CN104030879B - A kind of technique with coal bed gas for raw material production benzene - Google Patents
A kind of technique with coal bed gas for raw material production benzene Download PDFInfo
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- CN104030879B CN104030879B CN201410249485.8A CN201410249485A CN104030879B CN 104030879 B CN104030879 B CN 104030879B CN 201410249485 A CN201410249485 A CN 201410249485A CN 104030879 B CN104030879 B CN 104030879B
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- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 176
- 238000000034 method Methods 0.000 title claims abstract description 66
- 239000003245 coal Substances 0.000 title claims abstract description 39
- 239000002994 raw material Substances 0.000 title claims abstract description 21
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 14
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 104
- 239000007789 gas Substances 0.000 claims abstract description 101
- 238000005899 aromatization reaction Methods 0.000 claims abstract description 30
- 230000003134 recirculating effect Effects 0.000 claims abstract description 11
- 238000000746 purification Methods 0.000 claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims description 43
- 239000003054 catalyst Substances 0.000 claims description 40
- 230000008929 regeneration Effects 0.000 claims description 25
- 238000011069 regeneration method Methods 0.000 claims description 25
- 239000001257 hydrogen Substances 0.000 claims description 18
- 229910052739 hydrogen Inorganic materials 0.000 claims description 18
- 239000002245 particle Substances 0.000 claims description 15
- 239000000047 product Substances 0.000 claims description 15
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 14
- 238000005204 segregation Methods 0.000 claims description 11
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 10
- 239000011949 solid catalyst Substances 0.000 claims description 10
- 238000001179 sorption measurement Methods 0.000 claims description 8
- 239000002808 molecular sieve Substances 0.000 claims description 7
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 7
- 239000006227 byproduct Substances 0.000 claims description 6
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 5
- 238000010521 absorption reaction Methods 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 5
- 229910052750 molybdenum Inorganic materials 0.000 claims description 5
- 239000011733 molybdenum Substances 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 239000008246 gaseous mixture Substances 0.000 claims description 4
- 239000008187 granular material Substances 0.000 claims description 4
- 150000002431 hydrogen Chemical class 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 3
- 239000003463 adsorbent Substances 0.000 claims description 2
- 230000006837 decompression Effects 0.000 claims description 2
- 238000010926 purge Methods 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 238000011017 operating method Methods 0.000 claims 1
- 210000000952 spleen Anatomy 0.000 claims 1
- 239000003317 industrial substance Substances 0.000 abstract description 8
- 239000000446 fuel Substances 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 abstract description 2
- 238000002360 preparation method Methods 0.000 abstract description 2
- 239000003345 natural gas Substances 0.000 abstract 1
- 238000003860 storage Methods 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- HUMNYLRZRPPJDN-UHFFFAOYSA-N benzaldehyde Chemical compound O=CC1=CC=CC=C1 HUMNYLRZRPPJDN-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 238000005065 mining Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000004459 forage Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- QNGNSVIICDLXHT-UHFFFAOYSA-N para-ethylbenzaldehyde Natural products CCC1=CC=C(C=O)C=C1 QNGNSVIICDLXHT-UHFFFAOYSA-N 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The present invention relates to a kind of technique for producing benzene, with coal bed gas for raw material, purify through PSA and obtain methane gas, process through recirculating fluidized bed aromatisation and obtain benzene。The present invention is with existing with natural gas for compared with the technology of raw material production benzene, and economic benefits are very notable: this technique, with coal bed gas for raw material, expands raw material sources and significantly reduces cost；This technique is through purification processes, and the purity adding methane gas can direct aromatisation；The application of recirculating fluidized bed in this technique, makes aromatization process technique simple, and preparation is convenient, it is easy to operation, environment friendly and pollution-free；The high-purity benzene that the present invention prepares can meet the requirement doing industrial chemicals, has broken coal bed gas simultaneously and has only utilized system for the existing of fuel, has started new approach for coal bed gas as the utilization of industrial chemicals。
