CN200952872Y - Air-bearing coalbed methane liquefaction separation equipment - Google Patents
Air-bearing coalbed methane liquefaction separation equipment Download PDFInfo
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- CN200952872Y CN200952872Y CN 200620122543 CN200620122543U CN200952872Y CN 200952872 Y CN200952872 Y CN 200952872Y CN 200620122543 CN200620122543 CN 200620122543 CN 200620122543 U CN200620122543 U CN 200620122543U CN 200952872 Y CN200952872 Y CN 200952872Y
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- 238000000926 separation method Methods 0.000 title claims abstract description 51
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title description 21
- 238000005057 refrigeration Methods 0.000 claims abstract description 59
- 239000003245 coal Substances 0.000 claims abstract description 40
- 238000007906 compression Methods 0.000 claims abstract description 13
- 230000006835 compression Effects 0.000 claims abstract description 12
- 238000002309 gasification Methods 0.000 claims abstract description 12
- 239000003034 coal gas Substances 0.000 claims description 10
- 239000003507 refrigerant Substances 0.000 claims description 8
- 238000004140 cleaning Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 13
- 238000000746 purification Methods 0.000 abstract description 5
- 239000002994 raw material Substances 0.000 abstract 2
- 239000007789 gas Substances 0.000 description 98
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 18
- 239000007788 liquid Substances 0.000 description 15
- 239000002808 molecular sieve Substances 0.000 description 14
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 14
- 238000001035 drying Methods 0.000 description 12
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 8
- 238000001816 cooling Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 229910001868 water Inorganic materials 0.000 description 6
- 239000003949 liquefied natural gas Substances 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 235000019628 coolness Nutrition 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000002671 adjuvant Substances 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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Abstract
The utility model discloses a gasification and liquefaction separation equipment containing a air and coal layer, consisting of a compression purification equipment, a refrigeration equipment and a liquefaction separation equipment. The liquefaction separation equipment has a heat exchanging unit, the compression purification equipment is connected with a raw material air thermal medium channel of the heat exchanging unit in the liquefaction separation equipment, the refrigeration equipment is connected with a refrigerating medium channel of the heat exchanging unit in the liquefaction separation equipment, the liquefaction separation equipment consists of a fractionating tower connected with the heat exchanging unit, on the fractionating tower top part is provided with a condenser, on the fractionating tower bottom part is provided with a evaporator, the raw material air thermal medium channel of the heat exchanging unit is lead into the middle part of the fractionating tower, an air pipe provided to the upper part of the fractionating tower is lead into the heat exchanging unit. The utility model gasification and liquefaction separation equipment containing a air and coal layer is designed for the liquefaction separation process of the coal layer containing air specially, adopts a single stage rectifying equipment which is easier than the double stage rectifying process and more convenient to operate. The utility model is less cost and fit for popularizing in a large scale.
Description
Technical field
The utility model relates to a kind of gas liquefaction separation equipment, particularly contains the liquefaction separation equipment of air coal bed gas.
Background technology
Coal bed gas also claims unconventional natural gas or mine gas, and its main component is a methane.It is not only a kind of clean energy resource of preciousness, also is important chemical material.The coal bed gas resource of China is very abundant, but the exploitation fewer, almost do not have industrial application.It is reported, the coal bed gas that China enters atmosphere every year account for the whole world mine discharging the coal bed gas total amount 1/3rd, this has not only caused serious atmosphere pollution, also is the very big wasting of resources.
The characteristics of coal bed gas are that well yield is not really high, and except that using nearby, tubing is defeated outward usually uneconomical.Especially the coal bed gas of extraction in the coal mining process, because pressure is low, methane content is low, and wherein be mixed with air, airborne oxygen is dangerous combustion adjuvant, this has brought difficulty just for the processing and the transportation of coal bed gas, and it is just more serious that emptying is wasted, and this problem never is well solved.If contain the coal bed gas (mainly being methane) in the air coal bed gas and air separation is come out and will purify after coal gas gasification, this just is very easy to transportation and utilizes.
