CN101693645A - Methanol multitower rectifying process and rectifying equipment - Google Patents
Methanol multitower rectifying process and rectifying equipment Download PDFInfo
- Publication number
- CN101693645A CN101693645A CN200910075734A CN200910075734A CN101693645A CN 101693645 A CN101693645 A CN 101693645A CN 200910075734 A CN200910075734 A CN 200910075734A CN 200910075734 A CN200910075734 A CN 200910075734A CN 101693645 A CN101693645 A CN 101693645A
- Authority
- CN
- China
- Prior art keywords
- tower
- rectifying
- methanol
- waste liquid
- methyl alcohol
- 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.)
- Pending
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)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to production process and equipment of chemical products, in particular to a methanol multitower rectifying process and rectifying equipment. The methanol multitower rectifying process comprises methanol multitower rectifying process steps and is characterized in that two pre-tower re-boilers are arranged at the bottom of a rectifying tower, wherein one pre-tower re-boiler takes the steam condensate of a pressurizing tower as a heat source, and a heat source of the other pre-tower re-boiler is waste liquid discharged from the bottom of a normal-pressure rectifying tower; the waste liquid enters from the lower part, flows out from the upper part and exchanges heat with crude methanol, and the heat exchanging time is prolonged; the heat exchanging efficiency cannot be influenced within short time when the flow rate of the waste liquid is fluctuated; sewage is discharged from the bottom, thereby avoiding frostbite in winter; and finally the waste liquid is subjected to biochemical treatment after being cooled. The rectifying equipment sufficiently utilizes the heat of the waste liquid, is more energy-saving and environment friendly and increases the operational flexibility; in addition, the rectifying equipment is more stable and the quality of products is ensured.
Description
Technical field
The present invention relates to a kind of Chemicals production technique and equipment, specifically a kind of methanol multitower rectifying process and rectifying device.
Background technology
In methanol rectification technology, most of employing pre-rectifying tower and a king-tower or multitower rectifying.The wastewater temperature of discharging at the bottom of the atmospheric distillation Tata is about 107 ℃, contains small amount of methanol and micro-higher alcohols and send biochemical treatment after the cooling of raffinate condenser.Like this, energy utilizes unreasonable, does badly in energy-conservation aspect.
Summary of the invention
Purpose of the present invention provides a kind of methanol multitower rectifying process and rectifying device that makes full use of heat energy, energy-conserving and environment-protective.
Methanol multitower rectifying process of the present invention comprises the steps:
(1) with the pump that feeds intake thick methyl alcohol is squeezed into preheater, enter pre-rectifying tower after the preheating.Pre-tower reboiler to thick methyl alcohol carry out indirect heating to 75～85 ℃, light constituent dme that contains in the thick methyl alcohol and methyl formate are vaporized to rise and enter pre-tower condenser, cooled liquid enters gas-liquid separator, cooling fluid enters backflash, and the non-condensable gas that is not cooled enters letdown tank and absorbs directly discharging of back with soft water;
(2) liquid effluent at the bottom of the pre-rectifying tower tower, send into the rectifying of compression rectification tower, the pressurizing tower working pressure is≤0.6MPa, cat head methanol steam temperature is 110～128 ℃, go the atmospheric tower reboiler as thermal source, enter the pressurization backflash after the partial condensation of self lowering the temperature simultaneously, phlegma separates in groove with uncondensed gas, uncooled pneumatic transmission is toward the gas phase pipe (cat head methyl alcohol steam pipe) of atmospheric tower, and regulate the pressure of pressurizing tower with this, and a phlegma part refluxes, and another part refined methanol is from the backflash extraction, go to the refined methanol tank field after being cooled to normal temperature, compression rectification tower reboiler employing 〉=0.35MPa low-pressure steam is a thermal source;
(3) liquid effluent at the bottom of the compression rectification Tata, utilize the pressure reduction between two towers to be sent to the atmospheric distillation tower, during 63～66 ℃ of atmospheric distillation column overhead methanol steam temperature, after the cooling of atmospheric tower condenser, a phlegma part refluxes, and another part send methyl alcohol tank field refined methanol groove;
Two pre-tower reboilers are arranged at the bottom of the above-mentioned pre-rectifying tower tower, a pre-tower reboiler is a thermal source with the pressurizing tower steam condensate, the thermal source of another pre-tower reboiler is the waste liquid of discharging at the bottom of the atmospheric distillation Tata, go out on advancing under the waste liquid and thick methyl alcohol heat exchange, having increased heat-exchange time short period of time when the raffinate flow rate fluctuation can not influence the heat exchange effect, and at bottom blow-down, it is antifreeze to be used for winter, send biochemical treatment after the last waste liquid cooling.
