CN205079542U - System for prepare hydrogen rich gas and liquid methane - Google Patents
System for prepare hydrogen rich gas and liquid methane Download PDFInfo
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- CN205079542U CN205079542U CN201520715675.4U CN201520715675U CN205079542U CN 205079542 U CN205079542 U CN 205079542U CN 201520715675 U CN201520715675 U CN 201520715675U CN 205079542 U CN205079542 U CN 205079542U
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Abstract
The utility model relates to a system for prepare hydrogen rich gas and liquid methane. This system is mainly including speeding to exit purification unit and low temperature liquefaction separating element. The utility model discloses a mix cryogen compression cycle refrigeration, nitrogen gas circulation compression refrigeration and waste gas inflation refrigeration, synthetic ammonia or methyl alcohol speed to exit, and the rectification separation obtains hydrogen rich gas and liquid methane in high -efficient rectifying column, and the flow is simple, the energy consumption is low, and the rate of recovery is high. The utility model provides a good reliability, the system for prepare hydrogen rich gas and liquid methane that the running cost is low, product purity is high.
Description
Technical field
The utility model relates to gas separaion field, particularly a kind of system producing hydrogen rich gas and liquid methane from synthetic ammonia or methanol purge gas.
Background technology
Ammonia or methyl alcohol are all one of important source material of basic organic chemical industry, the synthesis of ammonia or methyl alcohol mainly with coal or natural gas for raw material, obtaining synthesis gas through certain conversion, will take coal as raw material at China's synthetic ammonia or methyl alcohol corporate boss processed, except producing active principle CO and H in building-up process
2outward, also CH is produced
4and N
2etc. invalid gas, along with a large amount of invalid component of carrying out of reaction assembles the conversion ratio affecting reaction, invalid component needs discharger to produce a large amount of synthetic ammonia or methanol purge gas, and periodic off-gases key component comprises H
2, CH
4, CO and N
2.
At present, synthetic ammonia or methanol purge gas generally carry hydrogen by UF membrane or transformation method of inhaling, and hydrogen recovery rate is low, also containing a large amount of H in residual gas
2, CH
4as fuel combustion, periodic off-gases utilizes still to be in a kind of low value level and carries out, deficiency in economic performance, and brings pollution to environment.
Liquid methane is a kind of clean, efficient energy, and calorific value is high is convenient to transport, in recent years because Natural Gas Demand rises and rise in price, pipe natural gas is by the restriction of pipeline delivery tube net, cost of transportation is higher, therefore separation of methane and hydrogen produce liquid methane from synthesis purge gas, not only synthesize periodic off-gases and be utilized effectively, economic benefit is also considerable.
Application number is 201320852728.8, name is called the Chinese patent of the device producing liquefied natural gas and rich hydrogen production from high methane gas, although be 201210065876.5 to application number, name is called dehydrogenation nitrogen from high methane gas and produces the technique of liquefied natural gas and the Chinese patent of device and application number to be 210010291609.5, name is called dehydrogenation from high methane gas, nitrogen, carbon monoxide the Chinese patent producing the technique of liquefied natural gas has some to improve in refrigeration, but be consume external chilled water for cost, and chilled water is obtained by the cooling of lithium cold mechanism of qi group, the work of lithium cold mechanism of qi group also needs to consume a part of steam, therefore certain limitation is caused to use, and cause a kind of waste.
Utility model content
The purpose of this utility model is that overcoming above-mentioned deficiency of the prior art provides the system producing hydrogen rich gas and liquid methane that a kind of good reliability, operating cost are low, product purity is high.
The technical solution of the utility model is achieved in that a kind of system producing hydrogen rich gas and liquid methane, and this system mainly comprises periodic off-gases clean unit and low-temperature liquefaction separative element; Described low-temperature liquefaction separative element comprises liquefaction cold box system, azeotrope circulation compressibility and nitrogen circulation compressibility; Described liquefaction cold box system comprises the first plate-fin heat exchanger, the second plate-fin heat exchanger, high-pressure rectification tower, low-pressure distillation tower and waste expansion machine; Described high-pressure rectification column overhead is provided with the first condenser, is provided with evaporimeter, tower top is provided with the second condenser at the bottom of described low-pressure distillation tower tower; Described azeotrope circulation compressibility comprises one-level azeotrope compressor, one-level cooler, secondary azeotrope compressor, secondary coolers and separator; Described nitrogen circulation nitrogen compressor that compressibility is drawn together and the 3rd cooler.
