CN104357117A - Non-circulating methanation process of coal-based synthetic natural gas and liquefied natural gas - Google Patents

Non-circulating methanation process of coal-based synthetic natural gas and liquefied natural gas Download PDF

Info

Publication number
CN104357117A
CN104357117A CN201410598644.5A CN201410598644A CN104357117A CN 104357117 A CN104357117 A CN 104357117A CN 201410598644 A CN201410598644 A CN 201410598644A CN 104357117 A CN104357117 A CN 104357117A
Authority
CN
China
Prior art keywords
methanation
gas
natural gas
synthetic
methanator
Prior art date
Application number
CN201410598644.5A
Other languages
Chinese (zh)
Inventor
张新波
杨宽辉
何洋
马磊
易竖棚
郑珩
陶鹏万
Original Assignee
西南化工研究设计院有限公司
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 西南化工研究设计院有限公司 filed Critical 西南化工研究设计院有限公司
Priority to CN201410598644.5A priority Critical patent/CN104357117A/en
Publication of CN104357117A publication Critical patent/CN104357117A/en

Links

Abstract

The invention belongs to the field of chemical industry and in particular relates to a non-circulating methanation process of coal-based synthetic natural gas and liquefied natural gas. The process comprises the following concrete steps: introducing coal-based synthetic gas subjected to sulfur-tolerant shift and low-temperature methanol elution desulfurization and decarbonization into an ultra-precision purifier; enabling the total sulfur content to be less than 0.02 ppm, the chlorine content to be less than 0.01 ppm and the heavy metal content to be less than 0.01 ppm in the synthetic gas entering the methanation process; dividing the synthetic gas into three, four or five parts; enabling the synthetic gas parts to enter main methanation reactors respectively; enabling all gas at the outlet of the final main methanation reactor to enter auxiliary methanation reactors for continuous methanation reaction in sequence; cooling and dehydrating to obtain the synthetic natural gas (SNG) meeting the requirements, or adding a cryogenic separation liquefication process to obtain the liquefied natural gas (LNG). The process has the advantages of no circulating compressor, low investment, high energy utilization rate and low running expense.

Description

A kind of coal synthetic natural gas and natural gas liquids without circulation methanation process
Technical field
The invention belongs to chemical field, relate to and be rich in H 2, CO and CO 2the technique of the methanation of gas, be specially a kind of coal synthetic natural gas and natural gas liquids without circulation methanation process.
Background technology
China's prediction coal reserves is about 5.47 trillion tons, and major part in Shanxi Province, the Inner Mongol and Xinjiang, spy is that Xinjiang is located in northwest, and conditions of transportation is poor.Meanwhile, China's conventional gas stock number is about 35 ~ 38,000,000,000,000 Nm 3, account for 2% of world's total amount; Wherein mining resources amount 10 ~ 12,000,000,000,000 Nm 3, Sweet natural gas residual recoverable reserves is only equivalent to 6% of world average level per capita, and China shows as the country of relative rich coal weak breath.And Sweet natural gas is as a kind of high-quality clean energy, the proportion at present in China's primary energy source consumption is only about 4.5%, well below the mean level (ML) in the world 23.7%.China's natural gas consumption speedup exceedes output speedup for many years, and import volume significantly increases year by year.Within 2013, China's natural gas consumption reaches 1,676 hundred million Nm 3, inlet natural gas 53,000,000,000 Nm 3.According to Development Research Center of the State Council's prediction, be increased to 3,000 hundred million Nm to the year two thousand twenty consumption 3, about have 40% dependence on import when the time comes.Can to predict future be domestic or abroad all there is very large breach for the demand of Sweet natural gas, therefore utilizes coal resources production synthetic natural gas will be that a kind of important Sweet natural gas of reality supplements source.
The methanation technology of existing coal synthetic natural gas uses the complex appts of multiple heat exchanger and a large amount of gas circulation to control methanation temperature out usually, the recycle ratio adopted is very high, the cost of hot gas cycle compressor is high, not only increase interchanger and methanator facility investment, and add methanation catalyst loadings, also significantly add unit product power consumption, therefore develop more energy-conservation, without circulator, lower-cost methanation process is real belongs to urgent.
 
