CN202730040U - Device for producing dimethyl ether - Google Patents
Device for producing dimethyl ether Download PDFInfo
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- CN202730040U CN202730040U CN 201220426187 CN201220426187U CN202730040U CN 202730040 U CN202730040 U CN 202730040U CN 201220426187 CN201220426187 CN 201220426187 CN 201220426187 U CN201220426187 U CN 201220426187U CN 202730040 U CN202730040 U CN 202730040U
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Abstract
The utility model discloses a device for producing dimethyl ether. The device comprises a raw material tank (1), and is characterized in that the raw material tank (1) is connected into a reaction kettle (2) through a pipeline, the reaction kettle (2) is connected with a condenser (3) through a pipeline, the condenser (3) is connected with a receiving kettle (4), the condenser (3) and the receiving kettle (4) are led to the reaction kettle (2) through reflux pipelines, and the reaction kettle (2) is sequentially connected with a concentrator (5), an alkaline washing tank (6), a water washing tank (7), a water absorbing layer (8), a water-gas separation dryer (9), a compressor (10), an oil-gas separation tank (11), a cooler (12), a pressure stabilizing cylinder (13) and a storage tank (14) through pipelines. Compared with a traditional device in a gas-phase reaction process, the device has the advantages of simple process, easiness in operation and maintenance, high conversion efficiency, good quality, less investment, rapidity in effectiveness and the like.
Description
Technical field
The utility model relates to the production equipment of industrial chemicals, refers to especially a kind of device of producing dme.
Background technology
In recent years, owing to containing a large amount of uses of fluorinated refrigerant, aerosol and propelling agent, so that atmospheric ozone layer is seriously damaged, ultraviolet radiation is aggravated, and " Greenhouse effect " of Global warming are threatening human healthy and existence.Therefore, the united nations environment protective tissue once sent out an urgent appeal: banned use of in the past by 2000 to contain fluorinated refrigerant.Europe, the United States, day etc. third generation refrigeration agent will be set about developing by state from 1998.China the Ministry of Chemical Industry also requires the cfc refrigeration agent of stopping using as scheduled recently, makes great efforts exploitation and substitutes articles for use.In view of this, the development of alternative chlorofluoro carbon and Application and Development are promising.At present, for meeting the surrogate aerosol requirement, that can substitute cfc just among affiliated unit of the Ministry of Chemical Industry conducts a research and manufactures experimently, and first-elected dme is preferred refrigerant.
Traditional dme production equipment is that to utilize be with gas phase building-up reactions method: namely methanol steam is under the pressure of 350 40CTC and 1.4709Mpa, and the effect by the aluminum phosphate solid catalyst makes through gas-phase dehydration again.Heating temperature is high, large, the shortcomings such as reaction is unstable, low conversion rate, production cost height of exerting pressure but this production equipment exists.
Summary of the invention
Problem to be solved in the utility model provides that a kind of Heating temperature is lower, pressure is not high, reacting balance, transformation efficiency is high, cost is low dme production equipment.
The utility model is that the technical solution problem is achieved through the following technical solutions:
A kind of device of producing dme, comprise liquid methanol head tank (1) is housed, head tank (1) is passed through in the pipeline ligation still (2), reactor (2) connects condenser (3) by pipeline, condenser (3) is accepted still (4), condenser (3) and accept still (4) and have reflux line to lead to reactor (2), in the reactor (2) not the liquid methanol of complete reaction by condenser (3) with accept still (4) and reflux; Described reactor (2) connects thickner (5), caustic treater (6), water washing tank (7), water accepting layer (8), aqueous vapor separate dryer (9), compressor (10), catch pot (11), water cooler (12), voltage stabilizing cylinder (13), hold-up vessel (14) by pipeline successively, and the cationic fluid catalyzer in the reactor (2) is multilayered structure.
The utility model comprises head tank, head tank is passed through in the pipeline ligation still, reactor connects condenser by pipeline, condenser is accepted still, condenser and accept still and have reflux line to lead to reactor, described reactor connects thickner, caustic treater, water washing tank, water accepting layer, aqueous vapor separate dryer, compressor, catch pot, water cooler, voltage stabilizing cylinder, hold-up vessel by pipeline successively.
The device of described production dme, described reactor is provided with well heater and voltate regulator.Catalyzer in the reactor needs optimum temps, and optimum pressure, therefore be provided with well heater and voltate regulator, guarantees the maximum catalytic effect of catalyzer.
The device of described production dme, described condenser and water cooler are the cold water circulating cooling pipe.The general cold water circulating cooling pipe of selecting in principle, under the same conditions, guarantees that the refrigerating unit of equal cooling performance can.
The device of described production dme.In the process of dry dme, the process that has a large amount of water vapors to produce, general drying installation is not suitable for the drying of a large amount of water vapors, therefore select the absorbent drying layer, can absorb in a large number water vapour, in principle, under equal conditions, the device that guarantees certain drying effect all can be selected.
Compared with prior art, the beneficial effects of the utility model are:
(1) the cationic fluid catalyzer in the reactor is multilayered structure in the utility model, and can be in reaction process required Heating temperature is lower, exerts pressure not high, reacts gentle stable, and less energy consumption is easy to control.
