CN101628198A - Pressure-swing adsorption method of directly enriching methane from coal bed gas - Google Patents
Pressure-swing adsorption method of directly enriching methane from coal bed gas Download PDFInfo
- Publication number
- CN101628198A CN101628198A CN200910194625A CN200910194625A CN101628198A CN 101628198 A CN101628198 A CN 101628198A CN 200910194625 A CN200910194625 A CN 200910194625A CN 200910194625 A CN200910194625 A CN 200910194625A CN 101628198 A CN101628198 A CN 101628198A
- Authority
- CN
- China
- Prior art keywords
- adsorption tower
- absorption
- pressure
- adsorption
- adsorbent
- 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.)
- Pending
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/20—Capture or disposal of greenhouse gases of methane
Landscapes
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention relates to a pressure-swing adsorption method of directly enriching methane from coal bed gas. The method comprises the following steps: pumping the coal bed gas in a multi-tower absorption device; absorbing N2 on adsorbent and directly collecting CH4 at an outlet by a pressure-swing adsorption technology; and desorbing in vacuum or by depressurization to regenerate and recycle the adsorbent. The pressure-swing adsorption technological parameters comprise pressurized adsorption pressure controlled in a range of 0.1-1 MPa, depressurization desorption pressure controlled in a range of 0.1-0 MPa and temperature controlled in a range from 80 DEG C below zero to 120 DEG C. The technology uses 4A, 5A zeolite molecular sieves and carbon molecular sieves with modified orifices as the adsorbent and obtains the CH4 with purity up to 95-99.9 percent by the steps. Compared with the prior technology of collecting the CH4 product gas on the adsorbent by enriching, depressurizing and absorbing the CH4 on the adsorbent, the invention has obvious advantages, comprehensively utilizes the drawing and the discharge of the low-concentration coal bed gas and has an important meaning to guarantee the safe production of mine, reduce the atmosphere pollution and improve and optimize the domestic energy structure. The technology has simple process, convenient operation and good safe performance and is beneficial to mass popularization.
Description
Technical field
The present invention relates to a kind of coalbed gas condensation method, belong to gas separation technique field.
Background technology
Along with the raising of people, attach great importance to the development and use of coal bed gas in recent years both at home and abroad to safety of coal mines, environmental protection consciousness.The active ingredient of coal bed gas is CH
4, CH
4Be a kind of energy and industrial chemicals of high effect cleaning, but also be a kind of greenhouse gases simultaneously.China is coal resources big countries, and the coal bed gas reserves are abundant, are 35 tcms, occupy the third place in the world.2000 meters of buried depths reach 31.46 tcms with interior coal bed gas resource amount, and wherein 1500 meters of buried depths are with interior 60% of the total resources that accounts for.And the coal bed gas that present China discharges because of mining every year accounts for 1/3 of world's coal bed gas total emission volumn more than 130 billion cubic meters, ranks first in the world.Under the situation of current China's natural gas energy deficiency, people constantly turn one's attention to unconventional natural gas when extensively paying attention to the conventional gas exploitation---the development and utilization of coal bed gas.If can effectively utilize these coal bed gas resources, improvement and optimization energy resource structure, guarantee Safety of Coal Mine Production, minimizing atmosphere pollution there is important meaning.
Coal bed gas is as a kind of high-efficiency cleaning energy, and main component is CH
4, secondly be N
2And O
2, also have a small amount of or micro-hydrocarbon gas and CO in addition
2, H
2, He, H
2S etc., hot average is 35800kJ/m
3(being equivalent to the 1.22kg standard coal), there is not flue dust in the combustion process substantially.CH
4Calorific value be 33500～33700kJ/m
3, by calorific value calculation, roughly 1000m
3CH
4Be equivalent to the 1t standard coal.The gas utilization of China is CH basically at present
4Concentration is civilian in being used for more than 35%, low concentration CH
4Then directly be discharged in the middle of the atmosphere.CH
4Be a kind of greenhouse gases, can have caused serious destruction to environment, its greenhouse effects compare CO
2Wanting big 20 times, it is entered atmosphere, not only because can cause unusual weather conditions by greenhouse effects, also can consume the ozone in the atmospheric advection layer, is CO to the depletion of the ozone layer ability
27 times.
The outer impurity content of deacration is less relatively in the coal bed gas, is CH through pretreated coal bed gas compositions such as desulfurization, dryings
4, N
2And O
2, with CH
4/ air or CH
4/ N
2Expression that is to say that the separation of coal bed gas comes down to CH after the preliminary clearning
4With N
2Between separation.
