CN202063851U - Device for preparing dimethyl ether through catalytic dehydration of gas-phase methanol - Google Patents
Device for preparing dimethyl ether through catalytic dehydration of gas-phase methanol Download PDFInfo
- Publication number
- CN202063851U CN202063851U CN2011201084379U CN201120108437U CN202063851U CN 202063851 U CN202063851 U CN 202063851U CN 2011201084379 U CN2011201084379 U CN 2011201084379U CN 201120108437 U CN201120108437 U CN 201120108437U CN 202063851 U CN202063851 U CN 202063851U
- Authority
- CN
- China
- Prior art keywords
- communicated
- tower
- rectifying tower
- shell side
- outlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a device for preparing dimethyl ether through the catalytic dehydration of gas-phase methanol. The device consists of a starting heater, a gas heat exchanger, a reactor, a vaporizing tower, a vaporizing tower reboiler, a methanol preheater, a crude methyl ether preheater, a crude methyl ether condenser, a crude methyl ether storage tank, a washing tower, a rectifying tower condenser, a return tank, kettle liquid storage tank, a rectifying tower, a rectifying tower reboiler, a gas cooler and an absorption liquid condenser; and the device for preparing the dimethyl ether through the catalytic dehydration of the gas-phase methanol is additionally provided with a secondary reboiler of the vaporizing tower. Compared with the prior art, in the device, reaction heat produced in the reaction can be sufficiently used, and heat supplied from the outside is reduced, thereby achieving the purposes of saving energy, reducing preparation cost and increasing economic benefit.
Description
Technical field
The utility model relates to a kind of methanol vapor phase catalytic dehydration preparing dimethy ether device, especially a kind ofly can make full use of reaction heat, reduces the external heat source supply, fuel economy, the methanol vapor phase catalytic dehydration preparing dimethy ether device that reduces production costs.
Background technology
The thick methyl ether gas that comes out through reactor in the methanol vapor phase catalytic dehydration preparing dimethy ether device is through after the condensation at present, enter thick methyl ether storage tank, get through thick methyl ether preheater by pump again, squeeze into the rectifying tower middle part, adopt outside heat to give the heating of rectifying tower reboiler in rectifier bottoms, in this process, both strengthen the consumption of outside heat, increased the consumption of water coolant simultaneously again.Therefore, designing and a kind ofly can make full use of reaction heat, reduce the external heat source supply, fuel economy, the methanol vapor phase catalytic dehydration preparing dimethy ether device that reduces production costs, is the present technical issues that need to address.
Summary of the invention
Technical problem to be solved in the utility model provides a kind ofly can make full use of reaction heat, reduce the external heat source supply, fuel economy, the methanol vapor phase catalytic dehydration preparing dimethy ether device that reduces production costs.
First technical scheme that the utility model solves its technical problem is:
Methanol vapor phase catalytic dehydration preparing dimethy ether device, by the well heater that goes into operation, gas heat exchanger, reactor, the vaporization tower, vaporization tower reboiler, methanol preheater, thick methyl ether preheater, thick methyl ether condenser, thick methyl ether basin, washing tower, the rectifying tower condenser, return tank, still liquid basin, rectifying tower, the rectifying tower reboiler, gas cooler and absorption liquid condenser are formed, the shell side import of methanol preheater is communicated with external methanol pipeline, the shell side outlet of methanol preheater is communicated with the import on vaporization tower top, the top exit of vaporization tower is communicated with the shell side import of gas heat exchanger, the tube side outlet of gas heat exchanger is communicated with the tube side import of methanol preheater and the bottom of reactor simultaneously, the bottom of reactor is communicated with the tube side import of gas heat exchanger simultaneously, the shell side outlet of gas heat exchanger is communicated with the tube side import and the Reactor inlet of the well heater that goes into operation simultaneously, the tube side outlet of well heater of going into operation is communicated with the top of reactor, the bottom of vaporization tower is communicated with the tube side import of vaporization tower reboiler and the waste water stripper pipeline that degass simultaneously, the shell side import of vaporization tower reboiler is communicated with the external heat source pipeline, the tube side outlet of vaporization tower reboiler is communicated with the middle and lower part of vaporization tower, the middle and upper part of vaporization tower is communicated with still liquid basin by the still liquid pump, be communicated with the shell side import of absorption liquid condenser by Y-tube being communicated with on the pipeline of vaporization tower and still liquid pump, the shell side outlet of absorption liquid condenser is communicated with the top of washing tower, the bottom of washing tower is communicated with the bottom of thick methyl ether basin, the top of washing tower is provided with the non-condensable gas pipeline, the outlet of thick methyl ether basin top is communicated with the middle part of washing tower by the shell side of gas cooler, thick methyl ether basin is communicated with by the shell side import of thick methyl ether pump with thick methyl ether preheater, the shell side outlet of thick methyl ether preheater is communicated with the rectifying tower middle part, the tube side import of thick methyl ether preheater is communicated with the outlet of the tube side of methanol preheater, the shell side outlet of rectifying tower condenser is communicated with the top inlet of return tank, the bottom of return tank is simultaneously adopted pipe outward with the upper inlet of rectifying tower and dme by the dme pump and is communicated with, the top exit of rectifying tower is communicated with the shell side import of rectifying tower condenser, the middle and lower part of rectifying tower is communicated with the tube side outlet of rectifying tower reboiler, the bottom of rectifying tower is communicated with the tube side import of rectifying tower reboiler, the shell side import of rectifying tower reboiler is communicated with the external heat source pipeline, the outlet at bottom of rectifying tower is communicated with still liquid basin, the bottom of rectifying tower has up and down, and two pipelines are communicated with still liquid basin, one of its middle and upper part is the gas-liquid equilibrium pipe, one of the bottom is the liquid phase upflow tube, the shell side top outlet of rectifying tower condenser is communicated with the outlet at return tank top, connecting pipe between the outlet at the outlet of the shell side top of rectifying tower condenser and return tank top exports with methyl ether basin top slightly and the connecting tube of gas housing of cooler journey import is communicated with, pipeline between the shell side outlet at bottom of gas cooler and washing tower and the thick methyl ether basin is communicated with, there is the fusel extraction pipeline of three parallel connections the middle and lower part of vaporization tower, methanol vapor phase catalytic dehydration preparing dimethy ether device has been set up the secondary reboiler of vaporization tower, connecting pipe between the tube side import of the tube side import of the secondary reboiler of vaporization tower and the bottom of vaporization tower and the tower reboiler of vaporizing is communicated with, the tube side outlet of the secondary reboiler of vaporization tower is communicated with the middle and lower part of vaporization tower, the shell side import of the secondary reboiler of vaporization tower is communicated with the outlet at bottom of reactor, the shell side outlet of the secondary reboiler of vaporization tower export with the tube side of gas heat exchanger and the tube side import of methanol preheater between connecting pipe be communicated with, to be communicated with the vaporization tower simultaneously is communicated with thick methyl ether basin with the pipeline of still liquid pump, the middle and lower part of rectifying tower is connected with the tube side outlet of thick methyl ether preheater, the shell side import of thick methyl ether condenser is communicated with the import of rectifying tower condenser shell side, the connecting pipe of the shell side import of the top exit of rectifying tower and thick methyl ether condenser and the shell side import of rectifying tower condenser is connected, the shell side outlet of thick methyl ether condenser is communicated with the back with the shell side outlet of rectifying tower condenser and is connected with the inlet pipeline of return tank, the top of return tank is communicated with connecting pipe between thick methyl ether tank top outlet and the import of gas housing of cooler journey, and the shell side top outlet of thick methyl ether condenser exports with the shell side top of rectifying tower condenser and is communicated with.
