CN203227322U - Extractive distillation tower - Google Patents
Extractive distillation tower Download PDFInfo
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- CN203227322U CN203227322U CN2013202294462U CN201320229446U CN203227322U CN 203227322 U CN203227322 U CN 203227322U CN 2013202294462 U CN2013202294462 U CN 2013202294462U CN 201320229446 U CN201320229446 U CN 201320229446U CN 203227322 U CN203227322 U CN 203227322U
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- extractive distillation
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Abstract
The utility model relates to an extractive distillation tower comprising an upper reflux distribution section, a solvent feed rectifying section, a material feed stripping section which are arranged on the upper, middle and lower three sections of the extractive distillation tower, respectively, wherein the upper reflux distribution section is arranged on the upper part of the extractive distillation tower, and comprises a steam outlet, a reflux distributor and an extraction separation packing; a reflux inlet is formed in the reflux distributor; the steam outlet is formed in the top of the tower; the solvent feed rectifying section comprises an extracting solvent feed distributor, an extractive distillation packing and a redistributor; the material feed stripping section is arranged under a material inlet, and comprises a feed distributor, a mass transfer tray and a liquid breaking disc. The extractive distillation tower has the advantages of being capable of realizing extractive distillation operation efficiently and continuously and has the operating characteristics of stacked double towers, a tower body at the upper part is used for realizing separation and purification of an extracting agent and a tower body at the lower part is used for realizing the extraction separation process of aromatic hydrocarbons and non-aromatic hydrocarbons, and therefore, the tower is capable of producing qualified rice solvent products.
Description
Technical field
The utility model relates to a kind of extraction distillation column, relates in particular to a kind of crude benzol cut extraction distillation column.
Background technology
In chemical industry, destilling tower is the distillation instrument of using always, be used for different boiling, proportion, volatile separating substances are come out, and the relative volatility of the saturated hydrocarbon that low temperature hydrogenation produces and benzene is less, differ also less with the boiling point of benzene, form azeotropic mixture easily, can not separate with the conventional distillation method, the benzaldehyde product of producing like this is second-rate, if adopt the method for extracting rectifying can obtain the higher benzaldehyde product of purity, this just needs a kind of equipment that can realize that the benzene class is separated with non-aromatics.
Summary of the invention
For overcoming the deficiencies in the prior art, the purpose of this utility model provides a kind of extraction distillation column, can realize extraction separation of benzol class and the non-aromatics of efficient stable.
For achieving the above object, the utility model is achieved through the following technical solutions:
A kind of extraction distillation column, comprise the top backflow dispensing section, solvent feed rectifying section, the material charging stripping section that are located at three sections of extraction distillation column upper, middle and lower respectively, described top backflow dispensing section is located at extraction distillation column top, comprise steam (vapor) outlet, reflux splitter and extract and separate filler, reflux splitter is provided with reflux inlet, steam (vapor) outlet is located at cat head, and the reflux splitter bottom is provided with the extract and separate filler;
Described solvent feed rectifying section comprises extractant feed distributor, extracting rectifying filler, redistributor, the extractant feed distributor is provided with the extractant entrance, extractant feed distributor bottom is provided with the extracting rectifying filler, and extracting rectifying filler bottom is provided with redistributor;
Described material charging stripping section is located at below the material inlet, comprises feed distributor, mass transfer tower tray, disconnected liquid dish, and feed distributor is provided with material inlet, and the feed distributor bottom is provided with the mass transfer tower tray, and mass transfer tower tray bottom is provided with disconnected liquid dish.
Be equipped with redistributor below two parts about described extracting rectifying filler is divided into, every part.
Described mass transfer tower tray is float valve tray, or is bubble cap tray, or is the vertical sieve tray tower tray.
Compared with prior art, the beneficial effects of the utility model are:
Can realize the extractive distillation operation in high-efficiency and continuous ground, have the operating characteristic of double tower stack, the separation of top tower body realization extractant is purified, and the bottom tower body is realized the extraction and separation technology of aromatic hydrocarbons and non-aromatics, can produce qualified rich solvent product; Mass-transfer efficiency height, degree of integration height, stable operation and easy to maintenance are realized the heat energy recycle height, have guaranteed the safe and stable operation of production process.
Description of drawings
Fig. 1 is structural representation of the present utility model.