Summary of the invention
The object of the invention is to for above technical problem, provide a kind of capacity usage ratio high, without circulation, invest less coal synthetic natural gas and natural gas liquids without circulation methanation process.
The object of the invention is realized by following technical proposals:
Coal synthetic natural gas and natural gas liquids without a circulation methanation process, this technique comprises the steps:
Coal is made synthetic gas after sulfur-resisting transformation and low-temperature rectisol desulfurization and decarburization, obtain the synthetic gas meeting methanation procedure calls.Then synthetic gas enters in superfinishing cleaner the poisonous substance such as sulphur, chlorine, heavy metal thoroughly removed in synthetic gas, and reaching total sulfur is less than 0.02ppm, and chlorine is less than 0.01ppm, and total heavy metal is less than 0.01ppm.Then the synthetic gas after thorough purification is divided into some stocks and does not enter main methanation main reactor, and methanation reaction is carried out after the import of the first main methanation main reactor R1 mixes a certain amount of water vapour, enter the second main methanation main reactor R2 after first main methanation main reactor R1 exit gas (stream stock 10) mixes with partial synthesis gas (flowing stock 6) after waste heat boiler recovery heat and proceed methanator, the like.After whole main methanation reaction, more successively by secondary methanator, and by the gas cooling after methanation before entering the secondary methanator of final stage, condensation separation water, then CO and CO to remnants 2carry out full methanation reaction, then cool, dehydration obtains meeting the synthetic natural gas SNG that Sweet natural gas national standard (GB 17820-2012) requires, or entering low temperature separation process operation again utilizes rectifying tower to make methane rich oxidizing gases be divided into three strands, first strand is natural gas liquids, and second strand is nitrogen-rich gas, and the 3rd strand is hydrogen-rich gas, and hydrogen-rich gas all turns back to the first main methanator R1 entrance, natural gas liquids is as product.
As preferably, the synthetic gas going out superfinishing cleaner is divided into 3 strands or 4 strands.
Described main methanation furnace temperature in is 563K-623K, and temperature out is 825K-967K, is 10000 h with the volume space velocity that dry gas calculates -1-50000 h -1; The volume space velocity that the dry gas of last secondary methanator described calculates is 4000 h -1-8000 h -1, methanation furnace temperature in is 513K-573K.
Enter the synthetic gas of the first main methanator and the mol ratio of water vapor is 0.48 ~ 1.51:1, and water vapor pressure P1 0.1MPa more than larger than methanation working pressure P2.
Main methanator is adiabatic methanation reactor, and secondary methanator is adiabatic or isothermal methanation reactor.Methanation catalyst in methanator take nickel as the methanation catalyst of main active component.
In described technological process, in being produced by waste heat boiler and superheater, pressure or high pressure steam reclaim the heat of the high-temperature gas of methanator outlet.
compared with prior art, beneficial effect of the present invention is:
Have without recycle compressor, reduced investment, capacity usage ratio is high, and working cost is low.Along with the research and development of coal preparing natural gas project methanation technology, a large amount of patent has done relevant elaboration to this, a large amount of patent have employed the methanation process of band circulator, the power consumption of methanation unit is higher, its Patent " method of production synthetic natural gas, device and natural gas product thereof " CN101812339A discloses a kind of methanation patented technology with circulation, the mol ratio of circulation gas and unstripped gas is 1 ~ 9:1, and loaded catalyst is larger.For 1,300,000,000 Nm 3the coal preparing natural gas project of/a, the lowest power of this patents circulate compressor is about 5375kwh, and energy consumption of unit product is higher.
Accompanying drawing explanation
The process flow sheet of Fig. 1 for adopting in embodiment 1-3;
The process flow sheet of Fig. 2 for adopting in embodiment 4;
The process flow sheet of Fig. 3 for adopting in embodiment 5.
 