Described clean unit, the first plate-fin heat exchanger hot junction, low-pressure distillation tower evaporimeter, the second plate-fin heat exchanger hot junction, high-pressure rectification tower, choke valve, low-pressure distillation tower connect successively; Low-pressure distillation tower bottom discharge mouth is connected successively with the second plate-fin heat exchanger hot junction, choke valve; Low-pressure distillation tower top discharge mouth is connected successively with the second plate-fin heat exchanger cold junction, waste expansion machine expanding end, the second plate-fin heat exchanger cold junction, the first plate-fin heat exchanger cold junction; High-pressure rectification column overhead discharging opening is connected successively with the second plate-fin heat exchanger cold junction, the first plate-fin heat exchanger cold junction.
Described nitrogen compressor, machine aftercooler, the first plate-fin heat exchanger hot junction, the second plate-fin heat exchanger hot junction connect successively; Second plate-fin heat exchanger cold junction, liquid nitrogen choke valve, three-way pipe, high-pressure rectification tower condenser are connected with low-pressure distillation tower condenser; Described high-pressure rectification tower condenser gas outlet is connected with low-pressure distillation tower condenser gas outlet, three-way pipe, the first plate-fin heat exchanger cold junction, the second plate-fin heat exchanger cold junction, nitrogen compressor entrance; Described nitrogen compressor forms closed circulation system.
Described one-level azeotrope compressor, one-level cooler, secondary azeotrope compressor, secondary coolers, separator inlet connect successively; The liquid-phase outlet of described separator, the first plate-fin heat exchanger hot junction, choke valve, three-way pipe connect successively; The gaseous phase outlet of described separator, the first plate-fin heat exchanger hot junction, the second plate-fin heat exchanger hot junction, choke valve, the second plate-fin heat exchanger cold junction, three-way pipe connect successively; Three-way pipe, the first plate-fin heat exchanger cold junction, one-level azeotrope suction port of compressor connect successively; Described azeotrope compressor forms closed circulation system.
The first described plate fin heat-exchanging and the second plate-fin heat exchanger, evaporimeter, the first condenser and the second condenser are as vacuum brazing plate-fin heat exchanger, and described high-pressure rectification tower and low-pressure distillation tower are packed tower.
Waste expansion machine is gas axle decompressor or oily axle decompressor, comprises pressurized end and expanding end.
Produce a method for hydrogen rich gas and liquid methane, the method comprises following process:
Synthetic ammonia or methanol purge gas through clean unit, by after the adsorbent in clean unit by the trace amounts of CO in off-gas
2remove with water, off-gas after imurity-removal enters the first plate-fin heat exchanger and is cooled to uniform temperature, enter described low-pressure distillation tower evaporimeter to be cooled further as thermal source, cooling in the second plate-fin heat exchanger is entered after cooling, cooled gas enters described high-pressure rectification tower and carries out rectifying separation, obtain hydrogen at tower top to enter the re-heat of backflowing of the second described plate-fin heat exchanger cold junction and the first plate-fin heat exchanger cold junction and obtain hydrogen rich gas product, at the bottom of high-pressure rectification tower tower, obtain CH
4the liquid section that purity is higher flows to and carries out rectifying separation into described low-pressure distillation tower, the liquid methane that purity is higher is obtained at the bottom of tower, liquid methane enters the second plate-fin heat exchanger hot junction and crosses cold throttling and to go out to liquefy cold box system, tower top obtains entering waste expansion machine expanding end swell refrigeration after waste gas enters the second described plate-fin heat exchanger cold junction re-heat, enter the re-heat of backflowing of the first plate-fin heat exchanger cold junction after again entering the second plate-fin heat exchanger cold junction re-heat after refrigeration to go out to liquefy cold box system, enter described waste expansion machine pressurized end supercharging;
Described azeotrope circulation compressibility, azeotrope cools and enters described separator after described one-level azeotrope compressor, secondary azeotrope compressor compresses to certain pressure, and liquid phase cryogen enters the first described plate-fin heat exchanger and is cooled to uniform temperature throttling refrigeration; Gas phase cryogen enters the first described plate-fin heat exchanger, the second plate-fin heat exchanger cooling throttling refrigeration, backflow and enter the second described plate-fin heat exchanger, be mixed into the first described plate-fin heat exchanger re-heat with cryogen after liquid phase throttling and enter described one-level azeotrope suction port of compressor, complete azeotrope kind of refrigeration cycle;
Described nitrogen circulation compressibility, nitrogen is compressed to certain pressure through described nitrogen compressor and enters the first described plate-fin heat exchanger and the second plate-fin heat exchanger is cooled to uniform temperature, described high-pressure rectification tower condenser is entered and low-pressure distillation tower condenser provides cold after throttling, backflow after gasification and enter the re-heat of backflowing of the second described plate-fin heat exchanger and the first plate-fin heat exchanger and enter described nitrogen compressor, complete nitrogen kind of refrigeration cycle.