Among the figure: the disconnected liquid dish 13-liquid phase outlet of 1-steam (vapor) outlet 2-reflux splitter 3-reflux inlet 4-extract and separate filler 5-extractant feed distributor 6-extractant entrance 7-redistributor 8-extracting rectifying filler 9-material inlet 10-feed distributor 11-mass transfer tower tray 12-14-steam inlet 15-bottoms material outlet 16-tower reactor.
The specific embodiment
Below in conjunction with Figure of description the utility model is described in detail, but should be noted that enforcement of the present utility model is not limited to following embodiment.
See Fig. 1, a kind of extraction distillation column, comprise the top backflow dispensing section, solvent feed rectifying section, the material charging stripping section that are located at three sections of extraction distillation column upper, middle and lower respectively, described top backflow dispensing section is located at extraction distillation column top, comprise steam (vapor) outlet 1, reflux splitter 2 and extract and separate filler 4, reflux splitter 2 is provided with reflux inlet 3, and steam (vapor) outlet 1 is located at cat head, and reflux splitter 2 bottoms are provided with extract and separate filler 4;
Described solvent feed rectifying section comprises extractant feed distributor 5, extracting rectifying filler 8, redistributor 7, extractant feed distributor 5 is provided with extractant entrance 6, extractant feed distributor 5 bottoms are provided with extracting rectifying filler 8, and extracting rectifying filler 8 bottoms are provided with redistributor 7;
Described material charging stripping section is located at material inlet below 9, comprise feed distributor 10, mass transfer tower tray 11, disconnected liquid dish 12, feed distributor 10 is provided with material inlet 9, and feed distributor 10 bottoms are provided with mass transfer tower tray 11, and mass transfer tower tray 11 bottoms are provided with disconnected liquid dish 12.
Be equipped with redistributor 7 below two parts about described extracting rectifying filler 8 is divided into, every part.
Described mass transfer tower tray 11 is float valve tray, or is bubble cap tray, or is the vertical sieve tray tower tray.
Extraction distillation column is to provide liquid phase in the thermic load heating tower reactor by tower bottom reboiler, the condenser of cat head provides cold, extractant is injected on top at tower, at the middle part of tower input material, gas phase upwards and downward liquid phase are finished the counter current contacting mass transfer at extraction tower inner transmission matter parts, finish the mixed process of extractant.
Top backflow dispensing section is positioned at extraction distillation column top, mainly comprise overhead vapor outlet 1, reflux splitter 2 and extract and separate filler 4, steam after the separation (Main Ingredients and Appearance is non-aromatics steam and part extractant) is discharged by the steam (vapor) outlet 1 of top of tower, after the condenser condenses, partial condensation liquid returns tower inside through reflux inlet 3, can regain the part extractant, under the effect of reflux splitter 2 and extract and separate filler 4, the benzene class aromatic hydrocarbon in top of tower extraction absorption tower in the steam.
Be used for refluxing and distribute and the reflux splitter 2 of extraction absorption benzene class aromatic hydrocarbon and the mass transfer core component that extract and separate filler 4 is the extractive distillation top of tower, its inner liquid phase is evenly distributed, and effectively heavy ends product in the absorption tower has double tower stack separation characteristic.
The solvent feed rectifying section is positioned at the extraction distillation column middle part, an amount of extractant is entered in the tower by 8 uniform distributions of extractant feed distributor, under the gravity effect, extractant flows downward, in extracting rectifying filler 8 inside, adverse current contacts with material to be extracted, the concentration difference effect, extractant absorbs waits to extract benzene class aromatic hydrocarbon in the material, finish the vapour-liquid mass separation process, behind 8 sections of the certain extracting rectifying fillers of experience, extractant enters in the tower redistributor 7 and redistributes, and enters 8 sections of next extracting rectifying fillers again and carries out the extract and separate operation.This two-section extraction fractional distillation filling-material 8 is mainly finished the distillation process that extractant absorbs benzene class aromatic hydrocarbon in the former material.
Material charging stripping section is positioned at material inlet below 9, aromatic hydrocarbons and non-aromatics mixture enter tower body by material inlet 9, feed distributor 10 can be realized the charging uniform distribution, after the extractant that feed material and top flow down mixes, through feed distributor 10 uniform distributions, enter the efficient vapour-liquid mass tower tray 11 of stripping section together, bottom gas phase and mixed material are finished extraction at efficient mass transfer tower tray 11 and are absorbed, and have both finished the separation process of aromatic hydrocarbons and non-aromatics.Converge on the disconnected liquid dish 12 through the liquid phase after 11 separation of multilayer mass transfer tower tray, flow to tower bottom reboiler through liquid phase outlet 13, the reboiler heating liquid becomes gas phase, enters tower reactor 16 by steam inlet 14.Tower bottom is bottoms material outlet 15, and the unnecessary rich extractant of tower bottom is delivered to next unit, realizes whole extractive distillation process.
