CN204932917U - Extractive distillation device in a kind of hydrofining process of crude benzene - Google Patents
Extractive distillation device in a kind of hydrofining process of crude benzene Download PDFInfo
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- CN204932917U CN204932917U CN201520668630.6U CN201520668630U CN204932917U CN 204932917 U CN204932917 U CN 204932917U CN 201520668630 U CN201520668630 U CN 201520668630U CN 204932917 U CN204932917 U CN 204932917U
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Abstract
The utility model discloses the extractive distillation device in a kind of hydrofining process of crude benzene, comprise mother tube, knockout tower, tower condenser, backflash, return duct, benzene cooler, purified petroleum benzin groove, the first reboiler and toluene groove, knockout tower comprises tower body, material inlet, purified petroleum benzin outlet, refluxing opening, toluene outlet, steam inlet, steam (vapor) outlet and isometrical tower tray, the middle part of tower body is provided with reducer, be furnished with reducing tower tray in reducer, every layer of tower tray of isometrical tower tray and reducing tower tray be all provided with down-flow plate, overflow weir and baffling parts.The utility model not only reduces the operation height of knockout tower, handled easily, eliminate the phenomenon that tower top heat supply is not enough, tower bottom heating is excessive, and the efficiency of heat transfer and mass transfer is higher, effectively ensure that the effect of extract and separate, further improve quality and the purity of product, have stable, yield is high, rectification effect good and energy-conservation advantage, be easy to promote the use of.
Description
Technical field
The utility model belongs to chemical mechanical equipment technical field, is specifically related to the extractive distillation device in a kind of hydrofining process of crude benzene.
Background technology
Benzene and Toluene and dimethylbenzene are all very important industrial chemicals, are mainly derived from the petrobenzene in petrochemical process and the coking crude benzene in coking industry, and above-mentioned change crude benzol is by techniques such as purification & isolation thus obtain pure Benzene and Toluene.At present, the process for refining of coking crude benzene mainly adopts hydrofinishing method, the hydrogenation technique of coking crude benzene, it comprise carry out in advance de-heavy, crude benzol is separated into heavy benzol and light benzene, hydrogenation in light benzene again, light benzene reacts under the catalytic action of catalyst, thus acquisition benzene, toluene and dimethylbenzene agent and other light hydrocarbon components, again through de-light process, light components in above-mentioned mixture and reaction impurities are removed, thus obtain half-finished benzene, the mixtures such as toluene dimethylbenzene and non-aromatics, also known as hydrogenated oil, hydrogenated oil is passing through extraction rectification technique, non-aromatic component in removing hydrogenated oil, obtain the mixture of Benzene and Toluene, the mixture of Benzene and Toluene passes in benzene knockout tower, Benzene and Toluene can be separated.The extractive distillation technique of existing Benzene and Toluene, its equipment mainly knockout tower, after raw material enters knockout tower, carry out heat exchange with the steam passed in knockout tower after, benzene is discharged from the top of knockout tower, by entering backflash after condenser, then by directly entering in purified petroleum benzin groove after the cooling of return duct charge air cooler, the dimethylbenzene after being separated then is discharged by bottom and is sent in toluene groove by reflux pump.Although above-mentioned technology all can reach the object to separation of products, the technique be separated is all very ripe, but, in the production of reality, number of trays in knockout tower is more, the height of tower is higher, tower diameter is just thinner by contrast, not only bad for the operation at scene, and it is less than being easier to make the load of liquid phase, position higher in tower is caused easily to produce middle heat loss, cause the phenomenon of heat supply deficiency, affect the separating effect of Benzene and Toluene and the quality of product, simultaneously, because the quantity of tower tray is many, make the consumption of steam larger, the impurity be mixed into is also relatively many, the equipment that easy blocking is follow-up, and affect the purity of product, be exactly the operating mode instability in tower in addition, the fluctuation range of operating pressure is larger, the number of times of artificial frequency modulation is higher, the normal processing power of device can be had a strong impact on.Therefore, develop a kind of easy to operate, mass-transfer efficiency is high, stable conditions, can improve the quality of products and separating effect, guarantee production capacity hydrofining process of crude benzene in extractive distillation device be desirability.
Summary of the invention
The purpose of this utility model be to provide a kind of easy to operate, mass-transfer efficiency is high, stable conditions, can improve the quality of products and separating effect, guarantee production capacity hydrofining process of crude benzene in extractive distillation device.