The liquefied natural gas technology has the history in three, 40 years so far since the just commercialization of the sixties in last century.China's liquefied natural gas industry is in developing stage, and domestic circulation to various liquefied natural gas is grasped substantially.No matter but be external or domestic, the liquefied natural gas technology all is higher at purity, not aeriferous natural gas.To the separation and the liquefaction of aeriferous coal bed gas, also do not cause people's attention, the phenomenon that contains air coal bed gas emptying discharging is still very serious.
Conventional separation method has absorption process, absorption method, film permeation method and cryogenic rectification method etc.The front several method, the purity of separation is difficult to reach requirement, and the rate of recovery that has is low, and therefore what have also needs heating, contains air coal bed gas explosive at high temperature, has potential safety hazard, is not applied.Proposing name on May 19th, 2006 the applicant is called in the patent application of " containing air coal gas gasification equipment ", proposition is applied in cryogenic rectification equipment in the separation and liquefaction that contains the air coal bed gas, a kind of technology of twin-stage rectifying has been described, but this process equipment needed thereby is more, technology is comparatively numerous and diverse, input cost is higher, is unfavorable for applying in small-scale colliery.
The utility model content
Technical problem to be solved in the utility model provides a kind of liquefaction separation equipment that contains the air coal bed gas, adopts the low-temperature single-stage rectificating method, and equipment is more simple.
For solving the problems of the technologies described above, technical solution adopted in the utility model is:
A kind of liquefaction separation equipment that contains the air coal bed gas, comprise the compression cleaning equipment, refrigeration plant and liquefaction separation equipment, described liquefaction separation equipment has heat exchanger, the raw gas heat medium channel of the heat exchanger in compression cleaning equipment and the separation equipment that liquefies is connected, refrigeration plant is connected with the heat exchanger refrigerant passage of liquefaction separation equipment, described liquefaction separation equipment comprises that a fractionating column links to each other with heat exchanger, the fractionating column top has condenser, the fractionating column bottom has evaporimeter, the raw gas heat medium channel of heat exchanger is introduced into the fractionating column middle part, and the top of described fractionating column has a gas piping to be introduced in the heat exchanger.
Wherein, described refrigeration plant is gas swell refrigeration equipment or mix refrigerant refrigeration plant; Described fractionating column top has gas piping that gas is incorporated in the gas swell refrigeration equipment; The refrigerant pipeline of the condenser of described fractionating column is communicated with the refrigeration air pipe of refrigeration plant; The evaporimeter heating pipe line of described fractionating column is with the refrigeration air pipe or contain air coal bed gas pipeline and be connected.
The beneficial effect that the utility model can reach is: it is to aim at the separation liquefaction process that contains the design of air coal bed gas that the utility model contains air coal gas gasification separation equipment, adopt the single-stage rectifying device, technology than twin-stage rectifying is simpler, more convenient operation, its input cost is lower, is beneficial to large-scale promotion.
Description of drawings
Fig. 1 is the utility model embodiment 1 and embodiment 2 compression cleaning equipment schematic diagrames;
Fig. 2 is the utility model embodiment 1 refrigeration plant and liquefaction separation equipment schematic diagram;
Fig. 3 is the utility model embodiment 2 refrigeration plants and liquefaction separation equipment schematic diagram.
The specific embodiment
Consult Fig. 1, Fig. 2, for the utility model embodiment 1 contains air coal gas gasification separation equipment schematic diagram, comprise the two large divisions, at first contain the compressed purification earlier of air coal bed gas unstripped gas, separate through liquefaction again and can obtain liquified natural gas, the required cold of separation process that wherein liquefies is provided by refrigeration system, and concrete equipment and technology are described below:
Consult Fig. 1, be the utility model compression cleaning equipment schematic diagram.Comprise filter 1, gas-liquid separator 2, compressor 3, cooler 4, molecular sieve equipment group, described molecular sieve drying equipment group comprises three molecular sieve drying machines 5,6,7, when 5 work of first molecular sieve drying machine, second molecular sieve drying machine 6 thermal regeneration, the 3rd molecular sieve drying machine 7 coolings are standby, switch once in per 8 hours.This molecular sieve drying equipment is mainly used to remove water, carbon dioxide.Filter 8 is arranged after the molecular sieve equipment group, go back having heaters 22.
