CN101607873A - Produce the method for dimethyl ether with high purity by one-step method from syngas - Google Patents
Produce the method for dimethyl ether with high purity by one-step method from syngas Download PDFInfo
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- CN101607873A CN101607873A CNA2009100553403A CN200910055340A CN101607873A CN 101607873 A CN101607873 A CN 101607873A CN A2009100553403 A CNA2009100553403 A CN A2009100553403A CN 200910055340 A CN200910055340 A CN 200910055340A CN 101607873 A CN101607873 A CN 101607873A
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- tower
- dme
- methanol
- absorption
- dimethyl ether
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- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 title claims abstract description 84
- 238000000034 method Methods 0.000 title claims abstract description 50
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 233
- 239000007789 gas Substances 0.000 claims abstract description 69
- 238000010521 absorption reaction Methods 0.000 claims abstract description 63
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 39
- 239000012071 phase Substances 0.000 claims abstract description 34
- 230000018044 dehydration Effects 0.000 claims abstract description 19
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 19
- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 14
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 13
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 239000000203 mixture Substances 0.000 claims abstract description 9
- 238000007599 discharging Methods 0.000 claims abstract description 8
- 239000007791 liquid phase Substances 0.000 claims abstract description 8
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 6
- 235000011089 carbon dioxide Nutrition 0.000 claims abstract description 6
- 238000009833 condensation Methods 0.000 claims abstract description 5
- 230000005494 condensation Effects 0.000 claims abstract description 5
- 239000002002 slurry Substances 0.000 claims abstract description 5
- 239000000047 product Substances 0.000 claims description 41
- 238000000926 separation method Methods 0.000 claims description 13
- 239000007795 chemical reaction product Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 241000282326 Felis catus Species 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 description 16
- 239000000243 solution Substances 0.000 description 10
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 9
- 239000000463 material Substances 0.000 description 5
- 239000007864 aqueous solution Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- 239000008234 soft water Substances 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 229910002059 quaternary alloy Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 235000003140 Panax quinquefolius Nutrition 0.000 description 1
- 240000005373 Panax quinquefolius Species 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The present invention is produced the method for dimethyl ether with high purity by one-step method from syngas, synthesis of dimethyl ether with synthesis gas one-step is divided into liquid and gas after condensation, gas phase enters the bottom, absorption tower, and water absorbs dme and carbonic acid gas, and mixed gas returns synthesis system and continues reaction; Liquid phase condensate thing and absorption liquid are formed liquid phase mixture and are entered dme rectifying tower bottom, and dme is by the side line discharging of tower top; Non-condensable gases is discharged from cat head and is reentered the bottom, absorption tower; Dme rectifying tower tower bottoms phase product enters the methanol rectifying tower bottom, and methyl alcohol enters methanol dehydration tower top after by cat head side line output, and the product behind the methanol dehydration enters the bottom on absorption tower; Methanol rectifying tower tower bottoms phase product is a pure water, can be used as absorption agent and uses; The present invention can adopt fixed-bed reactor, fluidized-bed reactor or three phase slurry bed bioreactor to react, and the dme purity of producing can reach more than 99.99%, therefore, has more industrial value, and Application Prospect is better.
Description
[technical field]
The present invention relates to chemical technology field, be specifically related to produce the method for dimethyl ether with high purity by one-step method from syngas.
[background technology]
With the coal be raw material through preparation of dimethyl ether from synthesis gas, be a non-oil resource route, be extremely important.
At present, both at home and abroad by producing dimethyl ether by synthesis gas, its reaction product is a multi-component mixture, and will obtain satisfying the dme product that technical grade purity requires, and must carry out refining accordingly the separation.The producing dimethyl ether by dehydrating methanol of comparing is wanted isolating unreacted synthesis gas and is produced methyl alcohol and the carbonic acid gas that produces in the process by preparation of dimethyl ether from synthesis gas, and its separating technology is more complicated.
