CN101125803A - Preparation method for dimethyl ether - Google Patents
Preparation method for dimethyl ether Download PDFInfo
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- CN101125803A CN101125803A CNA2007100708000A CN200710070800A CN101125803A CN 101125803 A CN101125803 A CN 101125803A CN A2007100708000 A CNA2007100708000 A CN A2007100708000A CN 200710070800 A CN200710070800 A CN 200710070800A CN 101125803 A CN101125803 A CN 101125803A
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Abstract
The invention relates to a method for producing dimethyl ether. The method can be used for the devices for producing dimethyl ether by using methanol. The procedures of the method are that: in the raw material input system taken methanol as principal component,, impurities such as high boiler, etc., is removed from the raw materials; the residual heat of the system can be used for heating the material so order to vaporize the liquid methanol in the material, after heat transferring under high temperature, the material and the vaporized methanol from a methanol recycle tower are put into a dimethyl ether synthesis reactor to carry out methanol dehydration reaction. The reaction products after the dehydration reaction are rectified and separated by heat transferring under high temperature and the dimethyl ether is produced. The invention has the advantages of simple and reliable technology, good stability, less heat energy consumption, high utilization rate and conversion rate of methano, less side reaction in the process of synthesis reaction, high activity and long service life of catalyst, low production cost and no environmental pollution.
Description
Technical field
The present invention relates to a kind of chemical products preparation method, especially a kind of method for preparing dme can be widely used in and uses preparing dimethyl ether from methanol.
Background technology
Dme is a kind of important carbinol derivatives and important chemical material, is again universally acknowledged ideal clean fuel.With methyl alcohol is that the chemical equation of feedstock production dme is as follows:
2CH
3OH→CH
3OCH
3+H
2O+23.4kJ
This reaction is thermopositive reaction, and the reaction heat of 1 mole of dme of every generation is 23.4kJ (5.59kcal), and therefore, the synthesising reacting heat of methanol dehydration dimethyl ether-preparing has very big recycling and is worth.
In the prior art, method with preparing dimethyl ether from methanol is: material benzenemethanol send the methanol gas phase dehydration reactive system to carry out dehydration reaction after methyl alcohol vaporization tower all heats vaporization, reaction product send the dme rectifying tower to separate, and obtains dme from dme rectifier or top.The mixed solution of the methyl alcohol of discharging from dme rectifying Tata still and water etc. is sent into methyl alcohol vaporization tower again and is carried out rectifying separation, from continuing raw material after recovered overhead gets methyl alcohol as the preparation dme, and from water discharge system that the tower still obtains.Existing is that the shortcoming of the method for feedstock production dme is to remove high boiling material and impurity by methyl alcohol vaporization tower with methyl alcohol, and these high boiling material and impurity can improve the boiling point of tower still still liquid, increase energy consumption in methyl alcohol vaporization tower; In methyl alcohol vaporization tower,, can increase the content of residual methanol in the still liquid, and contain methyl alcohol in the still liquid because of the discharge system, thereby not only reduce the utilization ratio of methyl alcohol, also pollute environment also because the existence of these materials is subjected to its influence to methyl alcohol avidity.In addition, when methanol gas phase dewatering preparing be equipped with in the dme reactive system methanol conversion one regularly owing to when dme rectifying tower bottoms enters methyl alcohol vaporization tower and carries out the methyl alcohol vaporization and reclaim, need to consume heat energy, and the original waste heat of system is not utilized well, has wasted heat resource.In addition, if the reaction heat in the dehydration reaction system does not in time shift out, to cause the temperature of dehydration reaction too high, not only influenced the equilibrium conversion of methyl alcohol, also generate hydro carbons (as methane, ethane, ethene, propylene etc.) impurity easily, and catalyzer coking, active decline, work-ing life are shortened.Thereby, not only increased the production cost of product dme, also influenced the stability of system.
Summary of the invention
Technical problem to be solved by this invention is: at the deficiencies in the prior art, provide a kind of heat energy consumption few, use ratio of methanol and transformation efficiency height, side reaction is few in the synthetic reaction process, catalyst activity height, long service life, low in the pollution of the environment, production cost is low, the processing method of the preparation dme that system stability is good.