At present, main concentrated coal bed gas technology has both at home and abroad:
(1) film separates: membrane separation technique is that the partial pressure difference with film both sides gas is a motive force, and the difference that produces transfer rate between component by steps such as dissolving, diffusion, desorptions realizes separating.Film separates and is used for coal bed gas CH
4/ N
2Separate have that equipment is simple, process does not have phase-state change, take up an area of less, advantage such as continuously-running; But the loss of product gas is inevitable in the film separation process, and production brings certain potential safety hazard to coal bed gas; The film effect of separating is strong to the masking technique dependence in addition, and technical also have the bigger space of improving.
(2) cryogenic rectification technology: the separation principle of cryogenic rectification technology is to utilize N
2With CH
4Boiling-point difference realize the two separation.Cryogenic rectification method separates N
2And CH
4Gaseous mixture technology maturation, product gas concentration height, purpose product yield height, but device is complicated, equipment investment is big, and the energy consumption height is applicable to the coal bed gas that treating capacity is big.
(3) Mehra technology: utilize hydrocarbon solvent Physical Absorption CH
4, realize N
2And CH
4The separation of mixture.This technology is to reclaiming gas reducing liquid simultaneously and carry dense nitrogenous natural gas certain economic value is arranged, but is used for separation of C H separately
4And N
2The time, CH
4Whether solubility amount low, that need absorbent is big in hydrocarbon solvent, feasible not appearing in the newspapers.
(4) Bend research institution adopts the Metal Substrate liquid-absorbant to remove N
2: this mechanism has prepared a kind of selective chemical absorption of N
2Metallo-organic complex.When admixture of gas when being dissolved with the solution of this complex compound, N
2Generate new material with complex compound reaction and be retained down by selectivity.This technology theory is feasible, but solution absorption and regeneration speed is slow, and efficient is low, only is fit to small amount of N
2Absorb, do not carry out the industry spot test at present as yet.
(5) transformation absorption (PSA): transformation absorption be utilize adsorbent to micropore in the kinetic effect of the adsorption strength of each component of admixture of gas, external diffusion in absorbent particles or the absorbent particles to the difference of each component molecule steric effect, circulation change with pressure serves as to separate motive force, and one or more components are concentrated or purifying.PSA realizes one of major technique that the industrialization gas absorption is separated at present, has been widely used in fields such as petrochemical industry, iron and steel, metallurgy.Transformation adsorption applications CH in coal bed gas
4And N
2Separate, have advantages such as energy consumption is low, flexible and convenient operation, the down continuous operation of normal temperature.But, most of industrialized, to use the most successful pressure-swing absorption process all be that weak absorbed component is a product, strong absorbed component is not used widely because of its concentration is low.Present industrialization transformation adsorbing separation CH
4/ N
2Mixed system mainly concentrates on the isolation technics based on balance, product gas CH
4Be stripping gas.The major defect of this pressure swing adsorption technique is exactly: CH
4Be stripping gas, contain a certain amount of light absorbed component in the stripping gas, cause the purity of product gas not high enough; And once absorption reach to put forward dense effect unsatisfactory.According to CH
4And N
2The difference of physical property, CH
4And N
2There is less but exercisable kinetic diameter difference: CH in molecule
4Kinetic diameter is 0.382nm, N
2Kinetic diameter is 0.368nm.If with dynamics is that separate on the basis, then CH
4/ N
2N in the mixed system separation process
2Diffusion on adsorbent is very fast, is easy absorbed component.Based on above-mentioned rerum natura difference, the researcher is N for stripping gas still to having done a large amount of basic research based on the isolation technics of dynamics
2, working off one's feeling vent one's spleen is product gas CH
4Pressure swing adsorption technique, do not appear in the newspapers as yet.
Summary of the invention
The object of the present invention is to provide a kind of pressure swing adsorption technique of directly enriching methane from coal bed gas, adopt pressure swing adsorption, by pressurization absorption, N
2Adsorb on the adsorbent in fixed adsorption bed, reach at the direct enrichment CH of outlet
4Purpose; Vacuum or depressurization desorption, the purpose that reaches adsorbent reactivation and recycle.This technology can realize the effective development and use and the environmental protection of coal bed gas.