Rectifying device in the methanol multitower rectifying process of the present invention: two pre-tower reboilers are arranged at the bottom of the pre-rectifying tower tower, the type of heating of pre-tower reboiler under go out on advancing, and at the bottom blow-down mouth.
The present invention has following advantage compared with prior art:
Make full use of the heat of waste liquid, energy-saving and environmental protection more, turndown ratio increases, and system is more stable, and quality product is guaranteed.
Description of drawings
The present invention is further described below in conjunction with drawings and Examples.
Fig. 1 is the process flow sheet of improvement part of the present invention.
Among the figure, 1. refined methanol water cooler, 2. pre-rectifying tower, 3. compression rectification tower, 4. backflash, 5. atmospheric distillation tower, 6. condenser, 7. backflash, 8. reflux pump, 9. atmospheric tower reboiler, 10. pressurizing tower reflux pump, 11. pressurizing tower reboilers, 12. prognosis methanol pump, 13. pre-tower reboiler, 14. pre-tower reboilers, 15. preheaters.
Embodiment
The present invention includes following steps:
(1) pump is squeezed into preheater 15 with thick methyl alcohol, enter pre-rectifying tower 2 after the preheating, pre-tower reboiler to thick methyl alcohol carry out indirect heating to 75～85 ℃, light constituent dme that contains in the thick methyl alcohol and methyl formate are vaporized to rise and enter pre-tower condenser, cooled liquid enters gas-liquid separator, cooling fluid enters backflash, and the non-condensable gas that is not cooled enters letdown tank and absorbs directly discharging of back with soft water;
(2) 75～85 ℃ liquid effluent at the bottom of pre-rectifying tower 2 towers, send into 3 rectifying of compression rectification tower by prognosis methanol pump 12 pressurization backs from the 8th block of column plate, the working pressure of compression rectification tower 3 is≤0.6MPa, cat head methanol steam temperature is 110～128 ℃, go atmospheric tower reboiler 9 as thermal source, enter pressurization backflash 4 after the partial condensation of self lowering the temperature simultaneously, phlegma separates in groove with uncondensed gas, uncooled pneumatic transmission is toward the gas phase pipe (cat head methyl alcohol steam pipe) of atmospheric tower 5, and regulate the pressure of pressurizing tower with this, a phlegma part is through the phegma of pressurizing tower reflux pump 10 as pressurizing tower 3, another part refined methanol is from backflash 4 extraction, after being sent to thick methanol preheater 15 and being used to heat thick methyl alcohol, when temperature is reduced to 50 ℃, go to the refined methanol tank field after refined methanol water cooler 1 is cooled to normal temperature, compression rectification tower reboiler 11 employing 〉=0.35MPa low-pressure steam are thermal source, material at the bottom of the pressurizing tower is heated to 118～135 ℃, and steam condenser pipe is delivered to outer tube;
(3) compression rectification tower 3 column bottom temperatures are 129 ℃ liquid effluent, utilize the pressure reduction between two towers to be sent to atmospheric distillation tower 5, the 16th, 18,20 column plate places enter atmospheric distillation tower 5, during 63～66 ℃ of atmospheric distillation tower 5 cat head methanol steam temperature, after atmospheric tower condenser 6 is cooled to 40 ℃, phlegma flows into atmospheric tower backflash 7, send phegma by atmospheric tower reflux pump 8 a pressurization back part back to from Atmospheric Tower as atmospheric tower 5, another part send methyl alcohol tank field refined methanol groove, atmospheric distillation tower 5 thermals source are compression rectification tower 3 cat head methanol steams, from atmospheric distillation tower the 8th, 10,12, the potato spirit of 14 column plate extraction enters the potato spirit storage tank after the cooling of potato spirit water cooler, go to the tank field by the potato spirit pumping toward potato spirit;
Two pre-tower reboilers 13,14 are arranged at the bottom of the above-mentioned pre-rectifying tower tower, pre-tower reboiler 13 is a thermal source with the pressurizing tower steam condensate, the thermal source of pre-tower reboiler 14 is the waste liquid of discharging at the bottom of the atmospheric distillation Tata, go out on advancing under the waste liquid with thick methyl alcohol heat exchange after send biochemical treatment, having increased heat-exchange time short period of time when the raffinate flow rate fluctuation can not influence the heat exchange effect, and at bottom blow-down, it is antifreeze to be used for winter.
Two pre-tower reboilers 13,14 are arranged at the bottom of the pre-rectifying tower tower, and the type of heating of pre-tower reboiler 13,14 goes out on advancing down, and tower reboiler 14 bottoms are provided with sewage draining exit in advance.
