CN211158657U - Epoxy chloropropane tail gas condensate liquid recovery unit - Google Patents
Epoxy chloropropane tail gas condensate liquid recovery unit Download PDFInfo
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- CN211158657U CN211158657U CN201921771430.8U CN201921771430U CN211158657U CN 211158657 U CN211158657 U CN 211158657U CN 201921771430 U CN201921771430 U CN 201921771430U CN 211158657 U CN211158657 U CN 211158657U
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Abstract
The utility model provides an epichlorohydrin tail gas condensation feed liquid recovery unit, including one-level glass condenser A, one-level glass condenser B, second grade glass condenser, tertiary glass condenser, one-level vapour and liquid separator A, one-level vapour and liquid separator B, second grade vapour and liquid separator, tertiary vapour and liquid separator, collection tank, feed liquid pump of beating, the upper portion of one-level glass condenser A, one-level glass condenser B is respectively through connecting tube connection epichlorohydrin tail gas house steward, and the upper portion of connecting tube connection one-level vapour and liquid separator A, one-level vapour and liquid separator B is passed through to the lower part. The utility model provides an among the epoxy chloropropane production tail gas temperature high, smuggle useful feed liquid secretly, influence system steady operation and exhaust emission concentration to and influence by-product hydrochloric acid quality scheduling problem, have better economic benefits and environmental protection benefit, just the utility model discloses equipment is simple, and the material is easy, the small investment.
Description
Technical Field
The utility model belongs to the technical field of epoxy chloropropane tail gas treatment, specifically speaking relates to epoxy chloropropane tail gas condensation feed liquid recovery unit.
Background
In the traditional epichlorohydrin production process, tail gas generated by a reaction kettle contains hydrogen chloride, chlorine, nitrogen, organic light components and entrained chlorinated liquid, and is conveyed to a hydrochloric acid procedure for treatment through a tail gas pipeline. The disadvantages of this process are: 1. as the operating temperature of the reaction kettle is high (up to 110 ℃) in the production process, the tail gas contains a large amount of organic light component substances and carries a large amount of chlorination liquid, the material waste is caused, and in case the liquid is gathered in a pipeline, the pipeline is blocked, the pressure of a tail gas system is high, and the safe and stable operation of the upstream and downstream processes is influenced. 2. Because the temperature of the tail gas is high, the load of a hydrochloric acid treatment system is increased, the treatment effect is influenced, the emission concentration of the tail gas does not reach the standard, and the environmental pollution is caused. 3. The chloridized material liquid in the tail gas enters a hydrochloric acid treatment system, and the quality of the byproduct hydrochloric acid is influenced.
SUMMERY OF THE UTILITY MODEL
The utility model provides an epichlorohydrin tail gas condensation feed liquid recovery unit has solved among the background art epichlorohydrin production tail gas temperature height, has smugglied useful feed liquid secretly, influence system safety and stability operation and exhaust emission concentration to and influence byproduct hydrochloric acid quality scheduling problem, have better economic benefits and environmental protection benefit.
The technical scheme of the utility model is realized like this: the utility model provides an epichlorohydrin tail gas condensate liquid recovery unit, includes first-order glass condenser A, first-order glass condenser B, second grade glass condenser, tertiary glass condenser, first-order vapour and liquid separator A, first-order vapour and liquid separator B, second grade vapour and liquid separator, tertiary vapour and liquid separator, collecting vessel, feed liquid pump, the upper portion of first-order glass condenser A, first-order glass condenser B is respectively through connecting tube connection epichlorohydrin tail gas house steward, the lower part is through connecting tube connection one-order vapour and liquid separator A, the upper portion of first-order vapour and liquid separator B; the upper part of the secondary glass condenser is connected with side air outlets of the primary gas-liquid separator A and the primary gas-liquid separator B through connecting pipelines, and the lower part of the secondary glass condenser is connected with the upper part of the secondary gas-liquid separator through connecting pipelines; the upper part of the three-stage glass condenser is connected with a side gas outlet of the second-stage gas-liquid separator through a connecting pipeline, and the lower part of the three-stage glass condenser is connected with the upper part of the three-stage gas-liquid separator through a connecting pipeline; the upper part of the collecting tank is connected with the lower parts of all stages of gas-liquid separators through connecting pipelines, and the lower parts of the collecting tank are connected with a feed liquid material pump;
preferably, a system air inlet valve and a system air outlet valve are arranged on the tail gas main pipe, and an air inlet valve A and an air inlet valve B are arranged between the upper parts of the primary gas-liquid separator A and the primary gas-liquid separator B and the system air inlet valve through connecting pipelines;
preferably, each stage of glass condenser consists of three sections, and a glass coil is arranged in each section;
preferably, all connecting pipes are made of polypropylene material;
preferably, a bypass valve is arranged between the condensation recovery system and the tail gas main pipe;
preferably, a balance valve is arranged between the collecting tank and the tail gas main pipe;
preferably, the feed openings at the lower parts of the gas-liquid separators are all provided with U-shaped water seals;
preferably, the feed pipe in the collection tank is inserted below the bottom liquid level in the collection tank.