Further, the present invention can be achieved through the following technical solutions:
The present invention may further comprise the steps (is the example explanation with first adsorption tower) at an operation cycle:
First step absorption: open unstripped gas delivery valve and product gas tank transfer valve, unstripped gas enters from the first adsorption tower arrival end and adsorbs, and product gas flows out from the first adsorption tower port of export and enters the product gas tank.
Parameter condition in the described step: temperature is controlled in-80～120 ℃ of scopes, and pressure is controlled in 0.1～1MPa scope.
Second step all pressed: with the adsorption tower of having taken out vacuum in advance first adsorption tower is carried out isostasy.All the purpose of Yaing is to reclaim mechanical energy, increases the rate of recovery of product gas.
The 3rd reverse decompression of step: after all pressure is finished, first adsorption tower is carried out the reverse atmospheric pressure that is decompressed to, reverse then vacuumizing makes adsorbent reactivation in the tower.
Parameter condition in the described step: vacuum is 0.1-0MPa.Vacuumize Controllable Temperature built in 80-150 ℃, high temperature helps desorb.
The 4th step pressurising: first adsorption tower vacuumizes when finishing, the tower of finishing absorption with this moment carries out the pressurising first time (this process also can be regarded pressure equalizing as a time) to first adsorption tower, with product gas first adsorption tower is finished again and finally be pressurized to operating pressure, so far finish the operation of one-period.
Parameter condition in the described step: temperature is controlled in-80～120 ℃ of scopes, and pressure is controlled in 0.1～1MPa scope;
The present invention realizes producing continuously realizing by the following method:
The 4th adsorption tower vacuumizes in the time of the absorption of first adsorption tower, and second adsorption tower and the 3rd adsorption tower are all pressed fast.Finish when the absorption of first adsorption tower, the 4th adsorption tower stops to vacuumize.The 4th adsorption tower is all pressed first adsorption tower, all press back first adsorption tower to enter the reverse decompression vacuum pumping stage, carry out product gas quick pressurising to the 3rd adsorption tower this moment, enter absorption phase, after absorption is finished, the 3rd adsorption tower carries out the pressurising first time (can regard as once and all press) to first adsorption tower of having taken out vacuum this moment, uses product gas then instead first adsorption tower is carried out whole pressurising, and then first adsorption tower enters absorption phase again.In a word, keep tower absorption in four towers, a tower vacuumizes, and two towers are all pressed, and realize producing continuously.
Described adsorbent is 4A, 5A zeolite molecular sieve and the carbon molecular sieve of aperture modification.
Described 4A through the aperture modification, 5A zeolite molecular sieve and carbon molecular sieve contain the micropore that most of aperture is 0.3nm-0.5nm.
The present invention has overcome the shortcoming of pressure swing adsorption technique in the prior art, adopts the adsorbent of modifying through the aperture, selects corresponding operating condition, has studied the separating technology based on dynamics, has realized the easy absorbed component N of enrichment on adsorbent
2, export direct enriched products gas CH
4Serialization production.N
2Can adopt to vacuumize desorb, the adsorbent reactivation ratio is easier to, and the rate of recovery of product gas also is improved, and adopts the absorption of multitower transformation to realize serialization production, CH
4Purity can reach 95%-99.9%, can use as a kind of energy and industrial chemicals efficient, cleaning, can also feed natural gas line.The present invention has important economy and Significance for Environment to incidence and the environmental protection that coal bed gas resource fully utilized, improved energy resource structure, reduction coal field accident.
Description of drawings
Fig. 1 is the process chart of case study on implementation 1, case study on implementation 2.C1-first adsorption tower among the figure, C2-second adsorption tower, C3-the 3rd adsorption tower, C4-the 4th adsorption tower, 5-product gas tank, 6-vavuum pump.
Fig. 2 is case study on implementation 4CH
4/ N
2The breakthrough curve figure of mixed system.Wherein, CH
4%: N
2%=55: 45.
The specific embodiment
The present invention may further comprise the steps (with the first adsorption tower C1 is the example explanation, is that the example explanation is the same with other adsorption towers, because these four tower apparatus belong to recycles) at an operation cycle:
First step absorption: open unstripped gas delivery valve and product gas tank 5 transfer valves, unstripped gas enters from the first adsorption tower C1 arrival end and adsorbs, and product gas flows out from the first adsorption tower C1 port of export and enters product gas tank 5.
Parameter condition in the described step: temperature is controlled in-80～120 ℃ of scopes, and pressure is controlled in 0.1～1MPa scope.
