CN1830934A - Method for producing dimethyl ether using methanol as raw material - Google Patents
Method for producing dimethyl ether using methanol as raw material Download PDFInfo
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- CN1830934A CN1830934A CN 200610020792 CN200610020792A CN1830934A CN 1830934 A CN1830934 A CN 1830934A CN 200610020792 CN200610020792 CN 200610020792 CN 200610020792 A CN200610020792 A CN 200610020792A CN 1830934 A CN1830934 A CN 1830934A
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Abstract
A process for preparing bimether as fuel from methanol by gas-phase dewatering includes such steps as dewatering reaction, heat exchanging, flowing in rectifier, cooling, condensing and separating to obtain bimether from the top of rectifier.
Description
Technical field:
The present invention is a kind of processing method of producing dme with methyl alcohol for the unstripped gas phase dehydration.
Background technology:
In the processing method of methanol gas phase dewatering preparing dimethy ether, now disclosed at home and abroad document and patent have several different methods, its basic technology is roughly similar, as Chinese patent application number is 95113028.5 dimethyl ether production methods: material benzenemethanol enters the multistage cold shock formula reactor that composite solid-acid catalyst is housed and carries out dehydration reaction after vaporization, the dehydration reaction crude product is moisture, dme, unreacted methanol and pair product light constituent, reacting coarse product is through cooling, after condensation removes the reaction non-condensable gases, the phlegma liquid phase enters carries out rectifying in the high efficiency packing tower, adjust as required reflux ratio on stripping section top or cat head obtain the dme product of different purity; The rectifying tower bottoms that contains the first alcohol and water enters methanol distillation column and carries out rectifying separation.Unreacted methanol obtains the back retrieval system in the Methanol Recovery column overhead and uses as raw material, and the water with the reaction generation that raw material is brought into is discharged system at the methanol distillation column still.
In the method, the pyritous reacting coarse product is through cooling condensation, remove the non-condensable gases in the reaction gas after the phlegma liquid phase enter in the rectifying tower, so both wasted the heat of taking out of in the reacting coarse product; Consumption is used for the required a large amount of colds of crude product cooling condensation again simultaneously, and will increase the heat that crude product needs in the vaporization of dme rectifying; Secondly, reclaim the methanol process special secondary school at the rectifying tower bottoms that contains component such as first alcohol and water and be provided with methanol distillation column, obtain methyl alcohol at the Methanol Recovery cat head, methyl alcohol must need consume a large amount of heats and cold through vaporization, condensation under certain reflux ratio, and the methyl alcohol that reclaims still needs to repeat vaporization when returning as raw material with liquid phase; In addition, when in this method use being contained the raw material of other light impurity component, because the vaporization tower does not possess the function of separating the light impurity component, contained light impurity component enters reactor participation reaction, separation etc. with the material benzenemethanol vaporization and not only can make the energy consumption increase in the raw material, and can reduce the efficient of reaction.The multistage cold shock formula adiabatic reactor that adopts in this method technological process because the catalyst bed reaction temperature difference is big, also can reduce the selectivity of reaction and the work-ing life of catalyzer.
The content of invention:
The purpose of this invention is to provide a kind of less investment, what energy consumption was low is the method for raw material production dme with methyl alcohol.
Technology of the present invention is achieved in that
The present invention's kind is that the method for raw material production dme comprises material benzenemethanol in methanol column 1 vaporization with methyl alcohol, gas-phase methanol is in dehydration reactor 3 dehydrations, dehydration reaction product rectifying in dme rectifying tower 6 obtains the dme step, the thick product of the reaction that dehydration reactor 3 comes out enters dme rectifying tower 6 with gas phase after heat exchange, finish the cooling of thick product at dme rectifying tower 6, condensation, separate and rectifying, overhead condensation at dme rectifying tower 6 obtains the dme product, the cat head byproduct of reaction does not coagulate tail gas emptying after alcohol is washed tower 9 washings, the part dme product reflux of dme rectifying tower 6 condensers 7 condensations is gone in the dme rectifying tower 6, contain water, the tower bottoms of methyl alcohol and a small amount of dme is sent methanol column 1 back to, and the working pressure of dme rectifying tower 6 is 0.3～1.5MPa.
Methanol column 1 cat head has condenser 10, and a small amount of dme and other light constituent return dme rectifying tower 6 by methanol column 1 cat head with gas phase, and the working pressure of methanol column is 0.3～1.5MPa, 110～200 ℃ of service temperatures.