Embodiment
Arbitrary feature disclosed in this specification sheets (comprising any accessory claim, summary), unless specifically stated otherwise, all can be replaced by other equivalences or the alternative features with similar object.That is, unless specifically stated otherwise, each feature is an example in a series of equivalence or similar characteristics.
Embodiment 1:
The present embodiment carries out according to technical process shown in Fig. 1, first the synthetic gas obtained after gasification is utilized sulfur-resisting transformation and low-temperature rectisol desulfurization and decarburization, then this synthetic gas enters in superfinishing cleaner T1 the poisonous substance such as sulphur, chlorine, heavy metal thoroughly removed in synthetic gas, obtain total sulfur and be less than 0.02ppm, chlorine is less than 0.01ppm, and total heavy metal is less than 0.01ppm, and pressure is 3MPa, flow is the synthetic gas of 10000kmol/h, and butt composition (with volume fraction) of synthetic gas is H 263.91%, CO 19.58%, CO 21.3%, CH 414.79%, N 20.42%.Synthetic gas is divided into stream stock 5, stream stock 6 and stream stock 7 and enters the first main methanation adiabatic reactor R1, the second main methanation adiabatic reactor R2 and the 3rd main methanation adiabatic reactor R3 respectively, and the flow that the flow wherein flowing stock 5 is 3100kmol/h, the flow of stream stock 6 is 3000kmol/h and stream stock 7 is 3900kmol/h.The flow of stream stock 4 water vapor is 2800kmol/h, and pressure is 3.2MPa.The temperature in of the first main methanation adiabatic reactor R1, the second main methanation adiabatic reactor R2 and the 3rd main methanation adiabatic reactor R3 is respectively 603K, 603K and 603K, temperature out is respectively as 908K, 908K and 908K, and dry gas air speed is respectively 30000 h -1, 20000 h -1with 10000 h -1.The temperature in of the first secondary methanator R4 is respectively 583K, and temperature out is 810K, and dry gas air speed is 15000 h -1.The temperature in of the second secondary methanator R5 is respectively 573K, and temperature out is 678K, and dry gas air speed is 15000 h -1.And utilize recirculated water gas cooling to below 333K after recycling the heat of the second secondary methanator R5 exit gas, be separated saturation water, then enter the 3rd secondary methanator R6 and proceed methanation reaction.The temperature in of the 3rd secondary methanator R6 is respectively 543K, and temperature out is 633K, and dry gas air speed is 6000 h -1.Butt composition (volume fraction) of the 3rd secondary methanator R6 exit gas stream stock 23 is CH 4account for 96.70%, CO 2account for 0.44%, N 2account for 1.14%, H 2account for 1.71%, butt flow is 3672Kmol/h, then cools, and dehydration obtains product synthetic natural gas.
embodiment 2:
The present embodiment carries out according to technical process shown in Fig. 1, first the synthetic gas obtained after gasification is utilized sulfur-resisting transformation and low-temperature rectisol desulfurization and decarburization, then this synthetic gas enters in superfinishing cleaner T1 the poisonous substance such as sulphur, chlorine, heavy metal thoroughly removed in synthetic gas, obtain total sulfur and be less than 0.02ppm, chlorine is less than 0.01ppm, and total heavy metal is less than 0.01ppm, and pressure is 3MPa, flow is the synthetic gas of 10000kmol/h, and butt composition (volume fraction) of synthetic gas is H 263.91%, CO 19.58%, CO 21.3%, CH 414.79%, N 20.42%.Synthetic gas is divided into stream stock 5, stream stock 6 and stream stock 7 and enters the first main methanation adiabatic reactor R1, the second main methanation adiabatic reactor R2 and the 3rd main methanation adiabatic reactor R3 respectively, and the flow that the flow wherein flowing stock 5 is 3100kmol/h, the flow of stream stock 6 is 3650kmol/h and stream stock 7 is 3250kmol/h.The flow of stream stock 4 water vapor is 1500kmol/h, and pressure is 3.5MPa.The temperature in of the first main methanation adiabatic reactor R1, the second main methanation adiabatic reactor R2 and the 3rd main methanation adiabatic reactor R3 is respectively 603K, 603K and 603K, temperature out is respectively as 967K, 967K and 937K, and dry gas air speed is respectively 50000 h -1, 40000 h -1with 12000 h -1.The temperature in of the first secondary methanator R4 is respectively 583K, and temperature out is 838K, and dry gas air speed is 10000 h -1.The temperature in of the second secondary methanator R5 is respectively 573K, and temperature out is 697K, and dry gas air speed is 12000 h -1.And utilize recirculated water gas cooling to below 323K after recycling the heat of the second secondary methanator R5 exit gas, be separated saturation water, then enter the 3rd secondary methanator R6 and proceed methanation reaction.The temperature in of the 3rd secondary methanator R6 is respectively 543K, and temperature out is 633K, and dry gas air speed is 4000 h -1.Butt composition (volume fraction) of the 3rd secondary methanator R6 exit gas stream stock 23 is CH 4account for 96.72%, CO 2account for 0.43%, N 2account for 1.14%, H 2account for 1.70%, butt flow is 3671Kmol/h, then cools, and dehydration obtains product synthetic natural gas.
embodiment 3:
The present embodiment carries out according to technical process shown in Fig. 1, first the synthetic gas obtained after gasification is utilized sulfur-resisting transformation and low-temperature rectisol desulfurization and decarburization, then this synthetic gas enters in superfinishing cleaner T1 the poisonous substance such as sulphur, chlorine, heavy metal thoroughly removed in synthetic gas, obtain total sulfur and be less than 0.02ppm, chlorine is less than 0.01ppm, and total heavy metal is less than 0.01ppm, and pressure is 3.5MPa, flow is the synthetic gas of 10000kmol/h, and butt composition (volume fraction) of synthetic gas is H 263.91%, CO 19.58%, CO 21.3%, CH 414.79%, N 20.42%.。