The utility model has the advantages that: the utility model provides an among the epoxy chloropropane production tail gas temperature high, smuggle useful feed liquid secretly, influence system steady operation and exhaust emission concentration to and influence by-product hydrochloric acid quality scheduling problem, have better economic benefits and environmental protection benefit, just the utility model discloses equipment is simple, and the material is easy, the small investment.
Drawings
Fig. 1 is a process flow diagram of the present invention.
Description of the parts: 1. the system comprises a first-stage glass condenser A, 2, a first-stage glass condenser B, 3, a second-stage glass condenser, 4, a third-stage glass condenser, 5, a first-stage gas-liquid separator A, 6, a first-stage gas-liquid separator B, 7, a second-stage gas-liquid separator, 8, a third-stage gas-liquid separator, 9, a collecting tank, 10, a feed liquid material pump, 11, a bypass valve, 12, a first-stage glass condenser A air inlet valve, 13, a first-stage glass condenser B air inlet valve, 14, a balance valve, 15, a U-shaped liquid seal, 16, a system air inlet valve, 17, a system air outlet valve.
Detailed Description
For a better understanding and appreciation of the invention, it will be further described in connection with the accompanying drawings: the utility model provides a epichlorohydrin tail gas condensate feed liquid recovery unit, includes one-level glass condenser A1 and B2, second grade glass condenser 3, tertiary glass condenser 4, one-level vapour and liquid separator A5 and B6, second grade vapour and liquid separator 7, tertiary vapour and liquid separator 8, accumulator tank 9, feed liquid pump 10, by-pass valve 11, balanced valve 14. The upper parts of the first-stage glass condensers A1 and B2 are connected with an epichlorohydrin tail gas main pipe 18 through connecting pipelines, the tail gas main pipe 18 is provided with a system air inlet valve 16 and a system air outlet valve 17, the upper parts of the first-stage gas-liquid separators A and B and the system air inlet valve are provided with an air inlet valve A12 and an air inlet valve B13 through connecting pipelines, the tail gas quantity distribution is controlled by the air inlet valves A12 and B13, and the lower parts of the first-stage glass condensers A5 and B6 are connected with the upper parts of the first-; the upper part of the secondary glass condenser 3 is connected with the side air outlets of the first-stage gas-liquid separator A5 and the B6 through connecting pipelines, and the lower part of the secondary glass condenser is connected with the upper part of the secondary gas-liquid separator 7 through connecting pipelines; the upper part of the third-stage glass condenser 4 is connected with a side gas outlet of the second-stage gas-liquid separator 7 through a connecting pipeline, and the lower part of the third-stage glass condenser is connected with the upper part of the third-stage gas-liquid separator 8 through a connecting pipeline; the upper part of the collecting tank 9 is connected with the lower parts of all stages of gas-liquid separators through connecting pipelines, and the lower part is connected with a feed liquid material pump 10. A bypass valve 11 is arranged between the condensate liquid recovery system and the tail gas main pipe 18, so that the condensate liquid recovery system and the exhaust system can be switched with each other, the maintenance is convenient, and the operation of upstream and downstream systems is not influenced. A balance valve 14 is arranged between the collecting tank 9 and the tail gas main pipe 18, so that the feed liquid in the gas-liquid separator can smoothly flow into the collecting tank. The feed opening at the lower part of each stage of gas-liquid separator is provided with a U-shaped water seal 15 which can prevent gas from entering the collecting tank 9, and the feed pipe of the collecting tank 9 is inserted below the liquid level at the bottom, so that the feed liquid in the collecting tank 9 can be reduced and carried to the tail gas main pipe 18.