Second step all pressed: with having taken out the adsorption tower C2 of vacuum (when the first adsorption tower C1 is in adsorbed state in advance, other several towers are one and are in the state of vacuumizing, all press fast for two and get final product, there be not defining of strict tower working condition, because be operating as cyclic process, so can be to inhale in the C1 adsorption process the second adsorption tower C2 or the 3rd adsorption tower C3 or the 4th adsorption tower C4 at first adsorption tower to be in the state of vacuumizing here in fact, vacuumize the adsorption tower that the back that finishes finishes to absorption and carry out pressurising) the first adsorption tower C1 is carried out isostasy.All the purpose of Yaing is to reclaim mechanical energy, increases the rate of recovery of product gas.
The 3rd reverse decompression of step: after all pressure is finished, the first adsorption tower C1 is carried out the reverse atmospheric pressure that is decompressed to, reverse then vacuumizing makes adsorbent reactivation in the tower.
Parameter condition in the described step: vacuum is 0.1～0MPa.Vacuumize Controllable Temperature built in 80～150 ℃, high temperature helps desorb.
The 4th step pressurising: the first adsorption tower C1 vacuumizes when finishing, the tower of finishing absorption with this moment carries out the pressurising first time (this process also can be regarded pressure equalizing as a time) to the first adsorption tower C1, with product gas the first adsorption tower C1 is finished again and finally be pressurized to operating pressure, so far finish the operation of one-period.
Parameter condition in the described step: temperature is controlled in-80～120 ℃ of scopes, and pressure is controlled in 0.1～1MPa scope.
The present invention realizes producing continuously realizing by the following method:
The 4th adsorption tower C4 vacuumizes in the time of first adsorption tower C1 absorption, and the second adsorption tower C2 and the 3rd adsorption tower C3 all press fast.Finish when first adsorption tower C1 absorption, the 4th adsorption tower C4 stops to vacuumize.The 4th adsorption tower C4 all presses the first adsorption tower C1, all press the back first adsorption tower C1 to enter the reverse decompression vacuum pumping stage, carry out product gas quick pressurising to the 3rd adsorption tower C3 this moment, enter absorption phase, after absorption is finished, the 3rd adsorption tower C3 carries out the pressurising first time (can regard as once and all press) to the first adsorption tower C1 that has taken out vacuum this moment, uses product gas then instead the first adsorption tower C1 is carried out whole pressurising, and then the first adsorption tower C1 enters absorption phase again.In a word, keep tower absorption in four towers, a tower vacuumizes, and two towers are all pressed, and realize producing continuously.
Vacuumize all and realize by vavuum pump 6.
Example 1:CH
4/ N
2Mixed system is carried dense, and wherein, temperature is 20 ℃, and pressure is 0.5MPa, and flow velocity is 0.32cm/s, CH
4%: N
2%=55: 45.
Concrete grammar is: at first with system pressure and temperature stabilization to setting value, unstripped gas is stable to be entered the first adsorption tower C1 and adsorbs, the absorption second adsorption tower C2 and the 3rd adsorption tower C3 is simultaneously all pressed, the 4th adsorption tower C4 vacuumizes.The adsorption and desorption time is suitable, and when absorption among the first adsorption tower C1 was finished, the 4th adsorption tower C4 vacuumized and stops.The 4th adsorption tower C4 all presses the first adsorption tower C1, all press the back first adsorption tower C1 to enter the reverse decompression vacuum pumping stage, carry out product gas quick pressurising to the 3rd adsorption tower C3 this moment, enter absorption phase, after absorption is finished, the 3rd adsorption tower C3 carries out the pressurising first time (can regard as once and all press) to the first adsorption tower C1 that has taken out vacuum this moment, uses product gas then instead the first adsorption tower C1 is carried out whole pressurising, and then the first adsorption tower C1 enters absorption phase again.So cycling, final CH
4Concentration can reach more than 99%.SECO is: adsorbed 180 seconds, all pressed 10 seconds, pressurising 10 seconds, desorb 180 seconds.