Synthetic gas is divided into stream stock 5, stream stock 6 and stream stock 7 and enters the first main methanation adiabatic reactor R1, the second main methanation adiabatic reactor R2 and the 3rd main methanation adiabatic reactor R3 respectively, and the flow that the flow wherein flowing stock 5 is 3970kmol/h, the flow of stream stock 6 is 3000kmol/h and stream stock 7 is 3030kmol/h.The flow of stream stock 4 water vapor is 6000kmol/h, and pressure is 4.0MPa.The temperature in of the first main methanation adiabatic reactor R1, the second main methanation adiabatic reactor R2 and the 3rd main methanation adiabatic reactor R3 is respectively 563K, 603K and 603K, temperature out is respectively as 833K, 835K and 825K, and dry gas air speed is respectively 40000 h -1, 30000 h -1with 20000 h -1.The temperature in of the first secondary methanator R4 is respectively 583K, and temperature out is 730K, and dry gas air speed is 20000 h -1.The temperature in of the second secondary methanator R5 is respectively 573K, and temperature out is 629K, and dry gas air speed is 20000 h -1.And utilize recirculated water gas cooling to below 323K after recycling the heat of the second secondary methanator R5 exit gas, be separated saturation water, then enter the 3rd secondary methanator R6 and proceed methanation reaction.The temperature in of the 3rd secondary methanator R6 is respectively 513K, and temperature out is 595K, and dry gas air speed is 4000 h -1.Butt composition (volume fraction) of the 3rd secondary methanator R6 exit gas stream stock 23 is CH 4account for 97.54%, CO 2account for 0.27%, N 2account for 1.15%, H 2account for 1.04%, butt flow is 3646Kmol/h, and then dehydration obtains product synthetic natural gas.
embodiment 4:
The present embodiment carries out according to technical process shown in Fig. 2, first the synthetic gas obtained after gasification is utilized sulfur-resisting transformation and low-temperature rectisol desulfurization and decarburization, then this synthetic gas enters in superfinishing cleaner T1 the poisonous substance such as sulphur, chlorine, heavy metal thoroughly removed in synthetic gas, obtain total sulfur and be less than 0.02ppm, chlorine is less than 0.01ppm, and total heavy metal is less than 0.01ppm, and pressure is 3.6MPa, flow is the synthetic gas of 10000kmol/h, and butt composition (volume fraction) of synthetic gas is H 263.91%, CO 19.58%, CO 21.3%, CH 414.79%, N 20.42%.Synthetic gas is divided into stream stock 5, stream stock 6, stream stock 7 and stream stock 8 and enters the first main methanation adiabatic reactor R1, the second main methanation adiabatic reactor R2, the 3rd main methanation adiabatic reactor R3 and the 4th main methanation adiabatic reactor R4 respectively, and the flow that the flow wherein flowing stock 5 is 3000kmol/h, the flow of stream stock 6 is 2450kmol/h, the flow of stream stock 7 is 3000kmol/h and stream stock 8 is 1550kmol/h.The flow of stream stock 4 water vapor is 3000kmol/h, and pressure is 4.5MPa.The temperature in of the first main methanation adiabatic reactor R1, the second main methanation adiabatic reactor R2, the 3rd main methanation adiabatic reactor R3 and the 4th main methanation adiabatic reactor R4 is respectively 563K, 603K, 603K and 563K, temperature out be respectively into 883K, 883,881K and 833K, dry gas air speed is respectively 40000 h -1, 30000 h -1, 30000 h -1with 20000 h -1.The temperature in of the first secondary methanator R4 is respectively 583K, and temperature out is 702K, and dry gas air speed is 10000 h -1.The temperature in of the second secondary methanator R5 is respectively 573K, and temperature out is 614K, and dry gas air speed is 12000 h -1.And utilize recirculated water gas cooling to below 323K after recycling the heat of the second secondary methanator R5 exit gas, be separated saturation water, then enter the 3rd secondary methanator R6 and proceed methanation reaction.The temperature in of the 3rd secondary methanator R6 is respectively 513K, and temperature out is 566K, and dry gas air speed is 6000 h -1.Butt composition (volume fraction) of the 3rd secondary methanator R6 exit gas stream stock 23 is CH 4account for 98.08%, CO 2account for 0.16%, N 2account for 1.16%, H 2account for 0.60%, butt flow is 3630Kmol/h, then cools, and dehydration obtains product synthetic natural gas.
embodiment 5:
The present embodiment carries out according to technical process shown in Fig. 3, first the synthetic gas obtained after gasification is utilized sulfur-resisting transformation and low-temperature rectisol desulfurization and decarburization, then this synthetic gas enters in superfinishing cleaner T1 the poisonous substance such as sulphur, chlorine, heavy metal thoroughly removed in synthetic gas, obtain total sulfur and be less than 0.02ppm, chlorine is less than 0.01ppm, and total heavy metal is less than 0.01ppm, and pressure is 6.0MPa, flow is the synthetic gas of 10000kmol/h, and butt composition (volume fraction) of synthetic gas is H 263.91%, CO 19.58%, CO 21.3%, CH 414.79%, N 20.42%.Synthetic gas is divided into stream stock 5, stream stock 6, stream stock 7 and stream stock 8 and enters the first main methanation adiabatic reactor R1, the second main methanation adiabatic reactor R2, the 3rd main methanation adiabatic reactor R3 and the 4th main methanation adiabatic reactor R4 respectively, and the flow that the flow wherein flowing stock 5 is 2300kmol/h, the flow of stream stock 6 is 2450kmol/h, the flow of stream stock 7 is 3000kmol/h and stream stock 8 is 2250kmol/h.The flow of stream stock 4 water vapor is 1500kmol/h, and pressure is 9.8MPa.The temperature in of the first main methanation adiabatic reactor R1, the second main methanation adiabatic reactor R2, the 3rd main methanation adiabatic reactor R3 and the 4th main methanation adiabatic reactor R4 is respectively 573K, 583K, 588K and 563K, temperature out is respectively as 932K, 933 K, 924K and 898K, and dry gas air speed is respectively 20000 h -1, 20000 h -1, 15000 h -1with 10000 h -1.And utilize recirculated water gas cooling to below 323K after recycling the heat of the 4th main methanator R4 exit gas, be separated saturation water, then enter the first secondary methanator R5 and proceed methanation reaction.First secondary methanator R5 adopts isothermal methanation reactor, and bed temperature is 603K, and dry gas air speed is 6000 h -1.Butt composition (volume fraction) of the first secondary methanator R5 exit gas stream stock 23 is CH 4account for 96.05%, CO 2account for 0.57%, N 2account for 1.14%, H 2account for 2.24%, butt flow is 3691Kmol/h, and then dehydration obtains product synthetic natural gas.