Description
Technical field
The invention belongs to a kind of technique producing benzene, relate in particular to a kind of with coal bed gas for raw material, purified by PSA and obtain methane gas, process the technique obtaining benzene through recirculating fluidized bed aromatisation。
Background technology
Coal bed gas is a kind of based on methane, containing the multiple gases mixture of a small amount of nitrogen, carbon dioxide and oxygen etc., is primarily present the accompanying gas in colliery, belongs to Unconventional forage。If first exploiting coal bed methane, both can avoid coal mine gas from explosion before mining, the energy of cleaning and the industrial chemicals of high-quality can be obtained again。
China's coal bed gas resource enriches, and mining resources amount about 10 tcm at present, owing to not finding the means that reasonably utilize, fails to make full use of, and major part coal bed gas finally still enters in air, wastes resource, pollutes environment。
Along with the demand of clean energy resource is increased by the world day by day, coal-bed gas exploitation and utilization receive the extensive concern of countries in the world。There is a lot of method about coal bed gas comprehensive utilization so far。
1, patent CN200510022208.4 discloses a kind of method that coal bed gas prepares hydrogen, the method will add suitable steam in coal bed gas, under catalyst action, utilize the reaction heat of the fuel gas in coal bed gas and oxygen, make methane and steam generation conversion reaction, generate the gaseous mixture rich in hydrogen, obtain high purity hydrogen product again through pressure-variable adsorption。
2, patent CN200510073346.5 discloses a kind of method utilizing hydrate to carry out Enriching Coalbed Methane and accumulating, the method is the difference utilizing methane and other component in gas phase and hydrate phase partitioning coefficient, make methane be enriched with mutually at hydrate by controlling the formation condition of hydrate, obtain the methane gas that purity is more than 90%。
3, patent CN200810231646.5 discloses a kind of method with coal bed gas for waste clean fuel oil, and in the method, the methane in coal bed gas is converted into hydrogen and carbon monoxide through non-catalytic partial oxidation technique, after purification, obtain synthetic fuel oil then through F-T synthesis operation。
But these methods are only that from a kind of fuel, coal bed gas is transformed into another kind of fuel, economically do not have too big advantage。At present, but without about coal bed gas is changed into industrial chemicals patent and paper publishing。
Benzene is a kind of to apply extremely wide industrial chemicals, and its market demand increases year by year, and added value of product is high。
The existing production method of benzene has following two:
1, one of crude refining product is benzene, accounts for more than the 90% of the existing benzaldehyde product in the world；
2, crude benzol can be obtained from coke-stove gas condensation process, process through crude benzole hydrogenation and obtain benzene。
The invention provides a kind of technique with coal bed gas for raw material production benzene, the production for benzene provides a new method。Meanwhile, the present invention changes coal bed gas and only utilizes system for the existing of fuel, has started new approach for coal bed gas as the utilization of industrial chemicals, has considerably increased the surcharge of coal bed gas。
Summary of the invention:
It is an object of the invention to provide a kind of with coal bed gas for raw material, purified by PSA and obtain methane gas, process the technique obtaining benzene through recirculating fluidized bed aromatisation。
For achieving the above object, the present invention is achieved through the following technical solutions:
A kind of with coal bed gas for raw material, purified by PSA and obtain methane gas, process the technique obtaining benzene through recirculating fluidized bed aromatisation。
First, using purifying as the methane in the coal bed gas of raw material, methane gas is obtained by pressure-variable adsorption (PSA) method；Secondly, the methane gas obtained is obtained benzene after recirculating fluidized bed aromatisation processes。
In the present invention, the technique for producing benzene includes purification system and recirculating fluidized bed aromatisation system, as shown in Figure 1。