Before production, a system air inlet valve 16 and a system air outlet valve 17 are opened, and the opening degrees of a first-stage glass condenser A air inlet valve 12 and a first-stage glass condenser B air inlet valve 13 are adjusted to balance the gas quantity entering the two groups of condensers; the cooling water system of each stage of the glass condenser is opened, and the balance valve 14 at the top of the collection tank 9 is opened. And (4) observing the reflux state of the condensate of the gas-liquid separator, observing the liquid level of the collecting tank 9, and starting the feed liquid pump 10 to pour the materials after the liquid level reaches a certain scale.
Claims (8)
1. The utility model provides an epichlorohydrin tail gas condensate liquid recovery unit, includes one-level glass condenser A (1), one-level glass condenser B (2), second grade glass condenser (3), tertiary glass condenser (4), one-level vapour and liquid separator A (5), one-level vapour and liquid separator B (6), second grade vapour and liquid separator (7), tertiary vapour and liquid separator (8), collection tank (9), feed liquid pump (10), its characterized in that the upper portion of one-level glass condenser A (1), one-level glass condenser B (2) is respectively through connecting tube connection epichlorohydrin tail gas house steward (18), the lower part is through connecting tube connection one-level vapour and liquid separator A (5), the upper portion of one-level vapour and liquid separator B (6); the upper part of the secondary glass condenser (3) is connected with the side gas outlets of the primary gas-liquid separator A (5) and the primary gas-liquid separator B (6) through connecting pipelines, and the lower part of the secondary glass condenser is connected with the upper part of the secondary gas-liquid separator (7) through connecting pipelines; the upper part of the three-stage glass condenser (4) is connected with a side gas outlet of the second-stage gas-liquid separator (7) through a connecting pipeline, and the lower part of the three-stage glass condenser is connected with the upper part of the three-stage gas-liquid separator (8) through a connecting pipeline; the upper part of the collecting tank (9) is connected with the lower parts of all stages of gas-liquid separators through connecting pipelines, and the lower part is connected with a feed liquid material pumping pump (10).
2. The epichlorohydrin condensed liquid recovery device according to claim 1, wherein the offgas header pipe (18) is provided with a system air inlet valve (16) and a system air outlet valve (17), and an air inlet valve A (12) and an air inlet valve B (13) are provided between the upper portions of the primary gas-liquid separator A (5) and the primary gas-liquid separator B (6) and the system air inlet valve (16) through connecting pipes.
3. The apparatus for recovering epichlorohydrin condensate feed liquid according to claim 1 or 2, wherein each stage of glass condenser is composed of three sections, and a glass coil is arranged in each section.
4. The apparatus for recovering epichlorohydrin condensate as set forth in claim 1 or 2, wherein all the connecting pipes are made of polypropylene.
5. The epoxychloropropane tail gas condensate liquid recovery device according to claim 1 or 2, characterized in that a bypass valve (11) is arranged between the condensate recovery system and the tail gas main pipe (18).
6. The recovery device for the epichlorohydrin condensate feed liquid in the claim 1 or 2, characterized in that a balance valve (14) is arranged between the collecting tank (9) and the offgas header pipe (18).
7. The epichlorohydrin tail gas condensate liquid recovery apparatus according to claim 1 or 2, wherein the feed openings at the lower parts of the gas-liquid separators are provided with U-shaped water seals (15).
8. The recovery device for the epichlorohydrin condensate feed liquid in claim 1 or 2, wherein the feed pipe in the collection tank (9) is inserted below the liquid level at the bottom of the collection tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921771430.8U CN211158657U (en) | 2019-10-22 | 2019-10-22 | Epoxy chloropropane tail gas condensate liquid recovery unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921771430.8U CN211158657U (en) | 2019-10-22 | 2019-10-22 | Epoxy chloropropane tail gas condensate liquid recovery unit |
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| Publication Number | Publication Date |
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| CN211158657U true CN211158657U (en) | 2020-08-04 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201921771430.8U Active CN211158657U (en) | 2019-10-22 | 2019-10-22 | Epoxy chloropropane tail gas condensate liquid recovery unit |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112870753A (en) * | 2021-01-26 | 2021-06-01 | 广东申菱环境系统股份有限公司 | Condensing type oil gas recovery device |
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2019
- 2019-10-22 CN CN201921771430.8U patent/CN211158657U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112870753A (en) * | 2021-01-26 | 2021-06-01 | 广东申菱环境系统股份有限公司 | Condensing type oil gas recovery device |
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