in that, in described low-temp reaction section, A2 and B2 thigh synthetic gas are introduced into 1# low-temp reaction device after merging and carry out methanation reaction for the third time, then the feed gas heater in two pyroreaction sections of parallel connection and unstripped gas do not carry out indirect heat exchange and are cooled to 220-300 DEG C to be divided into two stocks, then two strands of synthetic gas merge and send into 2# low-temp reaction device and carry out methanation reaction the 4th time, the synthetic gas that goes out 2# low temperature methanator again after reactor product cooler cooling in product separator separatory, obtain qualified synthetic natural gas.
5. the methanation process of entrained flow gasification as claimed in claim 2, is characterized in that, the inlet temperature of controlling described 1# high-temperature reactor is 260-340 DEG C, and temperature out is 580-700 DEG C; The inlet temperature of controlling 2# high-temperature reactor is that 260-350 DEG C, temperature out are 580-700 DEG C.
6. the methanation process of entrained flow gasification as claimed in claim 4, is characterized in that, the inlet temperature of controlling 1# low-temp reaction device is that 250-300 DEG C, temperature out are 400-480 DEG C; The inlet temperature of controlling 2# low-temp reaction device is that 220-300 DEG C, temperature out are 250-380 DEG C.
7. the methanation process of entrained flow gasification as claimed in claim 3, is characterized in that, the amount of filling into of described methane is 1-15%mol for making methane content in feeding gas; The amount of filling into of nitrogen is 1-3%mol for making a nitrogen content in feeding gas; The amount of filling into of oiler feed is 1-10%mol for making water-content in feeding gas.
8. the methanation process of entrained flow gasification as claimed in claim 2, it is characterized in that, unstripped gas after separator separates is divided into two stocks and does not enter 1# high-temperature reactor and 2# high-temperature reactor, and the first burst of total tolerance of unstripped gas that wherein enters 1# high-temperature reactor accounts for the 35-65%mol of total tolerance.
9. the methanation process of entrained flow gasification as claimed in claim 1 or 2, is characterized in that, sends into compressor compresses and account for as the tolerance of circulation gas the 55-80%mol of the total tolerance of synthetic gas after pyroreaction and heat recuperation.
10. the methanation process of entrained flow gasification as claimed in claim 2, is characterized in that, described in any in pyroreaction section, described in send into 1# high-temperature reactor circulation gas account for the 80-95%mol of total tolerance of the circulation gas of sending into this pyroreaction section.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104388139A (en) * | 2014-11-11 | 2015-03-04 | 上海鑫兴化工科技有限公司 | Direct methanation method and system for raw coal gas |
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| CN102899112A (en) * | 2012-10-29 | 2013-01-30 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
| CN103450960A (en) * | 2013-09-23 | 2013-12-18 | 中国五环工程有限公司 | Coal natural gas methanation technology and system thereof |
| CN103695058A (en) * | 2013-12-19 | 2014-04-02 | 中国海洋石油总公司 | Novel methanation reaction process for preparing synthetic natural gas |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102660339A (en) * | 2012-04-27 | 2012-09-12 | 阳光凯迪新能源集团有限公司 | Gas-steam efficient cogeneration process and system based on biomass gasification and methanation |
| CN102899112A (en) * | 2012-10-29 | 2013-01-30 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
| CN103450960A (en) * | 2013-09-23 | 2013-12-18 | 中国五环工程有限公司 | Coal natural gas methanation technology and system thereof |
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| CN104388139A (en) * | 2014-11-11 | 2015-03-04 | 上海鑫兴化工科技有限公司 | Direct methanation method and system for raw coal gas |
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