CN205398515U - Production system of methyl alcohol rectification - Google Patents
Production system of methyl alcohol rectification Download PDFInfo
- Publication number
- CN205398515U CN205398515U CN201620213697.5U CN201620213697U CN205398515U CN 205398515 U CN205398515 U CN 205398515U CN 201620213697 U CN201620213697 U CN 201620213697U CN 205398515 U CN205398515 U CN 205398515U
- Authority
- CN
- China
- Prior art keywords
- tower
- ether
- atmospheric distillation
- rectification
- distillation tower
- 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 - Fee Related
Links
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 provides a production system of methyl alcohol rectification, through the demineralized water tank to slightly adding water in the methyl alcohol, rectification extracts in taking off the ether tower, rely on to distillate fractionally the operating principle and detach low -boiling hydrocarbon and partly dissolved gases in the thick methyl alcohol, after taking off the processing of ether tower, according to the ejection of compact quality condition of taking off ether tower bottoms, handle respectively, the product that purity is high is directly sent into the ordinary pressure rectifying column and is handled, the product that purity is low gets into the pressurized rectification tower and handles, the condition of branch is handled can effectual saving energy consumption, the top of the tower liquid of pressurized rectification tower gets into ordinary pressure rectifying column reboiler and carries out the heat exchange, makes the top of the tower liquid of pressurized rectification tower obtain the cooling, also provides the heat for ordinary pressure rectifying column reboiler simultaneously, reaches the energy saving and consumption reduction purpose, the noncondensable gas that take off ether tower cooler ware, take off ether tower counter -flow vat, ordinary pressure rectifying column cooler produces reduces exhaust pollution respectively through taking off the evacuation more later of ether tower liquid seal groove and ordinary pressure rectifying column liquid seal groove, take off at the bottom of the cauldron of ether tower, pressurized rectification tower, ordinary pressure rectifying column liquid and all be connected with the accident groove, collect the processing to it, reduce the waste liquid and pollute.
Description
Technical field
This utility model relates to methanol production technical field, is specifically related to the production system of a kind of methanol rectification.
Background technology
Rectification and purification in methanol industry production process is very crucial, and methanol rectification technology is directly connected to the final methanol product quality prepared.Methanol rectification purification is last procedure of methanol production, and its power consumption accounts for 20% that methanol production always consumes energy.Select suitable rectification process, be the important channel reducing methanol production cost, energy efficient, raising product competitiveness.Applicant, on the basis of current methanol rectification technology, tries hard to find a kind of rectification effect good, and energy consumption is low, the methanol rectification technique that environmental pollution is little.
Utility model content
The purpose of this utility model is to provide that a kind of energy consumption is relatively low, the production system of eco-friendly methanol rectification.
nullIn order to realize object above，This utility model adopts the following technical scheme that the production system of a kind of methanol rectification，Including crude carbinol storage tank，Crude carbinol storage tank is connected with de-ether tower preheater，De-ether tower preheater is connected with the crude carbinol charging aperture of de-ether tower，The top exit of de-ether tower is connected with de-ether tower cooler device，The connection of de-ether tower cooler device bottom arranges de-ether tower backflash，Described de-ether tower backflash is connected with demineralized water tank and de-ether tower backflow import respectively by pipeline，Described de-ether tower cooler device and described de-ether tower backflash are provided with fixed gas outlet，The fixed gas outlet of de-ether tower cooler device and de-ether tower backflash is all connected with de-ether tower liquid seal trough，The bottom of described de-ether tower is connected with compression rectification tower preheater and atmospheric distillation tower charging aperture respectively by discharge nozzle，The kettle base solution outlet of described de-ether tower is connected with accident groove，Described compression rectification tower preheater is connected with compression rectification tower charging aperture by pipeline，The liquid of top of the tower outlet of described compression rectification tower is connected with the atmospheric distillation tower reboiler of atmospheric distillation tower，Atmospheric distillation tower reboiler is connected with compression rectification tower backflash，Compression rectification tower backflash is connected with compression rectification tower backflow import and compression rectification tower extraction cooler respectively by pipeline，Liquid outlet at the bottom of the tower of described compression rectification tower is connected with the charging aperture of atmospheric distillation tower，The kettle base solution outlet of compression rectification tower is connected with accident groove，The liquid of top of the tower outlet of atmospheric distillation tower is connected with atmospheric distillation tower cooler device，Atmospheric distillation tower cooler device is connected with atmospheric distillation tower backflash by pipeline，Atmospheric distillation tower backflash is connected with the backflow import of atmospheric distillation tower and refined methanol condenser respectively，The product extraction mouth of atmospheric distillation tower is connected with described refined methanol condenser，Described refined methanol condenser is connected with essence alcohol groove and accident groove respectively by pipeline，Described compression rectification tower extraction cooler is connected with described essence alcohol groove and accident groove respectively by pipeline，Described atmospheric distillation tower cooler device is provided with fixed gas outlet，The fixed gas outlet of atmospheric distillation tower cooler device is connected with atmospheric distillation tower liquid seal trough，The kettle base solution outlet of described atmospheric distillation tower is connected with accident groove.