Nitrogen compressor outlet pressure is: 2.0 ~ 3.0MPa; Azeotrope compressor second stage exit pressure is 3.0 ~ 4.0MPa.
In azeotrope circulation compressibility use that refrigerant medium is methane, ethene, propane, isopentane and nitrogen mix in a ratio.
Clean unit inlet pressure is: 1.6MPa ~ 7.0MPa; Described low-pressure distillation pressure tower is 0.4 ~ 0.8MPa; Described waste expansion machine expanding end outlet pressure is 0.035 ~ 0.05MPa.
The good effect that the technical solution of the utility model produces is as follows:
Utilize the waste expansion of low-pressure distillation column overhead to freeze, the internal circulating load of azeotrope can be reduced, according to different unstripped gas composition, power consumption about 1% ~ 11% can be saved.
Highly purified rich H not only can be obtained by this two-tower process
2and liquefied natural gas product, and H
2and CH
4the rate of recovery high, H
2the rate of recovery 98%, CH
4the rate of recovery 98.7%.
This device product hydrogen purity is high, enters and only extracts H at present
2pSA or membrane separation device, improve the H reclaiming hydrogen system into PSA or UF membrane
2concentration, thus the hydrogen recovery rate improving device, reduce the processing load of PSA or film separation system.
Described high-pressure rectification tower and low-pressure distillation tower adopt packed tower, resistance is little, rectification effect good, operating flexibility is large, is suitable for Off-design operation.
Accompanying drawing explanation
Fig. 1 is the structural representation that the utility model produces the system of hydrogen rich gas and liquid methane.
Be labeled as in figure: 1, the first plate-fin heat exchanger; 2, evaporimeter; 3, the second plate-fin heat exchanger; 4, high-pressure rectification tower; 5, second throttle; 6, low-pressure distillation tower; 7, the first condenser; 8, the second condenser; 9, the first three-way pipe; 10, the second three-way pipe; 11, the 3rd choke valve; 12, the 5th choke valve; 13, the 4th choke valve; 14, waste expansion machine; 15, expanding end; 16, pressurized end; 17, the 3rd three-way pipe; 18, first throttle valve; 19, nitrogen compressor; 20, the 3rd cooler; 21, one-level azeotrope compressor; 22, one-level cooler; 23, secondary azeotrope compressor; 24, secondary coolers; 25, separator; 26, clean unit; 27, low-pressure distillation tower bottom discharge mouth; 28, low-pressure distillation tower top of tower discharging opening; 29, high-pressure rectification column overhead discharging opening; 30, the cold junction of the second plate-fin heat exchanger; 31, the hot junction of the second plate-fin heat exchanger; 32, the cold junction of the first plate-fin heat exchanger; 33, the hot junction of the first plate-fin heat exchanger; 34, the first condenser gas outlet; 35, the second condenser gas outlet; 36, separator liquid phase outlet; 37, separator gaseous phase outlet.
