CN203419863U - Thermal coupling energy-saving system for reclaiming organic matters from propylene epoxidation waste water - Google Patents
Thermal coupling energy-saving system for reclaiming organic matters from propylene epoxidation waste water Download PDFInfo
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- CN203419863U CN203419863U CN201320462107.9U CN201320462107U CN203419863U CN 203419863 U CN203419863 U CN 203419863U CN 201320462107 U CN201320462107 U CN 201320462107U CN 203419863 U CN203419863 U CN 203419863U
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- tower
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The utility model relates to a thermal coupling energy-saving system for reclaiming organic matters from propylene epoxidation waste water. The thermal coupling energy-saving system adopts the structure that a steam pipe at the top of a pressurizing tower C2 is connected with the hot end of a light-off tower reboiler E1, and a liquid pipeline at the cold end of the light-off tower reboiler E1 is connected with a pressurizing tower C2 return tank V2; a light-off tower C1 is provided with a raw material waste water inlet, the outlet pipeline in the light-off tower C1, which extracts a propylene glycol monomethyl ether-water mixture 3 in a sliding manner, is connected with a material inlet preheater E3, the material outlet of the preheater E3 is connected with the pressurizing tower C2, and the heating pipeline of the preheater E3 is connected with a waste pipeline discharged out of the tower kettle of the pressurizing tower C2. Through the utilization of heat exchange of two materials together, thermal coupling of the two towers is realized; the propylene glycol monomethyl ether-water mixture is extracted at the lower part of the light-off tower in a sliding manner and serves as the incoming charge of the pressurizing tower after being heated by waste water discharged out of the tower kettle of the pressurizing tower; as the ether-water mixture is extracted in the light-off tower in a sliding manner and most waste water is dicharged, the energy consumption of the system is reduced.
Description
Technical field
The utility model belongs to distillation technology field, relate to a kind of organic thermal coupling energy-saving emission-reducing process that reclaims from production of propylene oxide waste water, particularly relate to a kind of waste water producing from propylene hydrogen peroxide oxidation method (HPPO method) device and reclaim organic thermal coupling energy-saving system and working method.
Background technology
By the novel process (being HPPO method) of hydrogen peroxide (hydrogen peroxide) catalysis epoxidation propylene propylene oxide processed, main propylene oxide and the water of generating in production process, technical process is simple, and product yield is high, substantially pollution-free, belongs to eco-friendly process for cleanly preparing.(former Degussa Degussa) is carrying out HPPO method production propylene oxide industrialization technology with Wood (Uhde) company, DOW Chemical and BASF (BASF) company and is promoting to win at present wound industrial group.
Win wound HPPO technology and be seen in patent WO2011017402A1, WO2012076538A1, US2012142950A1 etc.
From HPPO technique, generally in tubular reactor, carry out, use methyl alcohol as solvent, Ti-Si catalyst as TS-1 be catalyzer, propylene adopts H
2o
2by epoxidation, generate propylene oxide.Propylene oxide can react with methyl alcohol and generate by product propylene glycol monomethyl ether.Due to the asymmetry of propylene oxide molecule, there is the difference of open loop direction, so the propylene glycol monomethyl ether by product producing is two kinds of isomer.Final aqueous stream will contain the light constituents such as the propylene glycol monomethyl ether heavy constituent of 5% left and right and methyl alcohol.If directly discharge, certainly will cause large environmental pollution; If send sewage disposal, certainly will increase processing cost again; If can be from waste water the economic organism such as recovery propylene glycol monomethyl ether, be conducive to environmental friendliness can reduce production costs again, and the utilization that obtains of the propylene glycol monomethyl ether that makes to reclaim, turn waste into wealth.