Claims (2)
1. a methanol multitower rectifying process comprises the steps:
(1) with the pump that feeds intake thick methyl alcohol is squeezed into preheater, enter pre-rectifying tower after the preheating, tower bottom reboiler to thick methyl alcohol carry out indirect heating to 75～85 ℃, light constituent dme that contains in the thick methyl alcohol and methyl formate are vaporized to rise and enter pre-tower condenser, cooled liquid enters gas-liquid separator, cooling fluid enters backflash, and the non-condensable gas that is not cooled enters letdown tank and absorbs directly discharging of back with soft water;
(2) liquid effluent at the bottom of the pre-rectifying tower tower, send into the rectifying of compression rectification tower, the pressurizing tower working pressure is≤0.6MPa, cat head methanol steam temperature is 110～128 ℃, go the atmospheric tower reboiler as thermal source, enter the pressurization backflash after the partial condensation of self lowering the temperature simultaneously, phlegma separates in groove with uncondensed gas, uncooled pneumatic transmission is toward the cat head methyl alcohol steam pipe of atmospheric tower, and regulate the pressure of pressurizing tower with this, and a phlegma part refluxes, and another part refined methanol is from the backflash extraction, go to the refined methanol tank field after being cooled to normal temperature, compression rectification tower reboiler employing 〉=0.35MPa low-pressure steam is a thermal source;
(3) liquid effluent at the bottom of the compression rectification Tata, utilize the pressure reduction between two towers to be sent to the atmospheric distillation tower, during 63～66 ℃ of atmospheric distillation column overhead methanol steam temperature, after the cooling of atmospheric tower condenser, a phlegma part refluxes, and another part send methyl alcohol tank field refined methanol groove;
It is characterized in that at the bottom of the described pre-rectifying tower tower two pre-tower reboilers being arranged, a pre-tower reboiler is a thermal source with the pressurizing tower steam condensate, the thermal source of another pre-tower reboiler is the waste liquid of discharging at the bottom of the atmospheric distillation Tata, go out on advancing under the waste liquid and thick methyl alcohol heat exchange, prolong heat-exchange time, and, send biochemical treatment after the last waste liquid cooling at bottom blow-down.
2. the rectifying device in the methanol multitower rectifying process as claimed in claim 1 is characterized in that at the bottom of the pre-rectifying tower tower two pre-tower reboilers being arranged, wherein the type of heating of a pre-tower reboiler of Zeng Jiaing under go out on advancing, the bottom is provided with sewage draining exit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910075734A CN101693645A (en) | 2009-10-14 | 2009-10-14 | Methanol multitower rectifying process and rectifying equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910075734A CN101693645A (en) | 2009-10-14 | 2009-10-14 | Methanol multitower rectifying process and rectifying equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101693645A true CN101693645A (en) | 2010-04-14 |
Family
ID=42092660
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200910075734A Pending CN101693645A (en) | 2009-10-14 | 2009-10-14 | Methanol multitower rectifying process and rectifying equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101693645A (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102430254A (en) * | 2011-09-16 | 2012-05-02 | 徐建涛 | Rectification technology and apparatus of aqueous solution of methanol or ethanol |
| CN102886151A (en) * | 2012-10-08 | 2013-01-23 | 安徽晋煤中能化工股份有限公司 | Device and method for recovering heat from three-tower methanol rectification |
| CN104292075A (en) * | 2014-09-27 | 2015-01-21 | 安徽金禾实业股份有限公司 | Method for exchanging heat of crude alcohol in fine methanol production |
| CN108558603A (en) * | 2018-06-06 | 2018-09-21 | 天津奥展兴达化工技术有限公司 | A kind of refining crude methanol process of three towers triple effect |
| CN109745724A (en) * | 2019-01-24 | 2019-05-14 | 山东伯仲真空设备股份有限公司 | MVR rectifying stripping set composite and its process |
| CN109796309A (en) * | 2018-12-24 | 2019-05-24 | 安徽昊源化工集团有限公司 | A kind of recovery process of methanol production waste heat |
| CN110256202A (en) * | 2019-07-08 | 2019-09-20 | 张兵 | A kind of refining crude methanol process of four towers quadruple effect |
| CN112062654A (en) * | 2020-08-21 | 2020-12-11 | 陕西聚能新创煤化科技有限公司 | Ethylene glycol rectification system and rectification process |
| CN112902686A (en) * | 2021-01-26 | 2021-06-04 | 河北易高生物能源有限公司 | Furfural primary distillation tower steam recycling method |