The preferred version that the utility model solves first technical scheme of its technical problem is:
Methanol vapor phase catalytic dehydration preparing dimethy ether device has also been set up the secondary reboiler of rectifying tower, the tube side outlet of the secondary reboiler of rectifying tower is communicated with the middle and lower part of rectifying tower, the tube side import of the secondary reboiler of rectifying tower is communicated with the bottom of rectifying tower and the connecting pipe between the import of rectifying tower reboiler tube side, the shell side outlet and the waste water of the secondary reboiler of the rectifying tower stripper pipeline that degass is communicated with, and the connecting pipe between the tube side import of the shell side import of the secondary reboiler of rectifying tower and the bottom of the tower of vaporizing and the tower reboiler of vaporizing is communicated with.
Second technical scheme that the utility model solves its technical problem is:
Methanol vapor phase catalytic dehydration preparing dimethy ether device, by the well heater that goes into operation, gas heat exchanger, reactor, the vaporization tower, vaporization tower reboiler, methanol preheater, thick methyl ether preheater, thick methyl ether condenser, thick methyl ether basin, washing tower, the rectifying tower condenser, return tank, still liquid basin, rectifying tower, the rectifying tower reboiler, gas cooler and absorption liquid condenser are formed, the shell side import of methanol preheater is communicated with external methanol pipeline, the shell side outlet of methanol preheater is communicated with the import on vaporization tower top, the top exit of vaporization tower is communicated with the shell side import of gas heat exchanger, the tube side outlet of gas heat exchanger is communicated with the tube side import of methanol preheater and the bottom of reactor simultaneously, the bottom of reactor is communicated with the tube side import of gas heat exchanger simultaneously, the shell side outlet of gas heat exchanger is communicated with the tube side import and the Reactor inlet of the well heater that goes into operation simultaneously, the tube side outlet of well heater of going into operation is communicated with the top of reactor, the bottom of vaporization tower is communicated with the tube side import of vaporization tower reboiler and the waste water stripper pipeline that degass simultaneously, the shell side import of vaporization tower reboiler is communicated with the external heat source pipeline, the tube side outlet of vaporization tower reboiler is communicated with the middle and lower part of vaporization tower, the middle and upper part of vaporization tower is communicated with still liquid basin by the still liquid pump, be communicated with the shell side import of absorption liquid condenser by Y-tube being communicated with on the pipeline of vaporization tower and still liquid pump, the shell side outlet of absorption liquid condenser is communicated with the top of washing tower, the bottom of washing tower is communicated with the bottom of thick methyl ether basin, the top of washing tower is provided with the non-condensable gas pipeline, the outlet of thick methyl ether basin top is communicated with the middle part of washing tower by the shell side of gas cooler, thick methyl ether basin is communicated with by the shell side import of thick methyl ether pump with thick methyl ether preheater, the shell side outlet of thick methyl ether preheater is communicated with the rectifying tower middle part, the tube side import of thick methyl ether preheater is communicated with the outlet of the tube side of methanol preheater, the shell side outlet of rectifying tower condenser is communicated with the top inlet of return tank, the bottom of return tank is simultaneously adopted pipe outward with the upper inlet of rectifying tower and dme by the dme pump and is communicated with, the top exit of rectifying tower is communicated with the shell side import of rectifying tower condenser, the middle and lower part of rectifying tower is communicated with the tube side outlet of rectifying tower reboiler, the bottom of rectifying tower is communicated with the tube side import of rectifying tower reboiler, the shell side import of rectifying tower reboiler is communicated with the external heat source pipeline, the outlet at bottom of rectifying tower is communicated with still liquid basin, the bottom of rectifying tower has up and down, and two pipelines are communicated with still liquid basin, one of its middle and upper part is the gas-liquid equilibrium pipe, one of the bottom is the liquid phase upflow tube, the shell side top outlet of rectifying tower condenser is communicated with the outlet at return tank top, connecting pipe between the outlet at the outlet of the shell side top of rectifying tower condenser and return tank top exports with methyl ether basin top slightly and the connecting tube of gas housing of cooler journey import is communicated with, pipeline between the shell side outlet at bottom of gas cooler and washing tower and the thick methyl ether basin is communicated with, there is the fusel extraction pipeline of three parallel connections the middle and lower part of vaporization tower, methanol vapor phase catalytic dehydration preparing dimethy ether device has been set up the secondary reboiler of vaporization tower, connecting pipe between the tube side import of the tube side import of the secondary reboiler of vaporization tower and the bottom of vaporization tower and the tower reboiler of vaporizing is communicated with, the tube side outlet of the secondary reboiler of vaporization tower is communicated with the middle and lower part of vaporization tower, the shell side import of the secondary reboiler of vaporization tower is communicated with the outlet at bottom of reactor, the shell side outlet of the secondary reboiler of vaporization tower export with the tube side of gas heat exchanger and the tube side import of methanol preheater between connecting pipe be communicated with, to be communicated with the vaporization tower simultaneously is communicated with thick methyl ether basin with the pipeline of still liquid pump, the middle and lower part of rectifying tower is connected with the tube side outlet of thick methyl ether preheater, the top exit of rectifying tower is communicated with the import of rectifying tower condenser shell side, the shell side outlet of rectifying tower condenser is communicated with the shell side import of thick methyl ether condenser, the inlet pipeline of the shell side outlet return tank of thick methyl ether condenser connects, the top of return tank is communicated with connecting pipe between thick methyl ether tank top outlet and the import of gas housing of cooler journey, and the shell side top outlet of thick methyl ether condenser exports with the shell side top of rectifying tower condenser and is communicated with.