But because wastewater flow rate is large, reclaim constituent concentration low, process energy consumption high, and can there is azeotropic in propylene glycol monomethyl ether and water, use conventional rectificating method to be difficult to obtain qualified propylene glycol monomethyl ether product.In existing documents and materials, in order to solve water multipotency, consume high problem, conventionally adopt and before separated, use the methods such as pervaporation to remove part moisture (Zhang Xiaoying ，Deng Xinhua, Sun Yuan, the SiO in raw material
2fill PDMS membrane sepn propylene glycol monomethyl ether/aqueous solution, polymer material science and engineering, 2009,25(4), 159-162).Pervaporation is a kind of new membrane isolation technique of separating liquid mixture, compares with traditional separation method, pollute little, energy consumption is low.Can be used for dehydration of organic solvent, from water, remove the separation between organism and organism.In waste water due to the generation of HPPO method production propylene oxide process, also contain some other materials, and the existence of these materials affects pervaporation efficiency, in addition, pervaporation flux is less, facility investment is very large, and therefore, pervaporation also has at present certain limitation in application.
Summary of the invention
In order to solve the problem of prior art, the utility model is intended by thermal coupling technology, from propylene ring oxidation reaction waste water, reclaim propylene glycol monomethyl ether and the water mixture of light constituent as methyl alcohol and after concentrating, slough so most of water, a small amount of propylene glycol monomethyl ether and aqueous concentrate can further adopt the conventional modes such as azeotropic distillation to purify.Reach and from HPPO waste water, reclaim the organic while of low levels, reduce the energy consumption of whole retrieving arrangement, realize the object of energy-saving and emission-reduction.
The technical solution of the utility model is as follows:
Of the present utility modelly from propylene ring oxidation reaction waste water, reclaim organic thermal coupling energy-saving system, include lightness-removing column C1, pressurizing tower C2; The vapour pipe of pressurizing tower C2 tower top connects the hot junction of lightness-removing column reboiler E1, and the cold junction liquid line of lightness-removing column reboiler E1 connects pressurizing tower C2 return tank V2; Lightness-removing column C1 is provided with the import of raw material waste water, in lightness-removing column C1 tower, side line extraction propylene glycol monomethyl ether-water mixture 3 outlet lines connect material inlet preheater E3, preheater E3 material outlet connects pressurizing tower C2, and preheater E3 heating pipeline connects the waste line that pressurizing tower C2 tower reactor is discharged.
In lightness-removing column C1 tower, side line extraction propylene glycol monomethyl ether-water mixture (3) outlet position is lower than raw material waste water (1) import.
By the decompression operation of lightness-removing column, the pressurized operation of propylene glycol monomethyl ether upgrading tower, heats the liquid phase of lightness-removing column tower reactor with pressurizing tower overhead vapours liberated heat, utilize the coupling heat exchange of these two strands of materials, thereby realize the thermal coupling of two towers; At the bottom of lightness-removing column side line extraction propylene glycol monomethyl ether and water mixture, after the waste water heating of discharging through pressurizing tower tower reactor, be re-used as the charging of pressurizing tower.
The decompression operation of described lightness-removing column is preferably: working pressure is absolute pressure 0.02-0.1MPa.
The pressurized operation of described propylene glycol monomethyl ether upgrading tower is that absolute pressure is preferably 0.1-0.6MPa.
Described preferably refers to the waste water of propylene glycol monomethyl ether content below 10% from propylene ring oxidation reaction waste water.
Feature of the present utility model is: the energy consumption of lightness-removing column and propylene glycol monomethyl ether upgrading tower is larger, and the energy consumption of these two towers is more or less the same, now, the pressure of a tower is suitably improved, through another, his working pressure suitably reduces, the temperature of overhead condensation liquid of pressurizing tower and lightness-removing column tower reactor are boiled more than the difference of temperature of gas phase reaches the minimum thermal temperature difference again, and make pressurizing tower overhead condensation liberated heat and the lightness-removing column tower reactor required heat coupling matching of trying one's best that boils again.Like this, can heat the liquid phase of lightness-removing column tower reactor with pressurizing tower overhead vapours liberated heat, thereby utilize the coupling heat exchange of these two strands of materials to realize the thermal coupling of two towers, realize energy-conservation target.
