CN202786067U - Absorption and rectification device for separating carbon dioxide and epoxypropane mixture - Google Patents
Absorption and rectification device for separating carbon dioxide and epoxypropane mixture Download PDFInfo
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- CN202786067U CN202786067U CN 201220286062 CN201220286062U CN202786067U CN 202786067 U CN202786067 U CN 202786067U CN 201220286062 CN201220286062 CN 201220286062 CN 201220286062 U CN201220286062 U CN 201220286062U CN 202786067 U CN202786067 U CN 202786067U
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- rectifying tower
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Abstract
The utility model relates to an absorption and rectification device for separating a carbon dioxide and epoxypropane mixture. The absorption and rectification device comprises a mixed gas compressor (2), a heat exchanger (4), an absorption tower (6), a rectification tower material inlet pump (9), a rectification tower (11), a rectification tower condenser (13), a rectification tower backflow buffering tank (16) and a rectification tower reboiler (22), and is characterized in that a mixed raw material to be separated enters a system from the mixed gas compressor (2); an outlet of the mixed gas compressor (2) is connected with a material inlet of the absorption tower (6) through a pipeline by the heat exchanger (4); an absorbent inlet and a residual gas phase outlet are formed on the top of the absorption tower (6); and a liquid phase extraction opening is formed in the bottom of the absorption tower (6) and is connected with a material inlet of the rectification tower (11) through the rectification tower material inlet pump (9). The absorption and rectification device has the advantages that the purity of the extracted epoxypropane is high, and the yield is high; the energy consumption in a process can be greatly reduced; and the yearly economical benefit is greatly improved.
Description
Technical field
The utility model relates to carbonic acid gas and propylene oxide mixture separation technical field in the chemical field, particularly relates to the device that unreacted carbonic acid gas and propylene oxide mixture separation purification propylene oxide in the propylene carbonate process are produced in the carbon dioxide-epoxy propane copolymerization.
Background technology
Aliphatic Polycarbonate Copolymers is the type material of a class fully biodegradable, since aboveground auspicious equality first passage carbonic acid gas in 1969 and epoxy compounds reaction synthetic fat adoption carbonic ether, people are being that this research field of Fully-degradable compound has obtained lot of research with carbon dioxide fixation.Wherein carbonic acid gas is widely used in the different chemical field such as synthetic ammonia, natural gas conditioning, hydrogen manufacturing, textile printing and dyeing, oil production, metal extraction, raw lacquer softening agent from the reaction that propylene carbonate is produced in the propylene oxide copolymerization.
Propylene carbonate (PC) is the high bp polar solvent of a kind of very important Organic chemical products and excellent property.In fact pass through CO
2Under catalyst action, synthesize generation propylene carbonate by ring-opening polymerization with propylene oxide.This synthesis mode does not need to use the phosgene of severe toxicity, has greater advantage.The reaction of this copolymerization propylene carbonate can not be carried out remaining reactant CO after reaction is finished fully owing to be subject to the restriction of chemical equilibrium
2Discharge system with propylene oxide with the form of mixture.The direct discharging of residue unreacted reactant not only causes the pollution of environment but also causes the waste of raw material, in order further to reduce production costs, utilizes to greatest extent reactant, to unreacted CO
2Carry out the significant of Separation and Recovery recycling with propylene oxide.
Summary of the invention
The purpose of this utility model provides a kind of CO of being applicable to
2With the absorption-rectifier unit of propylene oxide mixture separation, the absorption-distillation and separation method that uses the utility model to provide, it is simple, easy to operate to have a technical process.The very high and rate of recovery of the purity that the lower and target product product propylene of energy consumption is separated is advantages of higher very.
CO of the present utility model
2With the propylene oxide mixture separation apparatus, wherein charging is CO
2The unreacted CO of residue become the propylene carbonate reaction to finish with epoxypropane copolymerization after
2With the propylene oxide mixture, opening for feed is arranged on the suction port of compressor, and the propylene oxide behind the separating-purifying is from the extraction of rectifying tower cat head, CO
2Discharge from absorption tower tower top outlet and rectifying tower cat head condenser drain.
Technology of the present utility model is as follows:
Device of the present utility model comprises mixed gas compressor (2), interchanger (4), absorption tower (6), rectifying tower fresh feed pump (9), rectifying tower (11), rectifying tower condenser (13), rectifying tower backflow surge tank (16), rectifying tower reboiler (22); It is characterized in that mixing raw material to be separated enters system from mixed gas compressor (2), mixed gas compressor (2) outlet links to each other through the opening for feed of interchanger (4) with absorption tower (6) by pipeline, the top of (6) is provided with absorption agent opening for feed and residue gaseous phase outlet on the absorption tower, being provided with liquid phase at the bottom of the tower of absorption tower (6) just exports, liquid phase extraction mouth is connected with the charging of rectifying tower (11) through rectifying tower fresh feed pump (9) by pipeline, the opening for feed of rectifying tower (11) is arranged on the middle and upper part of rectifying tower (11), rectifying tower (a 11) tower base stream part and the bottom of returning rectifying tower (11) after rectifying tower reboiler (22) is connected, another part converges as the absorption agent feed pipe of absorption agent extraction by pipeline and absorption tower (6).Rectifying tower (11) overhead stream links to each other with rectifying tower backflow surge tank (16) through rectifying tower condenser (13), rectifying tower condenser (13) is provided with drain, rectifying tower backflow surge tank (16) outlet at bottom is provided with feed back and material extraction mouth, and wherein the feed back mouth is connected with rectifying tower (11) top of tower by pipeline.
Wherein absorption system can adopt neat solvent to absorb, and also can adopt double solvents to absorb.
The flow process that operates according to device of the present utility model is: CO
2Enter system with propylene oxide mixed gas feed (1) from the inlet mouth of mixed gas compressor (2), mixed gas after compressed the boosting (3) enters absorption tower (6) through the rear supersaturated mixture body (5) that reduces temperature that forms of interchanger (4) cooling, through the gaseous phase materials (7) after absorption from the absorption tower top gaseous phase outlet discharge system of (6), the liquid phase material (8) that absorbed propylene oxide extraction at the bottom of the tower of absorption tower (6), the liquid phase material (8) of extraction enters rectifying tower (11) behind rectifying tower fresh feed pump (9) at the bottom of the tower of absorption tower (6), rectifying tower top gaseous phase product (12) enters rectifying tower backflow surge tank (16) behind rectifying tower condenser (13), the a part of material of material (17) (18) that flows out from rectifying tower backflow surge tank (16) returns rectifying tower (11) cat head as phegma, another part material (19) is as the product extraction, the a part of material of liquid product at the bottom of the rectifying tower (20) (21) returns at the bottom of rectifying tower (11) tower through rectifying tower reboiler (22), and another part material (24) turns back to absorption tower (6) cat head after converging as absorption agent and fresh absorbent (25).
The compressor outlet absolute pressure is 1-20atm, exchanger heat logistics temperature out is-and 50-100 ℃, the absolute pressure on absorption tower is 0.1-20atm.The rectifying tower reflux ratio is 0.5-8, and the absolute pressure of rectifying tower is 0.1-20atm, the overhead condensation actuator temperature is controlled at-and 50-100 ℃.
The utility model relates to CO
2Absorption-rectifier unit with the propylene oxide mixture separation.CO
2Thereby with the propylene oxide mixture through obtaining propylene oxide entering rectifying tower after the absorption process.The utility model has the advantages that and adopt absorption-rectifier unit, the propene oxide purity of purification is high, yield is large, can greatly reduce the process energy consumption, and a year economic benefit improves greatly.
Description of drawings
Fig. 1 is CO
2With the absorption of propylene oxide mixture-rectification and purification process flow diagram.
Embodiment
Below in conjunction with accompanying drawing device provided by the utility model is further detailed.
The utility model is achieved by the following technical solution:
As shown in Figure 1, mixed gas compressor (2), interchanger (4), absorption tower (6), rectifying tower fresh feed pump (9), rectifying tower (11), rectifying tower condenser (13), rectifying tower backflow surge tank (16), rectifying tower reboiler (22); It is characterized in that: mixing raw material to be separated enters system from mixed gas compressor (2), mixed gas compressor (2) outlet links to each other through the opening for feed of interchanger (4) with absorption tower (6) by pipeline, the top of (6) is provided with absorption agent opening for feed and residue gaseous phase outlet on the absorption tower, being provided with liquid phase at the bottom of the tower of absorption tower (6) just exports, liquid phase extraction mouth is connected with the charging of rectifying tower (11) through rectifying tower fresh feed pump (9) by pipeline, the opening for feed of rectifying tower (11) is arranged on the middle and upper part of rectifying tower (11), rectifying tower (a 11) tower base stream part and the bottom of returning rectifying tower (11) after rectifying tower reboiler (22) is connected, another part converges as the absorption agent feed pipe of absorption agent extraction by pipeline and absorption tower (6).Rectifying tower (11) overhead stream links to each other with rectifying tower backflow surge tank (16) through rectifying tower condenser (13), rectifying tower condenser (13) is provided with drain, rectifying tower backflow surge tank (16) outlet at bottom is provided with feed back and material extraction mouth, and wherein the feed back mouth is connected with rectifying tower (11) top of tower by pipeline.
CO
2Enter system with propylene oxide mixed gas feed (1) from the inlet mouth of mixed gas compressor (2), mixed gas after compressed the boosting (3) enters absorption tower (6) through the rear supersaturated mixture body (5) that reduces temperature that forms of interchanger (4) cooling, through the gaseous phase materials (7) after absorption from the absorption tower top gaseous phase outlet discharge system of (6), the main component great amount of carbon dioxide of gaseous phase materials (7), the propylene oxide mixed gas of a small amount of water and minute quantity, the liquid phase material (8) that absorbed propylene oxide extraction at the bottom of the tower of absorption tower (6), its main component is water, the carbonic acid gas of propylene oxide and minute quantity, the liquid phase material (8) of extraction enters rectifying tower (11) behind rectifying tower fresh feed pump (9) at the bottom of the tower of absorption tower (6), rectifying tower top gaseous phase product (12) enters rectifying tower backflow surge tank (16) behind rectifying tower condenser (13), the a part of material of material (17) (18) that flows out from rectifying tower backflow surge tank (16) returns rectifying tower (11) cat head as phegma, another part material (19) is as the product extraction, the a part of material of liquid product at the bottom of the rectifying tower (20) (21) returns at the bottom of rectifying tower (11) tower through rectifying tower reboiler (22), and another part material (24) turns back to absorption tower (6) cat head after converging as absorption agent and fresh absorbent (25).
The compressor outlet absolute pressure is 1-20atm, exchanger heat logistics temperature out is-and 50-100 ℃, the absolute pressure on absorption tower is 0.1-20atm.The rectifying tower reflux ratio is 0.5-8, and the absolute pressure of rectifying tower is 0.1-20atm, the overhead condensation actuator temperature is controlled at-and 50-100 ℃.
Equipment of the present utility model is widely used in all CO
2With propylene oxide mixture separation process, for the utility model being described better in the advantage aspect product purity and the yield, choose wherein that three application examples are illustrated, but therefore do not limit the scope of application of present technique and equipment.
The utility model device is used for CO
2With propylene oxide mixture separation process, the mixture gas treatment amount is 3.49 tons/hour, identical with the described flow process of invention, comprise mixed gas compressor, interchanger, absorption tower, rectifying tower fresh feed pump, rectifying tower, rectifying tower condenser, rectifying tower backflow surge tank, rectifying tower reboiler.Wherein the compressor outlet absolute pressure is 4atm, interchanger hot-fluid thigh temperature out is 15 ℃, the absolute pressure on absorption tower is 3.5atm, the fresh absorbent consumption is 5kg/h, the absolute pressure of rectifying tower is 4atm, and tower top temperature is 0 ℃, and column bottom temperature is 143.8 ℃, reflux ratio is 2.5, and mixed gas charging mole forms CO
2Be 0.9, propylene oxide is 0.1.
Behind said process, the purity of the high-purity product propylene of main products can reach 96.8%, and the propylene oxide yield can reach 98%.Compare with untreated residual reactant mixed gas, propene oxide purity is promoted to 99.9% by 10%.
The utility model device is used for CO
2With propylene oxide mixture separation process, the mixture gas treatment amount is 10.76 tons/hour, identical with the described flow process of invention, comprise mixed gas compressor, interchanger, absorption tower, rectifying tower, rectifying tower condenser, rectifying tower backflow surge tank, rectifying tower reboiler.Wherein the compressor outlet absolute pressure is 2atm, interchanger hot-fluid thigh temperature out is-50 ℃, the absolute pressure on absorption tower is 0.1atm, the fresh absorbent consumption is 14kg/h, the absolute pressure of rectifying tower is 0.1atm, and tower top temperature is-50 ℃, and column bottom temperature is 143.8 ℃, reflux ratio is 0.5, and mixed gas charging mole forms CO
2Be 0.5, propylene oxide is 0.5.
Behind said process, the purity of the high-purity product propylene of main products can reach 96.1%, and the propylene oxide yield can reach 98.3%.Compare with untreated residual reactant mixed gas, propene oxide purity is promoted to 99.9% by 50%.
The utility model device is used for CO
2With propylene oxide mixture separation process, the mixture gas treatment amount is 20.45 tons/hour, identical with the described flow process of invention, comprise mixed gas compressor, interchanger, absorption tower, rectifying tower, rectifying tower condenser, rectifying tower backflow surge tank, rectifying tower reboiler.Wherein the compressor outlet absolute pressure is 20atm, interchanger hot-fluid thigh temperature out is 100 ℃, the absolute pressure on absorption tower is 20atm, the fresh absorbent consumption is 26kg/h, the absolute pressure of rectifying tower is 20atm, and tower top temperature is 100 ℃, and column bottom temperature is 163.2 ℃, reflux ratio is 8, and mixed gas charging mole forms CO
2Be 0.1, propylene oxide is 0.9.
Behind said process, the purity of the high-purity product propylene of main products can reach 95.9%, and the propylene oxide yield can reach 97.8%.Compare with untreated residual reactant mixed gas, propene oxide purity is promoted to 99.9% by 90%.
By above embodiment as seen, utilize CO of the present utility model
2With the propylene oxide mixture absorption-the rectifying separation purifying plant is feasible, not only technological operation is simple, energy consumption is less but also separation efficiency is very high for whole separating-purifying process.
The CO that the utility model proposes
2With the absorption of propylene oxide mixture-rectifying separation purifying plant, be described by preferred embodiment, person skilled obviously can be changed or suitably change and combination equipment as herein described within not breaking away from content of the present invention, spirit and scope, realizes the utility model technology.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they are deemed to be included in the utility model spirit, scope and the content.
Claims (1)
1. separation of C O
2With the absorption of propylene oxide mixture-rectification and purification device, comprise mixed gas compressor (2), interchanger (4), absorption tower (6), rectifying tower fresh feed pump (9), rectifying tower (11), rectifying tower condenser (13), rectifying tower backflow surge tank (16), rectifying tower reboiler (22); It is characterized in that mixing raw material to be separated enters system from mixed gas compressor (2), mixed gas compressor (2) outlet links to each other through the opening for feed of interchanger (4) with absorption tower (6) by pipeline, the top of (6) is provided with absorption agent opening for feed and residue gaseous phase outlet on the absorption tower, be provided with liquid phase extraction mouth at the bottom of the tower of absorption tower (6), liquid phase extraction mouth is connected with the opening for feed of rectifying tower (11) through rectifying tower fresh feed pump (9) by pipeline, the opening for feed of rectifying tower (11) is arranged on the middle and upper part of rectifying tower (11), rectifying tower (a 11) tower base stream part with return rectifying tower (11) end as bottom steam after rectifying tower reboiler (22) is connected, another part merges into pipeline (26) as the absorption agent feed pipe (25) of absorption agent extraction by pipeline (24) and absorption tower (6); Rectifying tower (11) overhead stream (12) links to each other with rectifying tower backflow surge tank (16) opening for feed through rectifying tower condenser (13), rectifying tower condenser (13) is provided with drain, rectifying tower backflow surge tank (16) outlet at bottom is provided with feed back and material extraction mouth, and wherein the feed back mouth is connected with rectifying tower (11) top of tower by pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220286062 CN202786067U (en) | 2012-06-18 | 2012-06-18 | Absorption and rectification device for separating carbon dioxide and epoxypropane mixture |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220286062 CN202786067U (en) | 2012-06-18 | 2012-06-18 | Absorption and rectification device for separating carbon dioxide and epoxypropane mixture |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202786067U true CN202786067U (en) | 2013-03-13 |
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ID=47813372
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220286062 Withdrawn - After Issue CN202786067U (en) | 2012-06-18 | 2012-06-18 | Absorption and rectification device for separating carbon dioxide and epoxypropane mixture |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202786067U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102731438A (en) * | 2012-06-18 | 2012-10-17 | 天津大学 | Absorption-rectification method and apparatus for separation of carbon dioxide-epoxypropane mixture |
| CN112827325A (en) * | 2021-01-05 | 2021-05-25 | 南京佳华工程技术有限公司 | EO and/or PO tail gas recovery processing method and device |
-
2012
- 2012-06-18 CN CN 201220286062 patent/CN202786067U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102731438A (en) * | 2012-06-18 | 2012-10-17 | 天津大学 | Absorption-rectification method and apparatus for separation of carbon dioxide-epoxypropane mixture |
| CN102731438B (en) * | 2012-06-18 | 2014-05-07 | 天津大学 | Absorption-rectification method and apparatus for separation of carbon dioxide-epoxypropane mixture |
| CN112827325A (en) * | 2021-01-05 | 2021-05-25 | 南京佳华工程技术有限公司 | EO and/or PO tail gas recovery processing method and device |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20130313 Effective date of abandoning: 20140507 |
|
| RGAV | Abandon patent right to avoid regrant |