The present invention realizes by the following method:
A kind of method for preparing dme comprises the steps:
A, will contain 75%～99.5% methyl alcohol and the mixed solution of a certain amount of water is the raw material input system, carry out pre-treatment, remove the impurity such as a spot of methyl alcohol by-product high boiling material that contain in the stock liquid with 1 pair of raw material of pretreater;
B, the raw material after step a handles enter pre-heating system 2 and heat, and the methanol steam that produces after pre-heating system 2 heating enters dme synthesis reactor 6 by vapour liquid separator 3 with the methanol steam of discharging from methanol distillation column 4 and carries out Dehydration of methanol after high-temperature heat-exchanging 5 high temperature heat exchange; After the liquid methanol of vaporization does not separate by vapour liquid separator 3 fully in pre-heating system 2 in the raw material, enter methanol distillation column 4 and vaporize; Send vaporization and the recovery that methanol distillation column 4 carries out methyl alcohol again back to from the still liquid that dme rectifying tower 8 is discharged based on the first alcohol and water;
C, the reaction product based on dme, first alcohol and water of coming out after dehydration reaction are introduced into high-temperature heat-exchanging 5 and carry out heat exchange and heating methanol steam with methanol steam, incoming stock then pre-heating system 2 carries out heat exchange and heating raw liquid with stock liquid, make the operative liquid methyl alcohol vaporization in the stock liquid, enter dme rectifying tower 8 again and carry out rectifying separation, extraction dme product from dme rectifying tower 8.
In step a, pretreater 1 is the membrane separation apparatus of 0.01 μ m～5.0 μ m for separating the aperture.
In step b, also comprise the liquid raw material by entering methanol distillation column 4 behind the vapour liquid separator 3 separation of methanol steam and send the still liquid of methanol distillation column 4 back to from dme rectifying tower 8, under the pressure condition of 0.2～1.5MPa, carry out the vaporization of methyl alcohol.
In step b, comprise that also the tower still still liquid that discharge methanol distillation column 4 bottoms send pre-heating system 2 recovery waste heats, behind the heating methanol stock liquid, send into remaining small amount of methanol in the flasher 11 flash distillation still liquid, and reclaim methyl alcohol by tail gas absorber 10.
In step b, comprise that also the vapour condensation water of discharge from reboiler 12 and reboiler 13 is sent into pre-heating system 2 recovery waste heats, heating methanol stock liquid.
In step b, comprise that also vapour phase methyl alcohol is that 240 ℃～385 ℃, pressure are 0.05MPa～2.2MPa and carry out dehydration reaction under the katalysis of dme special-purpose catalyst in temperature.
In step c, comprise that also the methyl alcohol that reclaims with tail gas absorber 10 enters dme rectifying tower 8 after the reaction product mixed solution behind raw material preheating system 2 recovery waste heats and the heating methanol stock liquid enters vapour liquid separator 7 separation non-condensable gasess.
In step c, also comprise discharge from the top of dme rectifying tower 8 based on the mixture of dme behind vapour liquid separator 9 separation non-condensable gasess, extraction dme product; Further reclaim dme through vapour liquid separator 9 isolated non-condensable gasess and a small amount of dme with entering tail gas absorber 10 through vapour liquid separator 7 isolated non-condensable gasess, a small amount of dme.
The invention has the beneficial effects as follows: simple and reliable process, good stability, heat energy consumption is few, use ratio of methanol and transformation efficiency height, in the synthetic reaction process side reaction few, catalyst activity height, long service life, non-environmental-pollution, the production cost of product dme is low.
Description of drawings
Accompanying drawing is a kind of process flow sheet for preparing the method for dme with the methanol vapor phase dehydration among the present invention.Among the figure, with containing 75%～99.5% the methyl alcohol and the mixed solution of a certain amount of water is raw material input system (by weight percentage), process separation aperture is that the membrane separation apparatus of 0.01 μ m～5.0 μ m is that 1 pair of raw material of pretreater carries out pre-treatment, remove high boiling material and other impurity such as 0.01～0.3% the methyl alcohol by-product higher alcohols that contain in the stock liquid and aldehyde compound, to reduce the boiling point of methanol feedstock liquid, under the situation that consumes same heat energy, can improve the evaporating capacity of methyl alcohol effectively.Simultaneously, can also reduce higher alcohols and aldehyde compound, reduce the side reaction in the dme synthetic reaction process, prolong activity of such catalysts and work-ing life the active influence of dimethyl ether catalyst.