The technological process that compression purifies is as follows:
1, the air coal bed gas unstripped gas that contains that the self-discharging pipeline comes at first removes dust through filter 1;
2, after containing the air coal bed gas and enter gas-liquid separator 2 gas-liquid separations after the dedusting, gas enters compressor 3 compressions;
3, compression is after cooler 4 coolings;
4, contain the air coal bed gas and enter molecular sieve drying machine 5, deviate from water and carbon dioxide, a part of heater via 9 of the pure air that produces in the flow process is heated to 240-250 ℃, be used for the regeneration of molecular sieve drying machine 6, another part directly enters the good drying machine 7 of having regenerated, cooling molecular sieve, the temperature of reduction molecular sieve drying machine 7, use the air in the nitrogen replacement molecular sieve drying machine 7 then, standby;
6, through molecular sieve drying equipment remove water, carbon dioxide and oxygen contain air coal bed gas unstripped gas again through filter 8 can enter refrigeration, separation equipment liquefies.
Consult Fig. 2, for the utility model embodiment 1 contains air coal bed gas refrigeration, liquefaction separation equipment schematic diagram, comprise refrigeration plant and liquefaction separation equipment, the cold that refrigeration plant obtains is by heat exchanger 16,10, condenser 12 and its contain air coal bed gas heat exchange.Described liquefaction separation equipment comprises that the heat exchanger 16,10 and the bottom that connect successively have evaporimeter 11, top that the fractionating column 13 of condenser 12 is arranged.The refrigeration piping of condenser 12 links to each other with the pipeline of refrigeration system, the water back of evaporimeter 11 links to each other with the pipeline of unstripped gas between heat exchanger 16,10, the unstripped gas pipeline of heat exchanger 10 cold junctions links to each other with the fractionating column middle part, fractionating column 13 tops have gas pipeline to link to each other with heat exchanger 10,16 successively, fractionating column top also has pipeline to link to each other with heat exchanger 10,16 successively, and the fractionating column bottom also has liquid line that liquid natural gas is connected to output valve.
The liquefying separation process step is as follows:
1, compressed purification contains air coal bed gas (methane 50%, air 50%) enters in the heat exchanger 16 and refrigerant heat-shift wherein, after descending, temperature enters the water back of evaporimeter 11 again, cause the liquid evaporation in the evaporimeter, the gas self-temperature further descends, enter heat exchanger 10 again, make temperature drop to-168 ℃, pressure is 0.6Mpa;
2, the air coal bed gas that contains after temperature descends enters the middle part of fractionating column 13 through the valve 0.45MPa that reduces pressure, its liquid flows through column plate from top to bottom, part at the evaporimeter 11 contain air coal bed gas liquid of fractionating column 13 bottoms is evaporated to gas, heating-up temperature is about-140 ℃, and the gas that is evaporated upwards flows and the liquid that flows downward carries out heat, matter exchange;
3, on the top of fractionating column (more than the unstripped gas inlet), upwards the gas that flows arrives the fractionating column top, and by the condenser condenses at fractionating column top, wherein a part is condensed into liquid again, reflux downwards, carry out heat, matter exchange again as liquid distillate and gas equally.The condensation temperature of condenser 12 is about-180 ℃, and pressure is about 0.44Mpa;
4, on the top of fractionating column, temperature is outwards emitted a part of gas again for a column plate place of-180 ℃ between top of tower and unstripped gas inlet, flow is about 43% of unstripped gas, and this part gas is pure air, and its oxygen content is a little more than air, be 24%, contain methane content few (being 0.07%), temperature is about-176 ℃, and pressure is about 0.44MPa, this part gas enters heat exchanger 10,22 successively, reclaims cold;
5, the top from fractionating column emits a part of gas, and flow is about 7% of unstripped gas, and this part gas is very pure nitrogen, and purity is 99.95%, and temperature is about-180 ℃, and pressure is about 0.44MPa, also enters heat exchanger 10,16 successively, reclaims cold.