Detailed description of the invention
embodiment one
As shown in Figure 1, a kind of system producing hydrogen rich gas and liquid methane, mainly comprises periodic off-gases clean unit and low-temperature liquefaction separative element.Described low-temperature liquefaction separative element comprises liquefaction cold box system, azeotrope circulation compressibility and nitrogen circulation compressibility; Described liquefaction cold box system comprises the first plate-fin heat exchanger 1, second plate-fin heat exchanger 3, high-pressure rectification tower 4, low-pressure distillation tower 6 and waste expansion machine 14; Described high-pressure rectification tower 4 tower top is provided with the first condenser 7, is provided with evaporimeter 2, tower top is provided with the second condenser 8 at the bottom of described low-pressure distillation tower 6 tower; Described azeotrope circulation compressibility comprises one-level azeotrope compressor 21, one-level cooler 22, secondary azeotrope compressor 23, secondary coolers 24 and separator 25; Described nitrogen circulation nitrogen compressor that compressibility is drawn together 19 and the 3rd cooler 20.
The hot junction 33 of described clean unit 26, first plate-fin heat exchanger, the hot junction 31 of low-pressure distillation tower evaporimeter 2, second plate-fin heat exchanger, high-pressure rectification tower 4, second throttle 5, low-pressure distillation tower 6 connect successively; Hot junction 31, the 3rd choke valve 11 of low-pressure distillation tower bottom discharge mouth 27 and the second plate-fin heat exchanger are connected successively; Low-pressure distillation tower top of tower discharging opening 28 is connected successively with the cold junction 32 of cold junction 30, first plate-fin heat exchanger of expanding end 15, second plate-fin heat exchanger of the second plate-fin heat exchanger cold junction 30, waste expansion machine 14; High-pressure rectification column overhead discharging opening 29 is connected successively with the cold junction 32 of cold junction 30, first plate-fin heat exchanger of the second plate-fin heat exchanger.
The hot junction 31 of hot junction 33, second plate-fin heat exchanger of described nitrogen compressor 19, the 3rd cooler 20, first plate-fin heat exchanger connects successively; The cold junction 30 of the second plate-fin heat exchanger, the 5th choke valve 12, first three-way pipe 9, high-pressure rectification tower first condenser 7 are connected with low-pressure distillation tower second condenser 8; High-pressure rectification tower first condenser gas outlet 34 is connected with low-pressure distillation tower second condenser gas outlet 35, second three-way pipe 10, second plate-fin heat exchanger cold junction 30, first plate-fin heat exchanger cold junction 32, nitrogen compressor 19; Described nitrogen compressor forms closed circulation system.
Described azeotrope compressor one-level azeotrope compressor 21, one-level cooler 22, secondary azeotrope compressor 23, secondary coolers 24, separator 25 connect successively; The hot junction 33 of separator liquid phase outlet the 36, first plate-fin heat exchanger, first throttle valve 18, the 3rd three-way pipe 17 connect successively; The hot junction 31 of hot junction 33, second plate-fin heat exchanger of separator gaseous phase outlet 36, first plate-fin heat exchanger, the cold junction 30 of the 4th choke valve 13, second plate-fin heat exchanger, the 3rd three-way pipe 17 connect successively; Cold junction 32, the one-level azeotrope compressor 21 of the 3rd three-way pipe 17, first plate-fin heat exchanger connect successively; Described azeotrope compressor forms closed circulation system.
The first described plate fin heat-exchanging 1 and the second plate-fin heat exchanger 3, evaporimeter 2, first condenser 7 and the second condenser 8 are as vacuum brazing plate-fin heat exchanger, and described high-pressure rectification tower 4 and low-pressure distillation tower 6 are packed tower.
Described waste expansion machine 14 is gas axle decompressor or oily axle decompressor, comprises pressurized end 16 and expanding end 15.