Preferably, described de-ether tower liquid seal trough and described atmospheric distillation tower liquid seal trough are all connected with de-ether tower backflash by pipeline.
Preferably, the bottom of described atmospheric distillation tower is connected with Alcohols,fusel storage tank.
Preferably, the tower top temperature of described de-ether tower is 65-75 DEG C, and column bottom temperature is 65-80 DEG C, and emptying temperature is 35-55 DEG C.
Preferably, the tower top temperature of described compression rectification tower is 110-120 DEG C, and column bottom temperature is 123-130 DEG C, pressure reduction 0.16MPa.
Preferably, the tower top temperature of described atmospheric distillation tower is 63-80 DEG C, and column bottom temperature is 100-110 DEG C, and emptying temperature is 30-45 DEG C.
The production system of the methanol rectification that this utility model provides, added water in crude carbinol by demineralized water tank, extracting rectifying in de-ether tower, fractionation operation principle is relied on to remove the gas that in crude carbinol, lower boiling Hydrocarbon and a part are dissolved, after de-ether tower processes, the discharging quality condition according to de-ether tower bottom product, it is respectively processed, the product that purity is high is sent directly into atmospheric distillation tower and processes, and the low product of purity enters compression rectification tower and processes, and point situation processes can effective energy efficient；The liquid of top of the tower of compression rectification tower enters atmospheric distillation tower reboiler and carries out heat exchange, makes the liquid of top of the tower of compression rectification tower be cooled down, and also provides heat for atmospheric distillation tower reboiler simultaneously, reaches energy-saving and cost-reducing purpose；The fixed gas that de-ether tower cooler device, de-ether tower backflash, atmospheric distillation tower cooler device produce empties respectively through after de-ether tower liquid seal trough and atmospheric distillation tower liquid seal trough again, reduces exhaust emission；De-ether tower, compression rectification tower, atmospheric distillation tower kettle base solution be all connected with accident groove, it is collected process, minimizing waste liquor contamination.
Accompanying drawing explanation
Fig. 1 is the structural representation of the production system of a kind of methanol rectification that this utility model embodiment provides.
Detailed description of the invention
Below by specific embodiment, the technical solution of the utility model is described in detail.
Embodiment
nullAs shown in Figure 1，A kind of production system of methanol rectification，Including crude carbinol storage tank 8，Crude carbinol storage tank 8 is connected with de-ether tower preheater 7，De-ether tower preheater 7 is connected with the crude carbinol charging aperture of de-ether tower 6，The top exit of de-ether tower 6 is connected with de-ether tower cooler device 3，The connection of de-ether tower cooler device 3 bottom arranges de-ether tower backflash 2，De-ether tower backflash 2 is connected with the backflow import of demineralized water tank 1 and de-ether tower 6 respectively by pipeline，De-ether tower cooler device 3 and de-ether tower backflash 2 are provided with fixed gas outlet，The fixed gas outlet of de-ether tower cooler device 3 and de-ether tower backflash 2 is all connected with de-ether tower liquid seal trough 4，The bottom of de-ether tower 6 is connected with compression rectification tower preheater 9 and atmospheric distillation tower 13 charging aperture respectively by discharge nozzle，The kettle base solution outlet of de-ether tower 6 is connected with accident groove 17，Compression rectification tower preheater 9 is connected with compression rectification tower 10 charging aperture by pipeline，The liquid of top of the tower outlet of compression rectification tower 10 is connected with the atmospheric distillation tower reboiler 12 of atmospheric distillation tower 13，Atmospheric distillation tower reboiler 12 is connected with compression rectification tower backflash 11，Compression rectification tower backflash 11 is connected with the backflow import of compression rectification tower 10 and compression rectification tower extraction cooler 15 respectively by pipeline，Liquid outlet at the bottom of the tower of compression rectification tower 10 is connected with the charging aperture of atmospheric distillation tower 13，The kettle base solution outlet of compression rectification tower 10 is connected with accident groove 17，The liquid of top of the tower outlet of atmospheric distillation tower 13 is connected with atmospheric distillation tower cooler device 19，Atmospheric distillation tower cooler device 19 is connected with atmospheric distillation tower