Material benzenemethanol is washed tower 9 tops from alcohol and is entered alcohol and wash tower 9 washing and do not coagulate tail gas by the byproduct of reaction that dme rectifying tower 6 cats head come, after heating up, interchanger 5 enters first opening for feed of methanol column 1 from the methyl alcohol that contains a small amount of dme of tower bottom discharge, dme rectifying tower 6 tower bottomss enter second opening for feed of methanol column 1, methanol column 1 is made up of tower body and top condenser 10 thereof, condenser 10 condensation portion methyl alcohol and a small amount of dme, the cat head dme enters first opening for feed of dme rectifying tower 6 with gas phase, methanol steam enters dehydration reactor 3 after sending from the middle part of methanol column 1, and waste water is discharged from methanol column 1 tower still.
The number of theoretical plate of methanol column 1 is 38, first opening for feed is between the 4-16 piece plate of down counting from cat head, second opening for feed is between 18-24 piece plate, methanol steam enters dehydration reactor 3 from sending between the 4-10 piece column plate of methanol column 1 after gas heat exchanger 4 is overheated, a small amount of dme and other light constituent are discharged by methanol column 1 cat head and are sent into first opening for feed of dme rectifying tower 6 between 4-12 piece column plate, and methanol column 1 working pressure is 0.3～1.5MPa.
Dehydration reactor 3 is fixed-bed reactor, and working pressure is 0.3～1.5MPa, 220～380 ℃ of service temperatures.
Dehydration reactor 3 is a cylindrical container, its epimere 30 adiabatic sections, opening for feed 19 is arranged, its hypomere is the uniform heat exchanging pipe 31 of shell and tube, hypomere tubulation shell side has methanol steam inlet 17 and outlet 18, the import 19 of outlet 18 sections of connecting 30, and the reactant of dehydration reactor 3 lower tubular section 35 is sent to gas heat exchanger 4, interchanger 5 and is entered dme rectifying tower 6 through exporting 20, dehydration catalyst all is equipped with in each pipeline section and the bottom of dehydration reactor 3,220～380 ℃ of service temperatures.
The used methyl alcohol of the present invention is industrial methanol or thick methyl alcohol (half product before purifying in the industrial methanol production process, contain 65～95% methyl alcohol), material benzenemethanol is introduced into alcohol wash tower 9 usefulness material benzenemethanols and absorb the dme from the reaction by-product non-condensable gases that dme rectifying tower 6 overhead condensers 7 are sent, take out of after, absorption liquid as reaction raw materials through reacting thick product after interchanger 5 heat exchange with high temperature dehydration, send into the middle and upper part of methanol column 1, methanol column 1 top is provided with condenser and controls certain quantity of reflux with the less water cooling, the methanol column epimere is used to separate dimethyl ether by rectifying and methyl alcohol, and a small amount of gas phase dme and other light component push up to send from methanol column 1 and return dme rectifying tower 6 middle and upper parts and separate; The middle and lower part stripping section of methanol column 1 is used for separation of methanol and water, and dme rectifying tower 6 tower bottomss that contain methyl alcohol and water mixture are also sent into to vaporize in methanol column 1 middle and lower part and separated, and methanol steam is sent at methanol column 1 middle part; Waste water is discharged continuously from methanol column 1 tower still; The methanol steam that methanol column 1 middle part is sent is after gas heat exchanger 4 heat exchange, be introduced into the tubulation section shell side of dehydration reactor 3 middle and lower parts, react the heat that is produced with high-temperature catalytic in the absorption tube, methanol steam after overheated enters the adiabatic section on dehydration reactor 3 tops again and carries out dehydration reaction at beds, because further rising temperature, exothermic heat of reaction reached best temperature of reaction, reactant enters tubulation section tube side beds from top to bottom and continues reaction, because the heat exchange cooling that pipe is outer makes the reaction bed temperature substantially constant, maintain and carry out catalytic and dehydration reaction under the preferable states; The reacting coarse product that is come out by dehydration reactor 3 need not carry out completely the cooling condensation process and directly send into dme rectifying tower 6 with gas phase and separate after gas heat exchanger 4, interchanger 5 heat exchange; Reacting coarse product enters from dme rectifying tower 6 towers middle part, is the dme product of 85～99.5% (wt%s) from dme rectifying tower 6 cats head or tower top side line extraction mouth extraction purity guaranteeing under a certain amount of side reflux condition; The mixed solution that dme rectifying tower 6 tower bottomss contain methyl alcohol, water and micro-dme is sent back to vaporize into methanol column 1 middle and lower part and is separated; Non-condensable gasess such as a small amount of hydrogen that dehydration reaction produces, carbon monoxide, carbonic acid gas, methane enter alcohol from 7 discharges of dme rectifying tower 6 overhead condensers and wash the dme that tower 9 recovery are taken out of; Non-condensable gases enters that alcohol washes that tower 9 bottoms and cat head spray and methanol feedstock liquid counter-current absorption down dme on a small quantity wherein, and alcohol is washed tower 9 tower bottomss and sent methanol column 1 as raw material.
