CN101250079A - Heat-exchange network device for refining crude benzene and method of operation - Google Patents
Heat-exchange network device for refining crude benzene and method of operation Download PDFInfo
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- CN101250079A CN101250079A CNA2008100525610A CN200810052561A CN101250079A CN 101250079 A CN101250079 A CN 101250079A CN A2008100525610 A CNA2008100525610 A CN A2008100525610A CN 200810052561 A CN200810052561 A CN 200810052561A CN 101250079 A CN101250079 A CN 101250079A
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Abstract
The invention relates to a heat exchange network for refining crude benzene, which coprises a prelimineary distribution column, an extractive distillation column, a solvent recovery column and a benzene toluene column, wherein the four columns are both arranged with a reboiler, the extractive distillation column and the benzene toluene are both arranged with a feeding preheater. The operation method comprises feeding the bottom poor solvent at the bottom of the solvent recovery column into the middle reboiler of the extractive distillation column, the reboiler of the benzene toluene column, the reboiler of the solvent recovery column, the feeding preheater of the extractive distillation column and the feeding preheater of the benzene toluene column in turn to exchange heat or into the middle reboiler of the extractive distillation column, the reboiler of the prelimineary distribution column, the reboile rof the benzene toluene column, the reboiler of the solvent recovery column, the feeding preheater of the extractive distillation column and the feeding preheater of the benzene toluene column to exchange heat, and directly feeding the poor solvent after heat exchange into the extractive distillation unit to be circulated. Compared with acid washing method, the inventive separation process has no byproduct and no waste discharge, whose sulfur and nitrogen content in product is lower than 1ppm, and compared with the distillation of Krupp-Koppes method or the like, the invention can reduce 1/3-1/2 of cost and 20-30% of energy consumption.
Description
Technical field
The invention belongs to the distillation technology field, particularly relate to the heat exchanger network and the working method of crude benzene refining.
Background technology
Benzene, toluene are purposes basic Organic Chemicals very widely, and they are mainly derived from refining of petroleum and coal tar process.Coking crude benzene is to reclaim a kind of benzoline obtain from raw gas, and main component is mononuclear aromatics such as benzene,toluene,xylene, heavy aromatics, accounts for 90%, and wherein benzene accounts for 75%, toluene accounts for 8-20%, dimethylbenzene accounts for 2-5%.Still contain plurality of impurities in the coking crude benzene, can kind more than 90 just be arranged quantitative all the other components, influence the coking benzene deep processing greatly.Annual at present about 300,000,000 tons of the coke of producing of China, the crude benzol amount is about 2,800,000 tons, but about 1,700,000 tons of actual recovered crude benzol, the rate of recovery only is 60%, crude benzol does not have all major causes of recovery, being that the medium-sized and small enterprises rate of recovery is low does not build the crude benzol retrieving arrangement with simple and easy cokery, and coking crude benzene production is with a wide range of applications.
The coking benzene industrial production is a kind of extremely complicated technological process, the boiling-point difference of the unsaturated compound that contains in the benzene-toluene-xylene mixture of preliminary pre-rectifying and the boiling point of sulfide and benzene-type products is very little, in passing through the process of crude benzol low temperature hydrogenation refined products, its component is that 66～99 ℃ stable hydrocarbon and 103～120 ℃ unsaturated hydrocarbons form azeotrope with benzene and toluene respectively for boiling spread then, also have and benzene, some compounds such as hexanaphthene that the toluene boiling point is very approaching, therefore cyclopentenes etc. take very difficult clean cut separation of general conventional distillation method or process energy consumption higher.