embodiment two
Produce a method for hydrogen rich gas and liquid methane, pressure be the synthetic ammonia of 1.6MPa ~ 7.0MPa or methanol purge gas through clean unit 26, by after the adsorbent in clean unit by the trace amounts of CO in off-gas
2remove with water, off-gas after imurity-removal enters the first plate-fin heat exchanger 1 and is cooled to 145K ~ 165K, enter described low-pressure distillation tower evaporimeter 2 to be cooled further as thermal source, cooled temperature is 135K ~ 155K, enter in the second plate-fin heat exchanger 3 and be cooled to 110K ~ 117K, cooled gas enters described high-pressure rectification tower 4 and carries out rectifying separation, obtaining purity at high-pressure rectification tower top is that the re-heat of backflowing of the cold junction 32 of the cold junction 30 and the first plate-fin heat exchanger that the hydrogen of 91.4%mol enters the second described plate-fin heat exchanger obtains hydrogen rich gas product, CH is obtained at the bottom of the tower of high-pressure rectification tower 4
4the liquid that purity is higher enters described low-pressure distillation tower 6 through second throttle 5 throttling to 0.4 ~ 0.8MPa and carries out rectifying separation, the liquid methane that purity is 98.1%mol is obtained at the bottom of low-pressure distillation tower tower, liquid methane enters the second plate-fin heat exchanger hot junction 31 and is excessively chilled to 117K, be throttled to 0.15MPa by the 3rd choke valve 11 to go out to liquefy cold box system, low-pressure distillation column overhead obtains entering waste expansion machine expanding end expansion 15 to 0.035 ~ 0.05MPa refrigeration after waste gas enters the second described plate-fin heat exchanger cold junction 30 re-heat, enter the re-heat of backflowing of the first plate-fin heat exchanger cold junction 32 after again entering the second described plate-fin heat exchanger cold junction 30 re-heat after refrigeration to go out to liquefy cold box system, enter described waste expansion machine pressurized end 16 supercharging.
Described azeotrope circulation compressibility, mixing pressure by methane, ethene, propane, isopentane and nitrogen in a ratio is that the azeotrope of 0.25MPa ~ 0.35MPa is cooled to 313K through described one-level azeotrope compressor 21, secondary azeotrope compressor 23 and enters described separator 25 after being compressed to 3.0 ~ 4.0MPa, liquid phase cryogen enters the first described plate-fin heat exchanger 1 and is cooled to 145K ~ 165K, is throttled to 0.3 ~ 0.4MPa refrigeration by first throttle valve 18; Gas phase cryogen enters the first described plate-fin heat exchanger 1, second plate-fin heat exchanger 3 and is cooled to 110K ~ 117K, by the 4th choke valve 13 throttling to 0.35 ~ 0.45MPa refrigeration, backflow and enter the second described plate-fin heat exchanger 3, be mixed into the first described plate-fin heat exchanger 1 re-heat with cryogen after liquid phase throttling and enter described one-level azeotrope compressor 21, complete azeotrope kind of refrigeration cycle.
Described nitrogen circulation compressibility, the nitrogen of 0.25MPa ~ 0.4MPa is compressed to 2.0 ~ 3.0MPa through described nitrogen compressor 19 and enters the first described plate-fin heat exchanger 1 and the second plate-fin heat exchanger 3 cools 110 ~ 120K, by entering described high-pressure rectification tower first condenser 7 after the 5th choke valve 12 throttling to 0.3 ~ 0.5MPa and low-pressure distillation tower second condenser 8 provides cold, backflow after gasification and enter the re-heat of backflowing of the second described plate-fin heat exchanger 3 and the first plate-fin heat exchanger 1 and enter described nitrogen compressor 19, complete nitrogen kind of refrigeration cycle.
Claims (6)
1. produce a system for hydrogen rich gas and liquid methane, it is characterized in that: this system mainly comprises periodic off-gases clean unit and low-temperature liquefaction separative element; Described low-temperature liquefaction separative element comprises liquefaction cold box system, azeotrope circulation compressibility and nitrogen circulation compressibility; Described liquefaction cold box system comprises the first plate-fin heat exchanger, the second plate-fin heat exchanger, high-pressure rectification tower, low-pressure distillation tower and waste expansion machine; Described high-pressure rectification column overhead is provided with the first condenser, is provided with evaporimeter, tower top is provided with the second condenser at the bottom of described low-pressure distillation tower tower; Described azeotrope circulation compressibility comprises one-level azeotrope compressor, one-level cooler, secondary azeotrope compressor, secondary coolers and separator; Described nitrogen circulation nitrogen compressor that compressibility is drawn together and the 3rd cooler.
2. a kind of system producing hydrogen rich gas and liquid methane according to claim 1, is characterized in that: described clean unit, the first plate-fin heat exchanger hot junction, low-pressure distillation tower evaporimeter, the second plate-fin heat exchanger hot junction, high-pressure rectification tower, choke valve, low-pressure distillation tower connect successively; Low-pressure distillation tower bottom discharge mouth is connected successively with the second plate-fin heat exchanger hot junction, choke valve; Low-pressure distillation tower top discharge mouth is connected successively with the second plate-fin heat exchanger cold junction, waste expansion machine expanding end, the second plate-fin heat exchanger cold junction, the first plate-fin heat exchanger cold junction; High-pressure rectification column overhead discharging opening is connected successively with the second plate-fin heat exchanger cold junction, the first plate-fin heat exchanger cold junction.
3. a kind of system producing hydrogen rich gas and liquid methane according to claim 1, is characterized in that: described nitrogen compressor, machine aftercooler, the first plate-fin heat exchanger hot junction, the second plate-fin heat exchanger hot junction connect successively; Second plate-fin heat exchanger cold junction, liquid nitrogen choke valve, three-way pipe, high-pressure rectification tower condenser are connected with low-pressure distillation tower condenser; Described high-pressure rectification tower condenser gas outlet is connected with low-pressure distillation tower condenser gas outlet, three-way pipe, the first plate-fin heat exchanger cold junction, the second plate-fin heat exchanger cold junction, nitrogen compressor entrance; Described nitrogen compressor forms closed circulation system.
4. a kind of system producing hydrogen rich gas and liquid methane according to claim 1, is characterized in that: described one-level azeotrope compressor, one-level cooler, and secondary azeotrope compressor, secondary coolers, separator inlet connect successively; The liquid-phase outlet of described separator, the first plate-fin heat exchanger hot junction, choke valve, three-way pipe connect successively; The gaseous phase outlet of described separator, the first plate-fin heat exchanger hot junction, the second plate-fin heat exchanger hot junction, choke valve, the second plate-fin heat exchanger cold junction, three-way pipe connect successively; Three-way pipe, the first plate-fin heat exchanger cold junction, one-level azeotrope suction port of compressor connect successively; Described azeotrope compressor forms closed circulation system.
5. a kind of system producing hydrogen rich gas and liquid methane according to claim 1, it is characterized in that: the first described plate fin heat-exchanging and the second plate-fin heat exchanger, evaporimeter, the first condenser and the second condenser are as vacuum brazing plate-fin heat exchanger, and described high-pressure rectification tower and low-pressure distillation tower are packed tower.
6. a kind of system producing hydrogen rich gas and liquid methane according to claim 1, is characterized in that: waste expansion machine is gas axle decompressor or oily axle decompressor, comprises pressurized end and expanding end.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520715675.4U CN205079542U (en) | 2015-09-16 | 2015-09-16 | System for prepare hydrogen rich gas and liquid methane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520715675.4U CN205079542U (en) | 2015-09-16 | 2015-09-16 | System for prepare hydrogen rich gas and liquid methane |
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| Publication Number | Publication Date |
|---|---|
| CN205079542U true CN205079542U (en) | 2016-03-09 |
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ID=55431945
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520715675.4U Withdrawn - After Issue CN205079542U (en) | 2015-09-16 | 2015-09-16 | System for prepare hydrogen rich gas and liquid methane |
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| CN (1) | CN205079542U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105180595A (en) * | 2015-09-16 | 2015-12-23 | 开封空分集团有限公司 | System and method for preparing hydrogen rich gas and liquid methane |
| CN109028756A (en) * | 2018-05-23 | 2018-12-18 | 上海交通大学 | A method of coke-stove gas is separated using helium swell refrigeration |
-
2015
- 2015-09-16 CN CN201520715675.4U patent/CN205079542U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105180595A (en) * | 2015-09-16 | 2015-12-23 | 开封空分集团有限公司 | System and method for preparing hydrogen rich gas and liquid methane |
| CN105180595B (en) * | 2015-09-16 | 2017-06-27 | 开封空分集团有限公司 | A kind of system and method for producing hydrogen rich gas and liquid methane |
| CN109028756A (en) * | 2018-05-23 | 2018-12-18 | 上海交通大学 | A method of coke-stove gas is separated using helium swell refrigeration |
| CN109028756B (en) * | 2018-05-23 | 2019-09-27 | 上海交通大学 | A method of coke-stove gas is separated using helium swell refrigeration |
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| C14 | Grant of patent or utility model | ||
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Granted publication date: 20160309 Effective date of abandoning: 20170627 |