Example 2:CH
4/ N
2Mixed system is carried dense, and wherein, temperature is 20 ℃, and pressure is 0.5MPa, and flow velocity is 0.40cm/s, CH
4%: N
2%=30: 70
Concrete grammar is: at first system pressure and temperature stabilization are extremely set value, product gas is to its pressurising, use after stable that unstripped gas is stable to be entered adsorption tower and adsorb instead, the absorption second adsorption tower C2 and the 3rd adsorption tower C3 is simultaneously all pressed, and the 4th adsorption tower C4 vacuumizes.The adsorption and desorption time is suitable, and when absorption among the first adsorption tower C1 was finished, the 4th adsorption tower C4 vacuumized and stops.The 4th adsorption tower C4 all presses the first adsorption tower C1, all press the back first adsorption tower C1 to enter the reverse decompression vacuum pumping stage, carry out product gas quick pressurising to the 3rd adsorption tower C3 this moment, enter absorption phase, after absorption is finished, the 3rd adsorption tower C3 carries out the pressurising first time (can regard as once and all press) to the first adsorption tower C1 that has taken out vacuum this moment, uses product gas then instead the first adsorption tower C1 is carried out whole pressurising, and then the first adsorption tower C1 enters absorption phase again.So cycling, final CH
4Concentration requirement is 99% when above, and once through yield reaches 64.8%.SECO is: adsorbed 120 seconds, all pressed 10 seconds, pressurising 10 seconds, desorb 120 seconds.
Example 3:CH
4/ N
2Mixed system is carried dense, and wherein, temperature is 0 ℃, and pressure is 0.5MPa, and flow velocity is 0.32cm/s, CH
4%: N
2%=20: 80.
Concrete grammar is: at first with system pressure and temperature stabilization to setting value, unstripped gas is stable to be entered the first adsorption tower C1 and adsorbs, the absorption second adsorption tower C2 and the 3rd adsorption tower C3 is simultaneously all pressed, the 4th adsorption tower C4 vacuumizes.The adsorption and desorption time is suitable, and when absorption among the first adsorption tower C1 was finished, the 4th adsorption tower C4 vacuumized and stops.The 4th adsorption tower C4 all presses the first adsorption tower C1, all press the back first adsorption tower C1 to enter the reverse decompression vacuum pumping stage, carry out product gas quick pressurising to the 3rd adsorption tower C3 this moment, enter absorption phase, after absorption is finished, the 3rd adsorption tower C3 carries out the pressurising first time (can regard as once and all press) to the first adsorption tower C1 that has taken out vacuum this moment, uses product gas then instead the first adsorption tower C1 is carried out whole pressurising, and then the first adsorption tower C1 enters absorption phase again.So cycling, final CH
4Concentration can reach more than 99%.SECO is: adsorbed 150 seconds, all pressed 10 seconds, pressurising 10 seconds, desorb 150 seconds.
Example 4:CH
4/ N
2Mixed system is carried dense, and wherein, temperature is 60 ℃, and pressure is 0.5MPa, and flow velocity is 0.40cm/s, CH
4%: N
2%=55: 45.
Concrete grammar is: at first with system pressure and temperature stabilization to setting value, unstripped gas is stable to be entered the first adsorption tower C1 and adsorbs, the absorption second adsorption tower C2 and the 3rd adsorption tower C3 is simultaneously all pressed, the 4th adsorption tower C4 vacuumizes.The adsorption and desorption time is suitable, and when absorption among the first adsorption tower C1 was finished, the 4th adsorption tower C4 vacuumized and stops.The 4th adsorption tower C4 all presses the first adsorption tower C1, all press the back first adsorption tower C1 to enter the reverse decompression vacuum pumping stage, carry out product gas quick pressurising to the 3rd adsorption tower C3 this moment, enter absorption phase, after absorption is finished, the 3rd adsorption tower C3 carries out the pressurising first time (can regard as once and all press) to the first adsorption tower C1 that has taken out vacuum this moment, uses product gas then instead the first adsorption tower C1 is carried out whole pressurising, and then the first adsorption tower C1 enters absorption phase again.So cycling, final CH
4Concentration requirement 99% when above, once through yield reaches 75.6%, concentration requirement is 95% when above, once through yield reaches 67.7%.SECO is: adsorbed 120 seconds, all pressed 10 seconds, pressurising 10 seconds, desorb 120 seconds.
The above-mentioned description to embodiment is can understand and apply the invention for ease of those skilled in the art.The person skilled in the art obviously can easily make various modifications to these embodiment, and needn't pass through performing creative labour being applied in the General Principle of this explanation among other embodiment.Therefore, the invention is not restricted to the embodiment here, those skilled in the art should be within protection scope of the present invention for improvement and modification that the present invention makes according to announcement of the present invention.