This invention is the incorporate process for preparing dimethyl ether method of reactive distillation.System response pressure changes with dme rectifying tower 6 top condensers 7 condensate temperatures, according to different regions Various Seasonal (or general facilities condition change) at 0.3～1.5MPa.
This invention methanol column is the rectifying tower that two sections dischargings of two section feedings and top of tower are provided with condenser 10,38 of number of theoretical plates, methanol column 1 evaporator overhead condenser 10 condensation portion methyl alcohol and a small amount of dme, the cat head dme returns dme rectifying tower 6 middle and upper parts 4～12 tower piece plates with gas phase and (down counts from cat head, opening for feed down together), this gas phase reclaims the device structure and the flow process of dme, avoids dme to enter reactive system with methanol steam reaction is caused disadvantageous effect; And allow dme rectifying tower 6 still liquid to have a small amount of dme, and reduced the operation easier of dme rectifying tower 6, the packed height that reduces dme rectifying tower 6 and the reflux ratio of operation, reduced energy consumption; Methanol column 1 does not coexist according to raw materials used methyl alcohol composition and is provided with the methanol feeding mouth between 4～16 tower piece plates, dme rectifying tower 6 still liquid are provided with opening for feed between 18～24 tower piece plates of methanol column 1 middle and lower part, the first alcohol and water separates at methanol column 1 stripping section, need not can reach the separation purpose by ad hoc methanol distillation column like this, and send methanol steam, reduce raw material greatly and separate and the required energy consumption of vaporescence with recovery methyl alcohol; Methanol steam is sent between the 4th～10 tower piece plate.Methanol content is lower than 0.1% in the waste water that the tower still is discharged.
The fixed-bed reactor that catalytic and dehydration reaction device 3 in this invented technology combines for adiabatic and samming shell and tube, as shown in Figure 2: epimere 30 is a heat-insulating, hypomere 31 is the heat exchanging pipe formula, 17 places, bottom are the methanol steam admission port, 18 places are the methanol steam outlet after heat exchange heats up, reactor head 19 places are overheated methanol steam import, and 20 places, bottom are reacting product outlet, all adorn dehydration catalyst in 30 and 35 tubular barrels and in the pipe of heat exchanging pipe 31 among Fig. 2.Dehydration of methanol is thermopositive reaction, elevated temperature is unfavorable for improving the equilibrium conversion of dehydration reaction, but reaction must just can have speed of response and stability faster again more than 240 ℃, and elevated temperature helps the carrying out of side reaction, has reduced reaction preference; So when temperature of reaction rises to suitable temperature, draw heat of reaction in right amount, control catalyst bed temperature rise and to keep the uniform catalyst bed temperature be the principal element that guarantees reaction high conversion and highly selective.This is the ingenious part that adopts adiabatic samming combination type reactor in this invention.Material benzenemethanol steam enters the adiabatic reaction section earlier again after shell and tube section heat exchange absorption reaction heat heats up, carrying out along with reaction, reaction bed temperature raises gradually, after reaction proceeds to certain temperature (280～300 ℃), enter tubulation section beds and continue reaction, the heat that reactant produces is taken out of by the heat exchange of shell side raw material and has effectively been controlled the temperature rise of reaction, make stable reaction 280～320 ℃ optimal reaction temperature section, thereby avoided owing to the reaction of paying that causes that raises of reactor hypomere temperature increases defectives such as causing catalyst breakage with the beds temperature difference greatly.Zu He reactor is an autothermal reaction like this, has both reduced energy consumption, has made full use of reaction heat again to reach the purpose of temperature control, and catalyst efficiency is not fully exerted simultaneously.