Pre-heating system 2 has the functions such as heating raw materials, waste heat recovery, methyl alcohol vaporizing, such as, board-like changing Hot device or tubular heat exchanger etc. can be recycled dimethyl ether Heat of Formation, methanol distillation column 4 effectively The waste heat of the steam condensate (SC) that draining waste heat and reboiler 12, reboiler 13 are discharged. Methanol feedstock liquid is through pre-After 2 heating of hot system, liquid methanol part or major part in the material liquid are vaporized. In the raw material in advance After the liquid methanol of vaporization does not separate by vapour liquid separator 3 in the hot system 2, from the top of methanol distillation column 4 Enter methanol distillation column 4. This vapour liquid separator 3 can be established disc type flash vessel and mesh mist eliminator or rule for interior The GB150-1998 of the cylinder type of whole media assemblage; This methanol distillation column 4 can be packed tower or board-like Tower. Discharge from the bottom of dimethyl ether rectifying column 8 take water and methyl alcohol as main still liquid from methanol distillation column 4 Middle part or middle and lower part are sent methanol distillation column 4 back to; Vapour under the heat effect of the high-temperature vapour that reboiler 12 is imported Change the liquid methanol in the methanol distillation column 4; When vaporizing liquid methanol in the methanol distillation column 4 in order effectively to reduce Thermal energy consumption, the pressure in the methanol distillation column 4 should not be too high, is generally 0.2～1.5MPa.
The methanol steam that after pre-heating system 2 heating, produces and the first of discharging from the top of methanol distillation column 4 Alcohol steam, closes after the absorption dewatering reaction through high-temperature heat-exchanging 5 high temperature heat exchange together by vapour liquid separator 3 Become the heat energy in the product mixed liquor, improve the degree of superheat of methanol steam. Under the pressure of 0.05～2.2MPa Input dimethyl ether reactor 6, and make temperature maintenance in the reactor 240～385 through the heating by electric cooker that goes into operation ℃, at dimethyl ether special-purpose catalyst such as γ-Al2O
3Catalytic action under carry out Dehydration of methanol. Dimethyl ether Reactor 6 bottom catalyst temperatures generally should stably be controlled at about 310 ℃, to improve to greatest extent The conversion ratio of methyl alcohol. This dimethyl ether reactor 6 is isothermal synthesis reactor, and reactor is established first from top to bottom Alcohol distribution of steam district, Dehydration of methanol heat transfer zone and reactant and catalyst outlet district etc.
Tower reactor still liquid input pre-heating system 2 recovery waste heats of discharging from methanol distillation column 4 bottoms are used for heating Methanol feedstock liquid, the tower reactor still liquid behind recovery waste heat and heating methanol material liquid is sent into flash vessel 11 flash distillations The remaining a small amount of methyl alcohol of vaporizing reclaims methyl alcohol by tail gas absorber 10 after the condensation, discharges in the flash vessel 11 The waste water output system. Because of the methyl alcohol from the tower reactor still liquid that discharge methanol distillation column 4 bottoms by again Recycle, discharge the methyl alcohol that no longer contains methyl alcohol in the waste water of system or only contain denier, thereby, The waste water of discharge system can be secondary use, and effectively prevents the pollution of the environment, and preserves the ecological environment.
The steam condensing water that the steam condensate (SC) of discharging in the reboiler 12 is discharged in reboiler 13 send Enter pre-heating system 2 recovery waste heats, the heating methanol material liquid.
