CN103664481A - Method for refining petrobenzene and thiophene by adopting double-partition-wall extraction rectifying tower - Google Patents
Method for refining petrobenzene and thiophene by adopting double-partition-wall extraction rectifying tower Download PDFInfo
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Abstract
The invention creates and provides a method for refining petrobenzene and thiophene by adopting a double-partition-wall extraction rectifying tower, which comprises the following steps: using double-partition-wall extraction rectifying tower to replace a common rectifying tower, removing light and removing weight of coked crude benzene, and then refining to obtain benzene and thiophene. Two processes of benzene refining and thiophene refining are combined to simultaneously perform in the double-partition-wall extraction rectifying tower, the process flow is greatly simplified, and equipment investment and energy consumption are obviously reduced. The benzene product with a purity of 99.99% and the thiophene product with a purity of more than 99.5% are obtained, the quality of the benzene product achieves the standard of petrobenzene and is capable of substituting petrobenzene; the waste solid and waste liquid cannot be produced in the treatment process, environmental pollution is avoided, and the method is an energy-saving and environmental-friendly coked crude benzene refining method.
Description
Technical field
The invention relates to a kind of method that adopts two next door extractive distillation column turpentole benzene and thiophene, belongs to coked crude benzene refining technical field.
Background technology
Benzene is important basic organic chemical industry raw material, and main source is the coking crude benzene that coking industry produces.The composition of coking crude benzene is very complicated, and particularly sulfide thiophene has a significant impact the quality of benzaldehyde product.Traditional method for refining carbonization crude benzole has acid wash and shortening method, although acid wash technique is simple, suitability is wide, has produced acid tar and the waste residue that cannot process in a large number in treating processes, and serious environment pollution, is banned use of by country at present.Shortening method complex process, working condition harshness, high to catalyzer requirement, so the exploitation of high performance catalyst has become the main obstruction of this method development.Although above two kinds of methods can obtain the benzene of higher degree, quality and petroleum benzene differ greatly, and have destroyed valuable medical synthesis material-thiophene, cause the wasting of resources.
Along with field of fine chemical improving constantly the requirement of benzene quality, in industry, developed and take extracting rectifying as basic coked crude benzene refining technology, a large amount of improvement aspect production technique, have been done, overcome the deficiency that acid wash and shortening method exist, improved the purity of benzene, the recovery of thiophene has also been had to certain effect.But quality and the petroleum benzene of benzene still have gap, and the purity of thiophene and the rate of recovery are not high, various facility investment and the energy consumption of making for the treatment of step is quite large.In < < method for refining carbonization crude benzole > > as disclosed in CN101019918A, coking crude benzene is through crude benzol pre-treatment, two process procedures of benzene cut extracting rectifying, comprise eight rectifying tower, technical process is tediously long, and the facility investment causing and energy consumption are very large; The purity of benzene is 99.9%, and its quality does not reach the standard of petroleum benzene.
Summary of the invention
In order to overcome, prior art processes flow process is tediously long, facility investment and energy consumption is high, product quality is low problem, the invention provides a kind of method that adopts two next door extractive distillation column turpentole benzene and thiophene, refining two processes of benzene refining and thiophene are incorporated in a next door tower with two dividing plates and are carried out, by extracting rectifying, obtain high-quality benzaldehyde product and thiophene product simultaneously, simplify the flow process of existing extraction rectification technique, greatly reduced facility investment and energy consumption.
For solving the problems of the technologies described above, the technical scheme that the invention adopts is:
The method that adopts two next door extractive distillation column turpentole benzene and thiophene, described method is first raw material coking crude benzene to be added in lightness-removing column, the light constituent by overhead extraction boiling point lower than benzene, tower reactor material enters weight-removing column; Then the heavy constituent higher than benzene by weight-removing column tower reactor extraction boiling point, overhead extraction is rich in the crude benzol of thiophene and enters the extractive distillation column of two next doors from the middle part in extractive distillation column pre-separation district, two next door; Extraction agent carries out pre-separation with crude benzol reverse contact pre-separation district of being rich in thiophene to being rich in the crude benzol of thiophene from the pre-separation district of two next doors extractive distillation column and the middle and upper part charging in the first side exploiting field simultaneously, residual light constituent in overhead extraction crude benzol, the first side exploiting field obtains highly purified benzaldehyde product, the second side exploiting field obtains highly purified thiophene product, and tower reactor material enters recovery tower; Material from two next doors extractive distillation column tower reactor enters recovery tower, and pre-separation district and the first side exploiting field that the extraction agent after recovery returns to two next doors extractive distillation column by flow metering recycle;
Described pair of next door extractive distillation column is an extractive distillation column that two vertical partition plates are housed, tower body is divided into pre-separation district, public rectification zone, public stripping section, the first side exploiting field and the second side exploiting field five parts by two dividing plates, the middle part charging in the pre-separation district of raw material from the extractive distillation column of two next doors, extraction agent is from the middle and upper part charging in pre-separation district and the first side exploiting field, benzaldehyde product after the first side exploiting field is refining for extraction, the thiophene product after the second side exploiting field is refining for extraction.