In this invented technology process, the dehydration reaction crude product that comes out from dehydration reactor 3 does not need to pass through extraneous water quench, condensation again after heat exchange, enter and directly enter dme rectifying tower 6 middle parts the 12nd～18 tower piece plate place opening for feed with gas phase, save the heat that cold that the thick product gas of Yin Gaowen cools off, condensation is required and product rectifying vaporization need, greatly reduced energy consumption.Because a large amount of heats of bringing into of reacting coarse product, can make one ton of dme of every production save heating with 0.7～1.0 ton of water vapor, reduce and be used to cool off 70～100 tons of the water coolants that reacting coarse product need consume.The dme steam that dme rectifying tower 6 cats head steam is after overhead condenser 7 condensations, and a part is as the product extraction, and a part is gone into the tower from trim the top of column, and backflow and extraction ratio are 0.3: 1.0～1.0: 0.5, requires to adjust according to product purity; A small amount of non-condensable gases of dehydration reaction by-product is discharged and is entered alcohol and wash tower 9 assembling the back through overhead condenser 7, absorbs the dme that non-condensable gases is taken out of with material benzenemethanol, and non-condensable gases is washed tower 9 top discharges emptying or act as a fuel and send system after water seal from alcohol; Tower still material is sent the middle and lower part that enters methanol column 1 back to, because the special construction of methanol column 1 has the function that reclaims dme, so the packed height of dme rectifying tower 6 and operation side reflux have reduced than all with extraction, corresponding investment and energy consumption are lower, easier operation.The gas-phase dehydration that the present invention proposes, the refining incorporate producing and manufacturing technique of thick product separation in conjunction with adopting reactor adiabatic and that the samming tubulation combines, make that the reaction heat recovery utilization rate is the highest; And all even by product reduction than the feasible reaction of low reaction temperature rise, the service efficiency and the life-span of having improved catalyzer; Adopt alcohol to wash tower 9 usefulness material benzenemethanols and do not coagulate the tail gas counter-current absorption with a small amount of by-product, it is minimum to make device take dme out of; It is minimum to guarantee to implement under this technology supplies consumption like this.
This process methanol tower 1 and dme rectifying tower 6 need extraneous heat supply.With the steam of 0.5～2.0MPa or heat conduction wet goods thermal barrier directly or by material in the reboiler indirect heating tower still that links to each other with the tower still.
Description of drawings:
Fig. 1 is a process flow sheet of the present invention.
Fig. 2 is the structure iron of dehydration reaction.
Embodiment:
Process flow sheet of the invention process is shown in accompanying drawing one:
Flow process is described below: material benzenemethanol is washed 11 places, tower 9 tops at alcohol and is entered, incoagulability tail gas is sent into alcohol by the discharge of 25 places, dme overhead condenser 7 tops and is washed 26 places, tower 9 bottoms, alcohol is washed the methyl alcohol that contains a small amount of dme of discharging at 29 places, tower 9 bottoms and enter 12 places, methanol column 1 middle and lower part after interchanger 5 is heated up, after vaporizing in tower, a small amount of dme and methyl alcohol rises, behind methyl alcohol overhead condenser 10 cooling condensations, get off methyl alcohol and a small amount of dme phlegma of partial condensation passes back in the tower, and the gas phase dme is sent inlet 22 places to dme rectifying tower 6 by cat head 15 places; Methanol steam is sent after interchanger 4 heat exchange heat up by 13 places, methanol column 1 middle part, shell side 17 places by the lower columns pipeline section 31 of dehydration reactor 3 enter, methanol steam after dehydration reactor 3 lower columns heat transfer outside a tube heat up is sent by 18 places and is entered beds to 19 places and carry out catalytic and dehydration reaction, reaction mass enters bottom samming tubulation section 31 again behind adiabatic section 30, reaction is continued in adiabatic section 35, reaction product is sent by reactor bottom 20 places, through interchanger 4, after heat was reclaimed in 5 heat exchange, the reacting coarse product gas phase directly entered centre inlet 21 places of dme rectifying tower 6.Reacting coarse product is finished cooling, condensation simultaneously together, is separated and rectifying with a small amount of dme that methanol column returns in dme rectifying tower 6 towers, because the reacting coarse product gas phase is brought a large amount of sensible heats and latent heat into, satisfy the required most of energy of dme tower rectifying, needed the outside heat that provides seldom; Dme steam is sent by cat head 23 places, and after overhead condenser 7 condensations, a dme phlegma part is returned in the tower by dme rectifying tower top 26 places as phegma, another part as product by the extraction of 26 places.The dme rectifying tower 6 still liquid that contain methyl alcohol, water and micro-dme by tower at the bottom of 30 places discharge 14 places, middle and lower part that send back to methanol column, behind methanol column 1 Separation and Recovery methyl alcohol and dme, waste water is discharged by 16 places, methanol column 1 bottom.The a small amount of incoagulability tail gas that contains dme of being discharged by 25 places, dme overhead condenser 7 tops is admitted to alcohol and washes 28 places, tower 9 bottoms, and through methyl alcohol absorbing and removing dme, incoagulability tail gas is washed cat head 27 places by alcohol and discharged.
