CN204125402U - A kind of process unit reclaimed for by product propylene glycol monomethyl ether in methylcarbonate production - Google Patents
A kind of process unit reclaimed for by product propylene glycol monomethyl ether in methylcarbonate production Download PDFInfo
- Publication number
- CN204125402U CN204125402U CN201420437661.6U CN201420437661U CN204125402U CN 204125402 U CN204125402 U CN 204125402U CN 201420437661 U CN201420437661 U CN 201420437661U CN 204125402 U CN204125402 U CN 204125402U
- Authority
- CN
- China
- Prior art keywords
- tower
- product
- dehydrogenation
- condenser
- treating
- 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.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a kind of process unit reclaimed for by product propylene glycol monomethyl ether in methylcarbonate production.Technical scheme is: raw material storage tank is connected to dehydrogenation tower by pipeline, and the top of dehydrogenation tower connects dehydrogenation tower condenser, and the output terminal of dehydrogenation tower condenser is connected to dehydrogenation tower return tank, and dehydrogenation tower return tank is connected to dehydrogenation tower by pipeline and forms circulation; The output terminal of described dehydrogenation tower is connected to product purification tower by dehydrogenation tower transferpump, the top of described product purification tower connects treating tower condenser, treating tower condenser is connected to product purification tower by treating tower return tank and forms circulation, the middle part of described product purification tower is connected to product tundish, and product tundish are connected to treating tower product condenser by treating tower product transferpump and obtain propylene glycol monomethyl ether.Beneficial effect is: the benefit substantially increasing carbonate device, adopts continuous production technology, solves complex operation, and energy consumption is high obtains defect, environmentally safe.
Description
Technical field
The utility model relates to a kind of propylene glycol monomethyl ether retrieving arrangement, particularly a kind of process unit reclaimed for by product propylene glycol monomethyl ether in methylcarbonate production.
Background technology
Propylene glycol monomethyl ether is referred to as again propylene glycol monomethyl ether or 2-hydroxypropyl-methyl ether, is one of Main Derivatives of propylene oxide, has purposes widely.Propylene glycol monomethyl ether mainly reacts obtained by propylene oxide and methyl alcohol under catalyst action, and carbonate device generates a small amount of propylene glycol monomethyl ether in synthetic reaction process.
In current preparation facilities, Problems existing is: methylcarbonate production equipment is in joint production of propylene glycol process, understand some propylene glycol monomethyl ether by-product, the thick propylene glycol monomethyl ether material separated in methylcarbonate and propylene glycol purification process directly takes out sale as alcohol mixture always, of poor quality, price is low.The thick propylene glycol monomethyl ether device of existing purification carbonate device by product, adopts batch fractionating mostly, there is high, the ropy problem of energy consumption.
Summary of the invention
The purpose of this utility model is exactly in view of the foregoing defects the prior art has, a kind of process unit reclaimed for by product propylene glycol monomethyl ether in methylcarbonate production is provided, have employed one can industrialized continuous rectification apparatus, by control tower operating parameters, high-quality propylene glycol monomethyl ether can be obtained, improve the economic benefit of device.
Its technical scheme is: comprise raw material storage tank, dehydrogenation tower, dehydrogenation tower condenser, dehydrogenation tower return tank, product purification tower, treating tower condenser, treating tower return tank, product tundish, treating tower product condenser, described raw material storage tank is connected to dehydrogenation tower by pipeline, the top of dehydrogenation tower connects dehydrogenation tower condenser, the output terminal of dehydrogenation tower condenser is connected to dehydrogenation tower return tank, and dehydrogenation tower return tank is connected to dehydrogenation tower by pipeline and forms circulation; The output terminal of described dehydrogenation tower is connected to product purification tower by dehydrogenation tower transferpump, the top of described product purification tower connects treating tower condenser, treating tower condenser is connected to product purification tower by treating tower return tank and forms circulation, the middle part of described product purification tower is connected to product tundish, and product tundish are connected to treating tower product condenser by treating tower product transferpump and obtain propylene glycol monomethyl ether.
The bottom of above-mentioned dehydrogenation tower connects dehydrogenation tower reboiler.
The bottom of above-mentioned product purification tower connects treating tower reboiler.
The beneficial effects of the utility model are: the utility model successfully solves the recovery purification problem of carbonate device by product propylene glycol monomethyl ether, propylene glycol monomethyl ether purity after refining purification reaches more than 99.5%, indices all reaches the index request of technical grade propylene glycol monomethyl ether, substantially increases the benefit of carbonate device.Meanwhile, adopt continuous production technology, solve complex operation, energy consumption is high obtains defect, environmentally safe.