What 6, emit from fractionating column 13 bottoms is exactly the very high liquefaction coal bed gas of purity.Flow is 50% of a unstripped gas, and purity reaches more than 99.9%, and temperature is about-140 ℃, and pressure is about 0.44MPa.
Heat exchanger 16,10 and condenser 12 needed colds are provided by refrigeration plant in the above-mentioned liquefaction separation process, and refrigeration plant is the mix refrigerant refrigeration plant, comprises refrigeration machine 14 and compressor 15.
Consult Fig. 3, for the utility model embodiment 2 contains air coal bed gas refrigeration plant and liquefaction separation equipment schematic diagram.The liquefaction separation equipment comprises three grades of heat exchangers 23,24,25, fractionating column 26, and condenser 27 is arranged at the fractionating column top, and evaporimeter 28 is arranged at the fractionating column bottom, and the structure of fractionating column is identical with embodiment 1.Refrigeration plant is a gas compression-expansion refrigeration system, has adopted a compressor 22, cooler 29 and two turbo-expanders 17,18.Fractionating column condenser 27 has gas piping that gas is incorporated in the pipeline of refrigeration plant.The refrigeration piping of condenser 27 links to each other with the pipeline of refrigeration plant, and the water back of evaporimeter 28 links to each other with the pipeline of refrigeration gas between heat exchanger 23,24, and the air coal bed gas unstripped gas pipeline that contains of heat exchanger 25 cold junctions links to each other with the fractionating column middle part.
The liquefying separation process step is as follows:
1, the air coal bed gas unstripped gas (methane 50%, air 50%) that contains of compressed purification enters heat-shift in the heat exchanger 23,24,25, and reducing temperature, to reach-168 ℃, pressure be 0.63MPa;
2, the air coal bed gas that contains after temperature descends enters the middle part of fractionating column 26 through the valve 0.45MPa that reduces pressure, its liquid flows through column plate from top to bottom, part at the evaporimeter 28 contain air coal bed gas liquid of fractionating column 26 bottoms is evaporated to gas, heating-up temperature is about-140 ℃, and the gas that is evaporated upwards flows and the liquid that flows downward carries out heat, matter exchange;
3, on the top of fractionating column (more than the unstripped gas inlet), upwards the gas that flows arrives the fractionating column top, and by condenser 27 condensations at fractionating column top, wherein a part is condensed into liquid again, reflux downwards, carry out heat, matter exchange again as liquid distillate and gas equally.The condensation temperature of condenser 27 is about-180 ℃, and pressure is about 0.44MPa;
4, on the top of fractionating column, temperature is outwards emitted a part of gas again for a column plate place of-180 ℃ between top of tower and unstripped gas inlet, flow is about 43% of unstripped gas, this part gas is pure air, its oxygen content is a little more than air, be 24%, contain methane content few (being 0.07%), temperature is about-176 ℃, pressure is about 0.44MPa, and this part gas enters heat exchanger 25,24,23 successively, reclaims cold, after the re-heat, this part gas can be used as the thermal regeneration and the refrigerating gas of clarifier.
5, the top from fractionating column emits a part of gas, flow is about 7% of unstripped gas, this part gas is very pure nitrogen, purity is 99.95%, temperature is about-180 ℃, and pressure is about 0.44MPa, converges with refrigeration gas behind the 0.3MPa that reduces pressure, enter heat exchanger 25,24,23 successively, reclaim cold.
What 6, emit from fractionating column 26 bottoms is exactly the very high liquefaction coal bed gas of purity.Flow is 50% of a unstripped gas, and purity reaches more than 99.9%, and temperature is about-140 ℃, and pressure is about 0.44MPa.
1, before refrigeration system starts, is full of nitrogen in the system as refrigeration gas.