The experiment embodiment of this patent is provided below:
Embodiment 1:
Methanol column 1 working pressure 0.95MPa.
The charging 12 material benzenemethanol 2416kg/h of place, methyl alcohol 2036kg/h wherein, water 11kg/h, dme 369kg/h; The still liquid that the dme rectifying tower returns enters 1252kg/h by 14 places, methyl alcohol 678kg/h wherein, water 579kg/h.Methyl alcohol cat head 15 place's exhaust vapours contain methyl alcohol 2.2kg/h, dme 267kg/h; 13 places, tower middle and upper part go out methanol steam and contain methyl alcohol 2695kg/h, water 16.6kg/h, dme 2kg/h; Tower still 16 places discharge in the waste water and contain methyl alcohol 0.04%.
It is 220 ℃ of 0.3MPa its underpart tubulation section shell side 17 place's temperature that unstripped gas advances dehydration reactor 3 working pressures, 260 ℃ of import 19 place's temperature, 260～320 ℃ in temperature of reaction interval, dehydration reactor 3 outlets 20 obtain dehydration reaction product: methanol steam 674kg/h, water vapor 560kg/h, dme steam 1424kg/h, noncondensable gas 45Nm3/h; 145 ℃ enter 21 places, dme rectifying tower 6 middle parts after gas heat exchanger 4, interchanger 5 heat exchange, are 1.5,26 places extraction dme product 1424kg/h at the ratio of cat head 24 place's quantity of reflux and 26 place's produced quantities, dme content 99.0%.8 the outer water supply steam of need of dme rectifying tower 6 reboilers 200kg/h.
Product dme rectifying tower 6 working pressure 0.90MPa.
Embodiment 2:
Methanol column 1 working pressure 0.40MPa.
Material benzenemethanol 428.6kg/h is advanced at methanol column 1 charging 12 places, methyl alcohol 300kg/h wherein, water 128.6kg/h, dme 1.5kg/h; Return dme rectifying tower 6 still liquid and advance 14 362kg/h of place, methyl alcohol 180.7kg/h wherein, water 178.8kg/h, dme 2.5kg/h.15 places, methanol column 1 condenser, 10 tops discharge dme steam and contain methyl alcohol 0.05kg/h, dme 3.8kg/h; 13 places, tower middle and upper part send methanol steam and contain methyl ether 480kg/h, water 3.5kg/h; Tower still 16 places discharge in the waste water and contain methyl alcohol 0.2%.
Dehydration reactor and example 1 are similar, it is 1.5MPa that unstripped gas advances dehydration reactor 3 its working pressures, 200 ℃ of lower columns pipeline section shell side 17 place's temperature, 240 ℃ of import 19 place's temperature, 240～300 ℃ in temperature of reaction interval, dehydration reactor 3 outlets 20 obtain dehydration reaction product: methyl alcohol 48kg/h, water 125kg/h, dme 308kg/h, noncondensable gas 8Nm3/h; 125 ℃ enter 21 places, dme rectifying tower 6 middle parts after heat exchange, are 0.85,26 place extraction dme product 313.8kg/h at the ratio of cat head 24 place's quantity of reflux and 26 place's produced quantities, dme content 96%.
Product dme rectifying tower 6 working pressure 0.36MPa.