Chinese patent literature CN 1215716 discloses a kind of separation method of dme, it is characterized in that: after synthetic gas reacts in reactor, product gas carries out heat exchange through interchanger and material synthesis gas, go out liquid (being mainly water) in gas-liquid separator separates, remove methyl alcohol on the absorption tower, product dme in the reaction end gas in extraction tower by under the solution extraction, enter reactor after the compressed machine supercharging of unreacted material synthesis gas with after unstripped gas mixes, the dme solvent that is extracted enters desorb-separation column and carries out desorb, and further carry densely, the solvent cooling back that removes dme is returned extraction tower and is recycled.The deficiency of this method is: water loss is bigger, and the by-product carbonic acid gas in the separating technology is not separated further and utilizes.
Chinese patent literature CN 1351986A has proposed " a kind of directly produce the dimethyl ether and methanol water solution absorption technique by synthetic raw gas ", the characteristics of this technology are to-20～-10 ℃ with product synthetic gas cooling condensation, isolate part dme wherein, absorb uncooled dme with methanol aqueous solution, contain dme and methanol in water make high density through rectifying dme product.The deficiency of this technology is: unreasonable to utilizing of the energy: on the one hand, need to consume a large amount of external energies in sepn process, on the other hand, the waste heat that separating technology produces does not add utilization and effluxes in a large number, causes the waste of the energy.
The technology the most approaching with the present invention is that the patent No. is the Chinese patent (hereinafter to be referred as correlation technique) of ZL03134277.9.This patent has proposed " a kind of separation method of one-step method from syngas preparing dimethy ether ", the principal feature of this method is (seeing accompanying drawing 1): reacted gas (6) is through condenser (1) condensation, do not coagulate gas (16) and enter bottom, absorption tower (2), absorb with soft water (13), absorption tower (2) overhead product tail gas (15) enters gas holder, the underflow product ether aqueous solution (8) of the thick dme solution of the underflow product of condenser (1) (7) and absorption tower (2) enters flash tank (3), gas after the flash distillation (9) is sent into bottom, absorption tower (2), the pure ethereal solution of flash tank (3) underflow product (10) enters dme rectifying tower (4), overhead product is dme (12), and the underflow product is a thick methyl ether solution (11); Thick methanol solution (11) enters methanol distillation column (5), and its underflow product is soft water (13), and tower side line product is refined methanol (14).Condenser (1), absorption tower (2), flash tank (3), dme rectifying tower (4), methanol distillation column (5) are arranged in processing step.Dme that this separation method is produced and methanol product purity can only reach about 98%, can only produce alcohol-ether fuel, and dme and methanol product that can not manufacture level purity.
[summary of the invention]
The objective of the invention is on the basis of existing technology, provide a kind of new, processing step product purity more reasonable, that produce is higher, produced the method for dimethyl ether with high purity by one-step method from syngas.
On the basis of experimental determination carbonic acid gas-dme-methanol-water quaternary system vapor-liquid equilibrium data, (see " East China University of Science's journal " 2007 33 volumes the 3rd phase " mensuration and the prediction of carbonic acid gas-dme-methanol-water quaternary system vapor-liquid equilibrium " literary composition), mixed gas with coal based synthetic gas or coke(oven)gas or synthetic gas and coke(oven)gas is a raw material, form a kind of new separation method, the purity of dme product is reached more than 99.99%.
Purpose of the present invention is achieved through the following technical solutions:
Produce the method for dimethyl ether with high purity by one-step method from syngas, the operation that comprises reaction product condensation, absorption, dme rectifying, methanol rectification, dimethyl ether by methanol dehydration, it is characterized in that, reaction product is after the gas-to-gas heat exchanger heat exchange, gas phase is passed through water cooler again, enter the bottom, absorption tower based on the gas phase after the condenses of methyl alcohol, by absorbing pure water dme and the carbonic acid gas as absorption agent, mixed gas returns synthesis system by the top, absorption tower and continues reaction; The liquid phase mixture that the absorption liquid on water cooler and absorption tower forms enters dme rectifying tower bottom, and dme is by the top side line discharging of dme rectifying tower; Non-condensable gases reenters the bottom, absorption tower after by compressor pressurizes; Dme rectifying tower tower bottoms phase product enters the methanol rectifying tower bottom, methyl alcohol is entered from the methanol dehydration top of tower by the side line output intensification back, top of methanol rectifying tower, methanol dehydration product dme and water and a small amount of unreacted methanol gas phase are drawn from the bottom of methanol dehydration tower, enter the bottom on absorption tower after the pressurization; Methanol rectifying tower tower bottoms phase product is a pure water, can be after cooling for the absorption tower as absorption agent, and unnecessary water enters the plant water recycle system.