Claims (7)
1. the pressure swing absorption process of a directly enriching methane from coal bed gas is characterized in that: coal bed gas is fed the multitower adsorbent equipment, by pressure swing adsorption, adsorb N on adsorbent
2, at the direct enrichment CH of outlet
4
2. method according to claim 1 is characterized in that: also comprise vacuum or depressurization desorption, realize adsorbent reactivation and recycle.
3. method according to claim 1 is characterized in that: an operation cycle may further comprise the steps:
First step absorption: open unstripped gas delivery valve and product gas tank transfer valve, unstripped gas enters from the first adsorption tower arrival end and adsorbs, and product gas flows out from the adsorption tower port of export and enters the product gas tank;
Parameter condition in the described step: temperature is controlled in-80～120 ℃ of scopes, and pressure is controlled in 0.1～1MPa scope;
Second step all pressed: with the adsorption tower of having taken out vacuum in advance adsorption tower is carried out isostasy;
The 3rd reverse decompression of step: after all pressure is finished, adsorption tower is carried out the reverse atmospheric pressure that is decompressed to, reverse then vacuumizing makes adsorbent reactivation in the tower;
Parameter condition in the described step: vacuum is 0.1-0Mpa, vacuumizes Controllable Temperature built in 80-150 ℃;
The 4th step pressurising: adsorption tower vacuumizes when finishing, and the tower of finishing absorption with this moment carries out the pressurising first time to first adsorption tower, with product gas first adsorption tower is finished finally being pressurized to operating pressure again, so far finishes the operation of one-period;
Parameter condition in the described step: temperature is controlled in-80～120 ℃ of scopes, and pressure is controlled in 0.1～1MPa scope.
4. method according to claim 1 is characterized in that: realize producing continuously by following steps:
Keep adsorption tower absorption in four adsorption towers, an adsorption tower vacuumizes, and two adsorption towers are all pressed, and realizes producing continuously.
5. method according to claim 4 is characterized in that: the 4th adsorption tower vacuumizes in the time of the absorption of first adsorption tower, and second adsorption tower and the 3rd adsorption tower are all pressed fast; Finish when the absorption of first adsorption tower, the 4th adsorption tower stops to vacuumize; The 4th adsorption tower is all pressed first adsorption tower, all press back first adsorption tower to enter the reverse decompression vacuum pumping stage, carry out product gas quick pressurising to the 3rd adsorption tower this moment, enter absorption phase, after absorption is finished, first adsorption tower that the 3rd adsorption tower has been taken out vacuum to this moment carries out the pressurising first time, uses product gas then instead first adsorption tower is carried out whole pressurising, and then first adsorption tower enters absorption phase again.
6. method according to claim 1 is characterized in that: described adsorbent is 4A, 5A zeolite molecular sieve and the carbon molecular sieve of aperture modification.
7. method according to claim 6 is characterized in that: described 4A through the aperture modification, 5A zeolite molecular sieve and carbon molecular sieve contain the micropore that the aperture is 0.3nm-0.5nm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910194625A CN101628198A (en) | 2009-08-26 | 2009-08-26 | Pressure-swing adsorption method of directly enriching methane from coal bed gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910194625A CN101628198A (en) | 2009-08-26 | 2009-08-26 | Pressure-swing adsorption method of directly enriching methane from coal bed gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101628198A true CN101628198A (en) | 2010-01-20 |
Family
ID=41573578
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200910194625A Pending CN101628198A (en) | 2009-08-26 | 2009-08-26 | Pressure-swing adsorption method of directly enriching methane from coal bed gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101628198A (en) |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101828486A (en) * | 2010-05-11 | 2010-09-15 | 中国热带农业科学院南亚热带作物研究所 | Flower forcing method for inducing pineapple to bloom |
| CN101935032A (en) * | 2010-09-03 | 2011-01-05 | 同济大学 | Preparation method and use of carbon molecular sieve |
| CN102363117A (en) * | 2011-11-18 | 2012-02-29 | 淮北市森化碳吸附剂有限责任公司 | Carbon adsorbent special for methane in pressure swing adsorption and preparation method for carbon adsorbent |
| CN102380285A (en) * | 2011-10-11 | 2012-03-21 | 北京科技大学 | Multi-tower vacuum pressure swing adsorption based method and apparatus for concentrating coal mine ventilation air methane |
| CN102659496A (en) * | 2012-05-09 | 2012-09-12 | 同济大学 | Method for purifying methane in liquefied natural gas (LNG) vapor by low-temperature pressure swing adsorption |
| CN103146449A (en) * | 2013-02-25 | 2013-06-12 | 中煤科工集团重庆研究院 | Technology for making LNG (Liquefied Natural Gas) from low-concentration coal bed gas through pressure swing adsorption and cryogenic liquefaction |
| WO2013159670A1 (en) * | 2012-04-27 | 2013-10-31 | Li Kuanyi | Environmentally friendly and clean process using coal-bed gas to produce hydrocyanic acid derivatives |
| CN103933931A (en) * | 2014-04-09 | 2014-07-23 | 同济大学 | Low-pressure methane-adsorbed stratified molecular sieve adsorbent and preparation method thereof |
| CN104030879A (en) * | 2014-06-09 | 2014-09-10 | 沈建立 | Process for producing benzene by taking coal bed gas as raw material |
| CN105749699A (en) * | 2016-03-31 | 2016-07-13 | 四川天采科技有限责任公司 | Full-temperature-range pressure swing adsorption gas separation, refinement and purification method |
| CN107285279A (en) * | 2016-04-01 | 2017-10-24 | 四川天采科技有限责任公司 | A kind of method using the purified synthesis gas of complete warm journey pressure-variable adsorption with separating |
| CN107998822A (en) * | 2017-12-19 | 2018-05-08 | 池州山立分子筛有限公司 | The method of Pressure Swing Adsorption methane |
| CN108031240A (en) * | 2017-12-18 | 2018-05-15 | 洛阳健阳科技有限公司 | A kind of device based on HEU type zeolite molecular sieve separation of methane and nitrogen |
| CN109569182A (en) * | 2018-11-28 | 2019-04-05 | 中国矿业大学 | A kind of temperature and pressure collaboration gas absorption system for separating and purifying |
| CN109609223A (en) * | 2018-11-28 | 2019-04-12 | 中国矿业大学 | A kind of temperature and pressure collaboration gas absorption process for separation and purification |
| CN110452748A (en) * | 2019-07-12 | 2019-11-15 | 煤科集团沈阳研究院有限公司 | A kind of coal bed gas physical extraction enrichment system |
| GB2580758A (en) * | 2018-11-20 | 2020-07-29 | Gas Recovery And Recycle Ltd | Gas recovery method |
-
2009
- 2009-08-26 CN CN200910194625A patent/CN101628198A/en active Pending
Cited By (21)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101828486A (en) * | 2010-05-11 | 2010-09-15 | 中国热带农业科学院南亚热带作物研究所 | Flower forcing method for inducing pineapple to bloom |
| CN101935032A (en) * | 2010-09-03 | 2011-01-05 | 同济大学 | Preparation method and use of carbon molecular sieve |
| CN102380285A (en) * | 2011-10-11 | 2012-03-21 | 北京科技大学 | Multi-tower vacuum pressure swing adsorption based method and apparatus for concentrating coal mine ventilation air methane |
| CN102363117A (en) * | 2011-11-18 | 2012-02-29 | 淮北市森化碳吸附剂有限责任公司 | Carbon adsorbent special for methane in pressure swing adsorption and preparation method for carbon adsorbent |
| WO2013159670A1 (en) * | 2012-04-27 | 2013-10-31 | Li Kuanyi | Environmentally friendly and clean process using coal-bed gas to produce hydrocyanic acid derivatives |
| CN102659496A (en) * | 2012-05-09 | 2012-09-12 | 同济大学 | Method for purifying methane in liquefied natural gas (LNG) vapor by low-temperature pressure swing adsorption |
| CN103146449A (en) * | 2013-02-25 | 2013-06-12 | 中煤科工集团重庆研究院 | Technology for making LNG (Liquefied Natural Gas) from low-concentration coal bed gas through pressure swing adsorption and cryogenic liquefaction |
| CN103933931A (en) * | 2014-04-09 | 2014-07-23 | 同济大学 | Low-pressure methane-adsorbed stratified molecular sieve adsorbent and preparation method thereof |
| CN104030879A (en) * | 2014-06-09 | 2014-09-10 | 沈建立 | Process for producing benzene by taking coal bed gas as raw material |
| CN104030879B (en) * | 2014-06-09 | 2016-06-22 | 沈建立 | A kind of technique with coal bed gas for raw material production benzene |