backflash 18 by pipeline，Atmospheric distillation tower backflash 18 is connected with the backflow import of atmospheric distillation tower 13 and refined methanol condenser 20 respectively，The product extraction mouth of atmospheric distillation tower 13 is also connected with refined methanol condenser 20，Refined methanol condenser 20 is connected with essence alcohol groove 16 and accident groove 17 respectively by pipeline，Compression rectification tower extraction cooler 15 is connected with essence alcohol groove 16 and accident groove 17 respectively by pipeline，Atmospheric distillation tower cooler device 19 is provided with fixed gas outlet，The fixed gas outlet of atmospheric distillation tower cooler device 19 is connected with atmospheric distillation tower liquid seal trough 5，The kettle base solution of atmospheric distillation tower 13 is connected with accident groove 17.
De-ether tower liquid seal trough 4 and atmospheric distillation tower liquid seal trough 5 are all connected with de-ether tower backflash 2 by pipeline.
The bottom of atmospheric distillation tower 13 is connected with Alcohols,fusel storage tank 14.
The tower top temperature of de-ether tower 6 is 65-75 DEG C, and column bottom temperature is 65-80 DEG C, and emptying temperature is 35-55 DEG C.
The tower top temperature of compression rectification tower 10 is 110-120 DEG C, and column bottom temperature is 123-130 DEG C, pressure reduction 0.16MPa.
The tower top temperature of atmospheric distillation tower 13 is 63-80 DEG C, and column bottom temperature is 100-110 DEG C, and emptying temperature is 30-45 DEG C.
The work process of the production system of the methanol rectification that the present embodiment provides is: the crude carbinol in crude carbinol storage tank 8 is after de-ether tower preheater 7 preheating, send into de-ether tower 6, the top exit of de-ether tower 6 material out cools down through de-ether tower cooler device 3, enter de-ether tower backflash 2 afterwards, for the ease of removing the impurity in crude carbinol, according to the principle extracted, soft water is constantly added in de-ether tower backflash 2, it is back to again in de-ether tower 6 by the backflow import of de-ether tower 6 after liquid in de-ether tower backflash 2, the soft water added mixes with crude carbinol, extracting rectifying in de-ether tower 6, fractionation operation principle is relied on to remove the gas that in crude carbinol, lower boiling Hydrocarbon and a part are dissolved, the fixed gas produced in de-ether tower cooler device 3 and de-ether tower backflash 2 empties after de-ether tower liquid seal trough 4 again；Crude carbinol is after de-ether tower 6 processes, in the bottom of de-ether tower 6, the discharging quality according to discharging opening, the feeding atmospheric distillation tower 13 that purity is high, feeding compression rectification tower preheater 9 that purity is low is heated enters back into compression rectification tower 10 rectification process, and the kettle base solution of de-ether tower 6 is collected into accident groove 17；Compression rectification tower 10 liquid of top of the tower enters atmospheric distillation tower reboiler 12 heat exchange, utilize compression rectification tower 10 liquid of top of the tower heating atmospheric distillation tower reboiler 12, compression rectification tower 10 liquid of top of the tower of cooling enters compression rectification tower backflash 11, rear portion be back to compression rectification tower 10 and reflux, the pressurized rectifying column extraction cooler 15 of another part cools down further, up-to-standard through quality inspection, enters essence alcohol groove 16 as refined methanol product, quality inspection is defective, entrance accident groove 17；Liquid at the bottom of the tower of compression rectification tower 10 sends into the further rectification and purification of atmospheric distillation tower 13, the kettle base solution of compression rectification tower 10 enters accident groove 17, the liquid of top of the tower of atmospheric distillation tower 13 enters atmospheric distillation tower cooler device 19 and cools down, enter atmospheric distillation tower backflash 18 afterwards, then partly return back to atmospheric distillation tower 13 reflux, another part cools down through refined methanol condenser 20, the also extraction of the product of atmospheric distillation tower 13 cools down to refined methanol condenser 20, after up-to-standard through quality inspection, essence alcohol groove 16 is entered as refined methanol product, quality inspection is defective, entrance accident groove 17；The fixed gas that atmospheric distillation tower cooler device 19 produces empties after atmospheric distillation tower liquid seal trough 5, and the kettle base solution of atmospheric distillation tower 13 is also collected into accident groove 17.