The pressure that described reaction product enters gas-to-gas heat exchanger is 3.0～6.0Mpa, and temperature is 230～260 ℃.
The pressure that described gas phase enters water cooler is 3.0～6.0Mpa, and temperature is 80～110 ℃, is 40～60 ℃ as the temperature after the pure water heat exchange of absorption agent.
The described pressure that enters the absorption tower based on the gas phase after the condenses of methyl alcohol is 2.5～3.5Mpa, and temperature is 40～60 ℃.
The liquid phase mixture that the absorption liquid on described water cooler and absorption tower forms is 3.0～6.0Mpa at pressure, temperature is the bottom that enters the dme rectifying tower under 40～60 ℃ the condition, the dme product is that 0.5～1.5Mpa, temperature are by the top side line discharging of dme rectifying tower under 40～60 ℃ the condition at pressure, non-condensable gases is that 0.5～1.5Mpa, temperature are that discharge on the top from the dme rectifying tower under 20～30 ℃ the condition at pressure, by reentering the bottom on absorption tower after the compressor pressurizes.
Described dme rectifying tower tower bottoms phase product enters the methanol rectifying tower bottom under normal pressure, 160～180 ℃ condition, methyl alcohol is to enter methanol dehydration tower top under 240～340 ℃ in normal pressure, temperature after by the top side line output of methanol rectifying tower; The tower bottoms phase product pure water cooling back of methanol rectifying tower is 40～60 ℃ as the temperature of absorption agent utilization.
Separation method of the present invention is suitable for adopting fixed-bed reactor, fluidized-bed reactor or three phase slurry bed bioreactor to react the separation of the product dimethyl ether of generation, simultaneously, because this flow process has the isolating characteristics of methyl alcohol, water and non-condensable gases, also is applicable to the separation process of producing dimethyl ether by dehydrating methanol.
The present invention with the positively effect that prior art (correlation technique) is compared is:
Compare with the technology that Chinese patent ZL03134277.9 proposes, the reaction that patent of the present invention takes into full account directed preparing dimethyl ether by synthetic gas and methyl alcohol is the characteristics of reversible exothermic reaction, adopt the thermodynamic data of measuring, at first, use two interchanger, utilize reaction inlet gas and reaction mass to carry out heat exchange respectively, fully effectively utilize the reaction liberated heat; Secondly, absorption of dimethyl ether tower and dme rectifying tower are under high pressure operated, cancelled the flash tank between two towers, guarantee that dme rectifying tower side line output purity reaches the dme more than 99.99%; Increasing a methanol dehydration tower at last, is dme with the methanol conversion of by-product, thereby realizes the requirement by synthetic gas direct production dme.
The comparative result concrete with the ZL03134277.9 patented technology is:
(1) the ZL03134277.9 patented technology adopts a condenser on stream, under 200～300 ℃, 1.5～6.0Mpa condition with most of dme and whole methanol condensed; And the present invention adopts two interchanger: first interchanger utilizes reaction inlet gas and reactor outlet material to carry out heat exchange, under 4.0～8.0Mpa condition, reactor outlet material is dropped to 85～95 ℃ by 200～300 ℃, simultaneously reaction inlet gas is warming up to 170～200 ℃ by 20～30 ℃, has made full use of reaction heat; Second interchanger dropping to reactor outlet material about 40 ℃ by 85～95 ℃ under 4.0～8.0Mpa condition.
(2) the ZL03134277.9 patented technology on stream the working pressure of absorption of dimethyl ether tower be 2.0Mpa; And the thermodynamic data that the present invention measures by experiment determines that the absorption tower working pressure is between 2.5～3.5Mpa.