At present, industrial method by crude benzol scale operation benzene aromatic hydrocarbon has two kinds: acid wash and shortening method.Acid wash is earlier to isolate dithiocarbonic anhydride, cyclopentadiene etc. by primary tower by cat head, then introduces pickling reactor at the bottom of the tower, reaction product through mix with water, acid is separating of oil, acid regeneration, alkali cleaning separate, wash operations such as benzene separates.Though acid wash technology is simple, technology maturation, flexible operation, progressively is eliminated because of environmental problem is very outstanding, many countries ban use of, and China also requires to forbid to build at present, time limit eliminates.Since the 1950's, the U.S., Germany, Japan, France etc. develop the shortening method.China has mainly introduced German Crewe Pu-Kao Baisi (Krupp-Koppes) method and U.S. Lai Tuoer (Litol) method since the eighties in 20th century, and wherein Krupp-Koppes technology has material impact to China's crude benzene refining industry.Though these hydrogen addition technologies are advanced reliable aspect desulfurization removing nitric, but separation phase still adopts temperature height, flow process that pressure is high behind hydrogenation, heat exchange process is very complicated, and is strict to equipment, pipeline material and technological operation, and one-time investment is big, running cost is high.
Summary of the invention
The object of the invention is to provide the distillation process and the heat exchanger network of crude benzene refining, this method is used for crude benzol through the refining sepn process behind the shortening, this rectificating method and heat exchange process are finished under the mild operating conditions of low-temp low-pressure, the step of realizing energy reclaims and utilization, has advantages such as reduced investment, energy consumption is low, operational path is simple and direct in industrial application.
The present invention is realized by the following technical programs:
The heat-exchange network device of a kind of crude benzene refining of the present invention comprises and presorts tower, extractive distillation column, solvent recovery tower and benzene toluene tower; Wherein four towers are provided with reboiler, and extractive distillation column and benzene toluene tower are provided with feed preheater.
The heat-exchange network device of crude benzene refining of the present invention is: presort the tower middle part and establish opening for feed, overhead stream (13) pipeline is connected the back and links to each other with extractive distillation column as extractive distillation column master feeding line with extractive distillation column preheater (9), logistics (12) extraction is set at the bottom of presorting Tata; Extractive distillation column master opening for feed top is provided with the lean solvent feeding line, and the top rectifying section is provided with intermediate reboiler (5), and cat head is provided with material (14) extraction pipeline, material (15) extraction pipeline is set at the bottom of the tower and links to each other with the main feeding line of solvent recovery tower (3); The solvent recovery tower epimere is provided with intermediate reboiler (8), and material (17) extraction is set at the bottom of the tower, and cat head is provided with material (16) extraction and is connected the back with benzene toluene tower preheater (10) and links to each other with the benzene toluene tower as benzene toluene tower master feeding line; Material (19) extraction is set at the bottom of the benzene toluene Tata, and cat head is provided with material (18) extraction; Material (17) extraction is set at the bottom of the solvent recuperation Tata is divided into three sections: one section links to each other with benzene toluene tower reboiler (7), intermediate reboiler (8), preheater (9), one section with presort tower reboiler (6), preheater (9) links to each other, one section links to each other with intermediate reboiler (5), and three sections remerge the back and are connected with benzene toluene tower preheater (10) and then link to each other with extractive distillation column as the lean solvent feeding line.
The working method of the heat-exchange network device of crude benzene refining of the present invention is that lean solvent at the bottom of the solvent recuperation Tata is carried out heat exchange as extractive distillation column intermediate reboiler, benzene toluene tower reboiler, solvent recovery tower intermediate reboiler, extractive distillation column feed preheater, benzene toluene tower feed preheater successively; Or successively as the extractive distillation column intermediate reboiler, presort tower reboiler, benzene toluene tower reboiler, solvent recovery tower intermediate reboiler, extractive distillation column feed preheater, benzene toluene tower feed preheater and carry out heat exchange; Lean solvent recycles through can directly going back to the extracting rectifying unit after the heat exchange.
