CN102502634A - Technological method for preparing food-grade CO2 based on high-concentration carbon dioxide exhaust gas - Google Patents

Technological method for preparing food-grade CO2 based on high-concentration carbon dioxide exhaust gas Download PDF

Info

Publication number
CN102502634A
CN102502634A CN2011103642228A CN201110364222A CN102502634A CN 102502634 A CN102502634 A CN 102502634A CN 2011103642228 A CN2011103642228 A CN 2011103642228A CN 201110364222 A CN201110364222 A CN 201110364222A CN 102502634 A CN102502634 A CN 102502634A
Authority
CN
China
Prior art keywords
gas
heat exchange
carry out
condensable gases
purification
Prior art date
Legal status (The legal status 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 status listed.)
Granted
Application number
CN2011103642228A
Other languages
Chinese (zh)
Other versions
CN102502634B (en
Inventor
皮金林
徐建民
夏炎华
鞠水清
李繁荣
严义刚
刘伟
任春芳
杨建国
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Wuhuan Engineering Co Ltd
Original Assignee
China Wuhuan Engineering Co Ltd
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 China Wuhuan Engineering Co Ltd filed Critical China Wuhuan Engineering Co Ltd
Priority to CN201110364222.8A priority Critical patent/CN102502634B/en
Publication of CN102502634A publication Critical patent/CN102502634A/en
Application granted granted Critical
Publication of CN102502634B publication Critical patent/CN102502634B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Landscapes

  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention relates to a technological method for preparing food-grade CO2 based on high-concentration carbon dioxide exhaust gas, wherein, the technological method solves the problems of complicated preparation technology, high energy consumption, high equipment investment, high running cost and large occupied area of prior food-grade CO2. The technological method adopts the technical scheme as follows: feed gas of high-concentration carbon dioxide is processed through compression, purification edulcoration, dehydration, rectification and cooling, and then the food-grade CO2 is obtained. The technological method is characterized in that part of feed gas enters a CO2 medium-pressure low-temperature rectifying tower in a rectification step so as to supply heat to a reboiler at the tower bottom after feed gas is compressed to reach the gage pressure of 4 to 6 MpaG; and then part of feed gas that is processed through heat exchange and residual feed gas are mixed and then enter the purification edulcoration step. The technological method has the advantages of simple technological process, low energy consumption of system operation, small occupied area, low equipment investment and low running cost.