The utility model has the advantage of:
(1) lightness-removing column reboiler and pressurizing tower condenser are coupled, have reduced low-temperature heat source consumption; (2) side line extraction ether water mixture in lightness-removing column tower, most of waste water is discharged from, and has reduced system energy consumption; (3) the waste water heating that in lightness-removing column tower, side line extraction ether water mixture is discharged via pressurizing tower, sends into follow-up ether separation system, takes full advantage of heat energy.
Accompanying drawing explanation
Fig. 1: reclaim organic thermal coupling energy-saving system schematic diagram from propylene ring oxidation reaction waste water;
Fig. 2: comparative example schematic diagram;
In figure: S is that heating medium enters, SC is that heating medium goes out.
In accompanying drawing, the list of parts of each label representative is as follows: C1 lightness-removing column, C2 pressurizing tower; E1 lightness-removing column reboiler, E2 condenser of light component removal column, E3 pressurizing tower feed preheater; V1 lightness-removing column C1 return tank, V2 pressurizing tower C2 return tank.
In accompanying drawing, the stream thigh of each label representative is listed as follows: in the charging of 1HPPO waste water raw material, 2 lightness-removing column C1 overhead vapours, 3C1 tower, the ether water mixture of side line extraction, 4 lightness-removing column C1 tower reactor waste water discharges, 5 light constituent products (being mainly methyl alcohol etc.), 6 pressurizing tower C2 overhead vapours, 7C2 overhead vapours 6 become after heat exchange that partial condensation liquid or saturated liquid, 8C2 tower reactor waste water are discharged, the 9 ether water azeotropes containing propylene glycol monomethyl ether component.
Embodiment
Below in conjunction with drawings and Examples, describe the utility model in detail.Concerning those skilled in the art, should recognize it is the technology that disclosed technology represents the utility model people institute utility model in the following example, those skilled in the art should be appreciated that, based on these disclosures, in the situation that not departing from the utility model scope, can carry out many changes to specific embodiments disclosed herein, and still can obtain identical or similar results.
Thermal coupling energy-saving system of the present utility model, as shown in Figure 1, includes lightness-removing column C1, pressurizing tower C2; The vapour pipe of pressurizing tower C2 tower top connects the hot junction of lightness-removing column reboiler E1, and the cold junction liquid line of lightness-removing column reboiler E1 connects pressurizing tower C2 return tank V2; Lightness-removing column C1 is provided with the import of raw material waste water, in lightness-removing column C1 tower, side line extraction propylene glycol monomethyl ether-water mixture 3 outlet lines connect material inlet preheater E3, preheater E3 material outlet connects pressurizing tower C2, and preheater E3 heating pipeline connects the waste line that pressurizing tower C2 tower reactor is discharged.
In lightness-removing column C1 tower, side line extraction propylene glycol monomethyl ether-water mixture (3) outlet position is lower than raw material waste water (1) import.
The rising steam 6 of pressurizing tower C2 tower top enters the hot junction of lightness-removing column reboiler E1, and the material of the tower top after heat exchange becomes partial condensation liquid or saturated liquid 7, enters pressurizing tower C2 return tank V2; Raw material waste water 1 enters lightness-removing column C1, and overhead vapours 2 enters C1 return tank V1 through condenser E2, obtains light constituent 5, and tower reactor is discharged waste water 4; In C1 tower, side line extraction propylene glycol monomethyl ether-water mixture 3 enters C2 through preheater E3, waste water 8 heating that E3 is discharged by C2 tower reactor; Enriched material 9 containing propylene glycol monomethyl ether and water enters ether separating unit.
Embodiment 1
As shown in Figure 1.To process 35 tons per hour, to contain propylene glycol monomethyl ether 5%, methyl alcohol, 1%, ethanol 0.02%, 1,3 propylene glycol 0.6% and a small amount of heavy constituent waste water are example, the working pressure of lightness-removing column (lightness-removing column) is suitably reduced to absolute pressure 0.02MPa, and the working pressure of pressurizing tower is absolute pressure 0.1MPa, heats the liquid phase of lightness-removing column tower reactor with pressurizing tower overhead vapours 6 liberated heats by lightness-removing column reboiler E1, utilize the coupling heat exchange of these two strands of materials, thereby realize the thermal coupling of two towers; At the bottom of lightness-removing column side line extraction ether water mixture 3, after the waste water heating of discharging through pressurizing tower tower reactor, (being interchanger E3) enters pressurizing tower more in addition.Reboiler in two towers now, and the thermal load of pressurizing tower feed preheater is as shown in table 1.
Embodiment 2
As shown in Figure 1.To process 35 tons per hour, to contain propylene glycol monomethyl ether 5%, methyl alcohol, 1%, ethanol 0.02%, 1,3 propylene glycol 0.6% and a small amount of heavy constituent waste water are example, the working pressure of lightness-removing column (lightness-removing column) is suitably reduced to absolute pressure 0.08MPa, and the working pressure of pressurizing tower suitably rises to absolute pressure 0.2MPa, heats the liquid phase of lightness-removing column tower reactor with pressurizing tower overhead vapours 6 liberated heats by lightness-removing column reboiler E1, utilize the coupling heat exchange of these two strands of materials, thereby realize the thermal coupling of two towers; At the bottom of lightness-removing column side line extraction ether water mixture 3, after the waste water heating of discharging through pressurizing tower tower reactor, (being interchanger E3) enters pressurizing tower more in addition.Reboiler in two towers now, and the thermal load of pressurizing tower feed preheater is as shown in table 1.
As shown in Figure 1.To process 35 tons per hour, to contain propylene glycol monomethyl ether 5%, methyl alcohol, 1%, ethanol 0.02%, 1,3 propylene glycol 0.6% and a small amount of heavy constituent waste water are example, the working pressure of lightness-removing column (lightness-removing column) is absolute pressure 0.1MPa, and the working pressure of pressurizing tower suitably rises to absolute pressure 0.6MPa, heats the liquid phase of lightness-removing column tower reactor with pressurizing tower overhead vapours 6 liberated heats by lightness-removing column reboiler E1, utilize the coupling heat exchange of these two strands of materials, thereby realize the thermal coupling of two towers; At the bottom of lightness-removing column side line extraction ether water mixture 3, after the waste water heating of discharging through pressurizing tower tower reactor, (being interchanger E3) enters pressurizing tower more in addition.Reboiler in two towers now, and the thermal load of pressurizing tower feed preheater is as shown in table 1.
Comparative example 1
Adopt the non-thermal coupling technique of tradition as shown in Figure 2.The 35 tons of waste water per hour of take are example, and the working pressure of lightness-removing column is absolute pressure 0.1MPa, and the working pressure of pressurizing tower is absolute pressure 0.1MPa, at the bottom of lightness-removing column side line extraction ether water mixture 3, directly send into pressurizing tower in addition.The thermal load of the reboiler in two towers is now as shown in table 1.
Each interchanger of table 1 (or reboiler, interchanger) thermal load and energy-conservation
Claims (2)
1. from propylene ring oxidation reaction waste water, reclaim an organic thermal coupling energy-saving system, include lightness-removing column (C1), pressurizing tower (C2); It is characterized in that the vapour pipe of pressurizing tower (C2) tower top connects the hot junction of lightness-removing column reboiler (E1), the cold junction liquid line of lightness-removing column reboiler (E1) connects pressurizing tower (C2) return tank (V2); Lightness-removing column (C1) is provided with the import of raw material waste water, in lightness-removing column (C1) tower, side line extraction propylene glycol monomethyl ether-water mixture (3) outlet line connects material inlet preheater (E3), preheater (E3) material outlet connects pressurizing tower (C2), and preheater (E3) heating pipeline connects the waste line that pressurizing tower (C2) tower reactor is discharged.