That comes out after dehydration changes as main product is introduced into high temperature take dimethyl ether, first alcohol and water Hot device 5 such as plate type heat exchanger or tubular heat exchanger, carries out the high temperature heat exchange and heats first with methanol steam Alcohol steam enters then raw material preheating system 2 and carries out heat exchange and heating methanol material liquid with methanol feedstock liquid, Mixture of reaction products behind raw material preheating system 2 recovery waste heats and heating methanol material liquid enters vapour-liquid After separator 7 separated incoagulable gas, the methyl alcohol that reclaims with tail gas absorber 10, dimethyl ether were from diformazan The middle part of ether rectifying column 8 enters dimethyl ether rectifying column 8, under the effect of the heating steam that reboiler 13 is imported, Dimethyl ether in the vaporization dimethyl ether rectifying column 8 realizes that the rectifying of dimethyl ether separates. From dimethyl ether rectifying column 8 Top discharge take dimethyl ether as main mixture after vapour liquid separator 9 separates incoagulable gas, extraction Purity reaches 99%～99.99% dimethyl ether product. Perhaps, also can establish in addition a dimethyl ether rectifying column, The mixture take dimethyl ether as main component that is come out by first dimethyl ether rectifying column enters second diformazan The further rectifying separation of dimethyl ether of ether rectifying column, thus can be from second dimethyl ether rectifying column extraction more Highly purified dimethyl ether product. Dimethyl ether rectifying column 8 is plate column or packed tower, and top of tower is provided with condensed system The return-flow system of unifying, and can be according to the purity requirement of product dimethyl ether, the height of flexible modulation extraction mouth.
Through vapour liquid separator 9 isolated incoagulable gas and a small amount of dimethyl ether with through vapour liquid separator 7 minutes Enter together tail gas absorber 10 from the incoagulable gas that goes out, a small amount of dimethyl ether and further reclaim dimethyl ether. Discharge system from the tail gas that contains incoagulable gas that tail gas absorber 10 is discharged, send into the burning systems such as boiler The system use that acts as a fuel.
Because some field is not high to the purity requirement of product dimethyl ether such as the use that acts as a fuel, product two The light components such as the incoagulable gas in the methyl ether can separate. Therefore, in this process chart Can not establish vapour liquid separator 7 and vapour liquid separator 9, what the product dimethyl ether can be from dimethyl ether rectifying column 8 is upper Section is extraction after condensation, and the equipment of vapour liquid separator 7 and vapour liquid separator 9 that so not only can save is thrown Support, can also reduce the height of dimethyl ether rectifying column 8, the gross investment of this production system is obviously reduced.
The invention has the advantages that and fully recycled the reaction heat in the dehydration, methanol distillation column 4 The draining waste heat and the waste heat of reboiler 12, reboiler 13 steam condensate (SC) of discharging, saved dimethyl ether Energy resource consumption in the production process has realized the recycling of the energy, has reduced the production cost of dimethyl ether.
The present invention be advantageous in that owing to utilized the waste heat in the system to come the heating methanol material liquid, make former Part in the feed liquid or most of liquid methanol are vaporized, and have improved significantly the raw material that enters reactor The concentration of methyl alcohol in the gas, and can reduce methanol distillation column to the vaporization of the liquid methanol in the material liquid Workload, and then can in the certain situation of the production equivalent of product dimethyl ether, reduce methanol distillation column Diameter and the height, saved methanol distillation column equipment investment and the vaporization liquid methanol energy resource consumption.
The present invention be advantageous in that with membrane separator raw material is carried out preliminary treatment, methanol removal by-product high-carbon The high-boiling components such as alcohol and aldehyde compound and other impurity are to reduce the boiling point of methanol feedstock liquid, raising process Separating degree, in the situation of liquid methanol of the same equivalent of vaporization, can effectively reduce thermal energy consumption. Simultaneously, can also reduce the higher alcohols that produce in the methyl alcohol preparation process and aldehyde compound to dimethyl ether catalysis The impact of agent activity reduces the side reaction in the dimethyl ether synthetic reaction process, the activity of extending catalyst and Service life, the production cost of reduction dimethyl ether.
The present invention be advantageous in that the methyl alcohol from the tower reactor still liquid that the Methanol Recovery tower bottom is discharged is filled Divide to recycle, discharge the methyl alcohol that no longer contains methyl alcohol in the waste water of system or only contain denier, because of And can be secondary use, effectively prevent the pollution of the environment, preserve the ecological environment.