Embodiment 3:
Operational stage and embodiment 1 are similar substantially. methanol column 1 working pressure 1.5Mpa.Entering material from the methanol steam import 17 of dehydration reactor 3 is 2016kg/h, methyl alcohol 2000kg/h wherein, water 14.5kg/h, dme 1.5kg/h.Reaction pressure 0.57MPa, 290～320 ℃ in temperature of reaction interval; Advance to react thick product and be at opening for feed 21 places of dme rectifying tower 6: methyl alcohol 154kg/h, water 531kg/h, dme 1309kg/h, noncondensable gas 35Nm3/h; The reaction per pass conversion is greater than 91%, and the dme selectivity is greater than 98.5%.The working pressure of dme rectifying tower is 1.5MPa.
Claims (6)
1, a kind of is that the method for raw material production dme comprises material benzenemethanol is vaporized at methanol column (1) with methyl alcohol, gas-phase methanol is dewatered at dehydration reactor (3), dehydration reaction product rectifying in dme rectifying tower (6) obtains the dme step, it is characterized in that the thick product of reaction that dehydration reactor (3) comes out enters dme rectifying tower (6) with gas phase after heat exchange, finish the cooling of thick product at dme rectifying tower (6), condensation, separate and rectifying, overhead condensation at dme rectifying tower (6) obtains the dme product, the cat head byproduct of reaction does not coagulate tail gas emptying after alcohol is washed tower (9) washing, the part dme product reflux of dme rectifying tower (6) condenser (7) condensation is gone in the dme rectifying tower (6), contain water, the tower bottoms of methyl alcohol and a small amount of dme is sent methanol column (1) back to, and the working pressure of dme rectifying tower (6) is 0.3～1.5MPa.
2, according to the 1 described method that requires of right, it is characterized in that methanol column (1) cat head has condenser (10), a small amount of dme and other light constituent return dme rectifying tower (6) by methanol column (1) cat head with gas phase, the working pressure of methanol column is 0.3～1.5MPa, 110～200 ℃ of service temperatures.
3, method according to claim 1, it is characterized in that material benzenemethanol washes tower (9) top from alcohol and enter alcohol and wash tower (9) washing and do not coagulate tail gas by the byproduct of reaction that dme rectifying tower (6) cat head comes, after heating up, interchanger (5) enters first opening for feed of methanol column (1) from the methyl alcohol that contains a small amount of dme of tower bottom discharge, dme rectifying tower (6) tower bottoms enters second opening for feed of methanol column (1), methanol column (1) is made up of tower body and top condenser (10) thereof, condenser (10) condensation portion methyl alcohol and a small amount of dme, the cat head dme enters first opening for feed of dme rectifying tower (6) with gas phase, methanol steam enters dehydration reactor (3) after sending from the middle part of methanol column (1), and waste water is discharged from methanol column (1) tower still.
4, method according to claim 3, the number of theoretical plate that it is characterized in that methanol column (1) is 38, first opening for feed is between the 4-16 piece plate of down counting from cat head, second opening for feed is between 18-24 piece plate, methanol steam enters dehydration reactor (3) from sending between the 4-10 piece column plate of methanol column (1) after gas heat exchanger (4) is overheated, a small amount of dme and other light constituent are discharged by methanol column (1) cat head and are sent into first opening for feed of dme rectifying tower (6) between 4-12 piece column plate, and methanol column (1) working pressure is 0.3～1.5MPa.
5, method according to claim 1 is characterized in that dehydration reactor (3) is fixed-bed reactor, and working pressure is 0.3～1.5MPa, 220～380 ℃ of service temperatures.
6, method according to claim 5, it is characterized in that dehydration reactor (3) is a cylindrical container, its epimere (30) adiabatic section, opening for feed (19) is arranged, its hypomere is the uniform heat exchanging pipe of shell and tube (31), hypomere tubulation shell side has methanol steam inlet (17) and outlet (18), the import (19) of outlet (18) section of connecting (30), the reactant of dehydration reactor (3) lower tubular section (35) is sent to gas heat exchanger (4) through outlet (20), interchanger (5) enters dme rectifying tower (6), the agent of the anti-university of catalytic dehydration, 220～380 ℃ of service temperatures all are equipped with in each pipeline section of dehydration reactor (3) and bottom.