The purpose of this utility model is achieved in that and comprises mother tube, knockout tower, tower condenser, backflash, return duct, benzene cooler, purified petroleum benzin groove, first reboiler and toluene groove, knockout tower comprises tower body, material inlet, purified petroleum benzin exports, refluxing opening, toluene exports, steam inlet, steam (vapor) outlet and the isometrical tower tray be arranged in tower body, the middle part of tower body is provided with a reducer, reducing tower tray is furnished with in the cavity of reducer, every layer of tower tray of isometrical tower tray and reducing tower tray is all provided with down-flow plate, down-flow plate is located between the edge of tower tray and tower body and forms passage, and neighbouring down-flow plate staggers mutually, the upper surface of every layer of tower tray of isometrical tower tray and reducing tower tray is all connected to a pair overflow weir, and tower tray corresponding between often pair of overflow weir is all provided with overflow crest of weir, and the overflow crest of weir on neighbouring tower tray staggers mutually, the upper surface of every layer of tower tray of isometrical tower tray and reducing tower tray is all fixedly connected with the baffling parts that material baffling can be made to corresponding often pair of overflow weir place.
The utility model is by the reducer set up and baffling parts, not only farthest reduce the diameter of tower and the ratio of height, reduce the operation height of knockout tower, handled easily, prevent tower top heat supply not enough, the phenomenon generation that tower bottom heating is excessive, and material can be made to contact fully with steam fully on every layer of tower tray, the efficiency of heat transfer and mass transfer is higher, effectively ensure that the effect of extract and separate, further improve quality and the purity of product, ensure that the normal production capacity of device, have stable, yield is high, the advantage that rectification effect is good He energy-conservation, also greatly reduce the labour intensity of operating personnel, save production cost, there is good economic benefit, be easy to promote the use of.
Accompanying drawing explanation
Fig. 1 is overall structure schematic diagram of the present utility model;
Fig. 2 is the structural representation of knockout tower;
Fig. 3 is the top view of tower tray;
In figure: 1-mother tube, 2-knockout tower, 21-toluene exports, the anti-vortex board of 22-, the isometrical tower tray of 23-, 24-baffling parts, 2401-connecting plate, 2402-curved baffle, 2403-deflection plate, 25-tower body, 26-reducer, 27-reducing tower tray, 29 devices, the oil-poor import of 215-, the oil-poor outlet of 216-, 217-steam (vapor) outlet, 218-overflow crest of weir, 219-sieve aperture, 220-overflow weir, 3-tower condenser, 4-backflash, 5-return duct, 6-benzene cooler, 7-purified petroleum benzin groove, 8-toluene groove, 9-first reboiler, 10-second reboiler.
Detailed description of the invention
Be further described the utility model below in conjunction with accompanying drawing, but limited the utility model never in any form, any change done based on the utility model training centre or improvement, all belong to protection domain of the present utility model.
As shown in Figures 1 to 3, the utility model comprises mother tube 1, knockout tower 2, tower condenser 3, backflash 4, return duct 5, benzene cooler 6, purified petroleum benzin groove 7, first reboiler 9 and toluene groove 8, knockout tower 2 comprises tower body 25, material inlet 28, purified petroleum benzin outlet 29, refluxing opening 210, toluene outlet 21, steam inlet 213, steam (vapor) outlet 217 and the isometrical tower tray 23 be arranged in tower body 25, the middle part of tower body 25 is provided with a reducer 26, reducing tower tray 27 is furnished with in the cavity of reducer 26, every layer of tower tray of isometrical tower tray 23 and reducing tower tray 27 is all provided with down-flow plate 212, down-flow plate 212 is located between the edge of tower tray and tower body 25 and forms passage, and neighbouring down-flow plate 212 staggers mutually, the upper surface of every layer of tower tray of isometrical tower tray 23 and reducing tower tray 27 is all connected to a pair overflow weir 220, and tower tray corresponding between often pair of overflow weir 220 is all provided with overflow crest of weir 218, and the overflow crest of weir 218 on neighbouring tower tray staggers mutually, the upper surface of every layer of tower tray of isometrical tower tray 23 and reducing tower tray 27 is all fixedly connected with the baffling parts 24 that material baffling can be made to corresponding often pair of overflow weir 220 place.
Further, described baffling parts 24 comprise 1 pair of curved baffle 2402 and 2 ~ 4 pairs of deflection plates 2403, described curved baffle 2402 is fixed on the both sides of overflow weir 220 by connecting plate 2401, and leaving space between the other end of the arc opening of two curved baffles 2402 and the inwall of tower body 25, described 2 ~ 4 right deflection plates 2403 are arranged on the upper surface of two curved baffles 2402 and tower tray.
Further, every layer of tower tray of described isometrical tower tray 23 and reducing tower tray 27 is provided with several sieve apertures 219 all respectively uniformly, described sieve aperture 219 is up-small and down-big taper eyelet, the upper port diameter of described taper eyelet is between 1 ~ 1.5mm, between lower port between 3 ~ 4mm, arranging sieve aperture 219 is rates of climb in order to accelerate steam, allows steam fully be contacted with the material on tower tray by sieve aperture 219, allow bubbling on tower tray evenly, the air lift better effects if of steam.
Further, described tower body 25 is provided with oil-poor outlet 216 and oil-poor import 215, described oil-poor outlet 216 is connected with the second reboiler 10 by circulation carrier pipe, the outlet of described second reboiler 10 is connected with oil-poor import 215 by circulation carrier pipe, it is the material boiling in order to accelerate bottom tower body 25, increase the temperature of steam, promote the quick separating of material.
For the ease of the cleaning to tower tray, maintenance and maintenance, described tower body 25 is furnished with at least 2 manholes 211.
Further, the end of described steam inlet 213 is provided with steam distributor 214, is to make the distribution of steam entered in tower body 25 even, further improving the effect of mass transfer.
Further, toluene bottom described tower body 25 exports 21 places and is provided with anti-vortex board 22, when being to prevent toluene outflow toluene from exporting 21, the phenomenon of eddy current can not be produced, prevent from, because some impurity flow out by eddy current, affecting the quality of product, reduce tower internal cause eddy current and the loss that led out by toluene, to ensure the stable operation of liquid level in tower.
The course of work of the present utility model is: the mixture of Benzene and Toluene enters into tower tray by mother tube 1 from the material inlet 28 at knockout tower 2 top, enter material on tower tray successively by deflection plate 2403, fully contact with the steam entered in tower by steam inlet 213 under the effect of deflection plate 2403, the material flowing through deflection plate 2403 drops on lower one deck tower tray through down-flow plate 212, circulation like this carry out mass transfer with steam, thus realize the object of Benzene and Toluene separation, benzene after separation is discharged from the purified petroleum benzin outlet 28 of tower body 25, purified petroleum benzin gas condensation in tower condenser 3 of about 31 DEG C that eject, condensed fluid collection is in tower backflash 4, reflux pump is utilized to send back in knockout tower 2 by the phegma that distillation needs, benzaldehyde product is then discharged into the purified petroleum benzin groove 7 of reservoir area after benzene cooler 6 cools, and the toluene products of about 133 DEG C of discharging from toluene outlet 21 through toluene cooler is cold go after to be transported to the toluene groove 8 of reservoir area by reflux pump.
Claims (7)
1. the extractive distillation device in a hydrofining process of crude benzene, comprise mother tube (1), knockout tower (2), tower condenser (3), backflash (4), return duct (5), benzene cooler (6), purified petroleum benzin groove (7), first reboiler (9) and toluene groove (8), it is characterized in that: described knockout tower (2) comprises tower body (25), material inlet (28), purified petroleum benzin outlet (29), refluxing opening (210), toluene outlet (21), steam inlet (213), steam (vapor) outlet (217) and the isometrical tower tray (23) be arranged in tower body (25), the middle part of tower body (25) is provided with a reducer (26), reducing tower tray (27) is furnished with in the cavity of reducer (26), every layer of tower tray of isometrical tower tray (23) and reducing tower tray (27) is all provided with down-flow plate (212), down-flow plate (212) is located between the edge of tower tray and tower body (25) and forms passage, and neighbouring down-flow plate (212) staggers mutually, the upper surface of every layer of tower tray of isometrical tower tray (23) and reducing tower tray (27) is all connected to a pair overflow weir (220), and tower tray corresponding between often pair of overflow weir (220) is all provided with overflow crest of weir (218), and the overflow crest of weir (218) on neighbouring tower tray staggers mutually, the upper surface of every layer of tower tray of isometrical tower tray (23) and reducing tower tray (27) is all fixedly connected with the baffling parts (24) that material baffling can be made to correspondence often pair overflow weir (220) place.