The present invention be advantageous in that methanol distillation column, dimethyl ether rectifying column have cleverly structure, and use Unique technology is made, thereby in dimethyl ether separation and Methanol Recovery process, has the negative of permission The advantages such as the lotus fluctuation range is big, operation is convenient and reliable, the start-stop car is fast can energy efficient and saving The start up time.
Embodiment
Embodiment 1:
With methanol content be 95%, the methanol feedstock liquid that contains 0.03% methyl alcohol by-product high boiling material and water is through pump input dme production system, removes high boiling material by 1 μ m membrane separation apparatus; Remove methanol feedstock liquid behind the high boiling material in the raw material preheating system after heating, liquid methanol is able to the part vaporization; Entering methanol distillation column after Qi Hua liquid methanol does not separate by vapour liquid separator vaporizes.Methanol steam after the vaporization is at the beds that enters dimethyl ether reactor under the 0.8MPa pressure after by the high-temperature heat-exchanging heat exchange, at γ-Al
2O
3Carry out Dehydration of methanol under the katalysis of catalyzer, the reactor outlet temperature is 310 ℃, and methanol conversion is 83.5%; The dme reaction product is in reactor after heat-exchanging tube bundle, the heat exchange of the stock liquid pre-heating system cooling, import dme rectifying tower middle part through vapour liquid separator with pump, in temperature is that 45 ℃～165 ℃, pressure are that 1.0MPa, reflux ratio are to carry out the dme rectifying separation under 1.2 the condition, and the catch tray place extraction purity between overhead condenser and layer 5 structured packing section is 99.99% dme.
Embodiment 2:
With methanol content be 99.5% methanol feedstock liquid through pump input dme production system, remove micro-high boiling material by 0.5 μ m stainless steel membrane separator after, through heating, liquid methanol is able to the part vaporization to methanol feedstock liquid in the raw material preheating system; Entering methanol distillation column after Qi Hua liquid methanol does not separate by vapour liquid separator vaporizes.Methyl alcohol after the vaporization is heated to 270 ℃ of beds that enter dimethyl ether reactor by high-temperature heat-exchanging, the electric furnace that goes into operation under 1.1MPa pressure, at γ-Al
2O
3Carry out Dehydration of methanol under the katalysis of catalyzer, 315 ℃ of reactor outlet temperature, methanol conversion is 83%, obtains DME54.63%, H
2O 26.02%, CH
3The reaction product mixed solution of OH 19.08%; Dme reaction product mixed solution enters the dme rectifying tower after the heat exchange cooling, in temperature is that 35 ℃～155 ℃, pressure are that 0.85MPa, reflux ratio are to carry out the dme rectifying separation under 1.0 the condition, is 99.98% dme in the 65th column plate place extraction purity.
Embodiment 3:
Be 92%, contain 0.01～0.2% methyl alcohol by-product high boiling material and enter system with methanol content, carry out pre-treatment by 0.5 μ m membrane separation apparatus, remove high boiling material and impurity such as higher alcohols and aldehyde compound, decreasing ratio reaches 99%.
Embodiment 4:
With methanol content is that 95.2% methanol feedstock liquid enters system, under the 0.6MPa pressure after membrane separation apparatus carries out raw materials pretreatment, enter built-up type raw material preheating system, the liquid methanol of under 122 ℃ temperature, vaporizing, the vaporization rate of liquid methanol is about 55%.
Claims (8)
1. a method for preparing dme comprises the steps:
A, will contain 75%～99.5% methyl alcohol and the mixed solution of a certain amount of water is the raw material input system, raw material be carried out pre-treatment, remove the impurity such as a spot of methyl alcohol by-product high boiling material that contain in the stock liquid with pretreater (1);
B, the raw material after step a handles enter pre-heating system (2) and heat, and the methanol steam that produces after pre-heating system (2) heating enters dme synthesis reactor (6) by vapour liquid separator (3) with the methanol steam of discharging from methanol distillation column (4) and carries out Dehydration of methanol after high-temperature heat-exchanging (5) high temperature heat exchange; After the liquid methanol of vaporization does not separate by vapour liquid separator (3) fully in pre-heating system (2) in the raw material, enter methanol distillation column (4) and vaporize; Send vaporization and the recovery that methanol distillation column (4) carries out methyl alcohol again back to from the still liquid that dme rectifying tower (8) is discharged based on the first alcohol and water;
C, the reaction product based on dme, first alcohol and water of coming out after dehydration reaction are introduced into high-temperature heat-exchanging (5) and carry out heat exchange and heating methanol steam with methanol steam, incoming stock then pre-heating system (2) carries out heat exchange and heating raw liquid with stock liquid, make the operative liquid methyl alcohol vaporization in the stock liquid, enter dme rectifying tower (8) again and carry out rectifying separation, extraction dme product from dme rectifying tower (8).