The tower working method of presorting of the present invention is: crude benzol raw material (11) enters and presorts tower (1) separation system by presorting tower middle part, this tower is at normal pressure or be no more than under the pressure-fired of 130KPa and operate, tower top temperature is 80-120 ℃, control of reflux ratio is 1.5-3.5, distillate dimethylbenzene and above heavy aromatics (12) at the bottom of the tower, cat head distillates benzene, toluene and most of non-aromatics (13); Presorting the tower theoretical stage is 40-60, and column internals is the efficient Mellapak packing tower with performance of anti-blockage, or employing has the valve tray that pushes away the liquid function; Presort the column overhead cut and rise near entering extractive distillation column (2) behind the bubble point temperature by heat exchanger network and further separate continuously, tower bottom distillate then can adopt the gap distillation method to produce high-purity dimethylbenzene product.
Extractive distillation column working method of the present invention is: extractive distillation column is a positive pressure operation, corresponding tower top temperature is 85-135 ℃, and reflux ratio is 1-4, and extractant feed and material charging mass ratio are 3-10, the extraction tower cat head distillates non-aromatics (14), distillates benzene, toluene and solvent (15) at the bottom of the tower; The extractive distillation column theoretical stage is 50-65, and column internals adopts the mixed form of efficient Mellapak packing and valve tray, and wherein the following stripping section of charging is a tray structure; The extractive distillation column rectifying section is established intermediate reboiler (5), and heating medium is one section a lean solvent in the heat exchange process; The extractive distillation column tower bottom distillate is by pressing certainly or pump enters solvent recovery tower (3) and further separates continuously, and overhead fraction (14) goes out the battery limit (BL) as the chemical industry light oil product.
Described extraction agent is N-formyl morpholine, N-Methyl pyrrolidone, ring fourth maple or glycol; Or the compounding substances between them.
Solvent recovery tower working method of the present invention is: solvent recovery tower is a negative-pressure operation, and tower top pressure is 20-40KPa (a), and corresponding tower top temperature is 40-65 ℃, and reflux ratio is 1-2, and cat head distillates benzene and toluene (16), distillates solvent (17) at the bottom of the tower; The solvent recovery tower theoretical stage is 15-30, and column internals adopts efficient Mellapak packing, or the float valve tray column, or their mixed form; Solvent recovery tower rectifying section bottom is provided with intermediate reboiler (8), and heating medium is one section lean solvent in the heat exchange process; The solvent recovery tower overhead fraction enters benzene toluene tower (4) further continuously to be separated, and tower bottom distillate is that the lean solvent that is rich in calorific value enters heat exchange process Continuous Heat Transfer cooling back and goes back to the extracting rectifying unit and recycle.
Benzene toluene tower working method of the present invention is: the benzene toluene tower is normal pressure or the micro-pressure operation that is no more than 130KPa, and corresponding tower top temperature is 80-90 ℃, and reflux ratio is 1.5-2.5, and cat head distillates purified petroleum benzin product (18), distillates pure toluene product (19) at the bottom of the tower; Benzene toluene tower theoretical stage is 40-60, and column internals can adopt efficient structured packing or valve tray; Benzene toluene tower reboiler heating medium is one section lean solvent in the heat exchanger network.
With the coking crude benzene behind the hydrogenation is raw material, utilize extraction rectifying method and step Energy Saving Strategy to produce high pure benzene, toluene and dimethylbenzene product, sepn process is finished under the mild condition of low temperature, low pressure, the step of realizing energy reclaims and utilizes, and reaches that energy consumption is minimum, the investment purpose of province.Belong to the coking benzene purification techniques.
The present invention has following advantage: 1. sepn process is compared with acid wash does not have by product, does not have waste discharge, and product sulphur nitrogen content is lower than 1ppm; 2. course of processing benzene aromatic hydrocarbon product yield and purity are very high, and for example, benzaldehyde product purity can reach more than 99.9%, the rate of recovery can reach more than 99.5%, and the toluene product purity can reach more than 99.5%, the rate of recovery can reach more than 99.0%; 3. rectifying tower process conditions gentleness, generally below 0.1MPa (G), the process-stream temperature is below 200 ℃ for pressure; 4. the extracting rectifying unit extracts than low, the rectification efficiency height; 5. rectification process turndown ratio height, insensitive to the change in concentration of raw material treatment capacity and crude benzol composition, 6. heat exchanger network is flexible, can adaptive kinds of processes condition; The distillation process of 7. relative Krupp-Koppes method or similar approach, investment reduces 1/3-1/2, and energy consumption reduces 20-30%.