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| CN101643401A (en) * | 2008-08-10 | 2010-02-10 | 赵荣林 | Device for decreasing blanking temperature and improving operation environment |
| CN101195561B (en) * | 2007-12-26 | 2010-04-14 | 成都天成碳一化工有限公司 | Method for producing dimethyl ether with methanol gas-phase dehydration |
| DE102008058931A1 (en) | 2008-11-25 | 2010-06-02 | Lurgi Gmbh | Process and apparatus for producing dimethyl ether from methanol |
| CN101215224B (en) * | 2008-01-07 | 2010-06-02 | 烟台同业化工技术有限公司 | Low energy-consumption method for preparing dimethyl ether from methanol |
| CN101838185A (en) * | 2009-03-20 | 2010-09-22 | 上海吴泾化工有限公司 | Dehydration reactor |
| CN101412665B (en) * | 2008-11-27 | 2011-01-12 | 何东 | Apparatus for coproduction of refined methanol and dimethyl ether or production of each of refined methanol and dimethyl ether from coarse methyl alcohol |
| CN101139265B (en) * | 2007-08-08 | 2011-04-27 | 四川泸天化绿源醇业有限责任公司 | Process for pressurized synthesis of dimethyl ether |
| CN102471194A (en) * | 2009-07-03 | 2012-05-23 | 卢尔吉有限公司 | Method and system for producing methanol and dimethyl ether |
| US8541630B2 (en) | 2008-03-26 | 2013-09-24 | China Petroleum & Chemical Corporation | Process for producing dimethyl ether from methanol |
| CN104370710A (en) * | 2014-11-10 | 2015-02-25 | 中国海洋石油总公司 | Process method for producing dimethyl ether from methanol in gas phase at low temperature |
| CN104740889A (en) * | 2013-12-31 | 2015-07-01 | 财团法人工业技术研究院 | Gas treatment method and system |
| CN110550631A (en) * | 2019-08-29 | 2019-12-10 | 杭州杭氧股份有限公司 | device for producing ultrapure carbon dioxide by multi-tower circulation full-rectification |
| CN111285755A (en) * | 2018-12-06 | 2020-06-16 | 惠生工程（中国）有限公司 | Separation method of reaction product for preparing dimethyl ether by methanol dehydration |
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| CN101139265B (en) * | 2007-08-08 | 2011-04-27 | 四川泸天化绿源醇业有限责任公司 | Process for pressurized synthesis of dimethyl ether |
| CN101195561B (en) * | 2007-12-26 | 2010-04-14 | 成都天成碳一化工有限公司 | Method for producing dimethyl ether with methanol gas-phase dehydration |
| CN101215224B (en) * | 2008-01-07 | 2010-06-02 | 烟台同业化工技术有限公司 | Low energy-consumption method for preparing dimethyl ether from methanol |
| US8541630B2 (en) | 2008-03-26 | 2013-09-24 | China Petroleum & Chemical Corporation | Process for producing dimethyl ether from methanol |
| CN101643401A (en) * | 2008-08-10 | 2010-02-10 | 赵荣林 | Device for decreasing blanking temperature and improving operation environment |
| DE102008058931A1 (en) | 2008-11-25 | 2010-06-02 | Lurgi Gmbh | Process and apparatus for producing dimethyl ether from methanol |
| US8884074B2 (en) | 2008-11-25 | 2014-11-11 | Air Liquide Global E&C Solutions Germany Gmbh | Method and device for producing dimethyl ether from methanol |
| CN101412665B (en) * | 2008-11-27 | 2011-01-12 | 何东 | Apparatus for coproduction of refined methanol and dimethyl ether or production of each of refined methanol and dimethyl ether from coarse methyl alcohol |
| CN101838185A (en) * | 2009-03-20 | 2010-09-22 | 上海吴泾化工有限公司 | Dehydration reactor |
| CN102471194A (en) * | 2009-07-03 | 2012-05-23 | 卢尔吉有限公司 | Method and system for producing methanol and dimethyl ether |
| US9255052B2 (en) | 2009-07-03 | 2016-02-09 | Lurgi Gmbh | Method and system for producing methanol and dimethyl ether |
| CN105622340A (en) * | 2009-07-03 | 2016-06-01 | 卢尔吉有限公司 | Method and device for producing methanol and dimethyl ether |
| CN104740889A (en) * | 2013-12-31 | 2015-07-01 | 财团法人工业技术研究院 | Gas treatment method and system |
| CN104370710A (en) * | 2014-11-10 | 2015-02-25 | 中国海洋石油总公司 | Process method for producing dimethyl ether from methanol in gas phase at low temperature |
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