The utility model can be realized the extractive distillation operation in high-efficiency and continuous ground, operating characteristic with double tower stack, the top tower body is realized the separation purification of extractant, and the bottom tower body is realized the extraction and separation technology of aromatic hydrocarbons and non-aromatics, can produce qualified rich solvent product; Mass-transfer efficiency height, degree of integration height, stable operation and easy to maintenance are realized the heat energy recycle height, have guaranteed the safe and stable operation of production process.
Claims (3)
1. extraction distillation column, it is characterized in that, comprise the top backflow dispensing section, solvent feed rectifying section, the material charging stripping section that are located at three sections of extraction distillation column upper, middle and lower respectively, described top backflow dispensing section is located at extraction distillation column top, comprise steam (vapor) outlet, reflux splitter and extract and separate filler, reflux splitter is provided with reflux inlet, and steam (vapor) outlet is located at cat head, and the reflux splitter bottom is provided with the extract and separate filler;
Described solvent feed rectifying section comprises extractant feed distributor, extracting rectifying filler, redistributor, the extractant feed distributor is provided with the extractant entrance, extractant feed distributor bottom is provided with the extracting rectifying filler, and extracting rectifying filler bottom is provided with redistributor;
Described material charging stripping section is located at below the material inlet, comprises feed distributor, mass transfer tower tray, disconnected liquid dish, and feed distributor is provided with material inlet, and the feed distributor bottom is provided with the mass transfer tower tray, and mass transfer tower tray bottom is provided with disconnected liquid dish.
2. a kind of extraction distillation column according to claim 1 is characterized in that, described extracting rectifying filler is divided into up and down two parts, is equipped with redistributor below every part.
3. a kind of extraction distillation column according to claim 1 is characterized in that, described mass transfer tower tray is float valve tray, or is bubble cap tray, or is the vertical sieve tray tower tray.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013202294462U CN203227322U (en) | 2013-04-28 | 2013-04-28 | Extractive distillation tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013202294462U CN203227322U (en) | 2013-04-28 | 2013-04-28 | Extractive distillation tower |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203227322U true CN203227322U (en) | 2013-10-09 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013202294462U Expired - Lifetime CN203227322U (en) | 2013-04-28 | 2013-04-28 | Extractive distillation tower |
Country Status (1)
| Country | Link |
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| CN (1) | CN203227322U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104056463A (en) * | 2014-06-05 | 2014-09-24 | 洛阳凯美胜石化设备有限公司 | Distributor and distillation device with same |
| CN104645664A (en) * | 2014-05-06 | 2015-05-27 | 柳州蓓蒂芬科技有限公司 | Continuous countercurrent differential extraction method and continuous countercurrent differential extraction device |
| CN109179843A (en) * | 2018-11-14 | 2019-01-11 | 中国华能集团清洁能源技术研究院有限公司 | A kind of water-saving dry coal powder pressure gasifying usage on black water device |
| 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 |
-
2013
- 2013-04-28 CN CN2013202294462U patent/CN203227322U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104645664A (en) * | 2014-05-06 | 2015-05-27 | 柳州蓓蒂芬科技有限公司 | Continuous countercurrent differential extraction method and continuous countercurrent differential extraction device |
| CN104056463A (en) * | 2014-06-05 | 2014-09-24 | 洛阳凯美胜石化设备有限公司 | Distributor and distillation device with same |
| CN109179843A (en) * | 2018-11-14 | 2019-01-11 | 中国华能集团清洁能源技术研究院有限公司 | A kind of water-saving dry coal powder pressure gasifying usage on black water device |
| 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 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20180907 Address after: 116085 128 high energy street, Qixian Ling high tech Industrial Park, Dalian, Liaoning Patentee after: ACRE COKING & REFRACTORY ENGINEERING CONSULTING CORPORATION (DALIAN), MCC Address before: 116085 128 high energy street, Qixian Ling high tech Industrial Park, Dalian, Liaoning Patentee before: ACRE COKING & REFRACTORY ENGINEERING CONSULTING CORPORATION, MCC |
|
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20131009 |