Claims (8)

1. coal synthetic natural gas and natural gas liquids without a circulation methanation process, it is characterized in that this technique comprises the steps:
Coal is made synthetic gas after sulfur-resisting transformation and low-temperature rectisol desulfurization and decarburization, synthetic gas enters in superfinishing cleaner the sulphur, chlorine, the heavy metal poison that thoroughly remove in synthetic gas, then synthetic gas is divided into some stocks and does not enter main methanation main reactor, and with water vapour, the synthetic gas entering the first main methanation main reactor is diluted, then successively by secondary methanator, and by the gas cooling after methanation before entering the secondary methanator of final stage, be separated saturation water, then CO and CO to remnants 2carry out full methanation reaction, then cool, dehydration obtain satisfactory synthetic natural gas SNG, or enter again low temperature separation process operation carry out separations liquefy, obtain natural gas liquids, hydrogen-rich gas and nitrogen-rich gas, wherein natural gas liquids is as product.
2. coal synthetic natural gas according to claim 1 and natural gas liquids without circulation methanation process, it is characterized in that: the synthetic gas going out superfinishing cleaner is divided into 3 strands or 4 strands.
3. coal synthetic natural gas according to claim 1 and natural gas liquids without circulation methanation process, it is characterized in that: described main methanation furnace temperature in is 563K-623K, temperature out is 825K-967K, is 10000 h with the volume space velocity that dry gas calculates -1-50000 h -1; The volume space velocity that the dry gas of last secondary methanator described calculates is 4000 h -1-8000 h -1, methanation furnace temperature in is 513K-573 DEG C.
4. coal synthetic natural gas according to claim 1 and natural gas liquids without circulation methanation process, it is characterized in that: enter the synthetic gas of the first main methanator and the mol ratio of water vapor is 0.48 ~ 1.51:1, and water vapor pressure P1 0.1MPa more than larger than methanation working pressure P2.
5. coal synthetic natural gas according to claim 1 and natural gas liquids without circulation methanation process, it is characterized in that: main methanator is adiabatic methanation reactor, secondary methanator is adiabatic or isothermal methanation reactor.
6. coal synthetic natural gas according to claim 1 and natural gas liquids without circulation methanation process, it is characterized in that: the methanation catalyst in described methanator take nickel as the methanation catalyst of main active component.
7. coal synthetic natural gas according to claim 1 and natural gas liquids without circulation methanation process, it is characterized in that: in described technological process, in being produced by waste heat boiler and superheater, pressure or high pressure steam reclaim the heat of the high-temperature gas of methanator outlet.
8. coal synthetic natural gas according to claim 1 and natural gas liquids without circulation methanation process, it is characterized in that: if the finished product are natural gas liquids, then low temperature separation process liquefaction operation utilizes rectifying tower to make methane rich oxidizing gases be divided into three strands, first strand is natural gas liquids, second strand is nitrogen-rich gas, 3rd strand is hydrogen-rich gas, and hydrogen-rich gas all turns back to the first main methanator entrance.
CN201410598644.5A 2014-10-31 2014-10-31 Non-circulating methanation process of coal-based synthetic natural gas and liquefied natural gas CN104357117A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201410598644.5A CN104357117A (en) 2014-10-31 2014-10-31 Non-circulating methanation process of coal-based synthetic natural gas and liquefied natural gas