Description of drawings
Fig. 1: the schematic flow sheet of crude benzene refining;
Wherein 1 for presorting tower, 2 is extractive distillation column, 3 is solvent recovery tower, and 4 is the benzene toluene tower, and 5 is the extractive distillation column intermediate reboiler, 6 for presorting the tower reboiler, 7 is benzene toluene tower reboiler, and 8 is the solvent recovery tower intermediate reboiler, and 9 is the extractive distillation column feed preheater, 10 is benzene toluene tower feed preheater, 11 is the crude benzole hydrogenation liquid raw material, and 12 is heavy aromatics, and 13 is light fragrant non-aromatic mixture, 14 is non-aromatic chemical industry light oil, 15 is light fragrant solvent mixture, and 16 is the benzene toluene mixture, and 17 is lean solvent, 18 is purified petroleum benzin, and 19 is pure toluene.
Embodiment
Below in conjunction with embodiment and accompanying drawing the present invention is described in further detail, but the present invention is not limited to this.
Adopt the mode of connection of accompanying drawing, presort the tower middle part and establish opening for feed, overhead stream (13) pipeline is with after extractive distillation column preheater (9) is connected, and exports to link to each other with extractive distillation column as extractive distillation column master feeding line, logistics (12) extraction is set at the bottom of presorting Tata; Extractive distillation column master opening for feed top is provided with the lean solvent feeding line, the top rectifying section is provided with intermediate reboiler (5), cat head is provided with material (14) extraction pipeline, material (15) extraction pipeline is set at the bottom of the tower and is connected with solvent recovery tower (3) and as its main feeding line; The solvent recovery tower epimere is provided with intermediate reboiler (8), and material (17) extraction is set at the bottom of the tower, and material (16) extraction is set cat head and with after benzene toluene tower preheater (10) is connected, outlet links to each other with the benzene toluene tower as benzene toluene tower master feeding line; Material (19) extraction is set at the bottom of the benzene toluene Tata, and cat head is provided with material (18) extraction; Material (17) extraction is set at the bottom of the solvent recuperation Tata is divided into three sections: one section links to each other with benzene toluene tower reboiler (7), intermediate reboiler (8), preheater (9), one section with presort tower reboiler (6), preheater (9) links to each other, one section links to each other with intermediate reboiler (5), and three sections remerge the back and are connected with benzene toluene tower preheater (10) and then link to each other with extractive distillation column as the lean solvent feeding line.
Embodiment according to this device is as follows:
Embodiment 1:
Process 100,000 tons of/year crude benzol raw materials, benzene content 78%, toluene level 13%, choosing the N-formyl morpholine is solvent, solvent ratio is 5: 1.Presort column overhead pressure 0.01MPa (G), temperature is 80-90 ℃, reflux ratio is 1.5-1.7; Extractive distillation column tower top pressure 0.05MPa (G), temperature are 86-96 ℃, and reflux ratio is 1.0-1.2; Recovery tower tower top pressure-0.08MPa (G), temperature are 40-50 ℃, and reflux ratio is 1.0-1.2; Benzene toluene column overhead pressure 0.01MPa (G), temperature are 80-85 ℃, and reflux ratio is 1.5-1.7.Lean solvent carries out heat exchange as extractive distillation column intermediate reboiler, benzene toluene tower reboiler, solvent recovery tower intermediate reboiler, extractive distillation column feed preheater, benzene toluene tower feed preheater successively at the bottom of the solvent recuperation Tata.
Through behind the said process, main products benzene meets the country-level standard of coking benzene, and purity is 99.9%, the rate of recovery is 99.5%, and major product toluene meets the coking toluene national grade ii standard, and purity is 99.5%, the rate of recovery is 99.0%.It is 2.88MKJ that 1 ton of crude benzol of every processing needs the external source heating load.
Embodiment 2:
Process 50,000 tons of/year crude benzol raw materials, benzene content 73%, toluene level 15%, choosing N-Methyl pyrrolidone is solvent, solvent ratio is 7.5: 1.Presort column overhead pressure 0.1MPa (G), temperature is 100-120 ℃, reflux ratio is 3.5; Extractive distillation column tower top pressure 0.1MPa (G), temperature are 120-133 ℃, and reflux ratio is 3-4; Recovery tower tower top pressure-0.06MPa (G), temperature are 60-65 ℃; Benzene toluene column overhead pressure 0.05MPa (G), temperature are 90-95 ℃.At the bottom of the solvent recuperation Tata lean solvent successively as the extractive distillation column intermediate reboiler, presort tower reboiler, benzene toluene tower reboiler, solvent recovery tower intermediate reboiler, extractive distillation column feed preheater, benzene toluene tower feed preheater and carry out heat exchange.
Through behind the said process, main products benzene meets the country-level standard of coking benzene, and purity is 99.9%, the rate of recovery is 99.6%, and major product toluene meets the coking toluene national grade ii standard, and purity is 99.5%, the rate of recovery is 99.1%.It is 3.45MKJ that 1 ton of crude benzol of every processing needs the external source heating load.
Embodiment 3:
Process 150,000 tons of/year crude benzol raw materials, benzene content 74%, toluene level 17%, choosing the N-formyl morpholine is solvent, solvent ratio is 5.5: 1.Presort column overhead pressure 0.05MPa (G), temperature is 99 ℃; Extractive distillation column tower top pressure 0.09MPa (G), temperature are 96 ℃; Recovery tower tower top pressure-0.06MPa (G), temperature are 59 ℃; Benzene toluene column overhead pressure 0.02MPa (G), temperature are 85 ℃.Lean solvent carries out heat exchange as extractive distillation column intermediate reboiler, benzene toluene tower reboiler, solvent recovery tower intermediate reboiler, extractive distillation column feed preheater, benzene toluene tower feed preheater successively at the bottom of the solvent recuperation Tata.
Through behind the said process, main products benzene meets the country-level standard of coking benzene, and purity is 99.9%, the rate of recovery is 99.5%, and major product toluene meets the coking toluene national grade ii standard, and purity is 99.5%, the rate of recovery is 99.0%.It is 2.99MKJ that 1 ton of crude benzol of every processing needs the external source heating load.
Claims (8)
1. the heat-exchange network device of a crude benzene refining comprises and presorts tower, extractive distillation column, solvent recovery tower and benzene toluene tower; It is characterized in that four towers are provided with reboiler, extractive distillation column and benzene toluene tower are provided with feed preheater.
2. the heat-exchange network device of crude benzene refining as claimed in claim 1, it is characterized in that: presort the tower middle part and establish opening for feed, overhead stream (13) pipeline is connected the back and links to each other with extractive distillation column as extractive distillation column master feeding line with extractive distillation column preheater (9), logistics (12) extraction is set at the bottom of presorting Tata; Extractive distillation column master opening for feed top is provided with the lean solvent feeding line, and the top rectifying section is provided with intermediate reboiler (5), and cat head is provided with material (14) extraction pipeline, material (15) extraction pipeline is set at the bottom of the tower and links to each other with the main feeding line of solvent recovery tower (3); The solvent recovery tower epimere is provided with intermediate reboiler (8), and material (17) extraction is set at the bottom of the tower, and cat head is provided with material (16) extraction and is connected the back with benzene toluene tower preheater (10) and links to each other with the benzene toluene tower as benzene toluene tower master feeding line; Material (19) extraction is set at the bottom of the benzene toluene Tata, and cat head is provided with material (18) extraction; Material (17) extraction is set at the bottom of the solvent recuperation Tata is divided into three sections: one section links to each other with benzene toluene tower reboiler (7), intermediate reboiler (8), preheater (9), one section with presort tower reboiler (6), preheater (9) links to each other, one section links to each other with intermediate reboiler (5), and three sections remerge the back and are connected with benzene toluene tower preheater (10) and then link to each other with extractive distillation column as the lean solvent feeding line.
3. by the working method of the heat-exchange network device of claim 1 or 2 described crude benzene refinings, it is characterized in that lean solvent at the bottom of the solvent recuperation Tata is carried out heat exchange as extractive distillation column intermediate reboiler, benzene toluene tower reboiler, solvent recovery tower intermediate reboiler, extractive distillation column feed preheater, benzene toluene tower feed preheater successively; Or successively as the extractive distillation column intermediate reboiler, presort tower reboiler, benzene toluene tower reboiler, solvent recovery tower intermediate reboiler, extractive distillation column feed preheater, benzene toluene tower feed preheater and carry out heat exchange; Lean solvent recycles through can directly going back to the extracting rectifying unit after the heat exchange.
4. the working method of the heat-exchange network device of crude benzene refining as claimed in claim 3, it is characterized in that the described tower working method of presorting is: crude benzol raw material (11) enters and presorts tower (1) separation system by presorting tower middle part, this tower is at normal pressure or be no more than under the pressure-fired of 130KPa and operate, tower top temperature is 80-120 ℃, control of reflux ratio is 1.5-3.5, distillate dimethylbenzene and above heavy aromatics (12) at the bottom of the tower, cat head distillates benzene, toluene and most of non-aromatics (13); Presorting the tower theoretical stage is 40-60, and column internals is the efficient Mellapak packing tower with performance of anti-blockage, or employing has the valve tray that pushes away the liquid function; Presort the column overhead cut and rise near entering extractive distillation column (2) behind the bubble point temperature by heat exchanger network and further separate continuously, tower bottom distillate then can adopt the gap distillation method to produce high-purity dimethylbenzene product.
5. the working method of the heat-exchange network device of crude benzene refining as claimed in claim 3, it is characterized in that described extractive distillation column working method is: extractive distillation column is a positive pressure operation, corresponding tower top temperature is 85-135 ℃, reflux ratio is 1-4, solvent ratio is 3-10, the extraction tower cat head distillates non-aromatics (14), distillates benzene, toluene and solvent (15) at the bottom of the tower; The extractive distillation column theoretical stage is 50-65, and column internals adopts the mixed form of efficient Mellapak packing and valve tray, and wherein the following stripping section of charging is a tray structure; The extractive distillation column rectifying section is established intermediate reboiler (5), and heating medium is one section a lean solvent in the heat exchange process; The extractive distillation column tower bottom distillate is by pressing certainly or pump enters solvent recovery tower (3) and further separates continuously, and overhead fraction (14) goes out the battery limit (BL) as the chemical industry light oil product.
6. the working method of the heat-exchange network device of crude benzene refining as claimed in claim 5 is characterized in that described solvent is N-formyl morpholine, N-Methyl pyrrolidone, ring fourth maple or glycol; Or the compounding substances between them.
7. the working method of the heat-exchange network device of crude benzene refining as claimed in claim 3, it is characterized in that described solvent recovery tower working method is: solvent recovery tower is a negative-pressure operation, tower top pressure is 20-40KPa (a), corresponding tower top temperature is 40-65 ℃, reflux ratio is 1-2, cat head distillates benzene and toluene (16), distillates solvent (17) at the bottom of the tower; The solvent recovery tower theoretical stage is 15-30, and column internals adopts efficient Mellapak packing, or the float valve tray column, or their mixed form; Solvent recovery tower rectifying section bottom is provided with intermediate reboiler (8), and heating medium is one section lean solvent in the heat exchange process; The solvent recovery tower overhead fraction enters benzene toluene tower (4) further continuously to be separated, and tower bottom distillate is that the lean solvent that is rich in calorific value enters heat exchange process Continuous Heat Transfer cooling back and goes back to the extracting rectifying unit and recycle.
8. the working method of the heat-exchange network device of crude benzene refining as claimed in claim 3, it is characterized in that described benzene toluene tower working method is: the benzene toluene tower is normal pressure or the micro-pressure operation that is no more than 130KPa, corresponding tower top temperature is 80-90 ℃, reflux ratio is 1.5-2.5, cat head distillates purified petroleum benzin product (18), distillates pure toluene product (19) at the bottom of the tower; Benzene toluene tower theoretical stage is 40-60, and column internals can adopt efficient structured packing or valve tray; Benzene toluene tower reboiler heating medium is one section lean solvent in the heat exchanger network.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102116593A (en) * | 2011-01-30 | 2011-07-06 | 北京三博中自科技有限公司 | Structured heat exchange network system and construction method thereof |
| CN102553280A (en) * | 2012-03-07 | 2012-07-11 | 天津大沽化工股份有限公司 | Benzene/toluene tower type primary preheating device |
| CN102600628A (en) * | 2012-02-13 | 2012-07-25 | 云南昆钢煤焦化有限公司 | High-efficiency rectification device for dimethylbenzene |
| CN103232317A (en) * | 2013-04-05 | 2013-08-07 | 大连理工大学 | Aromatic hydrocarbon purification apparatus and process used in hydrofining of coking crude benzene |
| CN104230657A (en) * | 2014-09-16 | 2014-12-24 | 山东特普化工技术有限公司 | Novel energy-saving three-tower continuous extractive distillation technology and extractive distillation system thereof |
| CN105085152A (en) * | 2014-05-05 | 2015-11-25 | 北京华和拓科技开发有限责任公司 | Novel extraction process for aromatic hydrocarbons |
| CN109053356A (en) * | 2018-08-06 | 2018-12-21 | 宁夏宝丰能源集团股份有限公司 | A kind of extraction separating method and crude benzol processing technology of triphenyl fraction |
| CN111111248A (en) * | 2018-10-30 | 2020-05-08 | 中国石油化工股份有限公司 | Device and method for recovering toluene from organic solvent for preparing polyolefin catalyst |
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- 2008-03-28 CN CNA2008100525610A patent/CN101250079A/en active Pending
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102116593A (en) * | 2011-01-30 | 2011-07-06 | 北京三博中自科技有限公司 | Structured heat exchange network system and construction method thereof |
| CN102116593B (en) * | 2011-01-30 | 2013-01-02 | 北京三博中自科技有限公司 | Structured heat exchange network system and construction method thereof |
| CN102600628A (en) * | 2012-02-13 | 2012-07-25 | 云南昆钢煤焦化有限公司 | High-efficiency rectification device for dimethylbenzene |
| CN102600628B (en) * | 2012-02-13 | 2014-06-04 | 云南煤业能源股份有限公司 | High-efficiency rectification device for dimethylbenzene |
| CN102553280A (en) * | 2012-03-07 | 2012-07-11 | 天津大沽化工股份有限公司 | Benzene/toluene tower type primary preheating device |
| CN103232317A (en) * | 2013-04-05 | 2013-08-07 | 大连理工大学 | Aromatic hydrocarbon purification apparatus and process used in hydrofining of coking crude benzene |
| CN105085152A (en) * | 2014-05-05 | 2015-11-25 | 北京华和拓科技开发有限责任公司 | Novel extraction process for aromatic hydrocarbons |
| CN104230657A (en) * | 2014-09-16 | 2014-12-24 | 山东特普化工技术有限公司 | Novel energy-saving three-tower continuous extractive distillation technology and extractive distillation system thereof |
| CN109053356A (en) * | 2018-08-06 | 2018-12-21 | 宁夏宝丰能源集团股份有限公司 | A kind of extraction separating method and crude benzol processing technology of triphenyl fraction |
| CN111111248A (en) * | 2018-10-30 | 2020-05-08 | 中国石油化工股份有限公司 | Device and method for recovering toluene from organic solvent for preparing polyolefin catalyst |
| CN111111248B (en) * | 2018-10-30 | 2021-10-15 | 中国石油化工股份有限公司 | Device and method for recovering toluene from organic solvent for preparing polyolefin catalyst |
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