(2) owing to having adopted the cationic fluid catalyzer, thereby less investment, simple process is easily gone, the most outstanding advantage is: the regeneration of catalyzer and reaction (production) process is synchronous, therefore not only need not to increase step for regeneration and equipment, and can greatly improve quality, the quantity of product and reduce cost.
(3) prior art is to adopt " Gu gas------gas " operational path: methanol steam and solid catalyst surface contact area are limited, thereby low conversion rate, and gas of dimethyl ether and reaction gas (synthetic gas) are difficult for separating-purifying; The present invention adopts " liquid---liquid---gas " operational path, and methanol molecules contacts fully with catalyst molecule, thereby transformation efficiency is high, and gas of dimethyl ether very easily breaks away from liquid phase, thereby is easy to separating-purifying.
When (four) gas of dimethyl ether breaks away from liquid phase, also very easily reclaim even carry the unreacted methanol steam of minute quantity, reduced material consumption, reduced production cost.
Description of drawings
Fig. 1 is the apparatus structure schematic diagram that the utility model is produced dme.
Corresponding Reference numeral is in the accompanying drawing: 1. head tank, and 2. reactor, 3. condenser is 4. accepted still, 5. compressor, 6. caustic treater, 7. water washing tank, 8. water accepting layer, 9. aqueous vapor separate dryer, 10. compressor, 11. catch pot, 12. water coolers, 13. voltage stabilizing cylinders, 14. hold-up vessels.
Embodiment
The utility model is described in further detail below in conjunction with embodiment, but embodiment of the present utility model is not limited to this.
Embodiment:
The utility model comprises head tank 1, head tank 1 is passed through in the pipeline ligation still 2, reactor 2 connects condenser 3 by pipeline, condenser 3 is accepted still 4, condenser 3 and accept still 4 and have reflux line to lead to reactor 2, described reactor 2 connects thickner 5, caustic treater 6, water washing tank 7, water accepting layer 8, aqueous vapor separate dryer 9, compressor 10, catch pot 11, water cooler 12, voltage stabilizing cylinder 13, hold-up vessel 14 by pipeline successively.
The device of the described production dme of the present embodiment, reactor 2 is provided with well heater and voltate regulator.
The device of the described production dme of the present embodiment, condenser 3 and water cooler 12 are circulating cooling pipe.
The device of the described production dme of the present embodiment, the absorbent drying layer in the water accepting layer 8.
Principle of work of the present utility model is: liquid methanol is at lesser temps: react the esterification dehydration under 100 to 125 ℃ and normal pressure 0 0.50Mpa gauge pressure and the cationic fluid catalyst action and can produce gas of dimethyl ether, separate drying, compression, gas-oil separation, cooling, voltage stabilizing through condensation, alkali cleaning, washing, aqueous vapor, namely get dme liquid, its chemical equation is:
2CH
3OH→CH
30CH
3+H
20
In the following formula, CH
3OH: methyl alcohol, CH
3OCH
3: dme.
Its reaction characteristics: the regeneration of catalyzer and reaction (production) process is synchronous, has namely just finished the regeneration of catalyzer in aerogenesis, has realized the serialization of production process.
Claims (3)
1. device of producing dme, comprise liquid methanol head tank (1) is housed, head tank (1) is passed through in the pipeline ligation still (2), reactor (2) connects condenser (3) by pipeline, condenser (3) is accepted still (4), condenser (3) and accept still (4) and have reflux line to lead to reactor (2), in the reactor (2) not the liquid methanol of complete reaction by condenser (3) with accept still (4) and reflux; Described reactor (2) connects thickner (5), caustic treater (6), water washing tank (7), water accepting layer (8), aqueous vapor separate dryer (9), compressor (10), catch pot (11), water cooler (12), voltage stabilizing cylinder (13), hold-up vessel (14) by pipeline successively, and it is characterized in that: the cationic fluid catalyzer in the reactor (2) is multilayered structure.
2. the device of production dme according to claim 1, it is characterized in that: described reactor (2) is provided with well heater and voltate regulator.
3. the device of production dme according to claim 1, it is characterized in that: described condenser (3) and water cooler (12) are circulating cooling pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220426187 CN202730040U (en) | 2012-08-27 | 2012-08-27 | Device for producing dimethyl ether |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220426187 CN202730040U (en) | 2012-08-27 | 2012-08-27 | Device for producing dimethyl ether |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202730040U true CN202730040U (en) | 2013-02-13 |
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ID=47655759
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220426187 Expired - Fee Related CN202730040U (en) | 2012-08-27 | 2012-08-27 | Device for producing dimethyl ether |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202730040U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104926620A (en) * | 2015-05-15 | 2015-09-23 | 四川东晨燃气有限公司 | Dimethyl ether production system |
-
2012
- 2012-08-27 CN CN 201220426187 patent/CN202730040U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104926620A (en) * | 2015-05-15 | 2015-09-23 | 四川东晨燃气有限公司 | Dimethyl ether production system |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130213 Termination date: 20130827 |