The preferred version that the utility model solves second technical scheme of its technical problem is:
Methanol vapor phase catalytic dehydration preparing dimethy ether device has also been set up the secondary reboiler of rectifying tower, the tube side outlet of the secondary reboiler of rectifying tower is communicated with the middle and lower part of rectifying tower, the tube side import of the secondary reboiler of rectifying tower is communicated with the bottom of rectifying tower and the connecting pipe between the import of rectifying tower reboiler tube side, the shell side outlet and the waste water of the secondary reboiler of the rectifying tower stripper pipeline that degass is communicated with, and the connecting pipe between the tube side import of the shell side import of the secondary reboiler of rectifying tower and the bottom of the tower of vaporizing and the tower reboiler of vaporizing is communicated with.
The technical process of prior-art devices is: external methyl alcohol → methanol preheater → vaporization tower top, in vaporization tower reboiler, vaporization tower bottom still liquid is added thermal distillation with external heat source, processing wastewater after the distillation removes stripping tower, methanol gas → gas heat exchanger heating (using the well heater that goes into operation between the under-stream period) → reactor that comes out from the vaporization top of tower carries out catalyzed reaction, (the thick methyl ether gas after the part pyroreaction was without gas heat exchanger after reacted thick methyl ether gas entered gas heat exchanger and methanol gas heat exchange, directly mix from bypass with the thick methyl ether gas that gas heat exchanger comes out) → methanol preheater → thick methyl ether preheater → thick methyl ether condenser → thick methyl ether basin, thick methyl ether in the thick methyl ether basin is squeezed into → thick methyl ether preheater → rectifying tower middle part (profit reduction and reserving section top) by pump, rectifier bottoms liquid heats by external heat source through the rectifying tower reboiler, gas of dimethyl ether is from rectifying tower top → rectifying tower condenser → return tank, then squeezing into the rectifying tower top with reflux pump refluxes, control quality product, the product jar is squeezed in qualified dme product extraction.Rectifier bottoms still liquid is after distillation, mainly be water and methyl alcohol, still liquid basin is gone in overflow, and also have a gas-liquid equilibrium pipe to communicate between rectifying tower and the still liquid basin, squeeze into the vaporization tower by still liquid pump part still liquid, another part advances washing tower and goes in the washing system through the cooled noncondensable gas of gas cooler after the cooling of absorption liquid water cooler, noncondensable gas goes the boiler house use that acts as a fuel, and the washing tower bottoms returns thick methyl ether basin; And the processing wastewater of vaporization tower bottom still liquid after vaporization tower reboiler is by the external heat source heating directly goes stripping tower further to extract methyl alcohol in the waste water, and qualified waste water advances sewage works.The outlet of rectifying tower condenser shell side top is communicated with the back and inserts on the connecting tube of outlet of thick methyl ether basin top and gas cooler (20) shell side import with the return tank top exit, the gas cooler outlet at bottom is connected to washing tower to the pipeline of thick methyl ether basin, and there is the fusel extraction pipeline of three parallel connections the middle and lower part of vaporization tower.
Technical process of the present utility model is: methyl alcohol → methanol preheater → vaporization tower top that outer tube comes, vaporization tower bottom still liquid is outside former technology use vaporization tower reboiler is heated by external heat source, after the ordinary production, the pyroreaction gas that can utilize reactor to come out heats simultaneously to the secondary reboiler of vaporization tower, reduce vaporization tower reboiler external heat source consumption like this, reduce energy consumption.(the thick methyl ether gas after the part pyroreaction is without gas heat exchanger after the methanol gas that the vaporization top of tower comes out → gas heat exchanger heating (using the well heater that goes into operation between under-stream period) → reactor → gas heat exchanger and the methanol gas heat exchange, after the secondary reboiler heating of the tower that directly goes the to vaporize vaporization tower bottoms, mix with the thick methyl ether gas that gas heat exchanger comes out) → (thick methyl ether preheater is only as a passage in this reforming technology for methanol preheater → thick methyl ether preheater, generally not with thick methyl ether heat exchange), after directly enter rectifying tower (17) middle and lower part (carrying pars infrasegmentalis layer 2-3 column plate from rectifying tower enters).The gas of dimethyl ether that comes out from rectifying tower (17) top cools off through former rectifying tower condenser of serial or parallel connection and thick methyl ether condenser, enters return tank then, and is refluxed by reflux pump by return tank, the qualified product extraction.The outlet of rectifying tower condenser shell side top is communicated with the back and inserts on the connecting tube of outlet of thick methyl ether basin top and the import of gas cooler shell side with the return tank top exit, the gas cooler outlet at bottom is connected to washing tower to the pipeline of thick methyl ether basin, and there is the fusel extraction pipeline of three parallel connections the middle and lower part of vaporization tower.
Still liquid basin is gone in the overflow after retaining a percentage of the total profits for the enterprise's own use of rectifying tower bottoms, and there is a gas-liquid equilibrium pipe to communicate between rectifying tower and the still liquid basin, the rectifying tower bottoms is squeezed into the vaporization tower through a still liquid pump part, after another part still liquid cools off through the absorption liquid water cooler, remove washing tower washing noncondensable gas, contain dme liquid after the washing, flow into thick methyl ether basin, be communicated with a pipeline between still liquid pump outlet conduit and the thick methyl ether storage tank, having an accident is that still liquid can directly be squeezed into thick methyl ether storage tank, and according to thick methyl ether basin liquid level, through thick methyl ether preheater, progressively squeeze into the rectifying tower middle part, carry out rectifying.