(3) the ZL03134277.9 patented technology connects a flash tank behind the absorption of dimethyl ether tower on stream, and then enters the dme rectifying tower; And the thermodynamic data that the present invention measures by experiment thinks that the working pressure of dme rectifying tower should be similar to the absorption of dimethyl ether tower, and therefore, the reaction mass after the absorption directly enters the dme rectifying tower, does not need flash tank.
(4) the ZL03134277.9 patented technology on stream refining dimethyl ether by the discharging of dme rectifying tower cat head; And dme rectifying tower of the present invention is to operate under 2.5～3.5Mpa condition, refining dimethyl ether is the side line discharging at the dme rectifying tower, non-condensable gases is discharged by dme rectifying tower cat head, has so just guaranteed that the purity of dme product can reach more than 99.99%.
(5) the ZL03134277.9 patented technology has only a methanol rectifying tower on stream, and (slightly) methyl alcohol of Sheng Chaning does not have industrial application value like this; And the present invention increases a methanol dehydration tower in producing process, with the further producing dimethyl ether by dehydrating of by-product carbinol.
Summarize it, the present invention has realized the purpose by one-step method from syngas direct production dimethyl ether with high purity Industrial products, and be suitable for adopting fixed-bed reactor, fluidized-bed reactor or three phase slurry bed bioreactor to implement, the purity of the dme product of producing can reach more than 99.99%, have more industrial value, Application Prospect is better.
[description of drawings]
Label among the figure is respectively:
(1) condenser, (2) absorption tower, (3) flash tank,
(4) dme rectifying tower, (5) methanol distillation column, (6) reacted gas,
(7) thick dme solution, (8) ether aqueous solution, gas after (9) flash distillation,
(10) pure ethereal solution, (11) thick methyl ether solution, (12) dme,
(13) soft water, (14) refined methanol, (15) overhead product tail gas,
(16) do not coagulate gas;
Label among the figure is respectively:
1, gas-to-gas heat exchanger, 2, water cooler, 3, the absorption tower,
4, dme rectifying tower, 5, methanol rectifying tower, 6, the methanol dehydration tower,
7, reaction product, 8, gas phase,
9, based on the gas phase after the condenses of methyl alcohol, 10, liquid phase mixture,
11, non-condensable gases, 12, tower bottoms phase product, 13, dme,
14, methyl alcohol, 15, pure water, 16, unnecessary water,
17, the product of methanol dehydration, 18, mixed gas.
[embodiment]
Explain further that below in conjunction with accompanying drawing the present invention is produced the method for dimethyl ether with high purity by one-step method from syngas.
A kind of method of producing dimethyl ether with high purity by one-step method from syngas, reaction product (7) is 3.0～6.0Mpa at pressure, temperature is to enter gas-to-gas heat exchanger (1) under 230～260 ℃ the condition, after gas-to-gas heat exchanger (1) heat exchange, gas phase (8) is 3.0～6.0Mpa at pressure, temperature is to enter water cooler (2) under 80～110 ℃ the condition, wherein, is 40～60 ℃ as the cooled temperature of pure water (15) of absorption agent; Is that 2.5～3.5Mpa, temperature are to enter bottom, absorption tower (3) under 40～60 ℃ the condition based on the gas phase after the condenses of methyl alcohol (9) at pressure, absorb dme and carbonic acid gas by pure water (15) as absorption agent, its mixed gas (18) is drawn by top, absorption tower (3), returns synthesis system and continues reaction.
The liquid phase mixture (10) that the absorption liquid on water cooler (2) and absorption tower (3) forms is that 3.0～6.0Mpa, temperature are to enter dme rectifying tower (4) bottom under 230～260 ℃ the condition at pressure, after the reaction, dme (13) is 0.5～1.5Mpa at pressure, temperature be under 40～60 ℃ the condition by the top side line discharging of dme rectifying tower (4), can obtain purity and reach dme (13) product more than 99.99%.