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201410598644.5A CN104357117A (en) 2014-10-31 2014-10-31 Non-circulating methanation process of coal-based synthetic natural gas and liquefied natural gas

Publications (1)

Publication Number Publication Date
CN104357117A true CN104357117A (en) 2015-02-18

Family

ID=52524434

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201410598644.5A CN104357117A (en) 2014-10-31 2014-10-31 Non-circulating methanation process of coal-based synthetic natural gas and liquefied natural gas

Country Status (1)

Country Link
CN (1) CN104357117A (en)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105112111A (en) * 2015-09-24 2015-12-02 中国石化工程建设有限公司 Integration process and equipment for loop-free methanation of coal-based syngas to prepare natural gas
CN105296035A (en) * 2015-11-27 2016-02-03 中国海洋石油总公司 Hydrogen supplying methanation method for preparing synthetic natural gas
CN106190382A (en) * 2016-07-16 2016-12-07 中国科学院山西煤炭化学研究所 The technique that producing synthesis gas from coal carries out methanation synthesis substitute natural gas
CN106554830A (en) * 2015-09-30 2017-04-05 中国石油化工股份有限公司 Producing synthesis gas from coal prepares the technique for substituting natural gas
CN107868686A (en) * 2017-11-15 2018-04-03 太原理工大学 A kind of energy-saving method without circulation coal synthetic natural gas full methanation
CN108018103A (en) * 2017-12-15 2018-05-11 新地能源工程技术有限公司 A kind of volcano type temperature sequence process for synthesizing methane
CN111718760A (en) * 2020-06-23 2020-09-29 中国华能集团清洁能源技术研究院有限公司 Sulfur-tolerant methanation system and method for coal-based natural gas