De-ether tower liquid seal trough 4 and atmospheric distillation tower liquid seal trough 5 are regularly back to de-ether tower backflash 2 and use.
It is connected with Alcohols,fusel storage tank 14 in the bottom of atmospheric distillation tower 13, is collected Alcohols,fusel processing.Owing to the boiling point of Alcohols,fusel is between first alcohol and water, therefore, all it is difficult to it to remove from tower top and tower reactor, in tower on the column plate of bottom, Alcohols,fusel builds up the quality that can affect methanol product, therefore, it is provided with Alcohols,fusel storage tank 14, for extraction Alcohols,fusel in the bottom of tower.
The production system of methanol rectification that the present embodiment provides, what arrange compression rectification tower and atmospheric distillation tower two tower distillation operation is primarily intended to for steam saving, reduces energy consumption；Utilize the condensation heat of methanol steam of compression rectification column overhead as the thermal source of atmospheric distillation tower reboiler, significantly reduce the consumption of steam.Theoretically, the steam consumption of two tower distillation operations can save half than single tower distillation.Meanwhile, the production system of the methanol rectification that the present embodiment provides also improves the purity of refined methanol product.
Claims (6)
- null1. the production system of a methanol rectification，It is characterized in that，Including crude carbinol storage tank，Crude carbinol storage tank is connected with de-ether tower preheater，De-ether tower preheater is connected with the crude carbinol charging aperture of de-ether tower，The top exit of de-ether tower is connected with de-ether tower cooler device，The connection of de-ether tower cooler device bottom arranges de-ether tower backflash，Described de-ether tower backflash is connected with demineralized water tank and de-ether tower backflow import respectively by pipeline，Described de-ether tower cooler device and described de-ether tower backflash are provided with fixed gas outlet，The fixed gas outlet of de-ether tower cooler device and de-ether tower backflash is all connected with de-ether tower liquid seal trough，The bottom of described de-ether tower is connected with compression rectification tower preheater and atmospheric distillation tower charging aperture respectively by discharge nozzle，The kettle base solution outlet of described de-ether tower is connected with accident groove，Described compression rectification tower preheater is connected with compression rectification tower charging aperture by pipeline，The liquid of top of the tower outlet of described compression rectification tower is connected with the atmospheric distillation tower reboiler of atmospheric distillation tower，Atmospheric distillation tower reboiler is connected with compression rectification tower backflash，Compression rectification tower backflash is connected with compression rectification tower backflow import and compression rectification tower extraction cooler respectively by pipeline，Liquid outlet at the bottom of the tower of described compression rectification tower is connected with the charging aperture of atmospheric distillation tower，The kettle base solution outlet of compression rectification tower is connected with accident groove，The liquid of top of the tower outlet of atmospheric distillation tower is connected with atmospheric distillation tower cooler device，Atmospheric distillation tower cooler device is connected with atmospheric distillation tower backflash by pipeline，Atmospheric distillation tower backflash is connected with the backflow import of atmospheric distillation tower and refined methanol condenser respectively，The product extraction mouth of atmospheric distillation tower is connected with described refined methanol condenser，Described refined methanol condenser is connected with essence alcohol groove and accident groove respectively by pipeline，Described compression rectification tower extraction cooler is connected with described essence alcohol groove and accident groove respectively by pipeline，Described atmospheric distillation tower cooler device is provided with fixed gas outlet，The fixed gas outlet of atmospheric distillation tower cooler device is connected with atmospheric distillation tower liquid seal trough，The kettle base solution outlet of described atmospheric distillation tower is connected with accident groove.