| CN105749699A (en) * | 2016-03-31 | 2016-07-13 | 四川天采科技有限责任公司 | Full-temperature-range pressure swing adsorption gas separation, refinement and purification method |
| CN107285279A (en) * | 2016-04-01 | 2017-10-24 | 四川天采科技有限责任公司 | A kind of method using the purified synthesis gas of complete warm journey pressure-variable adsorption with separating |
| CN107285279B (en) * | 2016-04-01 | 2019-04-16 | 四川天采科技有限责任公司 | A method of purified synthesis gas using Quan Wencheng pressure-variable adsorption with separate |
| CN108031240A (en) * | 2017-12-18 | 2018-05-15 | 洛阳健阳科技有限公司 | A kind of device based on HEU type zeolite molecular sieve separation of methane and nitrogen |
| CN107998822A (en) * | 2017-12-19 | 2018-05-08 | 池州山立分子筛有限公司 | The method of Pressure Swing Adsorption methane |
| GB2580758A (en) * | 2018-11-20 | 2020-07-29 | Gas Recovery And Recycle Ltd | Gas recovery method |
| GB2580758B (en) * | 2018-11-20 | 2023-06-14 | Gas Recovery And Recycle Ltd | Gas recovery method |
| CN109569182A (en) * | 2018-11-28 | 2019-04-05 | 中国矿业大学 | A kind of temperature and pressure collaboration gas absorption system for separating and purifying |
| CN109609223A (en) * | 2018-11-28 | 2019-04-12 | 中国矿业大学 | A kind of temperature and pressure collaboration gas absorption process for separation and purification |
| CN110452748A (en) * | 2019-07-12 | 2019-11-15 | 煤科集团沈阳研究院有限公司 | A kind of coal bed gas physical extraction enrichment system |
| CN110452748B (en) * | 2019-07-12 | 2020-12-04 | 煤科集团沈阳研究院有限公司 | Physical extraction and enrichment system for coal bed gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101628198A (en) | Pressure-swing adsorption method of directly enriching methane from coal bed gas | |
| CN101596391B (en) | Method for pressure swing adsorption and staged concentration of low concentration gas | |
| CN101249370B (en) | Voltage transformation adsorption method for circulation valuable gas | |
| CN104986735B (en) | A kind of method for improving hydrogen recovery rate | |
| CN103071364B (en) | System and method for trapping carbon dioxide from flue gases in multi-stage manner | |
| CN104891439A (en) | Method for increasing of recovery rate of hydrogen from reformed gas | |
| CN101732947B (en) | Method for safe adsorption and enrichment of gas with low concentration | |
| CN103861422A (en) | New technique for concentrating methane in oxygen-containing coal bed gas | |
| CN109694073A (en) | Double high technologies of UF membrane high purity carbon monoxide and hydrogen in conjunction with pressure-variable adsorption | |
| CN202237712U (en) | Device for concentrating coal mine ventilation air methane through multi-tower vacuum pressure swing adsorption method | |
| CN100358609C (en) | Coalbed gas condensation method | |
| CN102380285B (en) | Multi-tower vacuum pressure swing adsorption based method and apparatus for concentrating coal mine ventilation air methane | |
| CN102389685A (en) | Coal mine methane gas enriching method comprising step of pumping at exhaust end of adsorption tower | |
| CN210613298U (en) | System device for concentrating methane by pressure swing adsorption of low-concentration gas in coal mine | |
| CN115155257B (en) | Method for extracting high-purity helium from low-helium-content BOG | |
| CN111773882A (en) | Micro-positive pressure vacuum pressure swing adsorption system and method for safely concentrating low-concentration gas | |
| CN102091501A (en) | Upper and lower pressure-equalizing pressure swing adsorption method | |
| CN109126380B (en) | Coal mine gas enrichment device with air exhaust end for boosting pressure and method thereof | |
| CN104128073B (en) | Saturation adsorption process of pressure swing adsorption decarburization and device thereof | |
| CN217148577U (en) | System for extracting high-purity helium from low-helium BOG | |
| CN105038881B (en) | A kind of method that pressure-variable adsorption continuously separates biogas | |
| CN203170184U (en) | Secondary adsorption and compression device of low-concentration coal bed gas | |
| CN202237711U (en) | Coal mine ventilation air methane enriching device having pumping and discharging step at exhaust end of adsorption tower | |
| CN102600699B (en) | Pressure-variable adsorption gas separation device | |
| CN114522504A (en) | Method for removing carbon dioxide in high-purity gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20100120 |