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101550053A (en) * 2008-11-19 2009-10-07 新奥新能(北京)科技有限公司 New process for producing firedamp by syngas
CN102776041A (en) * 2012-07-30 2012-11-14 西南化工研究设计院有限公司 Multilevel methanation preparation method of natural gas from semi-coke exhaust
CN102827657A (en) * 2012-08-27 2012-12-19 东华工程科技股份有限公司 Isothermal methanation process method for coal to substitute natural gas
CN103242921A (en) * 2012-02-09 2013-08-14 中国科学院大连化学物理研究所 Technology for preparing natural gas from synthetic gas
CN103409187A (en) * 2013-08-05 2013-11-27 西南化工研究设计院有限公司 Methanation technology for preparing non-recycling gas of SNG or LNG from coke-oven gas
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
AU2013270551A1 (en) * 2012-12-26 2014-07-10 Institute For Advanced Engineering Apparatus and method for producing synthetic natural gas using low H2/CO ratio synthesis gas
CN103952197A (en) * 2014-05-13 2014-07-30 西南化工研究设计院有限公司 Process for co-producing LNG (Liquefied Natural Gas) by using pyrolysis gas generated in power generation system
CN104087354A (en) * 2014-06-30 2014-10-08 西南化工研究设计院有限公司 Process of preparing synthetic natural gas by using yellow phosphorus tail gas

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101550053A (en) * 2008-11-19 2009-10-07 新奥新能(北京)科技有限公司 New process for producing firedamp by syngas
CN103242921A (en) * 2012-02-09 2013-08-14 中国科学院大连化学物理研究所 Technology for preparing natural gas from synthetic gas
CN102776041A (en) * 2012-07-30 2012-11-14 西南化工研究设计院有限公司 Multilevel methanation preparation method of natural gas from semi-coke exhaust
CN102827657A (en) * 2012-08-27 2012-12-19 东华工程科技股份有限公司 Isothermal methanation process method for coal to substitute natural gas
AU2013270551A1 (en) * 2012-12-26 2014-07-10 Institute For Advanced Engineering Apparatus and method for producing synthetic natural gas using low H2/CO ratio synthesis gas
CN103409187A (en) * 2013-08-05 2013-11-27 西南化工研究设计院有限公司 Methanation technology for preparing non-recycling gas of SNG or LNG from coke-oven gas
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
CN103952197A (en) * 2014-05-13 2014-07-30 西南化工研究设计院有限公司 Process for co-producing LNG (Liquefied Natural Gas) by using pyrolysis gas generated in power generation system
CN104087354A (en) * 2014-06-30 2014-10-08 西南化工研究设计院有限公司 Process of preparing synthetic natural gas by using yellow phosphorus tail gas

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105112111A (en) * 2015-09-24 2015-12-02 中国石化工程建设有限公司 Integration process and equipment for loop-free methanation of coal-based syngas to prepare natural gas
CN106554830A (en) * 2015-09-30 2017-04-05 中国石油化工股份有限公司 Producing synthesis gas from coal prepares the technique for substituting natural gas
CN105296035A (en) * 2015-11-27 2016-02-03 中国海洋石油总公司 Hydrogen supplying methanation method for preparing synthetic natural gas
CN105296035B (en) * 2015-11-27 2018-03-27 中国海洋石油总公司 A kind of benefit hydrogen methanation process for producing synthetic natural gas
CN106190382A (en) * 2016-07-16 2016-12-07 中国科学院山西煤炭化学研究所 The technique that producing synthesis gas from coal carries out methanation synthesis substitute natural gas
CN106190382B (en) * 2016-07-16 2019-08-06 中国科学院山西煤炭化学研究所 Producing synthesis gas from coal carries out the technique that methane is combined to substitute natural gas
CN107868686A (en) * 2017-11-15 2018-04-03 太原理工大学 A kind of energy-saving method without circulation coal synthetic natural gas full methanation
CN108018103A (en) * 2017-12-15 2018-05-11 新地能源工程技术有限公司 A kind of volcano type temperature sequence process for synthesizing methane
CN111718760A (en) * 2020-06-23 2020-09-29 中国华能集团清洁能源技术研究院有限公司 Sulfur-tolerant methanation system and method for coal-based natural gas