- 2. the production system of methanol rectification according to claim 1, it is characterised in that described de-ether tower liquid seal trough and described atmospheric distillation tower liquid seal trough are all connected with de-ether tower backflash by pipeline.
- 3. the production system of methanol rectification according to claim 2, it is characterised in that the bottom of described atmospheric distillation tower is connected with Alcohols,fusel storage tank.
- 4. the production system according to the arbitrary described methanol rectification of claim 1-3, it is characterised in that the tower top temperature of described de-ether tower is 65-75 DEG C, and column bottom temperature is 65-80 DEG C, and emptying temperature is 35-55 DEG C.
- 5. the production system of methanol rectification according to claim 4, it is characterised in that the tower top temperature of described compression rectification tower is 110-120 DEG C, and column bottom temperature is 123-130 DEG C, pressure reduction 0.16MPa.
- 6. the production system of methanol rectification according to claim 5, it is characterised in that the tower top temperature of described atmospheric distillation tower is 63-80 DEG C, and column bottom temperature is 100-110 DEG C, and emptying temperature is 30-45 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620213697.5U CN205398515U (en) | 2016-03-18 | 2016-03-18 | Production system of methyl alcohol rectification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620213697.5U CN205398515U (en) | 2016-03-18 | 2016-03-18 | Production system of methyl alcohol rectification |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205398515U true CN205398515U (en) | 2016-07-27 |
Family
ID=56423490
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620213697.5U Expired - Fee Related CN205398515U (en) | 2016-03-18 | 2016-03-18 | Production system of methyl alcohol rectification |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205398515U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111450571A (en) * | 2020-03-17 | 2020-07-28 | 安徽晋煤中能化工股份有限公司 | System for realizing continuous extraction of methanol oil by double-effect utilization of extraction water |
-
2016
- 2016-03-18 CN CN201620213697.5U patent/CN205398515U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111450571A (en) * | 2020-03-17 | 2020-07-28 | 安徽晋煤中能化工股份有限公司 | System for realizing continuous extraction of methanol oil by double-effect utilization of extraction water |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102190559B (en) | Method and device for refining methanol by using divided wall distillation column | |
| CN102320671B (en) | Method for treating waste water containing acid and ammonia | |
| CN1736527A (en) | Alcohol quinque-towel differential pressure distilling arrangement and technique thereof | |
| CN203007175U (en) | Heat integration device for methanol synthesis and rectification | |
| CN201482235U (en) | Ethanol distillation tower with energy saving control device | |
| CN102580338A (en) | Device and method for continuously rectifying 3-chloropropyl triethoxysilane | |
| CN101475435A (en) | Method for preparing industrial naphthalin by single-furnace double-tower vacuum distillation | |
| CN110698325A (en) | Production device and process for co-producing fuel ethanol and special grade edible alcohol | |
| CN205398515U (en) | Production system of methyl alcohol rectification | |
| CN106746118A (en) | A kind of system and method for utilization heat recovery from sewage alcohol ketone | |
| CN104086367B (en) | The processing method that methyl alcohol double tower double-effect rectification is energy-conservation | |
| CN103396297A (en) | Thermal coupling energy saving system and operation method for recovering organism from propylene epoxidation reaction wastewater | |
| CN102489030A (en) | Three-tower energy-saving differential pressure alcohol distillation production system and technological process thereof | |
| CN102886151B (en) | Device and method for recovering heat from three-tower methanol rectification | |
| CN104355345B (en) | A kind of negative pressure ammonia still and ammonia still process method | |
| CN204265469U (en) | A kind of negative pressure ammonia still | |
| CN205099600U (en) | Fuel ethanol purification system | |
| CN115212600A (en) | Energy-conserving high-efficient type cyclohexanone refined system | |
| CN212881084U (en) | Distilling device for purifying miscellaneous wine | |
| CN103184133B (en) | Method and special system for forced reflux of brandy/fruit wine for distillation | |
| CN210314061U (en) | Rectification and purification device for synthesizing dimethyl oxalate by carbonylation of coal-made ethylene glycol | |
| CN102080038A (en) | Alcohol distillation process | |
| CN205076831U (en) | Phenol ammonia sewage treatment economic benefits and social benefits rectification system | |
| CN106636223A (en) | Processing method for utilizing cassava residue and cassava to produce alcohol | |
| CN202989109U (en) | Novel reboiling device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160727 Termination date: 20180318 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |