CN203763884U - Secondary distillation and concentration device of cumyl hydroperoxide - Google Patents
Secondary distillation and concentration device of cumyl hydroperoxide Download PDFInfo
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- CN203763884U CN203763884U CN201420193125.6U CN201420193125U CN203763884U CN 203763884 U CN203763884 U CN 203763884U CN 201420193125 U CN201420193125 U CN 201420193125U CN 203763884 U CN203763884 U CN 203763884U
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- pipeline
- hydrogen phosphide
- phosphide cumene
- distillation concentration
- recooler
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Abstract
The utility model discloses a secondary distillation and concentration device of cumyl hydroperoxide. The device comprises a distillation and concentration tower, a gas-liquid separation collecting device, a reboiler, a cumyl hydroperoxide condenser, a cumyl hydroperoxide recooler, a condenser, a recooler, a vacuum system, a kettle liquid trough and a top liquid trough. According to the device, a mode of partial material reflux is adopted, so that the residence time of materials is long, and the concentration of the contracted materials is effectively improved; in addition, an external heating mode is adopted, so that the temperature of the materials during the distillation and the concentration is stabilized, and good stability of the high-concentration materials is realized; a cumene replenishing mode is adopted, so that the decomposing explosion of the cumyl hydroperoxide due to ultrahigh content of cumene is prevented. Thus, the operating safety during the production is improved.
Description
Technical field
The utility model relates to chemical plant installations field, is specifically related to a kind of for hydrogen phosphide cumene redistillation purifying plant.
Background technology
Prior art adopts the mode of vacuum flash conventionally to the distillation of hydrogen phosphide cumene, but the hydrogen phosphide cumene content obtaining is lower than 50%, and above-mentioned technology has following deficiency:
One, in flash process, the material separating effect that is heated is poor, and the time of staying is short, can not effectively improve the purity of required material.
Two, flash process is instant separation process, is subject to the impact of preheat temperature larger, and the stable content of the high concentration material obtaining is poor, and content deviation is larger.
Therefore, need a kind of new technical scheme to address the above problem.
Utility model content
Goal of the invention: the problem and shortage existing for above-mentioned prior art, the purpose of this utility model is to provide a kind of hydrogen phosphide cumene redistillation concentration unit, adopts tower distillation technology, and the hydrogen phosphide cumene content obtaining can reach 90% left and right.
Technical scheme: for realizing above-mentioned utility model object, the technical solution adopted in the utility model is a kind of hydrogen phosphide cumene redistillation concentration unit, comprises distillation concentration tower, gas-liquid separation gathering-device, reboiler, hydrogen phosphide cumene condenser, hydrogen phosphide cumene recooler, condenser, recooler, vacuum system, still liquid bath and top liquid bath; It is inner that described gas-liquid separation gathering-device is located at distillation concentration tower, one side of this distillation concentration tower be provided with connect the main charging aperture of charging hydrogen peroxide pipeline and be connected isopropylbenzene pipeline add light component charging aperture, the upper lower interface of described gas-liquid separation gathering-device passes through respectively the 13 pipeline and is connected with the import and export of reboiler with the 14 pipeline; A top discharging opening of described distillation concentration tower is connected with the top inlet of condenser by the 19 pipeline, and the end discharging opening of this distillation concentration tower is connected with the import of hydrogen phosphide cumene condenser by the 15 pipeline; The outlet of described hydrogen phosphide cumene condenser is connected with the import of hydrogen phosphide cumene recooler by the 16 pipeline, and the outlet of described hydrogen phosphide cumene recooler is connected with the charging aperture of described still liquid bath by the 17 pipeline; The top exit of described condenser is connected with the top inlet of recooler by the 20 pipeline, the outlet at bottom of condenser is connected with the outlet at bottom of recooler and passes through the 21 pipeline and is connected with the charging aperture of described top liquid bath, and the top exit of described recooler is connected with vacuum system.
Further, described the 13 pipeline is connected with the import of reboiler and is connected with respectively chilling isopropylbenzene pipeline and chilling water supply pipe, and is provided with automatic stop valve and interlock.
Further, another top discharging opening of described distillation concentration tower is provided with safety valve and is connected with discharge conduit.
Further, described distillation concentration tower outside is provided with teletransmission thermometer, distance-transmission pressure gauge and far transmission level meter from top to bottom successively, and described far transmission level meter is connected with the end discharging opening of distillation concentration tower.
Further, on described isopropylbenzene pipeline, be also provided with remote control liquid flowmeter and control valve.
Further, described reboiler is provided with independent heating agent, and thermal medium is steam.
Further, described hydrogen phosphide cumene condenser and hydrogen phosphide cumene recooler are equipped with independent refrigerant, and coolant media is respectively water and ethanolic solution; Described condenser and recooler are equipped with independent refrigerant, and this coolant media is respectively water and ethanolic solution.
Further, described still liquid bath inside is provided with spray equipment and blow-down pipe, and is connected with chilled water (chw) pipeline; In the liquid bath of described top, be provided with blow-down pipe.
Further, after described the 15 pipeline, the 16 pipeline, the 17 pipeline are connected with appliance arrangement with the 21 pipeline, effectively vertical height must remain on more than 12 meters.
Beneficial effect: the utility model adopts the mode of material partial reflux, makes residence time of material long, and the material concentration of extraction effectively improves; By the mode of external heat, during stable distillation concentrate, the temperature of material, makes high concentration material good stability in addition; The mode of isopropylbenzene is added in employing, can prevent because too high levels causes hydrogen phosphide cumene decomposition explosion, improves production operation security, the utlity model has good economical, societal benefits.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model;
In figure: 1-distills concentration tower, 2-gas-liquid separation gathering-device, 3-reboiler, 4-charging hydrogen peroxide pipeline, 5-isopropylbenzene pipeline, 6-hydrogen phosphide cumene condenser, 7-hydrogen phosphide cumene recooler, 8-condenser, 9-recooler, 10-vacuum system, 11-chilling water supply pipe, 12-chilling isopropylbenzene pipeline, 13-the 13 pipeline, 14-the 14 pipeline, 15-the 15 pipeline, 16-the 16 pipeline, 17-the 17 pipeline, 18-the 18 pipeline, 19-the 19 pipeline, 20-the 20 pipeline, 21-the 21 pipeline, 22-still liquid bath, 23-top liquid bath, TI-teletransmission thermometer, PI-distance-transmission pressure gauge, LI-far transmission level meter, XV-automatic stop valve, FI-remote control liquid flowmeter.
The specific embodiment
Below in conjunction with the drawings and specific embodiments, further illustrate the utility model, should understand these embodiment and only for the utility model is described, be not used in restriction scope of the present utility model, after having read the utility model, those skilled in the art all fall within the application's claims limited range to the modification of the various equivalent form of values of the present utility model.
The utility model proposes a kind of hydrogen phosphide cumene redistillation concentration unit, adopt the mode of external heat can stablize the temperature of material while distilling concentrate, the mode of employing partial reflux makes residence time of material long, the high and good stability of extracting concentration.
As shown in Figure 1, hydrogen phosphide cumene redistillation concentration unit of the present utility model, comprises distillation concentration tower 1, gas-liquid separation gathering-device 2, reboiler 3, hydrogen phosphide cumene (CHP) condenser 6, hydrogen phosphide cumene (CHP) recooler 7, condenser 8, recooler 9, vacuum system 10, still liquid bath 22 and top liquid bath 23.Gas-liquid separation gathering-device 2 is located at distillation concentration tower 1 inside, distillation concentration tower 1 outside is provided with teletransmission thermometer TI, distance-transmission pressure gauge PI and far transmission level meter LI from top to bottom successively, far transmission level meter LI is connected with the end discharging opening of distillation concentration tower 1, one side of distillation concentration tower 1 be respectively equipped with the main charging aperture that connects charging CHP pipeline 4 be connected isopropylbenzene pipeline 5 add light component charging aperture, on this isopropylbenzene pipeline 5, be also provided with remote control liquid flowmeter FI and control valve.The upper lower interface of gas-liquid separation gathering-device 2 is connected with the import and export of reboiler 3 with the 14 pipeline 14 by the 13 pipeline 13 respectively, a top discharging opening of distillation concentration tower 1 is connected with the top inlet of condenser 8 by the 19 pipeline 19, the end discharging opening of distillation concentration tower 1 is connected with the import of hydrogen phosphide cumene (CHP) condenser 6 by the 15 pipeline 15, and another top discharging opening of this distillation concentration tower 1 is provided with safety valve and is connected with discharge conduit and carries out discharging.
The 13 pipeline 13 is connected with the import of reboiler 3 and is connected with respectively chilling isopropylbenzene pipeline 12 and chilling water supply pipe 11, and is provided with automatic stop valve XV and interlock.The reboiler 3 that the utility model adopts is provided with independent heating agent, and thermal medium is steam.
The outlet of described hydrogen phosphide cumene (CHP) condenser 6 is connected with the import of hydrogen phosphide cumene (CHP) recooler 7 by the 16 pipeline 16, and the outlet of hydrogen phosphide cumene (CHP) recooler 7 is connected with the charging aperture of still liquid bath 22 by the 17 pipeline 17.Hydrogen phosphide cumene (CHP) condenser 6 and hydrogen phosphide cumene (CHP) recooler 7 that the utility model adopts are respectively equipped with independent refrigerant, and coolant media is respectively water and ethanolic solution.Still liquid bath 22 inside that the utility model adopts are provided with spray equipment, and are connected with chilled water (chw) pipeline, and the charging aperture pipeline of still liquid bath 22 need insert below liquid level, keep fluid-tight state, are also provided with blow-down pipe in still liquid bath 22.
After the 15 pipeline the 15, the 16 pipeline 16 that the utility model adopts is connected with appliance arrangement with the 17 pipeline 17, effectively vertical height must remain on more than 12 meters.
The top exit of condenser 8 is connected with the top inlet of recooler 9 by the 20 pipeline 20, after the outlet at bottom of the outlet at bottom of condenser 8 and recooler 9 gathers, by the 21 pipeline 21, be connected with the charging aperture of top liquid bath 23, the top exit of recooler 9 is connected with vacuum system 10.
Condenser 8 and recooler 9 that the utility model adopts are equipped with independent refrigerant, and this coolant media is respectively water and ethanolic solution.And the 21 pipeline 21 adopting, effectively vertical height must remain on more than 12 meters.The top liquid bath 23 charging aperture pipelines that adopt need insert below liquid level, keep fluid-tight state, in top liquid bath 23, are provided with blow-down pipe.
Embodiment:
The hydrogen phosphide cumene of low concentration enters distillation concentration tower 1 through charging CHP pipeline 4 and carries out negative pressure gas-liquid separation, pressure is≤-0.096Mpa, liquid in tower by gas-liquid separation gathering-device 2 after, after reboiler 3 heating, enter lower floor's distillation concentration tower 1 and carry out separation, obtain after the hydrogen phosphide cumene of high concentration again, after the cooling of hydrogen phosphide cumene (CHP) condenser 6 and hydrogen phosphide cumene (CHP) recooler 7, entering still liquid bath 22 stand-by.
Gas phase in distillation concentration tower 1 is lightweight isopropylbenzene, for keeping the valid density of isopropylbenzene, prevents security incident, and distillation concentration tower 1 carries out adding of isopropylbenzene by adding light component charging aperture, reduces gas phase temperature.After the cooling liquid of the gas phase isopropylbenzene of distillation concentration tower 1 by condenser 8 and recooler 9, enter top liquid bath 23 and recycle.
The steam pressure of the reboiler 3 that the present embodiment adopts is 0.4Mpa left and right, and temperature is 140 ℃ of left and right, and the inlet temperature of reboiler 3 is at 50 ~ 70 ℃, and when outlet temperature is increased to 60 ~ 90 ℃, feed back is to distilling in concentration tower 1.
Claims (9)
1. a hydrogen phosphide cumene secondary distillation concentration unit, is characterized in that: comprise distillation concentration tower (1), gas-liquid separation gathering-device (2), reboiler (3), hydrogen phosphide cumene condenser (6), hydrogen phosphide cumene recooler (7), condenser (8), recooler (9), vacuum system (10), still liquid bath (22) and top liquid bath (23); Described gas-liquid separation gathering-device (2) is located at distillation concentration tower (1) inside, one side of this distillation concentration tower (1) be provided with connect the main charging aperture of charging hydrogen peroxide pipeline (4) and be connected isopropylbenzene pipeline (5) add light component charging aperture, the upper lower interface of described gas-liquid separation gathering-device (2) passes through respectively the 13 pipeline (13) and is connected with the import and export of reboiler (3) with the 14 pipeline (14); A top discharging opening of described distillation concentration tower (1) is connected with the top inlet of condenser (8) by the 19 pipeline (19), and the end discharging opening of this distillation concentration tower (1) is connected with the import of hydrogen phosphide cumene condenser (6) by the 15 pipeline (15); The outlet of described hydrogen phosphide cumene condenser (6) is connected with the import of hydrogen phosphide cumene recooler (7) by the 16 pipeline (16), and the outlet of described hydrogen phosphide cumene recooler (7) is connected with the charging aperture of described still liquid bath (22) by the 17 pipeline (17); The top exit of described condenser (8) is connected with the top inlet of recooler (9) by the 20 pipeline (20), the outlet at bottom of condenser (8) is connected with the outlet at bottom of recooler (9) and passes through the 21 pipeline (21) and is connected with the charging aperture of described top liquid bath (23), and the top exit of described recooler (9) is connected with vacuum system (10).
