CN106916044A - A kind of method for refining carbonization crude benzole - Google Patents
A kind of method for refining carbonization crude benzole Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
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- C07C7/04—Purification; Separation; Use of additives by distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
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- C07C7/00—Purification; Separation; Use of additives
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- C—CHEMISTRY; METALLURGY
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- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
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Abstract
The present invention provides a kind of method for refining carbonization crude benzole, crude benzol obtains toluene and former cut by pre-distillation column distillation tower top, bottom of towe obtains dimethylbenzene and later cut, toluene and former cut enter extractive distillation unit after the removal of impurity is gone in hydrotreating and remove non-aromatic hydrocarbon-fraction, non-aromatic hydrocarbon product is obtained herein, remove the mixed fraction after non-aromatic hydrocarbon-fraction and obtain purified petroleum benzin product by tower top after purified petroleum benzin column distillation, bottom of towe obtains toluene product, tower top xylene fraction is processed by clay tower and obtains xylene product after dimethylbenzene and later cut feeding benzenol hydrorefining distillation, bottom of towe obtains heavy benzol product.The technical program reduces the energy consumption and plant energy consumption of pre-distillation column；The impurity content that hydrogenation system is brought into is reduced, hydrogen consumption is reduced；Extractive distillation system load is reduced, solvent ratio is reduced, plant energy consumption is reduced；The amount that heavy non-aromatics brings extractive distillation system into is reduced, it is advantageously ensured that the product quality of non-aromatics, purified petroleum benzin, toluene.
Description
Technical field
The present invention relates to coked crude benzene refining field, and in particular to a kind of method for refining carbonization crude benzole.
Background technology
Crude benzol obtains light benzene fraction (containing triphen) by pre-distillation column distillation tower top in the prior art, and bottom of towe obtains heavy benzol product,
Light benzene enters extractive distillation unit after the removal of impurity is gone in hydrotreating and removes non-aromatic hydrocarbon-fraction, and non-aromatic hydrocarbon product is obtained herein, goes
Unless the mixed fraction after aromatic fraction sequentially pass through pure benzene tower, benzene column, benzenol hydrorefining distillation after, respectively obtain purified petroleum benzin product,
Toluene product, xylene product.Crude benzene refining technological process is as shown in Figure 1.
Chinese Patent Application No. is CN200610031941.7, discloses a kind of method by preparing benzene aromatic hydrocarbon by crude benzene, and it is
The miscella of full cut crude benzol and other hydrocarbon ils is obtained high by processes such as hydrofinishing, reformation, solvent extraction distillation, rectifying
The benzene,toluene,xylene of yield, high-purity, is characterized in being lost without aromatic hydrocarbons, and aromatic hydrocarbons total recovery is more than 100%；Aromatic hydrocarbons
Product purity is high, up to more than 99.9%；Sulphur, nitrogen impurity content in aromatic hydrocarbon product is low, respectively less than 1ppm；Processing dress
The service cycle put is long.The refinery that the invention is particularly well-suited to possess hydrogenation plant and reformer carries out deep processing and the profit of crude benzol
With.Chinese Patent Application No. a kind of method for refining carbonization crude benzole for CN200710000044.4 is disclosed, it is characterised in that under
Row technical process is constituted：(1) crude benzol pretreatment and benzene fraction extracting rectifying process for refining a crude benzol pretreating process coking crude benzene warp
Divide tower, tower top to separate light component in advance, tower bottom distillate enters benzene blowing tower, heavy constituent is separated in this tower bottom of towe, overhead fraction enters narrow
Benzene column, the benzene fraction obtained in this column overhead enters benzene fraction extracting and refining technique, bottom of towe toluene, xylene fraction enter toluene,
Xylene fraction hydrofining technology.The benzene fraction that a technique unit is obtained on b benzene fraction extraction rectification techniques is extracted into benzene
Tower, tower top separates boiling point close with benzene or alkane of azeotropic and olefine fraction, and tower bottom distillate enters benzene refining tower, the benzene extraction tower
Extractant (extractant for mainly reclaiming also has the new plus extractant of a small amount of supplement) is from blender；In described benzene refining
Tower top obtains product high pure benzene (purity ＞ 99.9%, sulfur content ＜ 10ppm) in tower, and tower bottom distillate enters extractant recovery tower；
Extractant is separated with thiophene cut in extractant recovery tower, extractant is recycled into blender, thiophene cut enters thiophene
Extraction tower, subsequently into thiophene product is obtained after thiophene treating column, its purity is more than or equal to 99%, and extractant is circulated successively
Use.Described extractant is：Sulfolane, glycols, 1-METHYLPYRROLIDONE, N- formyl-morpholines or their mixing
Thing, than 2-10, in vacuum or normal pressing operation, benzene extracts 85-45 DEG C of column overhead temperatures, benzene refining column overhead temperatures to solvent
85-45 DEG C, thiophene 86-45 DEG C of column overhead temperatures of extraction.(2) toluene, xylene fraction hydrofining technology come from a upper technique
Toluene, the xylene fraction of unit enter catalysis through pre-hydrogenator after removing the easily component of coking such as phenylethylene, diene
Hydrogenation main reactor, after completion hydrogenation of unsaturated hydrocarbons generation alkane and hydrogenation remove the heteroatomic compounds such as sulphur removal, nitrogen, oxygen herein,
Into pre-distillation column, pre-distillation column tower bottom distillate enters xylene distillation tower, and benzenol hydrorefining tower top obtains 3 DEG C of dimethylbenzene of boiling range and produces
Product, bottom of towe obtains C9 cuts；The toluene fraction distillated from pre-distillation column tower top enters one-level extraction tower, is separated in this column overhead non-
Aromatic component, the toluene and extractant of bottom of towe enter extractant recovery tower, and the extractant distillated from this bottom of towe returns to extraction tower circulation
Use, tower top obtains nitration grade toluene；The nitration grade toluene of gained can be sold as product, can also pass through two grades of extraction towers and toluene
Treating column, can finally obtain product high purity toluene.The hydrogen source of the hydrofinishing is hydrogen, and pre-hydrogenator is thick with Ni-Mo
Benzene catalyst for pre-hydrogenation, hydrogenation temperature is 190~240 DEG C；The hydrogenation main reactor Co-Mo crude benzole hydrogenation refining catalytics
Agent, hydrogenation temperature is 320~370 DEG C, and operating pressure is 2.4~3.5MPa；Extractant used by the extracting rectifying is
N- formyl-morpholines, solvent ratio is 3~8, and I and II extraction tower top temperature is 92~110 DEG C, and extraction tower is at ambient pressure
Operation.(3) nitration grade toluene that toluene disproportionation technique is obtained by a upper technique unit as disproportionation technique raw material.Toluene and hydrogen
Gas is mixed into preheater, and disproportionation device is entered after preheating, and the condensed device condensation of reaction product, condensate liquid enters rectifying column and enters
Row separated obtains product high pure benzene and mixed xylenes, and unconverted toluene, and the latter and remaining hydrogen return to preheating
Device is recycled.Described toluene disproportionation technique can be general toluene disproportionation technique, or methylbenzene selective disproportionation work
Skill, the catalyst used by the two is different, and the ratio of three isomers is different in products obtained therefrom mixed xylenes, contains in the latter's product
There are the huge market demand of high concentration, added value paraxylene high.Additionally, can also mix (to go out with C9 cuts in raw material toluene
From xylene distillation bottom stream in a upper technique unit, main component is C9, C10 aromatic hydrocarbons), as disproportionation device
Mixed feeding, selects suitable catalyst else, then toluene disproportionation and transalkylation reaction occur simultaneously in the reactor, and gained is produced
Thing is still high pure benzene and mixed xylenes.
In prior art coked crude benzene refining, the energy consumption of pre-distillation column is higher；Liquid state change procedure often, hydrogenation system band
The impurity content for entering is high, increases hydrogen and consumes；Extractive distillation system load weight, solvent is than high；Heavy non-aromatics is brought extraction into and is steamed
The amount of system is evaporated, makes the product quality of non-aromatics, purified petroleum benzin, toluene impacted.
The content of the invention
In order to solve the above problems, it is an object of the invention to provide a kind of method for refining carbonization crude benzole, it is a kind of easy to operate
And the low crude benzene refining technological process of energy consumption.
Technical scheme is as follows：
A kind of method for refining carbonization crude benzole, comprises the following steps：
(1) coking crude benzene is distilled by pre-distillation column, controls tower top pressure, and tower top temperature is controlled at 62 DEG C~65 DEG C, control
Reflux ratio, column bottom temperature is controlled at 150 DEG C~155 DEG C, and tower top obtains toluene and the cut than toluene low boiling point, and bottom of towe obtains two
Toluene and later cut；
(2) toluene and than toluene low boiling point cut by mix with hydrogen after heat exchange and heat-conducting oil heating feeding pre-reactor in,
The control of pre-reactor inlet temperature at 160 DEG C~180 DEG C, after vaporizing send into main reactor, main reaction by product circulating hydrogen
Device inlet temperature is controlled at 280 DEG C~320 DEG C, and the cut feeding extractive distillation unit removing after the removal of impurity is gone in hydrotreating is non-
Aromatic fraction, extracts the non-aromatic hydrocarbon product of column overhead output, and bottom of towe extractant sends into solvent recovery tower, tower top control with aromatic hydrocarbons mixture
Pressing pressure, temperature 45 C~55 DEG C, bottom of towe 155~160 DEG C of temperature of control, solvent recovery column overhead mixed fraction is by pure benzene tower
Tower top obtains purified petroleum benzin product, bottom of towe and obtains toluene product after distillation；
(3) dimethylbenzene and the feeding benzenol hydrorefining distillation of later cut, control tower top pressure, tower top temperature be controlled to 150 DEG C~
160 DEG C, 5 layers of column plate control 165 DEG C~170 DEG C, output xylene fraction at 5 layers of column plate, xylene fraction control pressure, liquid
The xylene fraction of phase state enters in clay tower, and by obtaining xylene product after clay tower treatment, bottom of towe obtains heavy benzol product.
According to a kind of method for refining carbonization crude benzole of the present invention, further, extractant is ring fourth in the extractive distillation unit
Sulfone, extraction is than control 1：5~1.5.5.
According to a kind of method for refining carbonization crude benzole of the present invention, further, in the clay tower built with granular carclazyte, by white
Micro unsaturates and part sulphur, nitrogen impurity in native adsorbing and removing dimethylbenzene.
Further described granular carclazyte, specific surface area 320m2/g, free acid≤0.2%, particle diameter >=90%, initial activity≤
5.0mgBR2/100g。
According to a kind of method for refining carbonization crude benzole of the present invention, further, the amounts of hydrogen for adding system is 35NM3/h, and hydrogen is dense
Degree requires 99.9%, impurity：Total sulfur≤2ppm, CO+O2≤10ppm, water≤30ppm, O2≤10ppm.
According to a kind of method for refining carbonization crude benzole of the present invention, further, the cut than toluene low boiling point be mainly purified petroleum benzin,
Alkene, alkadienes and low boiling non-aromatics.
According to a kind of method for refining carbonization crude benzole of the present invention, further, the tower top pressure of pre-distillation column in the step (1)
Power is controlled in -55kpa, and reflux ratio is 0.5.
According to a kind of method for refining carbonization crude benzole of the present invention, further, product is by 380 DEG C in the step (2)
After circulating hydrogen vaporization in feeding main reactor；Tower top control pressure-the 55Kpa of the solvent recovery tower.
According to a kind of method for refining carbonization crude benzole of the present invention, further, the tower of benzenol hydrorefining distillation in the step (3)
Pressure on top surface is controlled in 80Kpa；Output xylene fraction at 5 layers of column plate, xylene fraction control pressure is 1.0Mpa, 140 DEG C of left sides
Right liquid phase state enters in clay tower.
Detailed technology scheme of the present invention：Crude benzol distills by pre-distillation column, and tower top pressure control is in -55kpa, tower top temperature control
At 62 DEG C~65 DEG C, reflux ratio is 0.5, and column bottom temperature is controlled at 150 DEG C~155 DEG C, and tower top obtains toluene and former cut,
Bottom of towe obtains dimethylbenzene and later cut.Toluene and former cut with hydrogen by mixing feeding after heat exchange and heat-conducting oil heating
In pre-reactor, the control of pre-reactor inlet temperature 160 DEG C~180 DEG C (inlet temperature regulates and controls according to reaction effect), produce by reaction
Thing is sent into main reactor after being vaporized by 380 DEG C of circulating hydrogens, and main reactor inlet temperature is controlled in 280 DEG C~320 DEG C (imports
Temperature regulates and controls according to reaction effect), the cut feeding extractive distillation unit removing non-aromatics after the removal of impurity is gone in hydrotreating evaporates
Point, extractant is sulfolane, and extraction is than control 1：5~1.5.5, extracts the non-aromatic hydrocarbon product of column overhead output, bottom of towe extractant
With aromatic hydrocarbons mixture send into solvent recovery tower, tower top control pressure -55Kpa, temperature 45 C~55 DEG C, bottom of towe control temperature 155~
160 DEG C, solvent recovery column overhead mixed fraction obtains purified petroleum benzin product, bottom of towe and obtains toluene product by tower top after purified petroleum benzin column distillation.
Dimethylbenzene and the feeding benzenol hydrorefining distillation of later cut, tower top pressure are controlled in 80Kpa, tower top temperature be controlled to 150 DEG C~
160 DEG C, 5 layers of column plate controls 165 DEG C~170 DEG C, output xylene fraction at 5 layers of column plate, and xylene fraction control pressure is
1.0Mpa, 140 DEG C or so of liquid phase state enters in clay tower, in clay tower built with acid centre adsorbent, by adsorbent
Micro unsaturates and part sulphur, nitrogen impurity in removing dimethylbenzene, by obtaining xylene product, bottom of towe after clay tower treatment
Obtain heavy benzol product.
The granular carclazyte, specific surface area 320m2/g, free acid≤0.2%, particle diameter >=90%, initial activity≤5.0mgBR2/100g；
The amounts of hydrogen of addition system is 35NM3/h, density of hydrogen requirement 99.9%, impurity：Total sulfur≤2ppm, CO+O2≤10ppm, water
≤ 30ppm, O2≤10ppm.
Beneficial effects of the present invention：
1st, in the case where keeping original agent set constant, guarantee product quality is reached by the change to technological process and parameter
And reduce the purpose of the energy；
2nd, due to the target fraction boiling range emphasis reduction for needing to obtain, about 110 DEG C, so cooling operation is carried out to pre-distillation column,
Pre-distillation column Stress control is consistent with former technique, 5 DEG C of tower top temperature reduction, reflux ratio reduction by 0.2,20 DEG C of column bottom temperature reduction,
The energy consumption of pre-distillation column is reduced by above measure；
3rd, dimethylbenzene and later cut cut out in pre-distillation column bottom of towe, reduce about 15% sulphur, nitrogen impurity and bring hydrogenation system into,
Reduce hydrogen consumption；
4th, non-aromatics load decline about 20%, the particularly non-aromatic hydrocarbon content of C8 classes heavy are essentially 0, institute in extraction distillation column charging
With extractive distillation unit solvent ratio by 1：7 are reduced to 1：5.5, solvent internal circulating load is reduced, so as to reduce extractive distillation system
Load, reduces solvent ratio, reduces plant energy consumption；
5th, into the aromatic hydrocarbons boiling range terminal reduction of solvent recovery tower, about 110 DEG C, so solvent recovery tower is also carried out cooling operation,
10 DEG C of tower top temperature reduction, 20 DEG C of column bottom temperature reduction, reduces the energy consumption of solvent recovery tower；
6th, in original technological process, obtaining xylene product is needed to carry out three vaporization and condensation processes, and technique is only needed once after change
Vaporization and condensation process, reduces energy consumption；
7th, technological process changes in addition to para-xylene product quality has an impact, and the acquisition process of remaining product is consistent with former technique,
So the problem in order to answer impurity content exceeding index in para-xylene product, increased one group of clay tower, diformazan is removed using adsorbent
Micro unsaturates, sulphur and nitrogen impurity in benzaldehyde product, reach the purpose for ensureing product quality.
The present invention greatly reduces the operation energy consumption of device on the premise of bulk product quality is ensured, public at me according to measuring and calculating
Can be the operating cost of device reduction about 20% under department's energy price system, be conducive to being lifted the profitability of crude benzene refining device.
Brief description of the drawings
Fig. 1：Existing crude benzene refining process chart；
Fig. 2：Improved crude benzene refining process chart.
Specific embodiment
Below by specific embodiment, the present invention is further elaborated, but the invention is not limited in these embodiments.
As shown in Fig. 2 crude benzol raw material is controlled in -55kpa, tower top temperature by being pumped into pre-distillation column, pre-distillation column tower top pressure
At 62 DEG C~65 DEG C, reflux ratio is 0.5 for degree control, and column bottom temperature is controlled at 150 DEG C~155 DEG C, and by distillation, tower top is obtained
Toluene and former cut, bottom of towe obtain dimethylbenzene and later cut.Toluene and former cut pass through and hydrogenation reaction section thing
Material heat exchange and heat-conducting oil heating after mix with hydrogen feeding pre-reactor in, pre-reactor inlet temperature control 160 DEG C~
180 DEG C (inlet temperature regulates and controls according to reaction effect), product is sent into main reactor after being vaporized by 380 DEG C of circulating hydrogens,
The control of main reactor inlet temperature is removed 280 DEG C~320 DEG C (inlet temperature regulates and controls according to reaction effect) by hydrotreating
Cut feeding extractive distillation unit after impurity.Hydrogenation section product is by being pumped into the charging of extraction distillation column middle part, 11 layers
It is cycling extraction agent to feed, and extractant is sulfolane, and extraction is than control 1：5~1.5.5, tower top temperature controls about 90 DEG C,
Tower top pressure is controlled to 80Kpa, the extraction non-aromatic hydrocarbon product of column overhead output (non-aromatic hydrocarbon content >=90%), bottom of towe extractant with
Aromatic hydrocarbons mixture feeding solvent recovery tower, tower top control pressure -55Kpa, temperature 45 C~55 DEG C, bottom of towe control temperature 155~
160 DEG C, the extractant after bottom of towe is purified sends 11 layers of extraction distillation column back to, and tower top obtains aromatic hydrocarbons mixture, solvent recovery tower
Tower top aromatic hydrocarbons mixture obtains purified petroleum benzin product, bottom of towe and obtains toluene product by tower top after purified petroleum benzin column distillation.Dimethylbenzene and later
Cut feeding benzenol hydrorefining distillation, tower top pressure is controlled in 80Kpa, and tower top temperature is controlled to 150 DEG C~160 DEG C, 5 layers of column plate
165 DEG C~170 DEG C of control, output xylene fraction at 5 layers of column plate, xylene fraction control pressure is 1.0Mpa, 140 DEG C of left sides
Right liquid phase state enters in clay tower, in clay tower built with acid centre adsorbent, by adsorbent removing dimethylbenzene
Micro unsaturates and part sulphur, nitrogen impurity, by obtaining xylene product after clay tower treatment, bottom of towe obtains heavy benzol product.
The granular carclazyte, specific surface area 320m2/g, free acid≤0.2%, particle diameter >=90%, initial activity≤5.0mgBR2/100g；
The amounts of hydrogen of addition system is 35NM3/h, density of hydrogen requirement 99.9%, impurity：Total sulfur≤2ppm, CO+O2≤10ppm, water
≤ 30ppm, O2≤10ppm.
Products obtained therefrom quality condition of the present invention：
Purified petroleum benzin：
Toluene：
Coking xylene：
Heavy benzol：
Non-aromatics：(following table primes)
Claims (9)
1. a kind of method for refining carbonization crude benzole, it is characterised in that comprise the following steps：
(1) coking crude benzene is distilled by pre-distillation column, controls tower top pressure, and tower top temperature is controlled at 62 DEG C~65 DEG C, control
Reflux ratio, column bottom temperature is controlled at 150 DEG C~155 DEG C, and tower top obtains toluene and the cut than toluene low boiling point, and bottom of towe is obtained
Dimethylbenzene and later cut；
(2) toluene and than toluene low boiling point cut by mix with hydrogen after heat exchange and heat-conducting oil heating feeding pre-reactor in,
The control of pre-reactor inlet temperature is sent into main reactor at 160 DEG C~180 DEG C after the vaporization of product circulating hydrogen, and master is anti-
Device inlet temperature is answered to control at 280 DEG C~320 DEG C, the cut feeding extractive distillation unit after the removal of impurity is gone in hydrotreating takes off
Unless aromatic fraction, extracts the non-aromatic hydrocarbon product of column overhead output, bottom of towe extractant sends into solvent recovery tower, tower with aromatic hydrocarbons mixture
Top control pressure, temperature 45 C~55 DEG C, bottom of towe 155~160 DEG C of temperature of control, solvent recovery column overhead mixed fraction is passed through
Tower top obtains purified petroleum benzin product, bottom of towe and obtains toluene product after purified petroleum benzin column distillation；
(3) dimethylbenzene and the feeding benzenol hydrorefining distillation of later cut, control tower top pressure, tower top temperature be controlled to 150 DEG C~
160 DEG C, 5 layers of 165 DEG C~170 DEG C of column plate control, output xylene fraction at 5 layers of column plate, xylene fraction control pressure,
The xylene fraction of liquid phase state enters in clay tower, and by obtaining xylene product after clay tower treatment, bottom of towe obtains heavy benzol product
Product.
2. a kind of method for refining carbonization crude benzole according to claim 1, it is characterised in that in the extractive distillation unit
Extractant is sulfolane, and extraction is than control 1：5~1.5.5.
3. a kind of method for refining carbonization crude benzole according to claim 1, it is characterised in that the clay tower built with
Grain carclazyte, the micro unsaturates and part sulphur, nitrogen impurity in dimethylbenzene are removed by bleaching earth adsorption.
4. a kind of method for refining carbonization crude benzole according to claim 3, it is characterised in that the granular carclazyte, specific surface area
320m2/g, free acid≤0.2%, particle diameter >=90%, initial activity≤5.0mgBR2/100g.
5. a kind of method for refining carbonization crude benzole according to claim 1, it is characterised in that the amounts of hydrogen for adding system is
35NM3/h, density of hydrogen requirement 99.9%, impurity：Total sulfur≤2ppm, CO+O2≤10ppm, water≤30ppm, O2
≤10ppm。
6. a kind of method for refining carbonization crude benzole according to claim 1, it is characterised in that the evaporating than toluene low boiling point
Divide predominantly purified petroleum benzin, alkene, alkadienes and low boiling non-aromatics.
7. a kind of method for refining carbonization crude benzole according to claim 1, it is characterised in that steamed in advance in the step (1)
The tower top pressure for evaporating tower is controlled in -55kpa, and reflux ratio is 0.5.
8. a kind of method for refining carbonization crude benzole according to claim 1, it is characterised in that the reaction in the step (2)
Product is sent into main reactor after being vaporized by 380 DEG C of circulating hydrogens；Tower top control pressure-the 55Kpa of the solvent recovery tower.
9. a kind of method for refining carbonization crude benzole according to claim 1, it is characterised in that the diformazan in the step (3)
The tower top pressure of benzene column distillation is controlled in 80Kpa；Output xylene fraction at 5 layers of column plate, xylene fraction control pressure is
1.0Mpa, 140 DEG C or so of liquid phase state enters in clay tower.
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| CN107200673A (en) * | 2017-07-07 | 2017-09-26 | 安徽卓泰化工科技有限公司 | A kind of xylene production device |
| CN108002974A (en) * | 2017-12-15 | 2018-05-08 | 武汉钢铁有限公司 | The process of refined coking crude benzene |
| CN108379866A (en) * | 2018-03-22 | 2018-08-10 | 马鞍山钢铁股份有限公司 | Four benzene extractive distillation systems of one kind and technique |
| 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 |
| CN111943796A (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 hydrogenation and extractive distillation of crude benzene |
| CN112250539A (en) * | 2020-11-13 | 2021-01-22 | 新奥科技发展有限公司 | Oil product separation and refining method |
| CN115193082A (en) * | 2022-09-16 | 2022-10-18 | 旭阳工程有限公司 | Novel crude benzene hydrofining separation system and process |
| CN115368202A (en) * | 2022-08-22 | 2022-11-22 | 山西诚宏福得一化工有限公司 | Benzene extraction process and extraction system for coking pure benzene |
| WO2024051737A1 (en) * | 2022-09-08 | 2024-03-14 | 淮北师范大学 | Method for producing high boiling point solvent oil byproduct in crude benzene refinement |
| CN118026803A (en) * | 2024-04-13 | 2024-05-14 | 潍坊三昌化工科技有限公司 | Crude benzene hydrofining device and method |
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| CN107200673A (en) * | 2017-07-07 | 2017-09-26 | 安徽卓泰化工科技有限公司 | A kind of xylene production device |
| CN108002974A (en) * | 2017-12-15 | 2018-05-08 | 武汉钢铁有限公司 | The process of refined coking crude benzene |
| CN108379866A (en) * | 2018-03-22 | 2018-08-10 | 马鞍山钢铁股份有限公司 | Four benzene extractive distillation systems of one kind and technique |
| 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 |
| CN111943796A (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 hydrogenation and extractive distillation of crude benzene |
| 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 |
| CN112250539A (en) * | 2020-11-13 | 2021-01-22 | 新奥科技发展有限公司 | Oil product separation and refining method |
| CN115368202A (en) * | 2022-08-22 | 2022-11-22 | 山西诚宏福得一化工有限公司 | Benzene extraction process and extraction system for coking pure benzene |
| WO2024051737A1 (en) * | 2022-09-08 | 2024-03-14 | 淮北师范大学 | Method for producing high boiling point solvent oil byproduct in crude benzene refinement |
| CN115193082A (en) * | 2022-09-16 | 2022-10-18 | 旭阳工程有限公司 | Novel crude benzene hydrofining separation system and process |
| CN118026803A (en) * | 2024-04-13 | 2024-05-14 | 潍坊三昌化工科技有限公司 | Crude benzene hydrofining device and method |
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