Rectifying tower is set up the secondary reboiler of a rectifying tower, utilize vaporization tower bottom waste water to give the heating of the secondary reboiler still of rectifying tower liquid, use the rectifying tower reboiler during driving, by the external heat source heat supply, use the secondary reboiler heat supply of rectifying tower after the ordinary production, reach further energy-saving effect, also can set up the secondary reboiler of rectifying tower, directly use the rectifying tower reboiler by the external heat source heat supply.
A bigger blow-down pipe is set up at the return tank top again, directly introduces the gas cooler inlet and is responsible for, and the thick methyl ether condenser of the gas-liquid equilibrium Guan Zaiyu that return tank is connected with the rectifying tower condenser connects a gas-liquid equilibrium pipe simultaneously, forms complete system.The gas cooler outlet at bottom is connected to washing tower to the pipeline of thick methyl ether basin.
Noncondensable gas in the system goes boiler house fuel use as a supplement after the washing tower washing, vaporization tower bottom waste liquid removes stripping tower, and is all identical with former technology.
Compared with prior art, the utility model can make full use of the reaction heat that the reaction back produces, and reduces the outside heat of supplying with, and to reach energy-saving effect, reduces cost of manufacture, increases the purpose of economic benefit.
Description of drawings
Fig. 1 is the system diagram of the utility model first scheme.
Fig. 2 is the system diagram of the utility model alternative plan.
Fig. 3 is prior art systems figure.
Embodiment
As shown in Figure 1, methanol vapor phase catalytic dehydration preparing dimethy ether device, by the well heater 1 that goes into operation, gas heat exchanger 2, reactor 3, vaporization tower 5, vaporization tower reboiler 6, methanol preheater 7, thick methyl ether preheater 8, thick methyl ether condenser 10, thick methyl ether basin 11, washing tower 12, rectifying tower condenser 13, return tank 14, still liquid basin 15, rectifying tower 17, rectifying tower reboiler 16, gas cooler 20 and absorption liquid condenser 9 are formed, the shell side import of methanol preheater 7 is communicated with external methanol pipeline, the shell side outlet of methanol preheater 7 is communicated with the import on vaporization tower 5 tops, the top exit of vaporization tower 5 is communicated with the shell side import of gas heat exchanger 2, the tube side outlet of gas heat exchanger 2 is communicated with the tube side import of methanol preheater 7 and the bottom of reactor 3 simultaneously, the bottom of reactor 3 is communicated with the tube side import of gas heat exchanger 2 simultaneously, the shell side outlet of gas heat exchanger 2 is communicated with the tube side import and the Reactor inlet of the well heater 1 that goes into operation simultaneously, the tube side outlet of well heater 1 of going into operation is communicated with the top of reactor 3, the bottom of vaporization tower 5 is communicated with the tube side import of vaporization tower reboiler 6 and the waste water stripper pipeline that degass simultaneously, the shell side import of vaporization tower reboiler 6 is communicated with the external heat source pipeline, the tube side outlet of vaporization tower reboiler 6 is communicated with the middle and lower part of vaporization tower 5, the middle and upper part of vaporization tower 5 is communicated with still liquid basin 15 by still liquid pump 18, be communicated with the shell side import of absorption liquid condenser 9 by Y-tube being communicated with on the pipeline of vaporization tower 5 and still liquid pump 18, the shell side outlet of absorption liquid condenser 9 is communicated with the top of washing tower 12, the bottom of washing tower 12 is communicated with the bottom of thick methyl ether basin 11, the top of washing tower 12 is provided with the non-condensable gas pipeline, the outlet of thick methyl ether basin 11 tops is communicated with the middle part of washing tower 12 by the shell side of gas cooler 20, thick methyl ether basin 11 is communicated with by the shell side import of thick methyl ether pump 4 with thick methyl ether preheater 8, the shell side outlet of thick methyl ether preheater 8 is communicated with rectifying tower 17 middle parts, the tube side import of thick methyl ether preheater 8 is communicated with the outlet of the tube side of methanol preheater 7, the shell side outlet of rectifying tower condenser 13 is communicated with the top inlet of return tank 14, the bottom of return tank 14 is adopted pipe outward with the upper inlet of rectifying tower 17 and dme simultaneously by dme pump 19 and is communicated with, the top exit of rectifying tower 17 is communicated with the shell side import of rectifying tower condenser 13, the middle and lower part of rectifying tower 17 is communicated with the tube side outlet of rectifying tower reboiler 16, the bottom of rectifying tower 17 is communicated with the tube side import of rectifying tower reboiler 16, the shell side import of rectifying tower reboiler 16 is communicated with the external heat source pipeline, the outlet at bottom of rectifying tower 17 is communicated with still liquid basin 15, the bottom of rectifying tower 17 has up and down, and two pipelines are communicated with still liquid basin 15, one of its middle and upper part is the gas-liquid equilibrium pipe, one of the bottom is the liquid phase upflow tube, the shell side top outlet of rectifying tower condenser 13 is communicated with the outlet at return tank 14 tops, connecting pipe between the outlet at the outlet of the shell side top of rectifying tower condenser 13 and return tank 14 tops exports with methyl ether basin 11 tops slightly and the connecting tube of gas cooler 20 shell side imports is communicated with, pipeline between the shell side outlet at bottom of gas cooler 20 and washing tower 12 and the thick methyl ether basin 11 is communicated with, there is the fusel extraction pipeline of three parallel connections the middle and lower part of vaporization tower 5, methanol vapor phase catalytic dehydration preparing dimethy ether device has been set up the secondary reboiler 22 of vaporization tower, connecting pipe between the tube side import of the tube side import of the secondary reboiler 22 of vaporization tower and the bottom of vaporization tower 5 and the tower reboiler 6 of vaporizing is communicated with, the tube side outlet of the secondary reboiler 22 of vaporization tower is communicated with the middle and lower part of vaporization tower 5, the shell side import of the secondary reboiler 22 of vaporization tower is communicated with the outlet at bottom of reactor 3, the shell side outlet of the secondary reboiler 22 of vaporization tower export with the tube side of gas heat exchanger 2 and the tube side import of methanol preheater 7 between connecting pipe be communicated with, to be communicated with vaporization tower 5 simultaneously is communicated with thick methyl ether basin 11 with the pipeline of still liquid pump 18, the middle and lower part of rectifying tower 17 is connected with the tube side outlet of thick methyl ether preheater 8, the shell side import of thick methyl ether condenser 10 is communicated with the 13 shell side imports of rectifying tower condenser, the connecting pipe of the shell side import of the top exit of rectifying tower 17 and thick methyl ether condenser 10 and the shell side import of rectifying tower condenser 13 is connected, the shell side outlet of thick methyl ether condenser 10 is communicated with the back with the shell side outlet of rectifying tower condenser 13 and is connected with the inlet pipeline of return tank 14, the top of return tank 14 is communicated with connecting pipe between thick methyl ether basin 11 top exits and the gas cooler 20 shell side imports, and the shell side top outlet of thick methyl ether condenser 10 exports with the shell side top of rectifying tower condenser 13 and is communicated with.
Methanol vapor phase catalytic dehydration preparing dimethy ether device has also been set up the secondary reboiler 21 of rectifying tower, the tube side outlet of the secondary reboiler 21 of rectifying tower is communicated with the middle and lower part of rectifying tower 17, the tube side import of the secondary reboiler 21 of rectifying tower is communicated with the bottom of rectifying tower 17 and the connecting pipe between the 16 tube side imports of rectifying tower reboiler, the shell side outlet and the waste water of the secondary reboiler 21 of the rectifying tower stripper pipeline that degass is communicated with, and the connecting pipe between the tube side import of the shell side import of the secondary reboiler 21 of rectifying tower and the bottom of the tower 5 of vaporizing and the tower reboiler 6 of vaporizing is communicated with.
As shown in Figure 2, methanol vapor phase catalytic dehydration preparing dimethy ether device, by the well heater 1 that goes into operation, gas heat exchanger 2, reactor 3, vaporization tower 5, vaporization tower reboiler 6, methanol preheater 7, thick methyl ether preheater 8, thick methyl ether condenser 10, thick methyl ether basin 11, washing tower 12, rectifying tower condenser 13, return tank 14, still liquid basin 15, rectifying tower 17, rectifying tower reboiler 16, gas cooler 20 and absorption liquid condenser 9 are formed, the shell side import of methanol preheater 7 is communicated with external methanol pipeline, the shell side outlet of methanol preheater 7 is communicated with the import on vaporization tower 5 tops, the top exit of vaporization tower 5 is communicated with the shell side import of gas heat exchanger 2, the tube side outlet of gas heat exchanger 2 is communicated with the tube side import of methanol preheater 7 and the bottom of reactor 3 simultaneously, the bottom of reactor 3 is communicated with the tube side import of gas heat exchanger 2 simultaneously, the shell side outlet of gas heat exchanger 2 is communicated with the tube side import and the Reactor inlet of the well heater 1 that goes into operation simultaneously, the tube side outlet of well heater 1 of going into operation is communicated with the top of reactor 3, the bottom of vaporization tower 5 is communicated with the tube side import of vaporization tower reboiler 6 and the waste water stripper pipeline that degass simultaneously, the shell side import of vaporization tower reboiler 6 is communicated with the external heat source pipeline, the tube side outlet of vaporization tower reboiler 6 is communicated with the middle and lower part of vaporization tower 5, the middle and upper part of vaporization tower 5 is communicated with still liquid basin 15 by still liquid pump 18, be communicated with the shell side import of absorption liquid condenser 9 by Y-tube being communicated with on the pipeline of vaporization tower 5 and still liquid pump 18, the shell side outlet of absorption liquid condenser 9 is communicated with the top of washing tower 12, the bottom of washing tower 12 is communicated with the bottom of thick methyl ether basin 11, the top of washing tower 12 is provided with the non-condensable gas pipeline, the outlet of thick methyl ether basin 11 tops is communicated with the middle part of washing tower 12 by the shell side of gas cooler 20, thick methyl ether basin 11 is communicated with by the shell side import of thick methyl ether pump 4 with thick methyl ether preheater 8, the shell side outlet of thick methyl ether preheater 8 is communicated with rectifying tower 17 middle parts, the tube side import of thick methyl ether preheater 8 is communicated with the outlet of the tube side of methanol preheater 7, the shell side outlet of rectifying tower condenser 13 is communicated with the top inlet of return tank 14, the bottom of return tank 14 is adopted pipe outward with the upper inlet of rectifying tower 17 and dme simultaneously by dme pump 19 and is communicated with, the top exit of rectifying tower 17 is communicated with the shell side import of rectifying tower condenser 13, the middle and lower part of rectifying tower 17 is communicated with the tube side outlet of rectifying tower reboiler 16, the bottom of rectifying tower 17 is communicated with the tube side import of rectifying tower reboiler 16, the shell side import of rectifying tower reboiler 16 is communicated with the external heat source pipeline, the outlet at bottom of rectifying tower 17 is communicated with still liquid basin 15, the bottom of rectifying tower 17 has up and down, and two pipelines are communicated with still liquid basin 15, one of its middle and upper part is the gas-liquid equilibrium pipe, one of the bottom is the liquid phase upflow tube, the shell side top outlet of rectifying tower condenser 13 is communicated with the outlet at return tank 14 tops, connecting pipe between the outlet at the outlet of the shell side top of rectifying tower condenser 13 and return tank 14 tops exports with methyl ether basin 11 tops slightly and the connecting tube of gas cooler 20 shell side imports is communicated with, pipeline between the shell side outlet at bottom of gas cooler 20 and washing tower 12 and the thick methyl ether basin 11 is communicated with, there is the fusel extraction pipeline of three parallel connections the middle and lower part of vaporization tower 5, methanol vapor phase catalytic dehydration preparing dimethy ether device has been set up the secondary reboiler 22 of vaporization tower, connecting pipe between the tube side import of the tube side import of the secondary reboiler 22 of vaporization tower and the bottom of vaporization tower 5 and the tower reboiler 6 of vaporizing is communicated with, the tube side outlet of the secondary reboiler 22 of vaporization tower is communicated with the middle and lower part of vaporization tower 5, the shell side import of the secondary reboiler 22 of vaporization tower is communicated with the outlet at bottom of reactor 3, the shell side outlet of the secondary reboiler 22 of vaporization tower export with the tube side of gas heat exchanger 2 and the tube side import of methanol preheater 7 between connecting pipe be communicated with, to be communicated with vaporization tower 5 simultaneously is communicated with thick methyl ether basin 11 with the pipeline of still liquid pump 18, the middle and lower part of rectifying tower 17 is connected with the tube side outlet of thick methyl ether preheater 8, the top exit of rectifying tower 17 is communicated with the shell side import of rectifying tower condenser 13, the shell side outlet of rectifying tower condenser 13 is communicated with the shell side import of thick methyl ether condenser 10, the shell side outlet of thick methyl ether condenser 10 is connected with the inlet pipeline of return tank 14, the top of return tank 14 is communicated with connecting pipe between thick methyl ether basin 11 top exits and the gas cooler 20 shell side imports, and the shell side top outlet of thick methyl ether condenser 10 exports with the shell side top of rectifying tower condenser 13 and is communicated with.
Methanol vapor phase catalytic dehydration preparing dimethy ether device has also been set up the secondary reboiler 21 of rectifying tower, the tube side outlet of the secondary reboiler 21 of rectifying tower is communicated with the middle and lower part of rectifying tower 17, the tube side import of the secondary reboiler 21 of rectifying tower is communicated with the bottom of rectifying tower 17 and the connecting pipe between the 16 tube side imports of rectifying tower reboiler, the shell side outlet and the waste water of the secondary reboiler 21 of the rectifying tower stripper pipeline that degass is communicated with, and the connecting pipe between the tube side import of the shell side import of the secondary reboiler 21 of rectifying tower and the bottom of the tower 5 of vaporizing and the tower reboiler 6 of vaporizing is communicated with.
Claims (4)
1. methanol vapor phase catalytic dehydration preparing dimethy ether device, by the well heater that goes into operation (1), gas heat exchanger (2), reactor (3), vaporization tower (5), vaporization tower reboiler (6), methanol preheater (7), thick methyl ether preheater (8), thick methyl ether condenser (10), thick methyl ether basin (11), washing tower (12), rectifying tower condenser (13), return tank (14), still liquid basin (15), rectifying tower (17), rectifying tower reboiler (16), gas cooler (20) and absorption liquid condenser (9) are formed, the shell side import of methanol preheater (7) is communicated with external methanol pipeline, the shell side outlet of methanol preheater (7) is communicated with the import on vaporization tower (5) top, the top exit of vaporization tower (5) is communicated with the shell side import of gas heat exchanger (2), the tube side outlet of gas heat exchanger (2) is communicated with the tube side import of methanol preheater (7) and the bottom of reactor (3) simultaneously, the bottom of reactor (3) is communicated with the tube side import of gas heat exchanger (2) simultaneously, the shell side outlet of gas heat exchanger (2) is communicated with the tube side import and the Reactor inlet of the well heater that goes into operation (1) simultaneously, the tube side outlet of well heater (1) of going into operation is communicated with the top of reactor (3), the bottom of vaporization tower (5) is communicated with the tube side import of vaporization tower reboiler (6) and the waste water stripper pipeline that degass simultaneously, the shell side import of vaporization tower reboiler (6) is communicated with the external heat source pipeline, the tube side outlet of vaporization tower reboiler (6) is communicated with the middle and lower part of vaporization tower (5), the middle and upper part of vaporization tower (5) is communicated with still liquid basin (15) by still liquid pump (18), be communicated with by the shell side import of Y-tube being communicated with on the pipeline of vaporization tower (5) and still liquid pump (18) with absorption liquid condenser (9), the shell side outlet of absorption liquid condenser (9) is communicated with the top of washing tower (12), the bottom of washing tower (12) is communicated with the bottom of thick methyl ether basin (11), the top of washing tower (12) is provided with the non-condensable gas pipeline, the outlet of thick methyl ether basin (11) top is communicated with the middle part of washing tower (12) by the shell side of gas cooler (20), thick methyl ether basin (11) is communicated with by the shell side import of thick methyl ether pump (4) with thick methyl ether preheater (8), the shell side outlet of thick methyl ether preheater (8) is communicated with rectifying tower (17) middle part, the tube side import of thick methyl ether preheater (8) is communicated with the outlet of the tube side of methanol preheater (7), the shell side outlet of rectifying tower condenser (13) is communicated with the top inlet of return tank (14), the bottom of return tank (14) is simultaneously adopted pipe outward with the upper inlet of rectifying tower (17) and dme by dme pump (19) and is communicated with, the top exit of rectifying tower (17) is communicated with the shell side import of rectifying tower condenser (13), the middle and lower part of rectifying tower (17) is communicated with the tube side outlet of rectifying tower reboiler (16), the bottom of rectifying tower (17) is communicated with the tube side import of rectifying tower reboiler (16), the shell side import of rectifying tower reboiler (16) is communicated with the external heat source pipeline, the outlet at bottom of rectifying tower (17) is communicated with still liquid basin (15), the bottom of rectifying tower (17) has up and down, and two pipelines are communicated with still liquid basin (15), one of its middle and upper part is the gas-liquid equilibrium pipe, one of the bottom is the liquid phase upflow tube, the shell side top outlet of rectifying tower condenser (13) is communicated with the outlet at return tank (14) top, connecting pipe between the outlet at the outlet of the shell side top of rectifying tower condenser (13) and return tank (14) top exports with methyl ether basin (11) top slightly and the connecting tube of gas cooler (20) shell side import is communicated with, pipeline between the shell side outlet at bottom of gas cooler (20) and washing tower (12) and the thick methyl ether basin (11) is communicated with, there is the fusel extraction pipeline of three parallel connections the middle and lower part of vaporization tower (5), it is characterized in that: methanol vapor phase catalytic dehydration preparing dimethy ether device has been set up the secondary reboiler (22) of vaporization tower, connecting pipe between the tube side import of the tube side import of the secondary reboiler of vaporization tower (22) and the bottom of vaporization tower (5) and the tower reboiler (6) of vaporizing is communicated with, the tube side outlet of the vaporization secondary reboiler of tower (22) is communicated with the middle and lower part of vaporization tower (5), the shell side import of the vaporization secondary reboiler of tower (22) is communicated with the outlet at bottom of reactor (3), the shell side outlet of the secondary reboiler of vaporization tower (22) export with the tube side of gas heat exchanger (2) and the tube side import of methanol preheater (7) between connecting pipe be communicated with, to be communicated with vaporization tower (5) simultaneously is communicated with thick methyl ether basin (11) with the pipeline of still liquid pump (18), the middle and lower part of rectifying tower (17) is connected with the tube side outlet of thick methyl ether preheater (8), the shell side import of thick methyl ether condenser (10) is communicated with rectifying tower condenser (13) shell side import, the top exit of rectifying tower (17) is connected with the shell side import of thick methyl ether condenser (10) and the connecting pipe of the shell side import of rectifying tower condenser (13), the shell side outlet of thick methyl ether condenser (10) is communicated with the back with the shell side outlet of rectifying tower condenser (13) and is connected with the inlet pipeline of return tank (14), the top of return tank (14) is communicated with connecting pipe between thick methyl ether basin (11) top exit and gas cooler (20) the shell side import, and the shell side top outlet of thick methyl ether condenser (10) exports with the shell side top of rectifying tower condenser (13) and is communicated with.
2. methanol vapor phase catalytic dehydration preparing dimethy ether device according to claim 1, it is characterized in that: methanol vapor phase catalytic dehydration preparing dimethy ether device has also been set up the secondary reboiler (21) of rectifying tower, the tube side outlet of the secondary reboiler of rectifying tower (21) is communicated with the middle and lower part of rectifying tower (17), the tube side import of the secondary reboiler of rectifying tower (21) is communicated with the bottom of rectifying tower (17) and the connecting pipe between rectifying tower reboiler (16) the tube side import, the shell side outlet and the waste water of the secondary reboiler of rectifying tower (21) the stripper pipeline that degass is communicated with, and the connecting pipe between the tube side import of the shell side import of the secondary reboiler of rectifying tower (21) and the bottom of the tower (5) of vaporizing and the tower reboiler (6) of vaporizing is communicated with.
3. methanol vapor phase catalytic dehydration preparing dimethy ether device, by the well heater that goes into operation (1), gas heat exchanger (2), reactor (3), vaporization tower (5), vaporization tower reboiler (6), methanol preheater (7), thick methyl ether preheater (8), thick methyl ether condenser (10), thick methyl ether basin (11), washing tower (12), rectifying tower condenser (13), return tank (14), still liquid basin (15), rectifying tower (17), rectifying tower reboiler (16), gas cooler (20) and absorption liquid condenser (9) are formed, the shell side import of methanol preheater (7) is communicated with external methanol pipeline, the shell side outlet of methanol preheater (7) is communicated with the import on vaporization tower (5) top, the top exit of vaporization tower (5) is communicated with the shell side import of gas heat exchanger (2), the tube side outlet of gas heat exchanger (2) is communicated with the tube side import of methanol preheater (7) and the bottom of reactor (3) simultaneously, the bottom of reactor (3) is communicated with the tube side import of gas heat exchanger (2) simultaneously, the shell side outlet of gas heat exchanger (2) is communicated with the tube side import and the Reactor inlet of the well heater that goes into operation (1) simultaneously, the tube side outlet of well heater (1) of going into operation is communicated with the top of reactor (3), the bottom of vaporization tower (5) is communicated with the tube side import of vaporization tower reboiler (6) and the waste water stripper pipeline that degass simultaneously, the shell side import of vaporization tower reboiler (6) is communicated with the external heat source pipeline, the tube side outlet of vaporization tower reboiler (6) is communicated with the middle and lower part of vaporization tower (5), the middle and upper part of vaporization tower (5) is communicated with still liquid basin (15) by still liquid pump (18), be communicated with by the shell side import of Y-tube being communicated with on the pipeline of vaporization tower (5) and still liquid pump (18) with absorption liquid condenser (9), the shell side outlet of absorption liquid condenser (9) is communicated with the top of washing tower (12), the bottom of washing tower (12) is communicated with the bottom of thick methyl ether basin (11), the top of washing tower (12) is provided with the non-condensable gas pipeline, the outlet of thick methyl ether basin (11) top is communicated with the middle part of washing tower (12) by the shell side of gas cooler (20), thick methyl ether basin (11) is communicated with by the shell side import of thick methyl ether pump (4) with thick methyl ether preheater (8), the shell side outlet of thick methyl ether preheater (8) is communicated with rectifying tower (17) middle part, the tube side import of thick methyl ether preheater (8) is communicated with the outlet of the tube side of methanol preheater (7), the shell side outlet of rectifying tower condenser (13) is communicated with the top inlet of return tank (14), the bottom of return tank (14) is simultaneously adopted pipe outward with the upper inlet of rectifying tower (17) and dme by dme pump (19) and is communicated with, the top exit of rectifying tower (17) is communicated with the shell side import of rectifying tower condenser (13), the middle and lower part of rectifying tower (17) is communicated with the tube side outlet of rectifying tower reboiler (16), the bottom of rectifying tower (17) is communicated with the tube side import of rectifying tower reboiler (16), the shell side import of rectifying tower reboiler (16) is communicated with the external heat source pipeline, the outlet at bottom of rectifying tower (17) is communicated with still liquid basin (15), the bottom of rectifying tower (17) has up and down, and two pipelines are communicated with still liquid basin (15), one of its middle and upper part is the gas-liquid equilibrium pipe, one of the bottom is the liquid phase upflow tube, the shell side top outlet of rectifying tower condenser (13) is communicated with the outlet at return tank (14) top, connecting pipe between the outlet at the outlet of the shell side top of rectifying tower condenser (13) and return tank (14) top exports with methyl ether basin (11) top slightly and the connecting tube of gas cooler (20) shell side import is communicated with, pipeline between the shell side outlet at bottom of gas cooler (20) and washing tower (12) and the thick methyl ether basin (11) is communicated with, there is the fusel extraction pipeline of three parallel connections the middle and lower part of vaporization tower (5), it is characterized in that: methanol vapor phase catalytic dehydration preparing dimethy ether device has been set up the secondary reboiler (22) of vaporization tower, connecting pipe between the tube side import of the tube side import of the secondary reboiler of vaporization tower (22) and the bottom of vaporization tower (5) and the tower reboiler (6) of vaporizing is communicated with, the tube side outlet of the vaporization secondary reboiler of tower (22) is communicated with the middle and lower part of vaporization tower (5), the shell side import of the vaporization secondary reboiler of tower (22) is communicated with the outlet at bottom of reactor (3), the shell side outlet of the secondary reboiler of vaporization tower (22) export with the tube side of gas heat exchanger (2) and the tube side import of methanol preheater (7) between connecting pipe be communicated with, to be communicated with vaporization tower (5) simultaneously is communicated with thick methyl ether basin (11) with the pipeline of still liquid pump (18), the middle and lower part of rectifying tower (17) is connected with the tube side outlet of thick methyl ether preheater (8), the top exit of rectifying tower (17) is communicated with the shell side import of rectifying tower condenser (13), the shell side outlet of rectifying tower condenser (13) is communicated with the shell side import of thick methyl ether condenser (10), the shell side outlet of thick methyl ether condenser (10) is connected with the inlet pipeline of return tank (14), the top of return tank (14) is communicated with connecting pipe between thick methyl ether basin (11) top exit and gas cooler (20) the shell side import, and the shell side top outlet of thick methyl ether condenser (10) exports with the shell side top of rectifying tower condenser (13) and is communicated with.
4. methanol vapor phase catalytic dehydration preparing dimethy ether device according to claim 3, it is characterized in that: methanol vapor phase catalytic dehydration preparing dimethy ether device has also been set up the secondary reboiler (21) of rectifying tower, the tube side outlet of the secondary reboiler of rectifying tower (21) is communicated with the middle and lower part of rectifying tower (17), the tube side import of the secondary reboiler of rectifying tower (21) is communicated with the bottom of rectifying tower (17) and the connecting pipe between rectifying tower reboiler (16) the tube side import, the shell side outlet and the waste water of the secondary reboiler of rectifying tower (21) the stripper pipeline that degass is communicated with, and the connecting pipe between the tube side import of the shell side import of the secondary reboiler of rectifying tower (21) and the bottom of the tower (5) of vaporizing and the tower reboiler (6) of vaporizing is communicated with.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201084379U CN202063851U (en) | 2011-04-11 | 2011-04-11 | Device for preparing dimethyl ether through catalytic dehydration of gas-phase methanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201084379U CN202063851U (en) | 2011-04-11 | 2011-04-11 | Device for preparing dimethyl ether through catalytic dehydration of gas-phase methanol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202063851U true CN202063851U (en) | 2011-12-07 |
Family
ID=45057720
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011201084379U Expired - Lifetime CN202063851U (en) | 2011-04-11 | 2011-04-11 | Device for preparing dimethyl ether through catalytic dehydration of gas-phase methanol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202063851U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102225888A (en) * | 2011-04-11 | 2011-10-26 | 河北裕泰化工有限公司 | Device for preparing dimethyl ether by methanol vapor-phase catalytic dehydration |
-
2011
- 2011-04-11 CN CN2011201084379U patent/CN202063851U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102225888A (en) * | 2011-04-11 | 2011-10-26 | 河北裕泰化工有限公司 | Device for preparing dimethyl ether by methanol vapor-phase catalytic dehydration |
| CN102225888B (en) * | 2011-04-11 | 2013-05-08 | 河北裕泰化工有限公司 | Device for preparing dimethyl ether by methanol vapor-phase catalytic dehydration |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100378051C (en) | Rectifying tech. and equipment of high purity methanol | |
| CN202214306U (en) | Process device for preparing ethanol by utilizing acetic acid | |
| CN203904327U (en) | White liquor distilling apparatus | |
| CN107812393A (en) | A kind of methanol three-effect rectification system and technique | |
| CN110436545A (en) | A kind of remained ammonia distilling apparatus of heat energy recycling | |
| CN103252105B (en) | Methyl alcohol pressure reducing and distilling device | |
| CN102225888B (en) | Device for preparing dimethyl ether by methanol vapor-phase catalytic dehydration | |
| CN110935186A (en) | Novel heat coupling rectification process in acetate production process | |
| CN202063851U (en) | Device for preparing dimethyl ether through catalytic dehydration of gas-phase methanol | |
| CN205115337U (en) | Low power consuming is by device of methyl alcohol preparation aerosol dimethyl ether | |
| CN101851149A (en) | Energy-saving method and energy-saving system for producing edible ethanol by five-tower three-stage differential distillation | |
| CN201785378U (en) | Heat recovery device for saccharification system | |
| CN107754365A (en) | A kind of double effect rectification for methanol refining plant and process | |
| CN205435021U (en) | System is used multipurposely to synthetic gas system ethylene glycol technology rectifying column overhead gas heat | |
| CN201832433U (en) | Methanol and ethanol extracting equipment | |
| CN212881084U (en) | Distilling device for purifying miscellaneous wine | |
| CN102503771B (en) | Refining system and method of ethanol-containing aqueous solution | |
| CN205323257U (en) | Ethanol differential pressure distillation plant with flash distillation | |
| CN203842338U (en) | Heat gradient utilization device in methanol rectification process | |
| CN204325191U (en) | A kind of potassium methylate aqueous methanol steam reutilization system | |
| CN211521661U (en) | Surplus ammonia water distillation plant that heat energy cyclic utilization | |
| CN210331712U (en) | Steam condensate waste heat recovery device in alcohol ether production | |
| CN101851152A (en) | Method for preparing dimethyl ether by methyl alcohol gaseous phase dehydration | |
| CN202144482U (en) | Methanol recovery device | |
| CN207532818U (en) | A kind of methanol three-effect rectification system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20111207 Effective date of abandoning: 20130508 |
|
| RGAV | Abandon patent right to avoid regrant |