Description

High concentration carbon dioxide discharging gas prepares food-class CO 2Process method
Technical field
The present invention relates to a kind of preparation food-class CO 2Process method, high concentration carbon dioxide discharging gas prepares food-class CO specifically 2Process method.
Background technology
Global warming has caused the extensive concern of countries in the world day by day to human and the issuable harm of whole global environment.In order to contain that the whole world increases warm trend, the Kyoto Protocol that passed through in 1997 will reduce global carbonic acid gas (CO 2) discharge and confirm as target from now on.How to reduce CO 2Discharging, become the problem of national governments and scientist's primary concern.The CO of domestic discharging 2Be mainly derived from fertilizer plant's tail gas, refinery exhaust, fermentation tail gas etc., be used for industries such as food, medicine, welding after reclaiming through appropriate technology, can either reduce CO 2Quantity discharged, can use it for industrial production again.
The method of separating purifying carbon dioxide gas has a lot, based on the source difference of carbon dioxide and user's requirement need not, generally can be divided into two types of chemical method and physics methods.Chemical method utilizes carbonic acid gas to carry out absorption extraction with the raw material of alkali substance reaction; Physical method comprises physical solvent absorption process, adsorption method of separation, film permeation method and cryogenic rectification method.
Cryogenic rectification method is claimed compression rectification technology again, at high concentration CO 2Discharging gas prepares food-class CO 2Method in, low-pressure process is produced food-class CO 2Pressure be 1.5MPaG, the temperature of saturation that this pressure is corresponding is-28.5 ℃, though this method CO 2Compressor efficiency is higher, but sink temperature must could liquefy about-35 ℃, to having relatively high expectations of ammonia refrigeration system.Middle-pressure process is produced food-class CO 2Pressure be generally 2.5MPaG, like (" chemical engineering design ", 2008 such as Yan Xiaoru; 18 (6)) proposed a kind of compression rectification technology, at first virgin gas has been compressed to 2.4MPaG, and after deliver to rectifier unit after the purifying treatment; And utilize the thermal source of LP steam as the rectifier unit reboiler; Its product purity can reach 99.99%, but owing to need to consume the thermal source of LP steam as rectifying tower, causes the energy consumption of device to increase.And high-pressure process is produced food-class CO 2The time, CO 2The about 8.0MPaG of preparation pressure, this pressure surpasses CO 2Emergent pressure, though just can cooling liquid with normal-temperature water, at least will be through 4～5 grades of compressions, so not only the compressor power consumption is too much, and system's requirement of withstand voltage is high, and is higher to the requirement of equipment, pipeline, instrument etc.In sum, so far, the preparation technology under the above-mentioned several kinds of pressure, its energy loss is all bigger, causes that complicated process of preparation, floor space are big, facility investment and running cost problem of higher.And through the non-condensable gases directly discharging usually of rectification process, cold is not well reclaimed and is utilized, and causes energy consumption to increase.
Summary of the invention
The objective of the invention is in order to solve the problems of the technologies described above, the high concentration carbon dioxide discharging gas that a kind of technical process largest optimization is provided, system's operation energy consumption is low, floor space is little, throwing is equipped with investment and running cost is low prepares food-class CO 2Process method.
Technology of the present invention comprises high concentration CO 2Virgin gas compression, purification and impurity removal, dehydration, rectifying and cooling obtain food-class CO 2, said virgin gas compression is to 4～6MPaG, and partial raw gas gets into the CO in the rectification step 2In to force down warm rectifying tower be the tower bottom reboiler heat supply, the part material device after the heat exchange is mixed into the purification and impurity removal step with surplus stock gas again.
In the said rectification step, the non-condensable gases that obtains after the rectifying carries out heat exchange with the purification virgin gas that after dehydrating step, obtains, and the non-condensable gases after the heat exchange gets into the adsorber regeneration of dehydrating step, the exhaust emissions after the regeneration.
Partial raw gas after the said heat exchange gets into the purification and impurity removal step again with being cooled to after surplus stock gas mixes below 40 ℃.
Said partial raw gas accounts for to 45～55% of compression back virgin gas TV.
Said non-condensable gases carry out earlier first heat exchange after-15～-5 ℃ again with purify virgin gas and carry out secondary heat exchange to 18～28 ℃ after, carry out the adsorber regeneration that three heat exchange (regenerative heater) get into dehydrating step after 180～200 ℃ again.