In purification system, described purification system is pressure-variable adsorption (PSA) device, adopts four tower endless form, and flow process is High Pressure Absorption, reverse decompression purging。Methane gas is absorbed by each adsorption tower through processes such as High Pressure Absorption, drop pressure, inverse put, boost pressures。Adsorbent adopts carbon molecular sieve and NACF。Operation pressure limit is 0.1-1.0Mpa。Methane content in the methane gas obtained is more than 95%。
In recirculating fluidized bed aromatisation process system, twin tower circulating fluidized bed reaction unit is adopted to carry out aromatisation process, as shown in Figure 2。This reaction unit is mainly made up of reaction tower, catalyst regeneration tower, cyclone separator and benzene segregation apparatus。Having air inlet pipe bottom reaction tower, lower straight fetches the overflow pipe from regenerator in succession, and catalyst riser is arranged at top, and catalyst riser top is directly connected to the import of cyclone separator。Catalyst regeneration tower bottom has air inlet pipe, bottom to have overflow pipe to be directly connected to the beds of reaction tower bottom, and top has regenerator to generate gas outlet。The solid ion recoverer of cyclone separator is directly connected to regenerator top, and gas outlet is directly connected to benzene segregation apparatus。Benzene segregation apparatus is made up of benzene knockout tower and pressure-variable adsorption (PSA) device。
Above-mentioned methane gas is passed in the reaction tower in twin tower circulating fluidized bed reaction unit, under molybdenum molecular sieve catalyst effect, carry out aromatisation process。Reaction after aromatisation processes generates gas and the boosted pipe racks of partially catalyzed agent granule enters in cyclone separator, and solid catalyst particle enters catalyst regeneration tower after cyclone separator separates, and gas enters in benzene segregation apparatus through cyclone separator top exit。This gas, after benzene knockout tower separates, obtains products benzene and side-product naphthalene etc.；Product hydrogen and methane gas is obtained after separating then through PSA device。The methane gas obtained is beaten and is recycled into reaction tower, and recycle ratio is 4。After cyclone separator separates, enter the solid catalyst particle in regenerator, entered by overflow pipe after regeneration in catalyst regeneration tower in the beds of reaction tower bottom and recycle。Reaction tower inlet temperature is 500-700 DEG C, and outlet temperature is 700-850 DEG C, and operation pressure is 0.1-0.6MPa；In cyclone separator, temperature is 650-850 DEG C；The catalyst regeneration gas inlet temperature of catalyst regeneration tower is 500-800 DEG C, outlet temperature is about 800-900 DEG C, the solid catalyst particle temperature entered in regenerator after cyclone separator separates is 600-800 DEG C, and the regenerated catalyst particle temperature entered by overflow pipe in the beds of reaction tower bottom is 700-850 DEG C。Benzene yield is 15%, and hydrogen yield is 70%；The purity of benzene is 99.5%, and the purity of hydrogen is 99.5%。The regeneration gas of catalyst regeneration tower import is hydrogen, the mixed air that gas is hydrogen and methane of regenerator outlet, and this gaseous mixture is returned system after PSA purifying plant separates respectively and recycled。
The present invention compared with prior art, has the advantage that
1) can directly with coal bed gas for raw material production benzene by the present invention, the high-purity benzene that the present invention prepares can meet the requirement doing industrial chemicals, and the production for benzene provides a new method；Break coal bed gas simultaneously and only utilized system for the existing of fuel, start new approach for coal bed gas as the utilization of industrial chemicals。
2) present invention is compared with traditional handicraft, and by methane direct aromatization chemical conversion benzene under anaerobic, and by-product naphthalene etc. is containing carbon products, and the total recovery of carbon is up to more than 95%。
3) hydrogen that by-product prepares further increases the benefit of this technique。
4) aromatization of this technique operates under anaerobic, without waste gas CO2Discharge, has contribution to improving environment。
5) technique is simple, and preparation is convenient, it is easy to operation, environment friendly and pollution-free。
The process chart of the present invention is as follows:
Fig. 1 is the process chart with coal bed gas for raw material production benzene of the present invention；
Fig. 2 be the present invention with coal bed gas be raw material production benzene twin tower circulating fluidized bed aromatisation process system process figure, capital equipment responds tower, catalyst regeneration tower, cyclone separator and benzene segregation apparatus。
Embodiment 1