Similar Documents

Publication Publication Date Title
CA2670395C (en) Improved absorbent regeneration
Descamps et al. Efficiency of an Integrated Gasification Combined Cycle (IGCC) power plant including CO2 removal
CN102115684B (en) Method for producing liquefied natural gas by using coke oven gas
CN101289620B (en) Integration process of coke dry quenching co-production synthesis gas and downstream products thereof of methanol
Zhou et al. CO2 emissions and mitigation potential in China’s ammonia industry
CN101597527B (en) Method for making synthetic natural gas by utilizing coke oven gas
CA2698906C (en) Improved method for regeneration of absorbent
WO2013131042A1 (en) Processes for producing synthetic hydrocarbons from coal, biomass, and natural gas
CN103275777B (en) Method for preparing hydrogen and liquefied natural gas through using gas retort raw gas
CN104945224B (en) A kind of methanol process
Sudiro et al. Synthetic Natural Gas (SNG) from coal and biomass: a survey of existing process technologies, open issues and perspectives
CN101649232B (en) Synthesis process of natural gas employing methanation of coke oven gas
CN102533365B (en) Process for coproducing liquefied natural gas (LNG) and synthetic ammonia
CN101293812B (en) Technique for joint production of methanol and natural gas with methyl hydride containing synthesis gas
Zhu et al. Thermodynamic analysis of H2 production from CaO sorption‐enhanced methane steam reforming thermally coupled with chemical looping combustion as a novel technology
CN101705128B (en) Adiabatic methanation process and device for preparing synthetic natural gas
WO2013053235A1 (en) Process for removing acid gas from flue gas by using waste heat of same
CN101245262B (en) Gas-steam combined cycle system and technique based on coal gasification and methanation
CN101649233B (en) Isothermal methanation process and device for the preparation of synthetic natural gas
Pattabathula et al. Introduction to ammonia production
CN104177227B (en) The method of coke(oven)gas and coal gas methanol with joint production Sweet natural gas
CN101892104B (en) Method for preparing liquefied natural gas by utilizing relief gas of methanol
CN103889546A (en) Methods and configurations for h2s concentration in acid gas removal
INGCHEM Zero Carbon Power Generation: IGCC as the Premium Option
CN104004547B (en) Coal gasification and coal coking co-supply and cogeneration system and method

Legal Events

Date Code Title Description
PB01 Publication
C06 Publication
SE01 Entry into force of request for substantive examination
C10 Entry into substantive examination
ASS Succession or assignment of patent right

Owner name: SOUTHWEST RESEARCH + DESIGN INSTITUTE OF CHEMICAL

Effective date: 20150519

Owner name: CNOOC GAS + POWER GROUP CO., LTD.

Free format text: FORMER OWNER: SOUTHWEST RESEARCH + DESIGN INSTITUTE OF CHEMICAL INDUSTRY CO., LTD.

Effective date: 20150519

CB03 Change of inventor or designer information

Inventor after: Hou Jianguo

Inventor after: Yi Shupeng

Inventor after: Mu Xiangyu

Inventor after: Zheng Hang

Inventor after: Zhang Bo

Inventor after: Tao Pengwan

Inventor after: Zhang Xinbo

Inventor after: Wang Xiulin

Inventor after: Yang Kuanhui

Inventor after: Gao Zhen

Inventor after: He Yang

Inventor after: Wang Chengshuo

Inventor after: Ma Lei

Inventor after: Li Ying

Inventor before: Zhang Xinbo

Inventor before: Yang Kuanhui

Inventor before: He Yang

Inventor before: Ma Lei

Inventor before: Yi Shupeng

Inventor before: Zheng Hang

Inventor before: Tao Pengwan

TA01 Transfer of patent application right

Effective date of registration: 20150519

Address after: 100027 Beijing city Chaoyang District East Third Ring Road No. 2 building comba

Applicant after: CNOOC Gas & Power Group

Applicant after: Southwest Chemical Research & Design Institute Co., Ltd.

Address before: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province in 610225

Applicant before: Southwest Chemical Research & Design Institute Co., Ltd.

C41 Transfer of patent application or patent right or utility model
C53 Correction of patent for invention or patent application
COR Change of bibliographic data

Free format text: CORRECT: INVENTOR; FROM: ZHANG XINBO YANG KUANHUI HE YANG MA LEI YI SHUPENG ZHENG HENG TAO PENGWAN TO: HOU JIANGUO ZHANG XINBO WANG XIULIN YANG KUANHUI GAO ZHEN HE YANG WANG CHENGSHUO MA LEI LI YING YI SHUPENG MU XIANGYU ZHENG HENG ZHANG BO TAO PENGWAN

RJ01 Rejection of invention patent application after publication

Application publication date: 20150218

RJ01 Rejection of invention patent application after publication