2, start refrigeration system, earlier compressed machine 22 compressions of refrigeration gas, 17,18 superchargings of turbine supercharger are passed through in cooling again in cooler 29, through cooler 19 coolings, enter 23 precoolings of first heat exchanger again, and temperature is reduced to-124 ℃.
3, refrigeration gas is further cooled to-137 ℃ through the pipeline (temperature is for-140 ℃) of evaporimeter 28 again, the gas that freezes then is divided into two-way, one tunnel tolerance is 30% to enter turbo-expander 20, the back temperature that expands is-169 ℃, another road tolerance is 70% to enter second heat exchanger 24, be-158 ℃ from heat exchanger 24 temperature of coming out, enter turbo-expander 21 swell refrigerations again.
4, the refrigeration temperature degree after expanding from turbo-expander 21 is-185 ℃, it is introduced into the refrigeration piping of condenser 13, for condenser 27 provides low-temperature receiver, subsequently, refrigeration temperature degree raises to-181.4 ℃, the nitrogen that comes out with the fractionating column top converges again, backflows to enter the 3rd heat exchanger 25 and be used for cooling off unstripped gas.
5, the refrigeration temperature degree that comes out from the hot junction of heat exchanger 11 raises and is-169 ℃, and the gas (temperature also is-169 ℃) after it and turbo-expander 20 expand converges, and enters heat exchanger 24,23 more successively, as the low-temperature receiver of heat exchanger.After this part gas re-heat, unnecessary nitrogen can be done the cold blowing displacement gas of clarifier, the then recompression of most of nitrogen, supercharging, cooling, swell refrigeration, so circulation.
Owing to itself can produce nitrogen in the flow process, enough be used for replenishing the leakage of refrigeration system, after therefore starting, do not need to buy again nitrogen.
Claims (5)
1, a kind of air coal gas gasification separation equipment that contains, comprise the compression cleaning equipment, refrigeration plant and liquefaction separation equipment, described liquefaction separation equipment has heat exchanger, the raw gas heat medium channel of the heat exchanger in compression cleaning equipment and the separation equipment that liquefies is connected, refrigeration plant is connected with the heat exchanger refrigerant passage of liquefaction separation equipment, described liquefaction separation equipment comprises that a fractionating column links to each other with heat exchanger, the fractionating column top has condenser, the fractionating column bottom has evaporimeter, it is characterized in that: the raw gas heat medium channel of heat exchanger is introduced into the fractionating column middle part, and the top of described fractionating column has a gas piping to be introduced in the heat exchanger.
2, a kind of air coal gas gasification separation equipment that contains according to claim 1, it is characterized in that: described refrigeration plant is gas swell refrigeration equipment or mix refrigerant refrigeration plant.
3, a kind of air coal gas gasification separation equipment that contains according to claim 2, it is characterized in that: described fractionating column top has gas piping that gas is incorporated in the gas swell refrigeration equipment.
4, a kind of air coal gas gasification separation equipment that contains according to claim 1, it is characterized in that: the refrigerant pipeline of the condenser of described fractionating column is communicated with the refrigeration air pipe of refrigeration plant.