As it is shown in figure 1, by raw material coal bed gas with 50m3The air inflow of N/h passes in purification system, methane gas is absorbed through four tower endless form。Operation pressure limit is 0.1-0.8Mpa。Wherein, methane gas yield is 40m3N/h, methane content, more than 95%, sends into methane gas storage tank。Methane gas from methane gas storage tank is with 30m3The air inflow of N/h passes into the reaction tower bottom inflow pipe in recirculating fluidized bed aromatisation process system, under molybdenum molecular sieve catalyst effect, carries out aromatisation process。Reaction after aromatisation processes generates gas and the boosted pipe racks of partially catalyzed agent granule enters in cyclone separator, and solid catalyst particle enters catalyst regeneration tower after cyclone separator separates, and gas enters benzene segregation apparatus through cyclone separator top exit。This gas, after benzene knockout tower separates, obtains products benzene and side-product naphthalene etc.。Product hydrogen and unreacted methane gas is obtained after separating from benzene knockout tower gas out then through PSA device。One way methane conversion is 25%, and the yield of benzene is 3.0 kilograms/h, and purity is 99.5%；The yield of hydrogen is 9.5m3N/h, purity is 99.5%。Unreacted methane gas is beaten and is recycled into reaction tower, and recycle ratio is 4。Reaction tower inlet temperature is 600 DEG C, and reaction tower catalyst bed temperature is 800 DEG C, and outlet temperature is 800 DEG C, and operation pressure is 0.2MPa；In cyclone separator, temperature is 780 DEG C；The catalyst regeneration gas inlet temperature of catalyst regeneration tower is 600 DEG C, and regenerator catalyst bed temperature is 820 DEG C, and regenerator outlet temperature is 820 DEG C。The solid catalyst particle temperature entered in regenerator after cyclone separator separates is 750 DEG C, and the regenerated catalyst particle temperature entered by overflow pipe in the beds of reaction tower bottom is 810 DEG C。
Embodiment 2
As it is shown in figure 1, by raw material coal bed gas with 50m3The air inflow of N/h passes in purification system, methane gas is absorbed through four tower endless form。Operation pressure limit is 0.1-0.8Mpa。Wherein, methane gas yield is 40m3N/h, methane content, more than 95%, sends into methane gas storage tank。Methane gas from methane gas storage tank is with 30m3The air inflow of N/h passes into the reaction tower bottom inflow pipe in recirculating fluidized bed aromatisation process system, under molybdenum molecular sieve catalyst effect, carries out aromatisation process。Reaction after aromatisation processes generates gas and the boosted pipe racks of partially catalyzed agent granule enters in cyclone separator, and solid catalyst particle enters catalyst regeneration tower after cyclone separator separates, and gas enters benzene segregation apparatus through cyclone separator top exit。This gas, after benzene knockout tower separates, obtains products benzene and side-product naphthalene etc.。Product hydrogen and unreacted methane gas is obtained after separating from benzene knockout tower gas out then through PSA device。One way methane conversion is 22%, and the yield of benzene is 2.9 kilograms/h, and purity is 99.5%；The yield of hydrogen is 9.0m3N/h, purity is 99.5%。Unreacted methane gas is beaten and is recycled into reaction tower, and recycle ratio is 4。Reaction tower inlet temperature is 650 DEG C, and reaction tower catalyst bed temperature is 820 DEG C, and outlet temperature is 820 DEG C, and operation pressure is 0.3MPa；In cyclone separator, temperature is 810 DEG C；The catalyst regeneration gas inlet temperature of catalyst regeneration tower is 650 DEG C, and regenerator catalyst bed temperature is 840 DEG C, and regenerator outlet temperature is 840 DEG C。The solid catalyst particle temperature entered in regenerator after cyclone separator separates is 800 DEG C, and the regenerated catalyst particle temperature entered by overflow pipe in the beds of reaction tower bottom is 820 DEG C。
Claims (4)
1. the technique with coal bed gas for raw material production benzene, it is characterised in that comprise the steps:
(1) with coal bed gas for raw material, processed by purification system, it is thus achieved that high-purity methane gas；
(2) above-mentioned methane gas is sent into twin tower circulating fluidized bed aromatisation and process system, process through aromatisation device and obtain benzene；
In wherein said purification system, four tower circulation variable pressure absorption (PSA) devices are adopted to carry out adsorption treatment；Its operating procedure is: (1) flow process is High Pressure Absorption, reverse decompression purging, and methane gas is absorbed by each adsorption tower through High Pressure Absorption, drop pressure, inverse put, boost pressure process；Its operating condition is: operation pressure limit is 0.1-1.0MPa；Adsorbent adopts carbon molecular sieve and NACF, and after purification, the methane content in methane gas is more than 95%；
When described twin tower circulating fluidized bed reaction unit carries out aromatisation process, operating condition is as follows: (1) is under molybdenum molecular sieve catalyst effect, reaction tower inlet temperature is 500-700 DEG C, and outlet temperature is 700-850 DEG C, and operation pressure is 0.1-0.6MPa；(2) in cyclone separator, temperature is 650-850 DEG C；(3) the catalyst regeneration gas inlet temperature of catalyst regeneration tower is 500-800 DEG C, and outlet temperature is 800-900 DEG C；(4) the solid catalyst particle temperature entered in regenerator after cyclone separator separates is 600-800 DEG C, and the regenerated catalyst particle temperature entered by overflow pipe in the beds of reaction tower bottom is 700-850 DEG C。
In described recirculating fluidized bed aromatisation process system, twin tower circulating fluidized bed reaction unit is adopted to carry out aromatisation process；This reaction unit is mainly made up of reaction tower, catalyst regeneration tower, cyclone separator and benzene segregation apparatus: have air inlet pipe bottom (1) reaction tower, lower straight fetches the overflow pipe from regenerator in succession, catalyst riser is arranged at top, and catalyst riser top is directly connected to the import of cyclone separator；(2) catalyst regeneration tower bottom has air inlet pipe, bottom to have overflow pipe to be directly connected to the beds of reaction tower bottom, and top has regenerator to generate gas outlet；(3) the solid particle recoverer of cyclone separator is directly connected to regenerator top, and gas outlet is directly connected to benzene segregation apparatus；(4) benzene segregation apparatus is made up of benzene knockout tower and pressure-variable adsorption (PSA) device。
2. a kind of technique with coal bed gas for raw material production benzene according to claim 1, it is characterized in that when described twin tower circulating fluidized bed reaction unit carries out aromatisation process, comprise the steps: that (1) methane gas passes in the reaction tower in twin tower circulating fluidized bed reaction unit, under molybdenum molecular sieve catalyst effect, carry out aromatisation process；(2) reaction after aromatisation processes generates gas and the boosted pipe racks of partially catalyzed agent granule and enters in cyclone separator, solid catalyst particle enters catalyst regeneration tower after cyclone separator separates, and gas enters in benzene segregation apparatus through cyclone separator top exit；(3) this gas is after benzene knockout tower separates, and obtains products benzene and side-product naphthalene, obtains product hydrogen and methane gas after separating then through PSA device, and the methane gas obtained is recycled into reaction tower, and recycle ratio is 4；(4) after cyclone separator separates, enter the solid catalyst particle in regenerator, entered by overflow pipe after regeneration in catalyst regeneration tower in the beds of reaction tower bottom and recycle。
3. a kind of technique with coal bed gas for raw material production benzene according to claim 1, it is characterized in that when described twin tower circulating fluidized bed reaction unit carries out aromatisation process, catalyst regeneration tower inlet gas is hydrogen, catalyst regeneration tower is worked off one's feeling vent one's spleen the gaseous mixture into hydrogen and methane, and this gaseous mixture is returned system after PSA purifying plant separates respectively and recycled。
4. a kind of technique with coal bed gas for raw material production benzene according to claim 1, it is characterised in that the yield of described products benzene is 15%, and the purity of benzene is 99.5%, and the purity of product hydrogen is 99.5%。
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101460432A (en) * | 2006-04-21 | 2009-06-17 | 埃克森美孚化学专利公司 | Production of aromatics from methane |
| CN101628198A (en) * | 2009-08-26 | 2010-01-20 | 同济大学 | Pressure-swing adsorption method of directly enriching methane from coal bed gas |
| CN101939278A (en) * | 2007-12-05 | 2011-01-05 | 陶氏环球技术公司 | Continuous process for oxygen-free conversion of methane |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101460432A (en) * | 2006-04-21 | 2009-06-17 | 埃克森美孚化学专利公司 | Production of aromatics from methane |
| CN101939278A (en) * | 2007-12-05 | 2011-01-05 | 陶氏环球技术公司 | Continuous process for oxygen-free conversion of methane |
| CN101628198A (en) * | 2009-08-26 | 2010-01-20 | 同济大学 | Pressure-swing adsorption method of directly enriching methane from coal bed gas |
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