CN202289880U - Ethylene glycol and dimethyl oxalate concentration and separation device - Google Patents
Ethylene glycol and dimethyl oxalate concentration and separation device Download PDFInfo
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- CN202289880U CN202289880U CN 201120287524 CN201120287524U CN202289880U CN 202289880 U CN202289880 U CN 202289880U CN 201120287524 CN201120287524 CN 201120287524 CN 201120287524 U CN201120287524 U CN 201120287524U CN 202289880 U CN202289880 U CN 202289880U
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- ethylene glycol
- dimethyl oxalate
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- enrichment facility
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Abstract
An ethylene glycol and dimethyl oxalate concentration and separation device comprises an ethylene glycol preconcentration device, a permeation and gasification film concentration device and an ethylene glycol rectification device, wherein a material outlet at the top of the ethylene glycol preconcentration device is communicated with a feed port of the permeation and gasification film concentration device through a pipeline; and a penetrants discharge outlet of the permeation and gasification film concentration device is communicated with the feed port of the ethylene glycol rectification device through a pipeline condenser, and the retaining materials of the permeation and gasification film concentration device are discharged by a retaining material discharge port. The ethylene glycol and dimethyl oxalate concentration and separation device has a simple structure, adopts a permeation and gasification film concentration and separation technology, and cannot be influenced by the azeotropic point of ethylene glycol and dimethyl oxalate, so the azeotrope of ethylene glycol and dimethyl oxalate is effectively separated, and the separation efficiency is high.
Description
Technical field
The utility model relates to the concentrating and separating technical field of ethylene glycol and dimethyl oxalate azeotropic mixture, is specifically related to the concentrating and separating device of a kind of ethylene glycol and dimethyl oxalate.
Background technology
Ethylene glycol is a kind of important Organic Chemicals.At present the yearly productive capacity of China's ethylene glycol is 2,400,000 tons, but annual requirement is more than 7,000,000 tons, and import volume reaches 5,000,000 tons.Traditional ethylene glycol production method is to walk the petrochemical industry route, though technology maturation, wide application, shortcoming is also fairly obvious, and dependence petroleum resources, water consume greatly, cost is high.Along with the minimizing day by day of world petroleum resource, opening up new process route becomes the task of top priority.China's petroleum resources lacks, rich coal resources, and exploitation " coal for replacing oil " technology has become the upsurge of domestic chemical circles.
The coal based synthetic gas preparing ethylene glycol has become a technology of world's common concern.In numerous research directions of " coal for replacing oil " technology; Be called as carbon one (C1) chemical technology with the coal gasification preparing synthetic gas as the further technology of synthetic engine fuel and petroleum chemicals raw material; Be since the seventies in last century oil crisis, one of popular research field of the academic and industrial quarters of chemical.Especially near ten or twenty is over year, because petroleum import increases fast, the C1 chemistry is very fast in China's development.
In coal based synthetic gas preparing ethylene glycol technology; Ethylene glycol is refining to be the key technology that guarantees the ethylene glycol product purity; In the refining isolation technics of numerous ethylene glycol; Conventional distillation technology exists that distillation process is long, the rectifying column height is too high, and the characteristics of rectification effect difference, must gather the needs that the all-in-one-piece separating technology could satisfy the ethylene glycol product purity with other isolation technics.The vaporization infiltration technology has separation and greatly, does not receive vapour-liquid equilibrium restriction, process simple, is applicable to separate separating of closely boil thing and azeotrope that rectifying is difficult to separate.
In the technology of synthesis gas preparing ethylene glycol; Accessory substance is many; And the intermediate product dimethyl oxalate can not be converted into ethylene glycol fully in the process of hydrogenation, in whole process flow, is divided into air separation unit, raw material gas purifying device, glycol unit three parts.Glycol unit by reaction zone, compression subregion, fractionation district, gas purification, supplement production district, etc. form.Fractionation zone oil dealcoholysis, degreasing, take off heavy, take off compositions such as light, product rectifying, recovery and methanol rectification, two esterifications, ammoxidation.
The utility model content
The purpose of the utility model is to provide the concentrating and separating device of a kind of ethylene glycol and dimethyl oxalate, and it is simple and reasonable for structure, and energy consumption is low, can effectively separate with dimethyl oxalate ethylene glycol, and separative efficiency is high.
For realizing above-mentioned purpose; The technical scheme that the utility model adopts is following: the concentrating and separating device of ethylene glycol of the utility model and dimethyl oxalate comprises ethylene glycol pre-concentration device, infiltration vaporization membrane enrichment facility and ethylene glycol rectifier unit, and the material outlet at ethylene glycol pre-concentration device top is communicated with through the charging aperture of pipeline with infiltration vaporization membrane enrichment facility; The penetrant discharging outlet of infiltration vaporization membrane enrichment facility is communicated with the charging aperture of ethylene glycol rectifier unit through tube condenser, and the material of holding back of infiltration vaporization membrane enrichment facility is discharged from holding back material outlet.