5, a kind of air coal gas gasification separation equipment that contains according to claim 1 is characterized in that: the evaporimeter heating pipe line of described fractionating column is with the refrigeration air pipe or contain air coal bed gas pipeline and be connected.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620122543 CN200952872Y (en) | 2006-07-03 | 2006-07-20 | Air-bearing coalbed methane liquefaction separation equipment |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200620124725 | 2006-07-03 | ||
| CN200620124725.2 | 2006-07-03 | ||
| CN 200620122543 CN200952872Y (en) | 2006-07-03 | 2006-07-20 | Air-bearing coalbed methane liquefaction separation equipment |
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| Publication Number | Publication Date |
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| CN200952872Y true CN200952872Y (en) | 2007-09-26 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 200620122543 Expired - Lifetime CN200952872Y (en) | 2006-07-03 | 2006-07-20 | Air-bearing coalbed methane liquefaction separation equipment |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100404988C (en) * | 2006-07-03 | 2008-07-23 | 中国科学院理化技术研究所 | Liquefaction separation process and equipment of air-bearing coalbed methane |
| CN101922849A (en) * | 2010-09-07 | 2010-12-22 | 上海交通大学 | Liquefaction and rectification method of oxygen-containing coalbed methane |
| CN102203530A (en) * | 2008-02-20 | 2011-09-28 | 国际壳牌研究有限公司 | Method and apparatus for cooling and separating a hydrocarbon stream |
| CN102713479A (en) * | 2008-11-03 | 2012-10-03 | 国际壳牌研究有限公司 | Method of rejecting nitrogen from a hydrocarbon stream to provide a fuel gas stream and an apparatus therefor |
| CN108728150A (en) * | 2017-04-19 | 2018-11-02 | 神华集团有限责任公司 | The heat-exchange method for the tail gas that the method and its system of DCL/Direct coal liquefaction and DCL/Direct coal liquefaction generate |
| CN111718769A (en) * | 2020-06-29 | 2020-09-29 | 山西晋煤天源化工有限公司 | Comprehensive utilization synthetic ammonia tail gas preparation PNG system |
-
2006
- 2006-07-20 CN CN 200620122543 patent/CN200952872Y/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100404988C (en) * | 2006-07-03 | 2008-07-23 | 中国科学院理化技术研究所 | Liquefaction separation process and equipment of air-bearing coalbed methane |
| CN102203530A (en) * | 2008-02-20 | 2011-09-28 | 国际壳牌研究有限公司 | Method and apparatus for cooling and separating a hydrocarbon stream |
| CN102713479A (en) * | 2008-11-03 | 2012-10-03 | 国际壳牌研究有限公司 | Method of rejecting nitrogen from a hydrocarbon stream to provide a fuel gas stream and an apparatus therefor |
| CN101922849A (en) * | 2010-09-07 | 2010-12-22 | 上海交通大学 | Liquefaction and rectification method of oxygen-containing coalbed methane |
| CN108728150A (en) * | 2017-04-19 | 2018-11-02 | 神华集团有限责任公司 | The heat-exchange method for the tail gas that the method and its system of DCL/Direct coal liquefaction and DCL/Direct coal liquefaction generate |
| CN108728150B (en) * | 2017-04-19 | 2020-11-13 | 神华集团有限责任公司 | Method and system for direct liquefaction of coal and heat exchange method for tail gas produced by direct liquefaction of coal |
| CN111718769A (en) * | 2020-06-29 | 2020-09-29 | 山西晋煤天源化工有限公司 | Comprehensive utilization synthetic ammonia tail gas preparation PNG system |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: PHYSICAL CHEMISTRY TECHNOLOGY INST., CHINESE ACAD Free format text: FORMER OWNER: BEIJING KERUI SAISI GAS LIQUEFACTION TECHNOLOGY CO., LTD. Effective date: 20080104 |
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| C41 | Transfer of patent application or patent right or utility model | ||
| C53 | Correction of patent of invention or patent application | ||
| CB03 | Change of inventor or designer information |
Inventor after: Yang Kejian Inventor after: Zhang Wu Inventor after: Ren Xiaokun Inventor after: Yang Zhongwei Inventor before: Yang Kejian |
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| COR | Change of bibliographic data |
Free format text: CORRECT: INVENTOR; FROM: YANG KEJIAN TO: YANG KEJIAN; ZHANG WU; REN XIAOKUN; YANG ZHONGWEI |
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| TR01 | Transfer of patent right |
Effective date of registration: 20080104 Address after: Beijing, Zhongguancun, Haidian District, No. 2, north, zip code: 100080 Patentee after: Technical Institute of Physics and Chemistry Chinese Academy of Sciences Address before: Room 1, building two, building 3, North 201, Beijing, Haidian District, Zhongguancun: 100080 Patentee before: Beijing Cryosys Technical Company of Gas Liquefaction Co.,Ltd. |
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| CX01 | Expiry of patent term |
Granted publication date: 20070926 |
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| EXPY | Termination of patent right or utility model |