2. method according to claim 1 is characterized in that be the membrane separation apparatus of 0.01 μ m～5.0 μ m at the pretreater (1) described in the step a for separating the aperture.
3. method according to claim 1, it is characterized in that in step b, also comprising the liquid raw material by entering methanol distillation column (4) behind vapour liquid separator (3) the separation of methanol steam and send the still liquid of methanol distillation column (4) back to, under the pressure condition of 0.2MPa～1.5MPa, carry out the vaporization of methyl alcohol from dme rectifying tower (8).
4. method according to claim 1, it is characterized in that in step b, also comprising that the tower still still liquid that discharge methanol distillation column (4) bottom send pre-heating system (2) recovery waste heat, behind the heating methanol stock liquid, send into remaining small amount of methanol in flasher (11) the flash distillation still liquid, and reclaim methyl alcohol by tail gas absorber (10).
5. method according to claim 1 is characterized in that also comprising that the vapour condensation water of discharge from reboiler (12) and reboiler (13) is sent into pre-heating system (2) recovery waste heat, heating methanol stock liquid in step b.
6. method according to claim 1 is characterized in that also comprising that vapour phase methyl alcohol is that 240 ℃～385 ℃, pressure are 0.05MPa～2.2MPa and carry out dehydration reaction under the katalysis of dme special-purpose catalyst in temperature in step b.
7. method according to claim 1, it is characterized in that in step c, also comprising that the methyl alcohol that reclaims with tail gas absorber (10) enters dme rectifying tower (8) after the reaction product mixed solution behind raw material preheating system (2) recovery waste heat and the heating methanol stock liquid enters vapour liquid separator (7) separation non-condensable gases.
8. according to the described method of claim 1-7, it is characterized in that in step c, also comprising discharge from the top of dme rectifying tower (8) based on the mixture of dme behind vapour liquid separator (9) separation non-condensable gases, extraction dme product; Through the isolated non-condensable gases of vapour liquid separator (9) and a small amount of dme with through the isolated non-condensable gases of vapour liquid separator (7), dme enters tail gas absorber (10) and further reclaims dme on a small quantity.
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|---|---|---|---|
| CNB2007100708000A CN100567238C (en) | 2007-08-17 | 2007-08-17 | A kind of method for preparing dme |
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|---|---|---|---|
| CNB2007100708000A CN100567238C (en) | 2007-08-17 | 2007-08-17 | A kind of method for preparing dme |
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| CN101851152A (en) * | 2010-05-07 | 2010-10-06 | 山东清大新能源有限公司 | Method for preparing dimethyl ether by methyl alcohol gaseous phase dehydration |
| CN102010301A (en) * | 2010-11-02 | 2011-04-13 | 东莞市九丰化工有限公司 | Low-energy-consumption process for producing dimethyl ether and production equipment thereof |
| CN102225889A (en) * | 2011-05-17 | 2011-10-26 | 神华宁夏煤业集团有限责任公司 | Method for preparing dimethyl ether by dehydration of methanol |
| CN102666460A (en) * | 2009-11-17 | 2012-09-12 | 鲁奇有限责任公司 | Manufacture of dimethyl ether from crude methanol |
| CN101550067B (en) * | 2009-05-15 | 2013-03-20 | 新奥新能(北京)科技有限公司 | Method for producing two-stage dimethyl ether |
| CN103012076A (en) * | 2012-12-24 | 2013-04-03 | 新奥科技发展有限公司 | Method and device of rectifying dimethyl ether and recovering dimethyl ether from non-condensable gas |
| CN101550066B (en) * | 2008-12-26 | 2013-06-05 | 新奥新能(北京)科技有限公司 | Production method of aerosol grade dimethyl ether |
| CN101712595B (en) * | 2009-10-15 | 2013-08-21 | 云南瑞升烟草技术（集团）有限公司 | Method for preparing high-purity dimethyl ether free from extraneous odour |
| CN103480161A (en) * | 2013-03-26 | 2014-01-01 | 新能(张家港)能源有限公司 | Control apparatus for methanol recovery tower reboiler |
| CN103508855A (en) * | 2013-03-26 | 2014-01-15 | 新能(张家港)能源有限公司 | Device and method for preparing dimethyl ether |
| CN104151145A (en) * | 2013-12-10 | 2014-11-19 | 中国平煤神马集团蓝天化工股份有限公司遂平化工厂 | Production method for dimethyl ether |
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| CN101550066B (en) * | 2008-12-26 | 2013-06-05 | 新奥新能(北京)科技有限公司 | Production method of aerosol grade dimethyl ether |
| CN101550067B (en) * | 2009-05-15 | 2013-03-20 | 新奥新能(北京)科技有限公司 | Method for producing two-stage dimethyl ether |
| CN101712595B (en) * | 2009-10-15 | 2013-08-21 | 云南瑞升烟草技术（集团）有限公司 | Method for preparing high-purity dimethyl ether free from extraneous odour |
| CN102666460A (en) * | 2009-11-17 | 2012-09-12 | 鲁奇有限责任公司 | Manufacture of dimethyl ether from crude methanol |
| CN101851152A (en) * | 2010-05-07 | 2010-10-06 | 山东清大新能源有限公司 | Method for preparing dimethyl ether by methyl alcohol gaseous phase dehydration |
| CN102010301A (en) * | 2010-11-02 | 2011-04-13 | 东莞市九丰化工有限公司 | Low-energy-consumption process for producing dimethyl ether and production equipment thereof |
| CN102225889A (en) * | 2011-05-17 | 2011-10-26 | 神华宁夏煤业集团有限责任公司 | Method for preparing dimethyl ether by dehydration of methanol |
| CN102225889B (en) * | 2011-05-17 | 2013-04-03 | 神华宁夏煤业集团有限责任公司 | Method for preparing dimethyl ether by dehydration of methanol |
| CN103012076A (en) * | 2012-12-24 | 2013-04-03 | 新奥科技发展有限公司 | Method and device of rectifying dimethyl ether and recovering dimethyl ether from non-condensable gas |
| CN103480161A (en) * | 2013-03-26 | 2014-01-01 | 新能(张家港)能源有限公司 | Control apparatus for methanol recovery tower reboiler |
| CN103508855A (en) * | 2013-03-26 | 2014-01-15 | 新能(张家港)能源有限公司 | Device and method for preparing dimethyl ether |
| CN104151145A (en) * | 2013-12-10 | 2014-11-19 | 中国平煤神马集团蓝天化工股份有限公司遂平化工厂 | Production method for dimethyl ether |
| CN104151145B (en) * | 2013-12-10 | 2016-01-20 | 中国平煤神马集团蓝天化工股份有限公司遂平化工厂 | A kind of dimethyl ether production method |
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| CN112358408A (en) * | 2020-11-30 | 2021-02-12 | 江苏凯美普瑞工程技术有限公司 | Production process and device of glycine |
| CN115321486A (en) * | 2022-07-23 | 2022-11-11 | 四川红华实业有限公司 | Electronic grade chlorine trifluoride purification method |
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Assignee: Hangzhou Kai Kai high efficiency energy saving Technology Co., Ltd. Assignor: Shen Jianchong Contract record no.: 2010330002082 Denomination of invention: Preparation method for dimethyl ether Granted publication date: 20091209 License type: Exclusive License Open date: 20080220 Record date: 20101021 |
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Address after: 310000, Hangzhou, Zhejiang province Binjiang District Jiangling road 567, New Oriental International Science and technology center, 18 South Patentee after: Shen Jianchong Address before: Hangzhou City, Zhejiang province 310009 Shangcheng District Jiangcheng Road No. 887 building, room 906 West Bank Patentee before: Shen Jianchong |