Owing to hold back still to contain in the material and do not permeate material on a small quantity; In order to make the further concentrating and separating of material; The charging aperture of material outlet through pipeline and ethylene glycol pre-concentration device of holding back of infiltration evaporation film condensing device is connected, and makes infiltrating and vaporizing membrane hold back concentrated dimethyl oxalate and is back to ethylene glycol pre-concentration device and carries out recycle.
In order to make full use of material, the residue outlet of ethylene glycol rectifier unit is connected through the charging aperture of pipeline with infiltration vaporization membrane enrichment facility, and the residual material after refining passes back into infiltration evaporation film device, recycle.
For the ease of passing through the film material through infiltrating and vaporizing membrane and be convenient to permeate material and get into the ethylene glycol refining plant and make with extra care; The utility model preferably is provided with the vacuum extraction device between infiltration evaporation film condensing device and ethylene glycol refining plant, utilize pumped vacuum systems for the infiltration evaporation film condensing device power to be provided.
Ethylene glycol pre-concentration device described in the utility model is preferably destilling tower.Described ethylene glycol rectifier unit is preferably rectifying column.
The course of work of the utility model is following: ethylene glycol and dimethyl oxalate mixed material are introduced into ethylene glycol pre-concentration destilling tower; Dimethyl oxalate through pre-concentration flows out from the bottom of ethylene glycol pre-concentration destilling tower device, and the entering of the material outlet from ethylene glycol pre-concentration destilling tower top infiltration vaporization membrane enrichment facility further concentrates and the dimethyl oxalate of process pre-concentration is from ethylene glycol mixture.The infiltrating and vaporizing membrane that the utility model is used has the selection trafficability characteristic; Comprising the process of selecting to see through absorption, vaporization and infiltration; The ethylene glycol osmotic vaporizing membrane penetrated preferably gets into the permeable membrane side; Dimethyl oxalate then is trapped within the opposite side of permeable membrane, and the ethylene glycol that sees through infiltrating and vaporizing membrane further is refined into the ethylene glycol finished product through getting into the ethylene glycol rectifier unit after the condenser condenses, and the finished product after making with extra care is discharged through the bottom of ethylene glycol treating column.
The utility model is simple in structure, and it adopts infiltration vaporization membrane concentrating and separating technology, can not receive the influence of ethylene glycol and dimethyl oxalate azeotropic point, and ethylene glycol is effectively separated with the dimethyl oxalate azeotropic mixture, and separative efficiency is high, and production technology is simple.Operating cost is low.
Description of drawings
Fig. 1 is the structural representation of the utility model embodiment 1.
The specific embodiment
The concentrating and separating device of the utility model ethylene glycol and dimethyl oxalate is as shown in Figure 1; Comprise ethylene glycol pre-concentration destilling tower 1, infiltration vaporization membrane enrichment facility 2 and ethylene glycol rectifying column 5, the material outlet at ethylene glycol pre-concentration destilling tower 1 top is communicated with through the charging aperture of pipeline with infiltration vaporization membrane enrichment facility 2; The penetrant discharging outlet of infiltration vaporization membrane enrichment facility 2 is communicated with the charging aperture of ethylene glycol rectifying column 5 through tube condenser 3, and the material of holding back of infiltration vaporization membrane enrichment facility 2 is discharged from holding back material outlet.
Owing to hold back still to contain in the material and do not permeate material on a small quantity; In order to make the further concentrating and separating of material; The charging aperture of material outlet through pipeline and ethylene glycol pre-concentration destilling tower 1 of holding back of infiltration evaporation film condensing device 2 is connected, and makes infiltrating and vaporizing membrane hold back concentrated dimethyl oxalate and is back to ethylene glycol pre-concentration device and carries out recycle.
In order to make full use of material, the residue outlet of ethylene glycol rectifying column is connected through the charging aperture of pipeline with infiltration vaporization membrane enrichment facility 2, and the residual material after refining passes back into infiltration evaporation film device, recycle.
For the ease of passing through the film material through infiltrating and vaporizing membrane and be convenient to permeate material and get into the ethylene glycol rectifier unit and make with extra care; Between infiltration evaporation film condensing device 2 and ethylene glycol rectifying column, be provided with vacuum extraction device 4, utilize pumped vacuum systems power to be provided for the infiltration evaporation film condensing device.
In the present embodiment, also can separate the separation between other accessory substances and ethylene glycol in the synthesis gas synthesizing glycol.
Other parts in the present embodiment can adopt prior art, repeat no more at this.