2. the system as claimed in claim 1, is characterized in that in lightness-removing column (C1) tower that side line extraction propylene glycol monomethyl ether-water mixture (3) outlet position is lower than raw material waste water (1) import.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320462107.9U CN203419863U (en) | 2013-07-30 | 2013-07-30 | Thermal coupling energy-saving system for reclaiming organic matters from propylene epoxidation waste water |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201320462107.9U CN203419863U (en) | 2013-07-30 | 2013-07-30 | Thermal coupling energy-saving system for reclaiming organic matters from propylene epoxidation waste water |
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| CN203419863U true CN203419863U (en) | 2014-02-05 |
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| CN201320462107.9U Expired - Fee Related CN203419863U (en) | 2013-07-30 | 2013-07-30 | Thermal coupling energy-saving system for reclaiming organic matters from propylene epoxidation waste water |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103396297A (en) * | 2013-07-30 | 2013-11-20 | 天津大学 | Thermal coupling energy saving system and operation method for recovering organism from propylene epoxidation reaction wastewater |
| CN110606799A (en) * | 2019-10-31 | 2019-12-24 | 胜帮科技股份有限公司 | System and method for recycling byproducts generated in production of propylene oxide by HPPO (propylene oxide process) |
| CN111559819A (en) * | 2020-04-30 | 2020-08-21 | 常州瑞华化工工程技术股份有限公司 | Method for recovering propylene glycol and other organic matters from propylene epoxidation alkaline washing wastewater |
| CN113135817A (en) * | 2021-04-22 | 2021-07-20 | 中建安装集团有限公司 | Method for recovering ether alcohol from wastewater generated in process of preparing epoxypropane by oxidizing propylene with hydrogen peroxide |
| CN110606799B (en) * | 2019-10-31 | 2024-04-26 | 胜帮科技股份有限公司 | System and method for recycling byproduct of propylene oxide production by HPPO method |
-
2013
- 2013-07-30 CN CN201320462107.9U patent/CN203419863U/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103396297A (en) * | 2013-07-30 | 2013-11-20 | 天津大学 | Thermal coupling energy saving system and operation method for recovering organism from propylene epoxidation reaction wastewater |
| CN103396297B (en) * | 2013-07-30 | 2017-05-10 | 天津大学 | Thermal coupling energy saving system and operation method for recovering organism from propylene epoxidation reaction wastewater |
| CN110606799A (en) * | 2019-10-31 | 2019-12-24 | 胜帮科技股份有限公司 | System and method for recycling byproducts generated in production of propylene oxide by HPPO (propylene oxide process) |
| CN110606799B (en) * | 2019-10-31 | 2024-04-26 | 胜帮科技股份有限公司 | System and method for recycling byproduct of propylene oxide production by HPPO method |
| CN111559819A (en) * | 2020-04-30 | 2020-08-21 | 常州瑞华化工工程技术股份有限公司 | Method for recovering propylene glycol and other organic matters from propylene epoxidation alkaline washing wastewater |
| CN113135817A (en) * | 2021-04-22 | 2021-07-20 | 中建安装集团有限公司 | Method for recovering ether alcohol from wastewater generated in process of preparing epoxypropane by oxidizing propylene with hydrogen peroxide |
| CN113135817B (en) * | 2021-04-22 | 2023-04-18 | 中建安装集团有限公司 | Method for recovering ether alcohol from wastewater generated in process of preparing epoxypropane by oxidizing propylene with hydrogen peroxide |
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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: 20140205 Termination date: 20160730 |
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| CF01 | Termination of patent right due to non-payment of annual fee |