Accompanying drawing explanation
Accompanying drawing 1 is structural representation of the present utility model;
In upper figure: transferpump 15, treating tower product transferpump 16, treating tower reflux pump 17 at the bottom of raw material storage tank 1, dehydrogenation tower 2, dehydrogenation tower condenser 3, dehydrogenation tower return tank 4, product purification tower 5, treating tower condenser 6, treating tower return tank 7, product tundish 8, treating tower product condenser 9, fresh feed pump 10, dehydrogenation tower reboiler 11, dehydrogenation tower reflux pump 12, dehydrogenation tower transferpump 13, treating tower reboiler 14, treating tower tower.
Embodiment
By reference to the accompanying drawings 1, the utility model will be further described:
The utility model comprises raw material storage tank 1, dehydrogenation tower 2, dehydrogenation tower condenser 3, dehydrogenation tower return tank 4, product purification tower 5, treating tower condenser 6, treating tower return tank 7, product tundish 8, treating tower product condenser 9, described raw material storage tank 1 is connected to dehydrogenation tower 2 by pipeline, the top of dehydrogenation tower 2 connects dehydrogenation tower condenser 3, the output terminal of dehydrogenation tower condenser 3 is connected to dehydrogenation tower return tank 4, and dehydrogenation tower return tank 4 is connected to dehydrogenation tower 2 by pipeline and forms circulation; The output terminal of described dehydrogenation tower 2 is connected to product purification tower 5 by dehydrogenation tower transferpump 13, the top of described product purification tower 5 connects treating tower condenser 6, treating tower condenser 6 is connected to product purification tower 5 by treating tower return tank 7 and forms circulation, the middle part of described product purification tower 5 is connected to product tundish 8, and product tundish 8 are connected to treating tower product condenser 9 by treating tower product transferpump 16 and obtain propylene glycol monomethyl ether.
Wherein, the bottom of dehydrogenation tower 2 connects dehydrogenation tower reboiler 11, and the bottom of above-mentioned product purification tower 5 connects treating tower reboiler 14.
Concrete making step is as follows:
Step 1: the collection of the thick propylene glycol monomethyl ether of carbonate device by product:
Thick propylene glycol monomethyl ether material from carbonate device refinement refining methanol tower tower reactor stores to raw material storage tank 1 through pump delivery.
Step 2: propylene glycol monomethyl ether is de-light:
From the propylene glycol monomethyl ether crude product in step 1 through fresh feed pump 10, be delivered in propylene glycol monomethyl ether dehydrogenation tower 2, control inlet amount 1500Kg/h.Control dehydrogenation tower 2 bottom temperature at 125 DEG C, tower top temperature 98 DEG C, tower top pressure 100KPa, control of reflux ratio is 7.Material in dehydrogenation tower is mainly propylene glycol monomethyl ether, is delivered to propylene glycol monomethyl ether treating tower 5 through dehydrogenation tower transferpump 13, controls load at about 1190Kg/h.
Step 3: propylene glycol monomethyl ether is refined:
In product purification tower 5, refining purification is carried out from the propylene glycol monomethyl ether crude product in step 2.Control this column overhead service temperature: 115 DEG C, top side line dipropylene glycol drop temperature 122 DEG C, tower reactor service temperature 150 DEG C, tower top working pressure 100KPa, control of reflux ratio: 15.The propylene glycol monomethyl ether crude product containing light constituent that tower top obtains returns in step 2.Propylene glycol monomethyl ether carries out extraction by rectifying tower side line, and purity can reach more than 99.5%, after cooling, enter propylene glycol monomethyl ether finished product tank field.
Claims (3)
1. the process unit reclaimed for by product propylene glycol monomethyl ether in methylcarbonate production, it is characterized in that: comprise raw material storage tank (1), dehydrogenation tower (2), dehydrogenation tower condenser (3), dehydrogenation tower return tank (4), product purification tower (5), treating tower condenser (6), treating tower return tank (7), product tundish (8), treating tower product condenser (9), described raw material storage tank (1) is connected to dehydrogenation tower (2) by pipeline, the top of dehydrogenation tower (2) connects dehydrogenation tower condenser (3), the output terminal of dehydrogenation tower condenser (3) is connected to dehydrogenation tower return tank (4), dehydrogenation tower return tank (4) is connected to dehydrogenation tower (2) by pipeline and forms circulation, the output terminal of described dehydrogenation tower (2) is connected to product purification tower (5) by dehydrogenation tower transferpump (13), the top of described product purification tower (5) connects treating tower condenser (6), treating tower condenser (6) is connected to product purification tower (5) by treating tower return tank (7) and forms circulation, the middle part of described product purification tower (5) is connected to product tundish (8), and product tundish (8) are connected to treating tower product condenser (9) by treating tower product transferpump (16) and obtain propylene glycol monomethyl ether.