Said non-condensable gases is the CO in rectification step earlier 2In force down warm rectifying tower built-in interchanger carry out first heat exchange.Said built-in interchanger is preferably disposed on CO 2In force down the cat head of warm rectifying tower.
The non-condensable gases that obtains after the said rectifying is at CO 2In force down in the warm rectifying tower and carry out multi-step pressure reduction to 0.2 earlier～carry out heat exchange again behind the 0.5MPaG, the cold that decompression obtains is used for precooling and gets into CO 2In force down warm rectifying tower and carry out the gas-liquid mixture before the rectifying.The preferred secondary of said multi-step pressure reduction or three grades of decompressions can prevent highly compressed CO 2The low temperature material grade that only after once reducing pressure, forms dry ice and reduce pipeline and equipment.Said gas-liquid mixture is the gas-liquid mixture that in the co 2 liquefaction device, forms after by partial liquefaction through the purification virgin gas after the dehydrating step.
Described high concentration CO 2Discharging gas (is claimed high concentration CO again 2Virgin gas) CO 2Concentration can be with in the full scale plants such as hydrogen manufacturing, synthesizing methanol, synthetic ammonia, oil refining, natural gas field or fermentation, with CO such as decarburizations more than 60% (mol%) 2The high concentration CO that the enrichment operation is discharged 2Tail gas is virgin gas, especially with the high concentration CO of acid gas removal operation by-product 2Discharging gas is the most suitable.
Said virgin gas compression grade is 4～6MPaG, and the pressure of preferred compressed machine outlet is 5.0MPaG.The contriver has carried out further investigation to the compression rectification technology under the various pressure and has analyzed; Discovery is when compressing virgin gas to 4～6MPaG; The middle sink temperature of cold method (1.5MPaG) neither can occur must could liquefy about-35 ℃, to the problem of having relatively high expectations of ammonia refrigeration system; Do not reach 8MPaG, both do not exceeded CO 2Emergent pressure, the power consumption that makes compressor again in tolerance interval, thereby can not bring simultaneously the high problem high of system's requirement of withstand voltage to the equipment requirement of withstand voltage; Under the pressure of this 4～6MPaG, the heat that the raw material power of compression produces fills enough supply CO again 2In to force down warm rectifying tower be tower bottom reboiler institute heat requirement, and need not to consume in addition the thermal source of LP steam as rectifying tower, realized the utilization that system capacity is maximum and reduced energy consumption.
Carry out the tolerance of the partial raw gas of heat exchange after the said compression and can carry out choose reasonable, utilize this strand used heat as much as possible, so that partial raw gas after the heat exchange and surplus stock gas are good below can hybrid cooling to 40 ℃ according to the thermal load of reboiler.
Further, non-condensable gases need carry out multi-step pressure reduction (preferred secondary or three grades) and can prevent highly compressed CO after the rectifying in rectifying tower 2Once the decompression back forms the low temperature material grade of dry ice and reduction pipeline and equipment, and the cold that is produced during decompression is used for precooling and gets into CO 2In force down warm rectifying tower and carry out the virgin gas before the rectifying, further to reach energy saving purposes.Post-decompression non-condensable gases can carry out heat exchange with the purification virgin gas that after dehydrating step, obtains, and reduce purifying the temperature of virgin gas, thereby reduces or need not to use in addition other heat-eliminating medium; Reduce facility investment and running cost; Non-condensable gases after the heat exchange is recycled to the adsorbent reactivation that gets into dehydrating step, and the adsorber of said dehydrating step comprises switchable at least two adsorbers, during work; At least one virgin gas that is used for behind the adsorption treatment purification and impurity removal; A non-condensable gases that is used for after the manipulation of regeneration heat exchange, non-condensable gases can directly discharge as tail gas, can not pollute environment.
Because the non-condensable gases temperature is lower, consider the optimization that thermal exchange and adsorber regeneration are handled, preferably the non-condensable gases after the rectifying is carried out three heat exchange, at CO 2In force down warm rectifying tower built-in interchanger carry out first heat exchange; Carry out secondary heat exchange with the purification virgin gas again, carry out three heat exchange through regenerator at last, its advantage is the Optimization of Heat Exchanger Networks design; The energy utilization efficiency of raising system reduces and uses electric consumption.
Beneficial effect:
(1) makes full use of in the technological process reaction temperature difference and carry out heat exchange; Realized the recycling of energy to the full extent; And then reduced the investment and the running cost of original heat exchange required equipment, can significantly reduce with respect to the process flow operation cost under 1.5MPaG, 2.5MPaG, the 8.0MPaG pressure rating.