2. the extractive distillation device in a kind of hydrofining process of crude benzene according to claim 1, it is characterized in that: described baffling parts (24) comprise 1 pair of curved baffle (2402) and 2 ~ 4 pairs of deflection plates (2403), curved baffle (2402) is fixed on the both sides of overflow weir (220) by connecting plate (2401), and leaving space between the inwall of the other end of the arc opening of two curved baffles (2402) and tower body (25), described 2 ~ 4 right deflection plates (2403) are arranged in two curved baffles (2402) with on the upper surface of tower tray.
3. the extractive distillation device in a kind of hydrofining process of crude benzene according to claim 1, it is characterized in that: every layer of tower tray of isometrical tower tray (23) and reducing tower tray (27) is provided with several sieve apertures (219) all respectively uniformly, sieve aperture (219) is up-small and down-big taper eyelet, the upper port diameter of taper eyelet between 1 ~ 1.5mm, between lower port between 3 ~ 4mm.
4. the extractive distillation device in a kind of hydrofining process of crude benzene according to claim 1, it is characterized in that: tower body (25) is provided with oil-poor outlet (216) and oil-poor import (215), described oil-poor outlet (216) is connected with the second reboiler (10) by circulation carrier pipe, and the outlet of described second reboiler (10) is connected with oil-poor import (215) by circulation carrier pipe.
5. the extractive distillation device in a kind of hydrofining process of crude benzene according to claim 1, is characterized in that: tower body (25) is furnished with at least 2 manholes (211).
6. the extractive distillation device in a kind of hydrofining process of crude benzene according to claim 1, is characterized in that: the end of steam inlet (213) is provided with steam distributor (214).
7. the extractive distillation device in a kind of hydrofining process of crude benzene according to claim 1, is characterized in that: toluene outlet (21) place of tower body (25) bottom is provided with anti-vortex board (22).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520668630.6U CN204932917U (en) | 2015-09-01 | 2015-09-01 | Extractive distillation device in a kind of hydrofining process of crude benzene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520668630.6U CN204932917U (en) | 2015-09-01 | 2015-09-01 | Extractive distillation device in a kind of hydrofining process of crude benzene |
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| Publication Number | Publication Date |
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| CN204932917U true CN204932917U (en) | 2016-01-06 |
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| CN201520668630.6U Active CN204932917U (en) | 2015-09-01 | 2015-09-01 | Extractive distillation device in a kind of hydrofining process of crude benzene |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109847396A (en) * | 2018-12-28 | 2019-06-07 | 广东新华粤华德科技有限公司 | A kind of device for hydrocarbon mixture extracting, rectifying and separating phenylethylene |
| CN111939584A (en) * | 2020-09-04 | 2020-11-17 | 中冶焦耐(大连)工程技术有限公司 | Process and system for evaporating crude benzene in benzene hydrogenation reaction system |
| CN114470834A (en) * | 2020-10-27 | 2022-05-13 | 湖南中岭化工有限责任公司 | Crude benzene hydrogenation extraction device |
| CN114534624A (en) * | 2020-11-11 | 2022-05-27 | 中国石油化工股份有限公司 | Tower-type pre-polycondensation reactor |
-
2015
- 2015-09-01 CN CN201520668630.6U patent/CN204932917U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109847396A (en) * | 2018-12-28 | 2019-06-07 | 广东新华粤华德科技有限公司 | A kind of device for hydrocarbon mixture extracting, rectifying and separating phenylethylene |
| CN111939584A (en) * | 2020-09-04 | 2020-11-17 | 中冶焦耐(大连)工程技术有限公司 | Process and system for evaporating crude benzene in benzene hydrogenation reaction system |
| CN111939584B (en) * | 2020-09-04 | 2023-09-15 | 中冶焦耐(大连)工程技术有限公司 | Crude benzene evaporation process and system in benzene hydrogenation reaction system |
| CN114470834A (en) * | 2020-10-27 | 2022-05-13 | 湖南中岭化工有限责任公司 | Crude benzene hydrogenation extraction device |
| CN114534624A (en) * | 2020-11-11 | 2022-05-27 | 中国石油化工股份有限公司 | Tower-type pre-polycondensation reactor |
| CN114534624B (en) * | 2020-11-11 | 2024-04-19 | 中国石油化工股份有限公司 | Tower type precondensation reactor |
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