The working pressure of described lightness-removing column is 50-101kPa, tower top temperature 50-80 ℃, tower reactor temperature 90-110 ℃; The working pressure 50-101kPa of described weight-removing column, tower top temperature 55-85 ℃, tower reactor temperature 95-120 ℃; The working pressure of described pair of next door extractive distillation column is 50-101kPa, solvent ratio is (1-10): 1, and tower top temperature 60-85 ℃, tower reactor temperature 100-140 ℃, it is 58-80 ℃ that temperature is controlled in the discharging in the first side exploiting field, and it is 60-85 ℃ that temperature is controlled in the discharging in the second side exploiting field; Recovery tower working pressure is 20-101kPa.
Preferably, the working pressure of described lightness-removing column is 80-101kPa, tower top temperature 65-80 ℃, tower reactor temperature 95-110 ℃; The working pressure 80-101kPa of described weight-removing column, tower top temperature 70-85 ℃, tower reactor temperature 105-120 ℃; The working pressure of described pair of next door extractive distillation column is 80-101kPa, and solvent ratio is (1-5): 1, and tower top temperature 75-85 ℃, tower reactor temperature 110-140 ℃; It is 73-80 ℃ that temperature is controlled in the discharging in the first side exploiting field, and it is 76-85 ℃ that temperature is controlled in the discharging in the second side exploiting field; Recovery tower working pressure is 50-101kPa.
Described extraction agent is the double solvents of ionic liquid or ionic liquid and organic solvent.
Preferably, described extraction agent is that ionic liquid 1-butyl-3-methyl imidazolium a tetrafluoro borate and organic solvent ethylene glycol are according to mass ratio 1:(1-5) mix or ionic liquid 1-butyl-3-methyl imidazolium a tetrafluoro borate and 1-ethyl-3-methylimidazole acetate according to mass ratio 1:(1-3) mix.
Another object of the present invention is to provide a kind of two next doors extractive distillation column of the method for turpentole benzene and thiophene, two vertical partition plates are equipped with in extractive distillation column inside, described pair of next door, and the first dividing plate is positioned at the left side of second partition, the two dividing plates parallel Ta Bishang that is fixed on that interlocks, wherein the upper end of the first dividing plate and the distance of tower top are less than the lower end of the first dividing plate and the distance at the bottom of tower, the upper end of second partition and the distance of tower top are greater than the lower end of second partition and the distance at the bottom of tower, described dividing plate is divided into pre-separation district by tower body, the first side exploiting field, the second side exploiting field, public rectification zone and public stripping zone five parts, from the upper end of the first dividing plate, to the region forming tower top, be wherein public rectification zone, the lower end of second partition is public stripping zone to the region forming between at the bottom of tower, the right side of second partition is the second side exploiting field, the right side of the first dividing plate and the region that is positioned at second partition upper end are the first side exploiting field, the remaining region that is positioned at the first dividing plate and second partition left side is pre-separation district, raw material is by the side charging of pre-separation district, and extraction agent is from pre-separation district and the first side exploiting field charging, and the first side exploiting field and the second side exploiting field are for the refining product of extraction process extracting rectifying.
The height of described the first dividing plate and second partition is all less than the height of tower, and the length of the first dividing plate is greater than the length of second partition.
Advantage and positively effect that the invention has are: (1) disclosed by the invention pair of next door extractive distillation column, refining two processes of benzene refining and thiophene are incorporated in same seat tower and are carried out, can obtain two kinds of high purity products simultaneously, greatly simplified the technical process of prior art, facility investment and energy consumption obviously reduce, facility investment is only the 40-50% of prior art, Energy Intensity Reduction more than 45%, simple technical process has also reduced the floor space of equipment;
(2) the present invention has obtained thiophene product more than 99.99% benzaldehyde product and 99.5%, the indexs such as the look of benzaldehyde product number, bromine valency, ctystallizing point, sulphur nitrogen impurity content all reach the standard of GB one-level petroleum benzene, can replace petroleum benzene to use, the rate of recovery of thiophene is greater than 97%, and the economic benefit that the inventive method increases thus reaches more than 50%;
(3) extraction agent adopting in the present invention is ionic liquid, has Heat stability is good, vapour pressure extremely low, lossless in use procedure, and nontoxic free from corrosion characteristic has also increased the security of production process.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of disclosed method in the present invention
In figure: 1-pre-separation district; The public rectification zone of 2-; The public stripping zone of 3-; 4-the first side exploiting field; 5-the second side exploiting field; 6-the first dividing plate; 7-second partition.
Embodiment
In technical process shown in figure l, comprise lightness-removing column, weight-removing column, two next doors extractive distillation column and recovery tower, wherein coking crude benzene obtains being rich in the crude benzol of thiophene after de-light, de-weight, then the crude benzol that is rich in thiophene enters in the extractive distillation column of two next doors and carries out obtaining pure petroleum benzene and thiophene after extracting rectifying, and rest materials enters the recycling that recovery tower carries out extraction agent.Wherein two vertical partition plates are equipped with in extractive distillation column inside, two next door, the two dividing plates parallel Ta Bishang that is fixed on that interlocks, first upper end of dividing plate 6 and the distance of tower top are less than the lower end of the first dividing plate 6 and the distance at the bottom of tower, the upper end of second partition 7 and the distance of tower top are greater than the lower end of second partition 7 and the distance at the bottom of tower, dividing plate is divided into pre-separation district 1 by tower body, the first side exploiting field 4, the second side exploiting field 5, public rectification zone 2 and public stripping zone 3 five parts: pre-separation district 1 is positioned at the left side of the first dividing plate 6, the first side exploiting field 4 is positioned at the right side of the first dividing plate 6, the second side exploiting field 5 is positioned at the right side of second partition 7, the public rectification zone 2 in pre-separation district 1 and the first side exploiting field 4 is positioned at the position near tower top, the public stripping zone 3 in pre-separation district 1 and the second side exploiting field 5 is positioned near the position at the bottom of tower.The height of the first dividing plate 6 and second partition 7 is all less than the height of tower, and the length of the first dividing plate 6 is greater than the length of second partition 7.
The mixture of the crude benzol that contains thiophene is from the middle part charging of tower, extraction agent is from the middle and upper part charging of tower, first enter the pre-separation district 1 of two dividing wall extractive distillation columns, because extraction agent has changed the relative volatility of each component in incoming mixture, light constituent through pre-separation district 1 rear portion boiling point lower than benzene steams from tower top, residue enters the first side exploiting field 4 on dividing plate one 6 right sides after 2 rectifying of public rectification zone containing the benzene of a small amount of light constituent, fully contact with the extraction agent being entered by the first side exploiting field 4, a small amount of light constituent is separated with benzene, the petroleum benzene that extraction is pure.
Behind pre-separation district 1, boiling point enters higher than the heavy constituent of benzene the public stripping zone 3 being positioned at the bottom of tower and carries and heating up in a steamer, by carrying the second side exploiting field 5 that makes to enter into containing the thiophene of a small amount of heavy constituent the right side that is positioned at second partition 7 after heating up in a steamer, and fully contact again with extraction agent in the second side exploiting field 5, make a small amount of heavy constituent thiophene separated, the thiophene that extraction is pure.
Other heavy constituent mixtures that contain extraction agent that are arranged in public stripping zone enter the further processing recovery of material recycle tower and obtain pure extraction agent recycling.
By following examples, the present invention is described in detail, although provided embodiment, also should be included under the condition that does not depart from the technology of the present invention scope, to those skilled in the art apparent various change.
Press technical process shown in Fig. 1, the main component of raw material coking crude benzene is benzene 64.8%(mass content, as follows), thiophene 5.2%, all the other are light constituent and heavy constituent.Concrete operation step is as follows:
(1) de-light: coking crude benzene is introduced into lightness-removing column, and the working pressure of lightness-removing column is 101kPa, 80 ℃ of tower top temperatures, 110 ℃ of tower reactor temperature, overhead extraction boiling point, lower than the light constituent of benzene, is mainly H
2s, CS
2, the unsaturated hydrocarbons such as amylene, ethylene methacrylic, pentamethylene, hexene, hexane, methylcyclopentane, tower reactor material enters weight-removing column;
(2) de-heavy: the material from lightness-removing column tower reactor enters weight-removing column, weight-removing column working pressure is 90kPa, 72 ℃ of tower top temperatures, 115 ℃ of tower reactor temperature, tower reactor extraction boiling point is higher than the heavy constituent of benzene, be mainly toluene, ethylbenzene, dimethylbenzene, vinylbenzene etc., tower top is the crude benzol that is rich in thiophene, enters two next doors extractive distillation column;
(3) benzene and thiophene are refining: be rich in the crude benzol of thiophene from the middle part charging in extractive distillation column pre-separation district, two next door, a part of extraction agent carries out pre-separation with crude benzol reverse contact pre-separation district of being rich in thiophene to being rich in the crude benzol of thiophene from the pre-separation district middle and upper part charging of two next doors extractive distillation column simultaneously, another part extraction agent is from the middle and upper part charging in the first side exploiting field, to entering the mixture in the first side exploiting field, carry out further separation, extraction agent is the double solvents that ionic liquid 1-butyl-3-methyl imidazolium a tetrafluoro borate and organic solvent ethylene glycol form with mass ratio 1:5, solvent ratio is 8:1, the working pressure of two next doors extractive distillation column is 85kPa, 74 ℃ of tower top temperatures, 128 ℃ of tower reactor temperature, it is 77 ℃ that temperature is controlled in the discharging in the first side exploiting field, it is 81 ℃ that temperature is controlled in the discharging in the second side exploiting field, residual light constituent in overhead extraction crude benzol, the first side exploiting field obtains 99.99% benzaldehyde product, its look number, bromine valency, ctystallizing point, the indexs such as sulphur nitrogen impurity content all reach the standard of GB one-level petroleum benzene, can replace petroleum benzene to use, the second side exploiting field obtains 99.8% thiophene product, and the rate of recovery is 99%, and tower reactor material enters recovery tower,
(4) extraction agent reclaims: the material from two next doors extractive distillation column tower reactor enters recovery tower, the working pressure of recovery tower is 20kPa, tower reactor is the extraction agent after reclaiming, and pre-separation district and the first side exploiting field of by flow metering, returning to two next doors extractive distillation column recycle.
Embodiment 2
Press technical process shown in Fig. 1, the main component of raw material coking crude benzene is benzene 74.2%, thiophene 6.1%, and all the other are light constituent and heavy constituent.Extraction agent is the double solvents that ionic liquid 1-butyl-3-methyl imidazolium a tetrafluoro borate and organic solvent ethylene glycol form with mass ratio 1:1, and solvent ratio is 1:1, and concrete operation step is with embodiment 1, and each tower operating parameters is as shown in the table:
The operating parameters of each tower in table 1 embodiment 2
From the benzaldehyde product of the first side exploiting field extraction 99.99% of two next doors extractive distillation column, the indexs such as its look number, bromine valency, ctystallizing point, sulphur nitrogen impurity content all reach the standard of GB one-level petroleum benzene, can replace petroleum benzene to use; From the thiophene product of the second side exploiting field extraction 99.6%, the rate of recovery is 97%, returns to pair pre-separation district and the first side exploiting field of next doors extractive distillation column recycle after extraction agent reclaims by flow metering.
Embodiment 3
Press technical process shown in Fig. 1, the main component of raw material coking crude benzene is benzene 59.7%, thiophene 8.3%, and all the other are light constituent and heavy constituent.Extraction agent is the double solvents that ionic liquid 1-butyl-3-methyl imidazolium a tetrafluoro borate and 1-ethyl-3-methylimidazole acetate form with mass ratio 1:1, and solvent ratio is 10:1, and concrete operation step is with embodiment 1, and each tower operating parameters is as shown in the table:
The operating parameters of each tower in table 2 embodiment 3
From the benzaldehyde product of the first side exploiting field extraction 99.99% of two next doors extractive distillation column, the indexs such as its look number, bromine valency, ctystallizing point, sulphur nitrogen impurity content all reach the standard of GB one-level petroleum benzene, can replace petroleum benzene to use; From the thiophene product of the second side exploiting field extraction 99.9%, the rate of recovery is 98%, returns to pair pre-separation district and the first side exploiting field of next doors extractive distillation column recycle after extraction agent reclaims by flow metering.
Press technical process shown in Fig. 1, the main component of raw material coking crude benzene is benzene 62.0%, thiophene 4.9%, and all the other are light constituent and heavy constituent.Extraction agent is the double solvents that ionic liquid 1-butyl-3-methyl imidazolium a tetrafluoro borate and 1-ethyl-3-methylimidazole acetate form with mass ratio 1:3, and solvent ratio is 4:1, and concrete operation step is with embodiment 1, and each tower operating parameters is as shown in the table:
The operating parameters of each tower in table 3 embodiment 4
From the benzaldehyde product of the first side exploiting field extraction 99.99% of two next doors extractive distillation column, the indexs such as its look number, bromine valency, ctystallizing point, sulphur nitrogen impurity content all reach the standard of GB one-level petroleum benzene, can replace petroleum benzene to use; From the thiophene product of the second side exploiting field extraction 99.7%, the rate of recovery is 97%, returns to pair pre-separation district and the first side exploiting field of next doors extractive distillation column recycle after extraction agent reclaims by flow metering.
Embodiment 5
Press technical process shown in Fig. 1, the main component of raw material coking crude benzene is benzene 62.0%, thiophene 4.9%, and all the other are light constituent and heavy constituent.Extraction agent is the double solvents that ionic liquid 1-ethyl-3-methylimidazole dimethyl phosphate salt and organic solvent alpha-pyrrolidone form with mass ratio 1:2, and solvent ratio is 5:1, and concrete operation step is with embodiment 1, and each tower operating parameters is as shown in the table:
The operating parameters of each tower in table 4 embodiment 5
From the benzaldehyde product of the first side exploiting field extraction 99.99% of two next doors extractive distillation column, the indexs such as its look number, bromine valency, ctystallizing point, sulphur nitrogen impurity content all reach the standard of GB one-level petroleum benzene, can replace petroleum benzene to use; From the thiophene product of the second side exploiting field extraction 99.8%, the rate of recovery is 97%, returns to pair pre-separation district and the first side exploiting field of next doors extractive distillation column recycle after extraction agent reclaims by flow metering.
Above the embodiment of the invention is had been described in detail, but described content is only the preferred embodiment of the invention, can not be considered to for limiting practical range of the present invention.All equalization variations of doing according to the invention scope and improvement etc., within all should still belonging to this patent covering scope.
Claims (7)
1. the method that adopts two next door extractive distillation column turpentole benzene and thiophene, is characterized in that: described method is first raw material coking crude benzene to be added in lightness-removing column, the light constituent by overhead extraction boiling point lower than benzene, and tower reactor material enters weight-removing column; Then the heavy constituent higher than benzene by weight-removing column tower reactor extraction boiling point, overhead extraction is rich in the crude benzol of thiophene and enters the extractive distillation column of two next doors from the middle part in extractive distillation column pre-separation district, two next door; Extraction agent carries out pre-separation with crude benzol reverse contact pre-separation district of being rich in thiophene to being rich in the crude benzol of thiophene from the pre-separation district of two next doors extractive distillation column and the middle and upper part charging in the first side exploiting field simultaneously, residual light constituent in overhead extraction crude benzol, the first side exploiting field obtains highly purified benzaldehyde product, the second side exploiting field obtains highly purified thiophene product, and tower reactor material enters recovery tower; Material from two next doors extractive distillation column tower reactor enters recovery tower, and pre-separation district and the first side exploiting field that the extraction agent after recovery returns to two next doors extractive distillation column by flow metering recycle;
Described pair of next door extractive distillation column is an extractive distillation column that two vertical partition plates are housed, tower body is divided into pre-separation district, public rectification zone, public stripping section, the first side exploiting field and the second side exploiting field five parts by two dividing plates, the middle part charging in the pre-separation district of raw material from the extractive distillation column of two next doors, extraction agent is from the middle and upper part charging in pre-separation district and the first side exploiting field, benzaldehyde product after the first side exploiting field is refining for extraction, the thiophene product after the second side exploiting field is refining for extraction.
2. method according to claim 1, is characterized in that: the working pressure of described lightness-removing column is 50-101kPa, tower top temperature 50-80 ℃, tower reactor temperature 90-110 ℃; The working pressure 50-101kPa of described weight-removing column, tower top temperature 55-85 ℃, tower reactor temperature 95-120 ℃; The working pressure of described pair of next door extractive distillation column is 50-101kPa, solvent ratio is (1-10): 1, and tower top temperature 60-85 ℃, tower reactor temperature 100-140 ℃, it is 58-80 ℃ that temperature is controlled in the discharging in the first side exploiting field, and it is 60-85 ℃ that temperature is controlled in the discharging in the second side exploiting field; Recovery tower working pressure is 20-101kPa.
3. method according to claim 2, is characterized in that: the working pressure of described lightness-removing column is 80-101kPa, tower top temperature 65-80 ℃, tower reactor temperature 95-110 ℃; The working pressure 80-101kPa of described weight-removing column, tower top temperature 70-85 ℃, tower reactor temperature 105-120 ℃; The working pressure of described pair of next door extractive distillation column is 80-101kPa, and solvent ratio is (1-5): 1, and tower top temperature 75-85 ℃, tower reactor temperature 110-140 ℃; It is 73-80 ℃ that temperature is controlled in the discharging in the first side exploiting field, and it is 76-85 ℃ that temperature is controlled in the discharging in the second side exploiting field; Recovery tower working pressure is 50-101kPa.
4. method according to claim 3, is characterized in that: described extraction agent is the double solvents of ionic liquid or ionic liquid and organic solvent.
5. method according to claim 4, is characterized in that: described extraction agent is that ionic liquid 1-butyl-3-methyl imidazolium a tetrafluoro borate and organic solvent ethylene glycol are according to mass ratio 1:(1-5) mix or ionic liquid 1-butyl-3-methyl imidazolium a tetrafluoro borate and 1-ethyl-3-methylimidazole acetate according to mass ratio 1:(1-3) mix.
6. the two next doors extractive distillation column for method described in claim 1-5 any one, it is characterized in that: two vertical partition plates are equipped with in extractive distillation column inside, described pair of next door, and the first dividing plate is positioned at the left side of second partition, the two dividing plates parallel Ta Bishang that is fixed on that interlocks, wherein the upper end of the first dividing plate and the distance of tower top are less than the lower end of the first dividing plate and the distance at the bottom of tower, the upper end of second partition and the distance of tower top are greater than the lower end of second partition and the distance at the bottom of tower, described dividing plate is divided into pre-separation district by tower body, the first side exploiting field, the second side exploiting field, public rectification zone and public stripping zone five parts, from the upper end of the first dividing plate, to the region forming tower top, be wherein public rectification zone, the lower end of second partition is public stripping zone to the region forming between at the bottom of tower, the right side of second partition is the second side exploiting field, the right side of the first dividing plate and the region that is positioned at second partition upper end are the first side exploiting field, the remaining region that is positioned at the first dividing plate and second partition left side is pre-separation district, raw material is by the side charging of pre-separation district, and extraction agent is from pre-separation district and the first side exploiting field charging, and the first side exploiting field and the second side exploiting field are for the refining product of extraction process extracting rectifying.
7. according to claim 6 pair of next door extractive distillation column, is characterized in that: the height of described the first dividing plate and second partition is all less than the height of tower, and the length of the first dividing plate is greater than the length of second partition.
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| CN104844559A (en) * | 2015-05-21 | 2015-08-19 | 天津大学 | Device and method for extracting thiophene before coking crude benzene hydrogenation |
| CN111050871A (en) * | 2017-09-28 | 2020-04-21 | 埃克森美孚研究工程公司 | Double dividing wall column with multiple products |
| CN112221181A (en) * | 2019-07-15 | 2021-01-15 | 中国石油化工股份有限公司 | Organic solvent recovery processing device and processing method |
| CN113209657A (en) * | 2021-05-08 | 2021-08-06 | 北京化工大学 | Double-partition reaction tower for inhibiting quaternary cascade side reaction and process thereof |
| CN113230682A (en) * | 2021-05-08 | 2021-08-10 | 北京化工大学 | Double-partition-wall reaction rectification structure and design method |
| CN114432727A (en) * | 2020-10-31 | 2022-05-06 | 中国石油化工股份有限公司 | Thermal coupling rectifying tower suitable for multi-component separation |
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