2. the process unit reclaimed for by product propylene glycol monomethyl ether in methylcarbonate production according to claim 1, is characterized in that: the bottom of described dehydrogenation tower (2) connects dehydrogenation tower reboiler (11).
3. the process unit reclaimed for by product propylene glycol monomethyl ether in methylcarbonate production according to claim 1, is characterized in that: the bottom of described product purification tower (5) connects treating tower reboiler (14).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420437661.6U CN204125402U (en) | 2014-08-05 | 2014-08-05 | A kind of process unit reclaimed for by product propylene glycol monomethyl ether in methylcarbonate production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420437661.6U CN204125402U (en) | 2014-08-05 | 2014-08-05 | A kind of process unit reclaimed for by product propylene glycol monomethyl ether in methylcarbonate production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204125402U true CN204125402U (en) | 2015-01-28 |
Family
ID=52381775
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420437661.6U Active CN204125402U (en) | 2014-08-05 | 2014-08-05 | A kind of process unit reclaimed for by product propylene glycol monomethyl ether in methylcarbonate production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204125402U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114230465A (en) * | 2021-12-13 | 2022-03-25 | 郑州中科新兴产业技术研究院 | Process for separating dimethyl carbonate and methanol azeotropic mixture |
-
2014
- 2014-08-05 CN CN201420437661.6U patent/CN204125402U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114230465A (en) * | 2021-12-13 | 2022-03-25 | 郑州中科新兴产业技术研究院 | Process for separating dimethyl carbonate and methanol azeotropic mixture |
| CN114230465B (en) * | 2021-12-13 | 2024-01-26 | 郑州中科新兴产业技术研究院 | Process for separating dimethyl carbonate and methanol azeotropic mixture |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101239886B (en) | Method for separating and reclaiming organic matter from high-temperature Fischer-Tropsch synthesis reaction water | |
| CN102633588B (en) | Method for preparing high-purity isobutene from raffinate C4 by means of separation | |
| CN101830799A (en) | Single-tower rectifying method for synthetizing ethyl acetate by esterification method | |
| CN101376630B (en) | Intermittent reaction rectification method and apparatus for synthesizing methyl formate | |
| CN105461515B (en) | A kind of method that cyclopentanol is prepared by cyclopentene | |
| CN103012332B (en) | Use the method for packing tower distillation separation of tetrahydrofuran-methanol-water solvent slop | |
| CN204125402U (en) | A kind of process unit reclaimed for by product propylene glycol monomethyl ether in methylcarbonate production | |
| CN104974034A (en) | Method of two-column separation of benzoic acid, benzaldehyde and methylbenzene | |
| CN102093176B (en) | Method for extracting and separating methylal-methanol mixture by using continuous countercurrent rotating disk | |
| CN102898321B (en) | A kind of method preparing N-fourth oxygen butoxalyl-alaninate | |
| CN106146299B (en) | The method for producing acetic acid esters and ethylene glycol | |
| CN105037155A (en) | Batch distillation process for separating tert-butyl alcohol-methyl propionate azeotrope by mixed extractant | |
| CN203639370U (en) | Continuous rectification system for m-toluic acid | |
| CN202526927U (en) | Device for producing high-purity benzene methanol | |
| CN104829451B (en) | Combined production method for acetic acid ester and glycol | |
| CN105481643B (en) | The method that the pentanediol diisobutyrate of 2,2,4 trimethyl 1,3 is prepared by Qing Ye oxanes | |
| CN204111623U (en) | A kind of process unit of purifying for by product diisopropyl ether in Virahol production | |
| CN103508886A (en) | Continuous production method for ethyl 2-methylbutyrate | |
| CN101250082A (en) | Preparation method of alpha-methylnaphthalene | |
| CN202415410U (en) | Multi-tower continuous operation system device for synthesizing methyl 3,3-dimethyl pentenoate | |
| CN104418734B (en) | From the industrial by-product of terephthalic acid (TPA), directly extract the method for high-purity methyl acetate | |
| CN102701920A (en) | Method for purifying vinyl isobutyl ether | |
| CN103613504B (en) | Be the method that methylcarbonate prepared by raw material with carbonic acid third (second) alkene ester and methyl alcohol | |
| CN107903150B (en) | Method for producing sec-butyl alcohol by continuous hydrolysis | |
| CN203382693U (en) | Device for synthesizing dipropylene glycol and co-produced tripropylene glycol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: 257000 23 Zoucheng Road, Shengli Industrial Park, Dongying District, Dongying City, Shandong Province Patentee after: Shandong Haike Xinyuan material technology Co., Ltd Address before: 257000 No. 23, Zoucheng Road, Dongying District, Shandong, Dongying Patentee before: DONGYING HI-TECH SPRING CHEMICAL INDUSTRY Co.,Ltd. |
|
| CP03 | Change of name, title or address |