CN202595005U - Optimized energy-saving dimethyl ether production device - Google Patents
Optimized energy-saving dimethyl ether production device Download PDFInfo
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- CN202595005U CN202595005U CN2012202315303U CN201220231530U CN202595005U CN 202595005 U CN202595005 U CN 202595005U CN 2012202315303 U CN2012202315303 U CN 2012202315303U CN 201220231530 U CN201220231530 U CN 201220231530U CN 202595005 U CN202595005 U CN 202595005U
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- methyl ether
- rectifying tower
- methanol
- gas
- preheater
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- 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
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Abstract
The utility model relates to an optimized energy-saving dimethyl ether production device. The optimized energy-saving dimethyl ether production device comprises a methanol vaporizing tower, a gas heat exchanger, a reactor, a coarse methyl ether condenser, a coarse methyl ether storage tank and a rectifying tower. Methanol from outside can enter into the methanol vaporizing tower for heating and vaporizing after being preheated, the methanol getting out from the methanol vaporizing tower can be divided into two parts to enter into the reactor after passing through the gas heat exchanger, the first part of the methanol enters into the reactor from the top part, the second part of the methanol is used as cold shock gas to enter into the reactor from the upper part of a second section, reaction gas getting out from the reactor can enter into the coarse methyl ether storage tank to be subjected to the gas-liquid separation after being subjected to respective heat recovery by the gas heat exchanger, a methanol preheater, a coarse methyl ether preheater and the coarse methyl ether condenser, the purification on dimethyl ether can be carried out when the liquid phase enters into the rectifying tower after being preheated by the coarse methyl ether preheater. The optimized energy-saving dimethyl ether production device disclosed by the utility model is characterized in that the bottom part of the rectifying tower is provided with a rectifying tower reboiler, reaction gas getting out from the reactor can be firstly subjected to heat exchange by the rectifying tower reboiler.
Description
Technical field
The utility model relates to the dme production technical field, particularly a kind ofly optimizes energy-conservation dme production unit.
Background technology
At present, the production technique of the dme of most domestic all adopts the methanol gas phase dewatering preparing dimethy ether method of comparative maturity; This method is mature and stable, but also exists steam consumption high, problems such as recirculated water large usage quantity; Particularly when the summer heavy-duty service; Because the increase of its consumption, causing whole dme device still is that the consumption of general facilities is all bigger than normal from raw material consumption, causes the uneconomical of system's operation.
The utility model content
In order to solve above-mentioned technical problem, the utility model provides a kind of energy-conservation dme production unit of optimizing, and on present dme production unit, improves, and reasonably optimizing utilizes the heat of reactant gases, can reduce its steam consumption greatly.
From typical process for preparing dimethyl ether equipment, the recovery of its heat is basically through following scheme: after getting into the methanol preheater preheating from out-of-bounds methyl alcohol, get into methyl alcohol vaporization tower, the steam reboiler through the tower still heats vaporization.The gasified methanol that comes out from methyl alcohol vaporization tower is divided into two strands of entering reactor drums after the gas heat exchanger heat exchange; First strand of methyl alcohol gas is superheated to about 275 ℃ of temperature of reaction, gets into reactor drum from the top; Two sections catalyst inlet temperature are regulated from the top entering reactor drum of second section beds after metering as quench gas in second burst of overheated slightly back of methyl alcohol gas (about 185 ℃).
The high-temperature reacting gas thick methyl ether basin of entering after gas heat exchanger, methanol preheater, thick methyl ether preheater heat exchange, thick methyl ether condensing surface are cooled to 220 ℃, 180 ℃, 110 ℃, 40 ℃ respectively that comes out from reactor drum carries out gas-liquid separation.Get into rectifying tower after liquid phase is preheated to about 80 ℃ through thick methyl ether preheater and carry out the purification of dme.
The technical scheme that the utility model adopts is following:
Find through analyzing; Before getting into water-cooled, the part heat of reaction gas also can further reclaim, and mainly can be used in the heating to the rectifying tower tower bottoms; Through the research of dme device reaction heat is adjusted; On the basis of current dme production unit, be provided with the rectifying tower reboiler in rectifier bottoms, the reactant gases that comes out from reactor drum carries out heat exchange through the rectifying tower reboiler earlier.
The high-temperature gas that described rectifying tower reboiler utilizes reactor drum to come out heats the methyl ether of rectifying tower.
Described rectifying tower reboiler is arranged between gas heat exchanger and the methanol preheater.
The beneficial effect of the production unit of the utility model is: mainly further optimize energy-conservation to the dme production unit: through the further reasonably optimizing utilization of the reaction heat of dme reaction gas, can reduce its steam consumption greatly; Through making full use of of rich heat, reduced the thermal load of systemic circulation water, thereby further reduced systemic circulation water load.
Description of drawings
Fig. 1 is the process flow sheet of the production unit of the utility model.
Embodiment
Embodiment describes in further detail the present invention below in conjunction with accompanying drawing.
As shown in Figure 1; A kind ofly optimize energy-conservation dme production unit; This equipment comprises methanol preheater 1, methyl alcohol vaporization tower 2, gas heat exchanger 3, reactor drum 4, rectifying tower reboiler 5, thick methyl ether preheater 6, thick methyl ether condensing surface 7, thick methyl ether basin 8, rectifying tower fresh feed pump 9 and rectifying tower 10.
The technical process of device fabrication dme is: get into after methanol preheater is preheated to about 130 ℃ from out-of-bounds about 40 ℃ methyl alcohol; Entering methyl alcohol vaporization tower heats vaporization through the steam reboiler of tower still; The gasified methanol that comes out from the vaporization tower divides two strands to get into reactor drum after the gas heat exchanger heat exchange; First strand of methyl alcohol gas is superheated to about 275 ℃ of temperature of reaction; Get into reactor drum from the top, two sections catalyst inlet temperature are regulated from the top entering reactor drum of second section beds after metering as quench gas in second burst of overheated slightly back of methanol gas (about 185 ℃).
The reactant gases (about 380 ℃) that comes out from reactor drum is cooled to about 220 ℃, rectifying reboiler through gas heat exchanger and is cooled to about 190 ℃, methanol preheater and is cooled to about 170 ℃, thick methyl ether preheater and is cooled to and gets into thick methyl ether basin after about 95 ℃, thick methyl ether condensing surface are cooled to about 40 ℃ and carry out gas-liquid separation; The thick methyl ether of liquid phase delivers into the purification that rectifying tower carries out dme through the rectifying tower fresh feed pump after being preheated to about about 85 ℃ through rectifying tower fresh feed pump, thick methyl ether preheater.
Claims (5)
1. optimize energy-conservation dme production unit for one kind; Comprise methyl alcohol vaporization tower, gas heat exchanger, reactor drum, thick methyl ether condensing surface, thick methyl ether basin and rectifying tower; Methyl alcohol gets into methanol vapor tower heating vaporization after preheating; Methyl alcohol after the vaporization is divided into two strands and gets into reactor drum behind gas heat exchanger; The reactant gases thick methyl ether basin of entering after interchanger, methanol preheater, thick methyl ether preheater, thick methyl ether condensing surface reclaim heat respectively that comes out from reactor drum carries out gas-liquid separation; Liquid phase gets into rectifying tower after through the preheating of thick methyl ether preheater and carries out the purification of dme, and it is characterized in that: described rectifier bottoms is provided with the rectifying tower reboiler, and the reactant gases that comes out from reactor drum carries out heat exchange through the rectifying tower reboiler earlier.
2. the dme production unit that optimization according to claim 1 is energy-conservation is characterized in that: also comprise methanol preheater, in methanol preheater, will be preheated to 130 ℃ through the gas after the heat exchange of rectifying tower reboiler from methyl alcohol out-of-bounds.
3. the dme production unit that optimization according to claim 1 is energy-conservation is characterized in that: first strand of vaporization back methyl alcohol gets into reactor drum from the top, and second strand gets into from second section top of reactor drum as quench gas.
4. the dme production unit that optimization according to claim 1 is energy-conservation is characterized in that: the high-temperature gas that described rectifying tower reboiler utilizes reactor drum to come out heats the methyl ether of rectifying tower.
5. the dme production unit that optimization according to claim 1 is energy-conservation is characterized in that: described rectifying tower reboiler is arranged between gas heat exchanger and the methanol preheater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012202315303U CN202595005U (en) | 2012-05-22 | 2012-05-22 | Optimized energy-saving dimethyl ether production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012202315303U CN202595005U (en) | 2012-05-22 | 2012-05-22 | Optimized energy-saving dimethyl ether production device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202595005U true CN202595005U (en) | 2012-12-12 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012202315303U Expired - Fee Related CN202595005U (en) | 2012-05-22 | 2012-05-22 | Optimized energy-saving dimethyl ether production device |
Country Status (1)
| Country | Link |
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| CN (1) | CN202595005U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103172501A (en) * | 2013-03-14 | 2013-06-26 | 天津天中福大科技发展有限公司 | Energy-conservation separation method and device for rectifying dimethyl ether |
-
2012
- 2012-05-22 CN CN2012202315303U patent/CN202595005U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103172501A (en) * | 2013-03-14 | 2013-06-26 | 天津天中福大科技发展有限公司 | Energy-conservation separation method and device for rectifying dimethyl ether |
| CN103172501B (en) * | 2013-03-14 | 2015-10-21 | 天津天中福大科技发展有限公司 | A kind of energy-saving separation method of dme rectifying and device |
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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: 20121212 Termination date: 20130522 |