2. a kind of hydrogen phosphide cumene secondary distillation concentration unit according to claim 1, it is characterized in that: described the 13 pipeline (13) is connected with the import of reboiler (3) and is connected with respectively chilling isopropylbenzene pipeline (12) and chilling water supply pipe (11), and is provided with automatic stop valve (XV) and interlock.
3. a kind of hydrogen phosphide cumene secondary distillation concentration unit according to claim 1, is characterized in that: another top discharging opening of described distillation concentration tower (1) is provided with safety valve and is connected with discharge conduit.
4. a kind of hydrogen phosphide cumene secondary distillation concentration unit according to claim 1, it is characterized in that: described distillation concentration tower (1) outside is provided with teletransmission thermometer (TI), distance-transmission pressure gauge (PI) and far transmission level meter (LI) from top to bottom successively, described far transmission level meter (LI) is connected with the end discharging opening of distillation concentration tower (1).
5. a kind of hydrogen phosphide cumene secondary distillation concentration unit according to claim 1, is characterized in that: on described isopropylbenzene pipeline (5), be also provided with remote control liquid flowmeter (FI) and control valve.
6. a kind of hydrogen phosphide cumene secondary distillation concentration unit according to claim 1 and 2, is characterized in that: described reboiler (3) is provided with independent heating agent, and thermal medium is steam.
7. a kind of hydrogen phosphide cumene secondary distillation concentration unit according to claim 1, it is characterized in that: described hydrogen phosphide cumene condenser (6) and hydrogen phosphide cumene recooler (7) are equipped with independent refrigerant, and coolant media is respectively water and ethanolic solution; Described condenser (8) and recooler (9) are equipped with independent refrigerant, and this coolant media is respectively water and ethanolic solution.
8. a kind of hydrogen phosphide cumene secondary distillation concentration unit according to claim 1, is characterized in that: described still liquid bath (22) inside is provided with spray equipment and blow-down pipe, and is connected with chilled water (chw) pipeline; In described top liquid bath (23), be provided with blow-down pipe.
9. a kind of hydrogen phosphide cumene secondary distillation concentration unit according to claim 1, it is characterized in that: after described the 15 pipeline (15), the 16 pipeline (16), the 17 pipeline (17) are connected with appliance arrangement with the 21 pipeline (21), effectively vertical height must remain on more than 12 meters.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420193125.6U CN203763884U (en) | 2014-04-21 | 2014-04-21 | Secondary distillation and concentration device of cumyl hydroperoxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420193125.6U CN203763884U (en) | 2014-04-21 | 2014-04-21 | Secondary distillation and concentration device of cumyl hydroperoxide |
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| Publication Number | Publication Date |
|---|---|
| CN203763884U true CN203763884U (en) | 2014-08-13 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420193125.6U Expired - Fee Related CN203763884U (en) | 2014-04-21 | 2014-04-21 | Secondary distillation and concentration device of cumyl hydroperoxide |
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| CN (1) | CN203763884U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104447629A (en) * | 2014-12-01 | 2015-03-25 | 中石化上海工程有限公司 | Method for by-producing steam from oxidation unit of epoxypropane device |
| CN107970631A (en) * | 2017-11-29 | 2018-05-01 | 湖北东方化工有限公司 | Nitrotoleune decoking tower bottoms stripping system and method |
| CN112250610A (en) * | 2020-09-29 | 2021-01-22 | 中石化南京工程有限公司 | Method and system for concentrating alkyl peroxide |
-
2014
- 2014-04-21 CN CN201420193125.6U patent/CN203763884U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104447629A (en) * | 2014-12-01 | 2015-03-25 | 中石化上海工程有限公司 | Method for by-producing steam from oxidation unit of epoxypropane device |
| CN107970631A (en) * | 2017-11-29 | 2018-05-01 | 湖北东方化工有限公司 | Nitrotoleune decoking tower bottoms stripping system and method |
| CN107970631B (en) * | 2017-11-29 | 2019-11-08 | 湖北东方化工有限公司 | Nitrotoleune decoking tower bottoms stripping system and method |
| CN112250610A (en) * | 2020-09-29 | 2021-01-22 | 中石化南京工程有限公司 | Method and system for concentrating alkyl peroxide |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140813 Termination date: 20200421 |