| CN116785744A (en) * | 2023-06-25 | 2023-09-22 | 新疆广汇新能源有限公司 | High-efficiency crude methanol rectifying device and method |
-
2009
- 2009-10-14 CN CN200910075734A patent/CN101693645A/en active Pending
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102430254B (en) * | 2011-09-16 | 2013-09-04 | 徐建涛 | Rectification technology and apparatus of aqueous solution of methanol or ethanol |
| CN102430254A (en) * | 2011-09-16 | 2012-05-02 | 徐建涛 | Rectification technology and apparatus of aqueous solution of methanol or ethanol |
| CN102886151A (en) * | 2012-10-08 | 2013-01-23 | 安徽晋煤中能化工股份有限公司 | Device and method for recovering heat from three-tower methanol rectification |
| CN104292075A (en) * | 2014-09-27 | 2015-01-21 | 安徽金禾实业股份有限公司 | Method for exchanging heat of crude alcohol in fine methanol production |
| CN104292075B (en) * | 2014-09-27 | 2016-02-03 | 安徽金禾实业股份有限公司 | The method of thick alcohol heat exchange is given in refined methanol production |
| CN108558603B (en) * | 2018-06-06 | 2021-08-03 | 天津奥展兴达化工技术有限公司 | Three-tower three-effect crude methanol refining process method |
| CN108558603A (en) * | 2018-06-06 | 2018-09-21 | 天津奥展兴达化工技术有限公司 | A kind of refining crude methanol process of three towers triple effect |
| CN109796309A (en) * | 2018-12-24 | 2019-05-24 | 安徽昊源化工集团有限公司 | A kind of recovery process of methanol production waste heat |
| CN109745724A (en) * | 2019-01-24 | 2019-05-14 | 山东伯仲真空设备股份有限公司 | MVR rectifying stripping set composite and its process |
| CN110256202A (en) * | 2019-07-08 | 2019-09-20 | 张兵 | A kind of refining crude methanol process of four towers quadruple effect |
| CN110256202B (en) * | 2019-07-08 | 2024-04-19 | 张兵 | Four-tower four-effect crude methanol refining process method |
| CN112062654A (en) * | 2020-08-21 | 2020-12-11 | 陕西聚能新创煤化科技有限公司 | Ethylene glycol rectification system and rectification process |
| CN112902686A (en) * | 2021-01-26 | 2021-06-04 | 河北易高生物能源有限公司 | Furfural primary distillation tower steam recycling method |
| CN116785744A (en) * | 2023-06-25 | 2023-09-22 | 新疆广汇新能源有限公司 | High-efficiency crude methanol rectifying device and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101693645A (en) | Methanol multitower rectifying process and rectifying equipment | |
| CN100584421C (en) | Differential pressure low-energy-consumption distillation method and equipment | |
| CN101570466B (en) | Multi-effect rectifying process of methanol | |
| CN101503337B (en) | Technological process for methanol distillation by using fiver-tower heat integration apparatus | |
| CN100378051C (en) | Rectifying tech. and equipment of high purity methanol | |
| CN109675333B (en) | Benzene tower fractionation device and method driven by heat pump | |
| CN102070401B (en) | Energy-saving process for preparing absolute ethanol from bioethanol aqueous solution | |
| CN102936198B (en) | Produce the method for vinyl acetate | |
| CN104744194B (en) | A kind of isobutene. device takes off light weight-removing column and is thermally integrated technique | |
| CN106075947A (en) | Methanol four tower double-effect heat pump energy-saving equipment and method | |
| CN201473512U (en) | Distilling system provided with preheating device | |
| CN101357879B (en) | Methanol three-tower rectification system and technique | |
| CN201735201U (en) | Rectifying tower top gaseous phase heat recycling device | |
| CN101492346A (en) | Multi/dual-purpose distillation system for methanol | |
| CN101058534B (en) | Device and method for preparing dimethyl ether from methanol | |
| CN204767516U (en) | Rectification forced circulation heating device | |
| CN104744195B (en) | After a kind of ether, carbon four purifies de-dimethyl ether tower energy saving technique | |
| CN201746534U (en) | White spirit distillation air cooler | |
| CN101550065B (en) | Energy-saving and water-saving type high-low pressure double-tower process for preparing dimethyl ether by rectifying methanol | |
| CN202020931U (en) | Constant-pressure alcohol recycling device | |
| CN105646147B (en) | A kind of Methanol Recovery method | |
| CN210314061U (en) | Rectification and purification device for synthesizing dimethyl oxalate by carbonylation of coal-made ethylene glycol | |
| CN205435021U (en) | System is used multipurposely to synthetic gas system ethylene glycol technology rectifying column overhead gas heat | |
| CN102489030A (en) | Three-tower energy-saving differential pressure alcohol distillation production system and technological process thereof | |
| CN101851152A (en) | Method for preparing dimethyl ether by methyl alcohol gaseous phase dehydration |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20100414 |