Non-condensable gases (11) is that 0.5～1.5Mpa, temperature are that discharge on the top from dme rectifying tower (4) under 20～30 ℃ the condition at pressure, by reentering the bottom of absorption tower (3) after the compressor pressurizes; Dme rectifying tower (4) tower bottoms phase product (12) is to enter methanol rectifying tower (5) bottom under 160～180 ℃ the condition in normal pressure, temperature, methyl alcohol (14) is by the top side line output of methanol rectifying tower (5), after the intensification, be to enter from methanol dehydration tower (6) top under 240～340 ℃ the condition in normal pressure, temperature, methanol dehydration product dme and water and a small amount of unreacted methanol (17) are drawn from the bottom of methanol dehydration tower (6), enter the bottom of absorption tower (3) after pressurization; Methanol rectifying tower (5) tower bottoms phase product is pure water (15), and it can supply absorption tower (3) as the absorption agent utilization after cooling, is 40～60 ℃ as the temperature of absorption agent utilization; Unnecessary water (16) then enters the plant water recycle system.
The method that the present invention produces dimethyl ether with high purity by one-step method from syngas is suitable for adopting fixed-bed reactor, fluidized-bed reactor or three phase slurry bed bioreactor to react; Also be applicable to the separation process of producing dimethyl ether by dehydrating methanol.
Claims (9)
1, a kind of method of producing dimethyl ether with high purity by one-step method from syngas, the operation that comprises reaction product condensation, absorption, dme rectifying, methanol rectification, dimethyl ether by methanol dehydration, it is characterized in that, reaction product (7) is after gas-to-gas heat exchanger (1) heat exchange, gas phase (8) is again by water cooler (2), enter bottom, absorption tower (3) based on the gas phase after the condenses of methyl alcohol (9), absorb dme and carbonic acid gas by the pure water (15) as absorption agent, mixed gas (18) returns synthesis system by top, absorption tower (3) and continues reaction; Water cooler (2) enters dme rectifying tower (4) bottom with the liquid phase mixture (10) of the absorption liquid formation on absorption tower (3), and dme (13) is by the top side line discharging of dme rectifying tower (4); Non-condensable gases (11) is by reentering bottom, absorption tower (3) after the compressor pressurizes; Dme rectifying tower (4) tower bottoms phase product (12) enters methanol rectifying tower (5) bottom, methyl alcohol (14) is entered from methanol dehydration tower (6) top by the side line output intensification back, top of methanol rectifying tower (5), methanol dehydration product dme and water and a small amount of unreacted methanol gas phase (17) are drawn from the bottom of methanol dehydration tower (6), enter the bottom of absorption tower (3) after the pressurization; Methanol rectifying tower (5) tower bottoms phase product is pure water (15), can supply absorption tower (3) as absorption agent after cooling, and unnecessary water (16) enters the plant water recycle system.
2, according to claim 1ly produce the method for dimethyl ether with high purity by one-step method from syngas, it is characterized in that the pressure that described reaction product (7) enters gas-to-gas heat exchanger (1) is 3.0～6.0Mpa, temperature is 230～260 ℃.
3, the method for producing dimethyl ether with high purity by one-step method from syngas according to claim 1, it is characterized in that, the pressure that described gas phase (8) enters water cooler (2) is 3.0～6.0Mpa, and temperature is 80～110 ℃, is 40～60 ℃ as the temperature after pure water (15) heat exchange of absorption agent.
4, according to claim 1ly produce the method for dimethyl ether with high purity by one-step method from syngas, it is characterized in that, the described pressure that enters absorption tower (3) based on the gas phase after the condenses of methyl alcohol (9) is 2.5～3.5Mpa, and temperature is 40～60 ℃.
5, the method of producing dimethyl ether with high purity by one-step method from syngas according to claim 1, it is characterized in that, described water cooler (2) is 3.0～6.0Mpa with the liquid phase mixture (10) of the absorption liquid formation on absorption tower (3) at pressure, temperature is the bottom that enters dme rectifying tower (4) under 40～60 ℃ the condition, dme (13) product is 0.5～1.5Mpa at pressure, temperature is by the top side line discharging of dme rectifying tower (4) under 40～60 ℃ the condition, non-condensable gases (11) is 0.5～1.5Mpa at pressure, temperature is that discharge on the top from dme rectifying tower (4) under 20～30 ℃ the condition, by reentering the bottom of absorption tower (3) after the compressor pressurizes.
6, the method for producing dimethyl ether with high purity by one-step method from syngas according to claim 1, it is characterized in that, the tower bottoms phase product (12) of described dme rectifying tower (4) enters methanol rectifying tower (5) bottom under normal pressure, 160～180 ℃ condition, methyl alcohol (14) is to enter methanol dehydration tower (6) top under 240～340 ℃ in normal pressure, temperature after by the top side line output of methanol rectifying tower (5).
7, according to claim 6ly produce the method for dimethyl ether with high purity, it is characterized in that tower bottoms phase product pure water (15) the cooling back of methanol rectifying tower (5) is 40～60 ℃ as the temperature of absorption agent utilization by one-step method from syngas.
8, the method for producing dimethyl ether with high purity by one-step method from syngas according to claim 1, it is characterized in that method of the present invention adopts fixed-bed reactor, fluidized-bed reactor or three phase slurry bed bioreactor to react the separation of the product dimethyl ether of generation.
9, according to claim 1ly produce the method for dimethyl ether with high purity, it is characterized in that method of the present invention also is applicable to the separation process of producing dimethyl ether by dehydrating methanol by one-step method from syngas.
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| CN2009100553403A CN101607873B (en) | 2009-07-24 | 2009-07-24 | Method for preparing dimethyl ether with high purity by syngas one-step method |
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| CN2009100553403A CN101607873B (en) | 2009-07-24 | 2009-07-24 | Method for preparing dimethyl ether with high purity by syngas one-step method |
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| CN101607873A true CN101607873A (en) | 2009-12-23 |
| CN101607873B CN101607873B (en) | 2012-06-27 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104258588A (en) * | 2014-09-03 | 2015-01-07 | 中国科学院广州能源研究所 | Device assembly and method for purifying dimethyl ether in biomass by rectification |
| WO2015104290A1 (en) * | 2014-01-07 | 2015-07-16 | Linde Aktiengesellschaft | Processing by a separation technique of a gas mixture formed from a product stream of a dimethyl reactor |
| CN108707064A (en) * | 2018-06-28 | 2018-10-26 | 鹤壁宝发能源科技股份有限公司 | A kind of production method of blast furnace gas combined producing dimethyl ether |
| EP4110748A4 (en) * | 2020-02-27 | 2024-05-29 | Amol Carbons Private Limited | Process for synthesis of dimethyl ether |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DK171707B1 (en) * | 1995-02-03 | 1997-04-01 | Topsoe Haldor As | Process for producing fuel grade dimethyl ether |
-
2009
- 2009-07-24 CN CN2009100553403A patent/CN101607873B/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2015104290A1 (en) * | 2014-01-07 | 2015-07-16 | Linde Aktiengesellschaft | Processing by a separation technique of a gas mixture formed from a product stream of a dimethyl reactor |
| CN105873661A (en) * | 2014-01-07 | 2016-08-17 | 林德股份公司 | Processing by a separation technique of a gas mixture formed from a product stream of a dimethyl reactor |
| RU2669290C2 (en) * | 2014-01-07 | 2018-10-09 | Линде Актингезелльшафт | Processing by separation technique of gas mixture formed from product stream of dimethyl reactor |
| CN104258588A (en) * | 2014-09-03 | 2015-01-07 | 中国科学院广州能源研究所 | Device assembly and method for purifying dimethyl ether in biomass by rectification |
| CN104258588B (en) * | 2014-09-03 | 2016-02-24 | 中国科学院广州能源研究所 | A kind of integrated and method of living beings dimethyl ether rectification and purification device |
| CN108707064A (en) * | 2018-06-28 | 2018-10-26 | 鹤壁宝发能源科技股份有限公司 | A kind of production method of blast furnace gas combined producing dimethyl ether |
| CN108707064B (en) * | 2018-06-28 | 2024-01-02 | 鹤壁宝发能源科技股份有限公司 | Production method for co-producing dimethyl ether by using blast furnace gas |
| EP4110748A4 (en) * | 2020-02-27 | 2024-05-29 | Amol Carbons Private Limited | Process for synthesis of dimethyl ether |
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| Publication number | Publication date |
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| CN101607873B (en) | 2012-06-27 |
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