The course of work of present embodiment is: ethylene glycol and dimethyl oxalate mixed material are introduced into ethylene glycol pre-concentration destilling tower; The dimethyl oxalate of process pre-concentration flows out from the bottom of ethylene glycol pre-concentration destilling tower 1, and further concentrated from the material outlet entering infiltration vaporization membrane enrichment facility 2 at ethylene glycol pre-concentration destilling tower 1 top through the dimethyl oxalate of pre-concentration.The infiltrating and vaporizing membrane that the utility model is used has the selection trafficability characteristic; The ethylene glycol osmotic vaporizing membrane penetrated preferably gets into the permeable membrane side; Dimethyl oxalate then is trapped within the opposite side of permeable membrane; Get into ethylene glycol rectifying column 5 after ethylene glycol process condenser 3 condensations through infiltrating and vaporizing membrane and further be refined into the ethylene glycol finished product, the finished product after making with extra care is discharged through the bottom of ethylene glycol rectifying column 5.Hold back and contain a spot of material that do not permeate in the material, be connected, make infiltrating and vaporizing membrane hold back concentrated dimethyl oxalate and be back to ethylene glycol pre-concentration tower 1 and carry out recycle through the charging aperture of pipeline with ethylene glycol pre-concentration destilling tower 1.
Claims (6)
1. the concentrating and separating device of ethylene glycol and dimethyl oxalate; It is characterized in that: comprise ethylene glycol pre-concentration device, infiltration vaporization membrane enrichment facility and ethylene glycol rectifier unit, the material outlet at ethylene glycol pre-concentration device top is communicated with through the charging aperture of pipeline with infiltration vaporization membrane enrichment facility; The penetrant discharging outlet of infiltration vaporization membrane enrichment facility is communicated with the charging aperture of ethylene glycol rectifier unit through tube condenser, and the material of holding back of infiltration vaporization membrane enrichment facility is discharged from holding back material outlet.
2. according to the concentrating and separating device of right 1 described ethylene glycol and dimethyl oxalate, it is characterized in that: the material outlet of holding back of infiltration vaporization membrane enrichment facility is connected with the charging aperture of ethylene glycol pre-concentration device through pipeline.
3. according to the concentrating and separating device of right 1 or 2 described ethylene glycol and dimethyl oxalate, it is characterized in that: the residue outlet of ethylene glycol rectifier unit is connected through the charging aperture of pipeline with infiltration vaporization membrane enrichment facility.
4. according to the concentrating and separating device of right 1 or 2 described ethylene glycol and dimethyl oxalate, it is characterized in that: be provided with the vacuum extraction device at the penetrant discharging opening of infiltration vaporization membrane enrichment facility and the pipeline between the ethylene glycol rectifier unit.
5. according to the concentrating and separating device of right 1 or 2 described ethylene glycol and dimethyl oxalate, it is characterized in that: described ethylene glycol pre-concentration device is a destilling tower.
6. according to the concentrating and separating device of right 1 or 2 described ethylene glycol and dimethyl oxalate, it is characterized in that: described ethylene glycol rectifier unit is a rectifying column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201120287524 CN202289880U (en) | 2011-08-09 | 2011-08-09 | Ethylene glycol and dimethyl oxalate concentration and separation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201120287524 CN202289880U (en) | 2011-08-09 | 2011-08-09 | Ethylene glycol and dimethyl oxalate concentration and separation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202289880U true CN202289880U (en) | 2012-07-04 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201120287524 Expired - Fee Related CN202289880U (en) | 2011-08-09 | 2011-08-09 | Ethylene glycol and dimethyl oxalate concentration and separation device |
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| CN (1) | CN202289880U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108017517A (en) * | 2017-12-29 | 2018-05-11 | 华东理工大学 | Using the method for azeotropic distillation separating low concentration 1,2- butanediols from ethylene glycol |
| CN108191608A (en) * | 2017-12-29 | 2018-06-22 | 华东理工大学 | Using the method for azeotropic distillation separating low concentration 1,2- propylene glycol from ethylene glycol |
| CN109771981A (en) * | 2019-02-02 | 2019-05-21 | 南京工业大学 | A kind of method of novel energy-saving rectifying-embrane method-rectifying integrated separation azeotropic organic solvent |
-
2011
- 2011-08-09 CN CN 201120287524 patent/CN202289880U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108017517A (en) * | 2017-12-29 | 2018-05-11 | 华东理工大学 | Using the method for azeotropic distillation separating low concentration 1,2- butanediols from ethylene glycol |
| CN108191608A (en) * | 2017-12-29 | 2018-06-22 | 华东理工大学 | Using the method for azeotropic distillation separating low concentration 1,2- propylene glycol from ethylene glycol |
| CN108017517B (en) * | 2017-12-29 | 2020-09-01 | 华东理工大学 | Method for separating low-concentration 1, 2-butanediol from ethylene glycol by azeotropic distillation |
| CN108191608B (en) * | 2017-12-29 | 2020-11-06 | 华东理工大学 | Method for separating low-concentration 1, 2-propylene glycol from ethylene glycol by azeotropic distillation |
| CN109771981A (en) * | 2019-02-02 | 2019-05-21 | 南京工业大学 | A kind of method of novel energy-saving rectifying-embrane method-rectifying integrated separation azeotropic organic solvent |
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| Date | Code | Title | Description |
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| 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: 20120704 Termination date: 20190809 |
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| CF01 | Termination of patent right due to non-payment of annual fee |