(2) directly discharge can be used as tail gas after the non-condensable gases recycling, not only environmentally friendly, also reduced the required refluxing unit of otherwise processed non-condensable gases, further reduced facility investment.
(3) technical process of the present invention is simple, and withstand voltage or heatproof requires lowlyer to equipment, and floor space is little, and is easy and simple to handle, be easy to control, the liquid food grade CO of production 2The standard-required that meets the state food grade carbon-dioxide, carbon dioxide purity>=99.9% (V/V), content of impurities≤0.1% (V/V).
Description of drawings
Fig. 1 is a process flow sheet of the present invention.
1-surge tank, 2-feed gas compressor, 3-de-oiling device, 4-devulcanizer, 5-dehydration tower, A-adsorber, B-adsorber, 6-regenerative heater, 7-co 2 heat exchanger, 8-co 2 liquefaction device, 9-rectifying tower, the built-in interchanger of 9.1-.
Embodiment
By 100,000 tons of/year food-class COs 2Design, virgin gas are the high concentration carbon dioxide discharging gas of synthetic ammonia installation by-product, and its concrete specification is seen table 1:
Table 1 virgin gas technical specification
Sequence number Title Specification (mol%) Remarks
1 CO 2 88.8
2 CO 40ppm
3 H 2 0.2
4 N 2 10.9
5 H 2S 3ppm
6 CH 4O 130pm
7 CH 4 15ppm
8 Ar 15ppm
9 Temperature, ℃ 25
10 Pressure, MPaG 0.04
Concrete technical process is:
From the high concentration CO that contains that out-of-bounds comes 2Discharging gas gets into feed gas compressor 2 and carries out the virgin gas compression after surge tank 1 voltage stabilizing, after virgin gas was compressed into 4～6MPa, the partial raw gas that wherein accounts for total raw material gas 45～55% got into rectifying tower 9 (CO again 2In force down warm rectifying tower) for the tower bottom reboiler heat supply; Mix the back after the heat exchange with surplus stock gas and be cooled to 40 ℃ and get into again and purify the de-oiling desulphurization system and carry out purification and impurity removal; Wherein, The de-oiling desulphurization system is made up of de-oiling device 3 and devulcanizer 4, said de-oiling device 3 and devulcanizer 4 series connection (also can be parallelly connected, all can realize virgin gas de-oiling desulfurization).Get into dehydration tower 5 through the virgin gas after the de-oiling desulfurization and carry out dehydrating step; Said dehydration tower is provided with two adsorber A, B; Be used for the virgin gas that adsorption treatment comes from the de-oiling desulphurization system when one; Then another then is used for the non-condensable gases of manipulation of regeneration after from the heat exchange of rectifying tower, two adsorber order switch operatings; Carry out rectifying through getting into again after the entering of the purification virgin gas after the dehydration co 2 heat exchanger 7 heat exchange cooling again after co 2 liquefaction device 8 partial condensations formation gas-liquid mixture is sent into rectifying tower 9 precoolings, obtain liquid CO after the rectification and purification 2Again through the cooling after see the battery limit (BL) off, can be used as product and send into downstream user, perhaps get into memory cell, low-temperature receiver from the refrigeration operation liquefied ammonia or other refrigeration agents.The liquid CO that generates 2Specification is seen table 2.
The by product non-condensable gases that the purification back produces carry out multi-step pressure reduction to 0.2～0.5MPaG at rectifying tower 9 tops, and the cold that decompression obtains is used for the gas-liquid mixture before precooling entering rectifying tower 9 carries out rectifying; Said post-decompression non-condensable gases is after 9.1 heat exchange of built-in interchanger of cat head are to-15～-5 ℃; Again in co 2 heat exchanger 7 with purify virgin gas and carry out secondary heat exchange to 18～28 ℃ after, at last through regenerative heater 6 carry out getting into behind three heat exchange to 180～200 ℃ be used for manipulation of regeneration in the dehydration tower 5 adsorber regeneration back as exhaust emissions.
100,000 tons of/year food-class COs in the present embodiment technology 2Design, than the production technique under the 2.5MPaG, but every year 1010000 tons in economized cycle water, save electricity 1,199 ten thousand kW can save about 5,000,000 yuan every year.
Table 2 product specification
Sequence number Project Unit Requirement Index
1 CO 2 vol％ ≥ 99.9
2 H 2O voL?ppm ≤ 20
3 Acidity Qualified
4 NO voL?ppm ≤ 2.5
5 NO 2 voL?ppm ≤ 2.5
6 SO 2 voL?ppm ≤ 1
7 Total sulfur (SO 2Except) voL?ppm ≤ 0.1
8 Hydrocarbon polymer (with methanometer) voL?ppm ≤ 50 (wherein methane<=20)
9 Benzene voL?ppm ≤ 0.02
10 Methyl alcohol voL?ppm ≤ 10
11 Ethanol voL?ppm ≤ 10
12 Acetaldehyde voL?ppm ≤ 0.2
13 Other oxygen-bearing organic matter voL?ppm ≤ 1
14 Vinylchlorid voL?ppm ≤ 0.3
15 Grease mass?ppm ≤ 5
16 Aqueous solution smell, taste and outward appearance Qualified
17 Residue on evaporation mass?ppm ≤ 10
18 O 2 voL?ppm ≤ 30
Sequence number Project Unit Requirement Index
19 CO voL?ppm ≤ 10
20 NH 3 voL?ppm ≤ 2.5
21 H 3P voL?ppm ≤ 0.3
22 HCN voL?ppm ≤ 0.5

Claims (7)

1. a high concentration carbon dioxide discharging gas prepares food-class CO 2Process method, comprise high concentration CO 2Virgin gas compression, purification and impurity removal, dehydration, rectifying and cooling obtain food-class CO 2, it is characterized in that said virgin gas compression is to 4～6MPaG, partial raw gas gets into the CO in the rectification step 2In to force down warm rectifying tower be the tower bottom reboiler heat supply, the part material device after the heat exchange is mixed into the purification and impurity removal step with surplus stock gas again.
2. process method as claimed in claim 1; It is characterized in that in the said rectification step, the non-condensable gases that obtains after the rectifying carries out heat exchange with the purification virgin gas that after dehydrating step, obtains; Non-condensable gases after the heat exchange gets into the adsorber regeneration of dehydrating step, the exhaust emissions after the regeneration.
3. process method as claimed in claim 1 is characterized in that, gets into the purification and impurity removal step again below partial raw gas after the said heat exchange and the surplus stock gas hybrid cooling to 40 ℃.
4. like claim 1 or 3 described process methodes, it is characterized in that said partial raw gas accounts for to 45～55% of compression back virgin gas TV.
5. process method as claimed in claim 2; It is characterized in that; Said non-condensable gases carry out earlier first heat exchange to-15～--after 5 ℃, again with purify virgin gas and carry out secondary heat exchange to 18～28 ℃ after, carry out getting into behind three heat exchange to 180～200 ℃ the adsorber regeneration of dehydrating step again.
6. process method as claimed in claim 2 is characterized in that, said non-condensable gases is the CO in rectification step earlier 2In force down warm rectifying tower built-in interchanger carry out first heat exchange.
7. like claim 1 or 2 or 6 described process methodes, it is characterized in that the non-condensable gases that obtains after the said rectifying is at CO 2In force down in the warm rectifying tower and carry out multi-step pressure reduction to 0.2 earlier～carry out heat exchange again behind the 0.5MPaG, the cold that decompression obtains is used for precooling and gets into CO 2In force down the gas-liquid mixture of warm rectifying tower.
CN201110364222.8A 2011-11-17 2011-11-17 Technological method for preparing food-grade CO2 based on high-concentration carbon dioxide exhaust gas Active CN102502634B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201110364222.8A CN102502634B (en) 2011-11-17 2011-11-17 Technological method for preparing food-grade CO2 based on high-concentration carbon dioxide exhaust gas

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201110364222.8A CN102502634B (en) 2011-11-17 2011-11-17 Technological method for preparing food-grade CO2 based on high-concentration carbon dioxide exhaust gas

Publications (2)

Publication Number Publication Date
CN102502634A true CN102502634A (en) 2012-06-20
CN102502634B CN102502634B (en) 2014-03-12

Family

ID=46214785

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201110364222.8A Active CN102502634B (en) 2011-11-17 2011-11-17 Technological method for preparing food-grade CO2 based on high-concentration carbon dioxide exhaust gas

Country Status (1)

Country Link
CN (1) CN102502634B (en)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106185935A (en) * 2016-08-31 2016-12-07 苏州制氧机股份有限公司 A kind of liquefaction purifying technique of co 2 liquefaction purifying plant
CN106348297A (en) * 2016-08-25 2017-01-25 重庆同辉气体有限公司 Process for producing food-grade carbon dioxide by virtue of resolving gas of decarburization procedure of synthesis ammonia MDEA method
CN107934963A (en) * 2017-11-28 2018-04-20 西南化工研究设计院有限公司 The preparation system and preparation method of a kind of food-class high-purity liquid CO 2
CN111389169A (en) * 2020-02-27 2020-07-10 大连中鼎化学有限公司 Device and method for recovering high-purity ammonia from compound semiconductor tail gas
CN112357923A (en) * 2020-11-10 2021-02-12 杨意斌 Production process and device of high-purity liquid carbon dioxide
CN117704745A (en) * 2023-12-05 2024-03-15 南京佳华科技股份有限公司 Efficient energy-saving preparation of food-grade CO 2 Method and system of (2)

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101040674A (en) * 2007-04-29 2007-09-26 湖南凯美特气体有限公司 Method for producing food level liquid carbon dioxide product
CN101538040A (en) * 2009-04-28 2009-09-23 文斌洁 Method for coproducing or singly producing food grade carbon dioxide and industrial grade carbon dioxide by utilizing industrial waste gas

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101040674A (en) * 2007-04-29 2007-09-26 湖南凯美特气体有限公司 Method for producing food level liquid carbon dioxide product
CN101538040A (en) * 2009-04-28 2009-09-23 文斌洁 Method for coproducing or singly producing food grade carbon dioxide and industrial grade carbon dioxide by utilizing industrial waste gas

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106348297A (en) * 2016-08-25 2017-01-25 重庆同辉气体有限公司 Process for producing food-grade carbon dioxide by virtue of resolving gas of decarburization procedure of synthesis ammonia MDEA method
CN106348297B (en) * 2016-08-25 2018-09-04 重庆同辉气体有限公司 The technique for producing food-grade carbon-dioxide using the resolution gas of synthesis ammonia MDEA method decarbonization process
CN106185935A (en) * 2016-08-31 2016-12-07 苏州制氧机股份有限公司 A kind of liquefaction purifying technique of co 2 liquefaction purifying plant
CN106185935B (en) * 2016-08-31 2018-01-23 苏州制氧机股份有限公司 A kind of liquefaction purifying technique of co 2 liquefaction purifying plant
CN107934963A (en) * 2017-11-28 2018-04-20 西南化工研究设计院有限公司 The preparation system and preparation method of a kind of food-class high-purity liquid CO 2
CN107934963B (en) * 2017-11-28 2019-08-23 西南化工研究设计院有限公司 A kind of preparation system and preparation method of food-class high-purity liquid CO 2
CN111389169A (en) * 2020-02-27 2020-07-10 大连中鼎化学有限公司 Device and method for recovering high-purity ammonia from compound semiconductor tail gas
CN112357923A (en) * 2020-11-10 2021-02-12 杨意斌 Production process and device of high-purity liquid carbon dioxide
CN117704745A (en) * 2023-12-05 2024-03-15 南京佳华科技股份有限公司 Efficient energy-saving preparation of food-grade CO 2 Method and system of (2)
CN117704745B (en) * 2023-12-05 2024-05-24 南京佳华科技股份有限公司 Efficient energy-saving preparation of food-grade CO2Method and system of (2)

Also Published As

Publication number Publication date
CN102502634B (en) 2014-03-12

Similar Documents

Publication Publication Date Title
CN101040674B (en) Method for producing food level liquid carbon dioxide product
CN102115684B (en) Method for producing liquefied natural gas by using coke oven gas
CN102502634B (en) Technological method for preparing food-grade CO2 based on high-concentration carbon dioxide exhaust gas
CN201729816U (en) Liquid nitrogen washing device for purifying synthesis gas
CN103011198B (en) Process for preparing synthetic ammonia with coke-oven gas
CN102079999A (en) Method for producing liquefied natural gas and synthetic gas by taking coke oven gas as raw material
CN102538398A (en) Process and system for purifying, separating and liquefying nitrogen-and-oxygen-containing coal mine methane (CMM)
CN106000000B (en) A kind of the multistage flash distillation parsing separator and method of synthesis ammonia decarburization absorption tower bottom rich solution
CN101575540A (en) Method for producing liquefied natural gas and carbinol simultaneously
CN101929788A (en) Device for preparing liquefied natural gas by oxygen-bearing coal mine methane
CN102977960A (en) Process for co-producing and synthetic natural gas and food-grade carbon dioxide by using calcium carbide furnace gas
CN104031710A (en) Process for producing liquefied natural gas by using coke-oven gas
CN102765733B (en) Device and technique of producing liquid ammonia by coke oven gas and methanol relief gas
CN102435045A (en) Liquid nitrogen washing purified synthetic gas and device for cryogenically separating and recovering LNG (liquefied natural gas) thereof
CN103695043B (en) Method for drying, purifying and cooling conversion rough synthesized gas and SNG product gas through low-temperature methanol washing and device thereof
CN104557386A (en) Refinery mixed dry gas recovery system and recovery method
CN105258452A (en) Gas separation device and method of pyrolysis gas
CN103030494B (en) Absorption and hydration coupling device and method for separating ethylene and ethane in catalytic cracking dry gas or ethylene pyrolysis gas
CN204508803U (en) The device of a kind of high efficiency separation synthetic gas hydrogen making and carbon monoxide
CN104194852A (en) High-yield light hydrocarbon recovery method from low-pressure natural gas
CN103396853A (en) Technology for preparing natural gas by purifying biogas
CN101637694B (en) Method for separating and recycling CO2 from mixed gas containing CO2
CN202382518U (en) Device for washing and purifying synthesis gas with liquid nitrogen and cryogenically separating and recovering LNG (liquefied natural gas)
CN102634395A (en) Process and system for purifying and refining coal-bed gas
CN116839310A (en) Process method for preparing food-grade liquid carbon dioxide by utilizing decarburization exhaust gas of LNG (liquefied Natural gas) plant

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant