CN101967078A - Crude benzene hydrofining method - Google Patents
Crude benzene hydrofining method Download PDFInfo
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- CN101967078A CN101967078A CN2010105176810A CN201010517681A CN101967078A CN 101967078 A CN101967078 A CN 101967078A CN 2010105176810 A CN2010105176810 A CN 2010105176810A CN 201010517681 A CN201010517681 A CN 201010517681A CN 101967078 A CN101967078 A CN 101967078A
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Abstract
The invention discloses a crude benzene hydrofining method, and belongs to the application field of crude benzene deep processing. The method sequentially comprises the following steps of: A, crude benzene pretreatment; B, crude benzene hydrogenation; C, pre-rectification; and D, rectification for obtaining pure benzene. The pure benzene obtained in the step D can be used for preparing cyclohexane by hydrogenation, and the cyclohexane is prepared into crude alcoholic ketone by oxidization and decomposition reaction. The method optimizes the crude benzene refining flow and the hydrogenation process parameters; the method is particularly suitable for the condition that the product obtained after the crude benzene hydrofining is used as a raw material for producing the cyclohexane; by implementing the method, the yield of the crude benzene hydrofining product is improved by over 4 percent, and the energy is saved by over 32 percent; and the pure benzene produced by crude benzene hydrogenation fully meet the preparation requirement of cyclohexanone.
Description
Technical field
The present invention relates to a kind of crude benzol deep process technology, be specifically related to a kind of hydrofinishing method for crude benzol.
Background technology
Crude benzol is a kind of benzoline that obtains of reclaiming from the pyrogenic raw gas of coal, and main component is a benzene,toluene,xylene, also contains a spot of non-aromatic component.
At present, for the utilization of crude benzol, main method is:
1, utilizes the distillation principle, propose its mid-boiling point and carry out the hydrogenation pre-treatment at the above material of dimethylbenzene;
2, under temperature 190-220 ℃, pressure 2.5MPa, Ni-Mo catalyst action, unsaturated compound is converted into saturated compound;
Under temperature 190-220 ℃, pressure 2.5MPa, Co-Mo catalyst action, desulfurization, denitrogenation and the olefin saturation of raw material takes place;
3, adopt advanced extraction rectification technique, produce the highly purified pure benzene,toluene,xylene that meets the petroleum benzene requirement;
It is further used, and the purified petroleum benzin that utilizes gained exactly is the hydrogenation preparing cyclohexane under temperature 140-180 ℃, pressure 0.65MPa, Ni catalyst action, and hexanaphthene is by reaction preparing cyclohexanones such as oxidation, decomposition.
Wherein, above-mentioned rectification process, generally adopt following steps:
Pre-rectifying: the hydrogenated oil that is come by lightness-removing column enters fractionation by distillation in the tower by the pre-rectifying tower middle part.The operation tower top pressure is that 0.35～0.50MPa, tower top temperature are that 140～160 ℃, tower still temperature are 200～230 ℃, and the cat head extraction mainly contains the BT liquid of benzene and toluene, enters tank field BT jar, and the XS liquid that mainly contains dimethylbenzene of tower still extraction enters tank field XS jar;
Extraction: entered in the tower by the extraction tower middle part from the BT liquid of tank field, extraction tower operation tower top pressure is that normal pressure, tower top temperature are that 95～105 ℃, tower still temperature are 135～150 ℃.BT mixes in tower with cycling extraction agent (NFM), and extraction agent (NFM) mixes the back and enters regenerator column by the tower still with benzene, toluene in the BT liquid; Not with extraction agent blended non-aromatics,, deliver to tank field non-aromatics jar through the extraction of extraction cat head;
Regeneration: in the regenerator column system, the operation tower top pressure is-55～-70KPa, tower top temperature are that 55～65 ℃, tower still temperature are 160～180 ℃.Pure aromatics (benzene, toluene) is by the cat head extraction, and after water-and-oil separator separated, pure aromatics entered the purified petroleum benzin Tower System; Tower still extraction liquid is squeezed into extractor system by recycle pump and is recycled;
The purified petroleum benzin Tower System: the pure aromatics that is come by the regenerator column system enters in the purified petroleum benzin tower and distills, and the operation tower top pressure is that normal pressure, tower top temperature are that 80～85 ℃, tower still temperature are 110～120 ℃.The purified petroleum benzin of cat head extraction enters water-and-oil separator, and the purified petroleum benzin after the separation is sent to the tank field and does pimelinketone raw material or export trade.The toluene of tower still extraction is sent to tank field toluene jar export trade after cooling.
The benzenol hydrorefining system: the XS that the tank field is come enters in the benzenol hydrorefining system, and after distillation, cat head extraction dimethylbenzene is sent to the tank field export trade, tower still solvent oil barrelling export trade.
In present this technology, technical process is longer, and equipment is many, causes big energy-consuming, and production efficiency is low;
Simultaneously, certain side reaction can take place in the hydrogenation process, benzene in the stock oil and toluene are depressed at certain temperature, pressure, hydrogen branch, and hydrogenation reaction generation hexanaphthene and methylcyclohexane can take place, and when adopting the import BASF Catalysts, the side reaction about 1.5% can take place; When adopting domestic catalyst, the side reaction about 2%-3% can take place, in order to remove the purified petroleum benzin that this part by product can lose 1%-2%, cause yield low.
Summary of the invention
The objective of the invention is according to the characteristics of existing technology and the requirement of preparation pimelinketone, provide a kind of cost is low, efficient is high new crude benzole hydrogenation to prepare the method for pimelinketone.
The technical scheme that the present invention solves the problems of the technologies described above is: a kind of hydrofinishing method for crude benzol may further comprise the steps successively:
A, crude benzol pre-treatment: coking crude benzene is entered fractionation by distillation in the tower by the pretreater middle part, remove heavy aromatics;
B, crude benzole hydrogenation: under catalyst action, earlier unsaturates is converted into saturates through the material after the A step, desulfurization, denitrification reaction and olefin saturation take place then, what wherein produce contains H
2S gas is separated from stablizing cat head, and the material of tower still is sent to pre-rectifying tower.
C, pre-rectifying: the material of the tower still of process B step enters fractionation by distillation the pre-rectifying tower from the pre-rectifying tower middle part, and the extraction of distillation tower cat head mainly contains the BT liquid of benzene and toluene, enters tank field BT jar; The XS liquid that contains dimethylbenzene of tower still extraction enters tank field XS jar;
D, rectifying system purified petroleum benzin, toluene: enter in the purified petroleum benzin tower by the BT liquid that comes in the BT jar and to distill, the operation tower top pressure is that normal pressure, tower top temperature are that 80～85 ℃, tower still temperature are 110～120 ℃, the purified petroleum benzin of cat head extraction enters water-and-oil separator, obtains purified petroleum benzin after the separation, and the extraction of tower still obtains toluene.
As preferably: in the described A step, the operation tower top pressure is a normal pressure, and tower top temperature is 80～100 ℃, and tower still temperature is 165～195 ℃.
As preferably: in the described B step, during shortening, the volume ratio of hydrogen and material is 400: 1～800: 1.
As preferably: in the described B step, during shortening, volume space velocity 0.5h
-1～1.5h
-1
As preferably: in the described B step, during shortening, 190-220 ℃ of pre-reactor temperature, the temperature when being about to unsaturates and being converted into saturates are 280-370 ℃ of 190-220 ℃, main reactor temperature, and temperature was 280-370 ℃ when desulfurization, denitrification reaction and olefin saturation promptly took place.
As preferably: in the described B step, during shortening, pressure is 2.0-3.0MPa.
As preferably: in the described C step, the operation tower top pressure is that 0.35～0.50MPa, tower top temperature are that 140～160 ℃, tower still temperature are 200～230 ℃.
The purified petroleum benzin that the present invention is particularly useful for producing is used to prepare the situation of pimelinketone raw material, when need production when making the purified petroleum benzin of raw material, is carried out following optimization flow process for pimelinketone device: keep existing crude benzol pre-treatment, hydrogenation, to take off light industry preface flow process constant; Adjust simultaneously and strict control hydrogenation procedure technology controlling index: hydrogen-oil ratio (volume ratio) 400: 1～800: 1, volume space velocity 0.5h
-1～1.5h
-1, 190-220 ℃ of pre-reactor temperature, 280-370 ℃ of main reactor temperature, pressure 2.0-3.0MPa, guarantee that thiophene is less than lowering the amount that side reaction generates methylcyclohexane under the 1ppm situation as far as possible; Pre-distillation process remains unchanged; Stop the circulation that the extraction tower charging stops extraction tower and regenerator column simultaneously, stop by the orderly shutdown program extraction tower regenerator column two systems to be stopped behind the two tower steam sources.
BT liquid directly is sent to the purified petroleum benzin tower by transforming newly-increased pipeline by the tank field, obtains can be used for the purified petroleum benzin of Cyclohexanone Production raw material after the separation, wherein contains hexanaphthene about 1.5%.
When promptly being used to make pimelinketone raw material purified petroleum benzin, will extract, the flow process of regenerating omits, directly enter the purified petroleum benzin tower and handle by transforming pipeline.
Adopt present method, compared with prior art, in the purified petroleum benzin, hexanaphthene content raises, and wherein the hexanaphthene of Zeng Jiaing is not had separated removing because having lacked extraction step, and the by-product cyclic hexane can be utilized effectively, and has improved product yield.Hexanaphthene can be used as the raw material of producing pimelinketone, and has saved purified petroleum benzin hydrogenation preparing cyclohexane step, has saved the energy, has promptly simplified the crude benzole hydrogenation rectification flow, has saved the energy, has improved yield, has reduced the loss of purified petroleum benzin.
In addition, methylcyclohexane wherein and other light constituents can be taken out with the extraction of lightweight oil form in the light tower of preparation pimelinketone device, do not influence the ordinary production of pimelinketone.
Compared with prior art, beneficial effect of the present invention is:
1, reduce cost: whole device no longer needs extraction agent, also no longer needs extractor system, regenerator column system, thereby reduces the fixed capital input;
2, because whole processing line shortens, energy consumption reduces, and is energy-conservation more than 32%;
3, reduce manipulation strength, reduce workload;
4, improve yield: present method can make crude benzole hydrogenation purified product yield improve more than 4%; It is about 40% that non-aromatics contains benzene, about 1400 tons/year of prior art production non-aromatics, non-aromatics price by 2000 yuan/ton, benzene price by 6000 yuan/ton, annual about 2,240,000 yuan of the economic benefit that increases behind the adjusting process;
5, make full use of hexanaphthene: non-aromatics contains that hexanaphthene is about 20%, and about 1400 tons/year of former explained hereafter non-aromatics will be saved 280 tons/year of hexanaphthenes, and the hexanaphthene price is by 7000 yuan/ton, annual about 1,400,000 yuan of the economic benefit that increases behind the adjusting process.
Embodiment
The present invention is described in further detail below in conjunction with embodiment.But this should be interpreted as that the scope of the above-mentioned theme of the present invention only limits to following embodiment.
Embodiment 1
A kind of hydrofinishing method for crude benzol, the raw material of present embodiment are 1 ton of crude benzol, and its constituent mass percentage composition is a benzene: 80.57% toluene: 12.49% dimethylbenzene: 2.24% light constituent: 0.66% heavy constituent: 4.04%, may further comprise the steps successively:
A, crude benzol pre-treatment: coking crude benzene enters fractionation by distillation in the tower by pretreater middle part, and the operation tower top pressure is that normal pressure, tower top temperature are that 80 ℃, tower still temperature are 165 ℃, removes heavy aromatics;
B, crude benzole hydrogenation and steady component: the material of process steps A is at hydrogen-oil ratio 400: 1, volume space velocity 0.5h
-1, under 195 ℃ of the temperature, pressure 2.0MPa, Ni-Mo catalyst action, unsaturated compound is converted into saturated compound; At hydrogen-oil ratio 400: 1, volume space velocity 0.5h
-1, under 280 ℃ of the temperature, pressure 2.0MPa, Co-Mo catalyst action, desulfurization, denitrogenation and the olefin saturation of raw material takes place; Crude benzole hydrogenation produces and contains H
2S gas is separated from stablizing cat head, and the BTXS of tower still is sent to pre-rectifying.
C, pre-rectifying: the hydrogenated oil that is come by lightness-removing column enters fractionation by distillation in the tower by the pre-rectifying tower middle part, and the operation tower top pressure is that 0.35MPa, tower top temperature are that 140 ℃, tower still temperature are 200 ℃, and the cat head extraction mainly contains the BT liquid of benzene and toluene, enters tank field BT jar; The XS liquid that contains dimethylbenzene of tower still extraction enters tank field XS jar;
D, rectifying system purified petroleum benzin: enter in the purified petroleum benzin tower by the BT liquid that comes in the BT jar and to distill, the operation tower top pressure is that normal pressure, tower top temperature are that 80 ℃, tower still temperature are 110 ℃, the purified petroleum benzin of cat head extraction enters water-and-oil separator, obtains purified petroleum benzin after the separation, and the extraction of tower still obtains toluene; Wherein, the component of the purified petroleum benzin of gained sees Table 1;
Rectifying system dimethylbenzene: the XS liquid that the tank field is come enters in the benzenol hydrorefining system, and after distillation, the cat head extraction obtains dimethylbenzene.
Table 1: adopt the method for embodiment 1 and the component (mass percent) of the intermediate product purified petroleum benzin that adopts prior art to make
Can calculate from table 1, present embodiment is with respect to prior art, and product yield has improved 4.07%.
The energy consumption of present embodiment and the energy consumption of prior art are relatively referring to table 2
Table 2: the energy consumption of 1 ton of crude benzol of processing relatively
| Water (m 3) | Electricity (Kw/h) | Steam (ton) | |
| Prior art | 1.5 | 170 | 1.8 |
| Embodiment 1 | 1.3 | 154 | 1.0 |
Can calculate from table 2, present embodiment is with respect to prior art, and energy consumption has reduced by 32.11%.
Embodiment 2
A kind of crude benzole hydrogenation prepares the method for pimelinketone, the raw material of present embodiment is 1.2 tons of crude benzol, its constituent mass percentage composition is a benzene: 80.57% toluene: 12.49% dimethylbenzene: 2.24% light constituent: 0.66% heavy constituent: 4.04%, may further comprise the steps successively:
A, crude benzol pre-treatment: coking crude benzene enters fractionation by distillation in the tower by pretreater middle part, and the operation tower top pressure is that normal pressure, tower top temperature are that 95 ℃, tower still temperature are 195 ℃, removes heavy aromatics;
B, crude benzole hydrogenation and steady component: the material of process steps A is at hydrogen-oil ratio 800: 1, volume space velocity 1.50h
-1, under 220 ℃ of the temperature, pressure 3.0MPa, Ni-Mo catalyst action, unsaturated compound is converted into saturated compound; At hydrogen-oil ratio 800: 1, volume space velocity 1.5h
-1, under 370 ℃ of the temperature, pressure 3.0MPa, Co-Mo catalyst action, desulfurization, denitrogenation and the olefin saturation of raw material takes place; Crude benzole hydrogenation produces and contains H
2S gas is separated from stablizing cat head, and the BTXS of tower still is sent to pre-rectifying.
C, pre-rectifying: the hydrogenated oil that is come by lightness-removing column enters fractionation by distillation in the tower by the pre-rectifying tower middle part, and the operation tower top pressure is that 0.50MPa, tower top temperature are that 160 ℃, tower still temperature are 230 ℃, and the cat head extraction mainly contains the BT liquid of benzene and toluene, enters tank field BT jar; The XS liquid that contains dimethylbenzene of tower still extraction enters tank field XS jar;
D, rectifying make purified petroleum benzin: entered in the purified petroleum benzin tower by the BT liquid that comes in the BT jar and distill, the operation tower top pressure is that normal pressure, tower top temperature are that 85 ℃, tower still temperature are 120 ℃, the purified petroleum benzin of cat head extraction enters water-and-oil separator, obtains purified petroleum benzin after the separation, and the extraction of tower still obtains toluene; Wherein, the component of the purified petroleum benzin of gained sees Table 3;
Rectifying system dimethylbenzene: the XS liquid that the tank field is come enters in the benzenol hydrorefining system, and after distillation, the cat head extraction obtains dimethylbenzene.
Table 3: adopt the method for embodiment 2 and the component of the intermediate product purified petroleum benzin that adopts prior art to make
Can calculate from table 3, present embodiment is with respect to prior art, and product yield has improved 4.2%.
The energy consumption of present embodiment and the energy consumption of prior art are relatively referring to table 4
Table 4: the energy consumption of 1.2 tons of crude benzol of present embodiment processing relatively
| Water (m 3) | Electricity (Kw/h) | Steam (ton) | |
| Prior art | 1.8 | 200 | 2.1 |
| Embodiment 2 | 1.5 | 180 | 1.18 |
Can calculate from table 4, present embodiment is with respect to prior art, and energy consumption has reduced by 32.25%.
Embodiment 3
A kind of crude benzole hydrogenation prepares the method for pimelinketone, the raw material of present embodiment is 1.5 tons of crude benzol, its constituent mass percentage composition is a benzene: 80.57% toluene: 12.49% dimethylbenzene: 2.24% light constituent: 0.66% heavy constituent: 4.04%, may further comprise the steps successively:
A, crude benzol pre-treatment: coking crude benzene enters fractionation by distillation in the tower by pretreater middle part, and the operation tower top pressure is that normal pressure, tower top temperature are that 95 ℃, tower still temperature are 175 ℃, removes heavy aromatics;
B, crude benzole hydrogenation and steady component: the material of process steps A is at hydrogen-oil ratio 600: 1, volume space velocity 0.90h
-1, under 200 ℃ of the temperature, pressure 2.5MPa, Ni-Mo catalyst action, unsaturated compound is converted into saturated compound; At hydrogen-oil ratio 600: 1, volume space velocity 0.9h
-1, under 305 ℃ of the temperature, pressure 2.5MPa, Co-Mo catalyst action, desulfurization, denitrogenation and the olefin saturation of raw material takes place; Crude benzole hydrogenation produces and contains H
2S gas is separated from stablizing cat head, and the BTXS of tower still is sent to pre-rectifying.
C, pre-rectifying: the hydrogenated oil that is come by lightness-removing column enters fractionation by distillation in the tower by the pre-rectifying tower middle part, and the operation tower top pressure is that 0.50MPa, tower top temperature are that 160 ℃, tower still temperature are 230 ℃, and the cat head extraction mainly contains the BT liquid of benzene and toluene, enters tank field BT jar; The XS liquid that contains dimethylbenzene of tower still extraction enters tank field XS jar;
D, rectifying make purified petroleum benzin: entered in the purified petroleum benzin tower by the BT liquid that comes in the BT jar and distill, the operation tower top pressure is that normal pressure, tower top temperature are that 85 ℃, tower still temperature are 120 ℃, the purified petroleum benzin of cat head extraction enters water-and-oil separator, obtains purified petroleum benzin after the separation, and the extraction of tower still obtains toluene; Wherein, the component of the purified petroleum benzin of gained sees Table 3;
Rectifying system dimethylbenzene: the XS liquid that the tank field is come enters in the benzenol hydrorefining system, and after distillation, the cat head extraction obtains dimethylbenzene.
Table 5: adopt the method for embodiment 3 and the component of the intermediate product purified petroleum benzin that adopts prior art to make
Can calculate from table 5, present embodiment is with respect to prior art, and product yield has improved 4.3%.
The energy consumption of present embodiment and the energy consumption of prior art are relatively referring to table 6
Table 6: the energy consumption of 1.5 tons of crude benzol of present embodiment processing relatively
| Water (m 3) | Electricity (Kw/h) | Steam (ton) | |
| Prior art | 2.2 | 245 | 2.6 |
| Embodiment 3 | 1.9 | 223 | 1.4 |
Can calculate from table 6, present embodiment is with respect to prior art, and energy consumption has reduced by 33.30%.
Claims (8)
1. a hydrofinishing method for crude benzol is characterized in that, may further comprise the steps successively:
A, crude benzol pre-treatment: coking crude benzene is separated, remove heavy aromatics;
B, crude benzole hydrogenation: under catalyst action, just unsaturates is converted into saturates earlier, and desulfurization, denitrification reaction and olefin saturation take place then through the material after the A step, and what wherein produce contains H
2S gas is separated from stablizing cat head, and the material of tower still is sent to pre-rectifying tower.
C, pre-rectifying: the material of the tower still of process B step enters fractionation by distillation the pre-rectifying tower from the pre-rectifying tower middle part, and the extraction of distillation tower cat head mainly contains the BT liquid of benzene and toluene, enters tank field BT jar;
D, rectifying system purified petroleum benzin, toluene: directly enter in the purified petroleum benzin tower by the BT liquid that comes in the BT jar and to distill, the operation tower top pressure is that normal pressure, tower top temperature are that 80～85 ℃, tower still temperature are 110～120 ℃, the purified petroleum benzin of cat head extraction enters water-and-oil separator, obtain purified petroleum benzin after the separation, the extraction of tower still obtains toluene.
2. a kind of hydrofinishing method for crude benzol according to claim 1 is characterized in that: in the described A step, the operation tower top pressure is a normal pressure, and tower top temperature is 80～100 ℃, and tower still temperature is 165～195 ℃.
3. a kind of hydrofinishing method for crude benzol according to claim 1 is characterized in that: in the described B step, during shortening, the volume ratio of hydrogen and material is 400: 1～800: 1.
4. a kind of hydrofinishing method for crude benzol according to claim 3 is characterized in that: in the described B step, and during shortening, volume space velocity 0.5h
-1～1.5h
-1
5. a kind of hydrofinishing method for crude benzol according to claim 4 is characterized in that: in the described B step, and during shortening, 190-220 ℃ of pre-reactor temperature, 280-370 ℃ of main reactor temperature.
6. a kind of hydrofinishing method for crude benzol according to claim 5 is characterized in that: in the described B step, during shortening, pressure is 2.0-3.0MPa.
7. a kind of hydrofinishing method for crude benzol according to claim 1 is characterized in that: in the described C step, the operation tower top pressure is that 0.35～0.50MPa, tower top temperature are that 140～160 ℃, tower still temperature are 200～230 ℃.
8. a kind of hydrofinishing method for crude benzol according to claim 1 is characterized in that: in the described D step, when being used to prepare the raw material purified petroleum benzin of pimelinketone, BT liquid directly enters the purified petroleum benzin tower, is met after the separation in the purified petroleum benzin of Cyclohexanone Production ingredient requirement.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102320910A (en) * | 2011-06-02 | 2012-01-18 | 湖南长岭石化科技开发有限公司 | Crude benzene hydrogenation method |
| CN103910596A (en) * | 2013-12-04 | 2014-07-09 | 徐州龙辉化工科技有限公司 | Full fraction crude benzene hydrogenation method and catalyst |
| CN104672043A (en) * | 2015-02-04 | 2015-06-03 | 沾化瑜凯新材料科技有限公司 | Light benzene hydrogenation method |
| CN104974006A (en) * | 2015-06-24 | 2015-10-14 | 武汉科林精细化工有限公司 | Whole fraction crude benzene hydrogenation process |
| CN108002974A (en) * | 2017-12-15 | 2018-05-08 | 武汉钢铁有限公司 | The process of refined coking crude benzene |
| CN111348981A (en) * | 2019-12-24 | 2020-06-30 | 国家能源集团煤焦化有限责任公司 | Crude benzene hydrofining method and device |
| CN112939722A (en) * | 2021-02-03 | 2021-06-11 | 山东汇能新材料科技股份有限公司 | Low-temperature hydrogenation process for crude benzene |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB814784A (en) * | 1956-04-11 | 1959-06-10 | Metallgesellschaft Ag | Process of recovering pure aromatic compounds from crude benzol |
| US3992465A (en) * | 1973-01-10 | 1976-11-16 | Institut Francais Du Petrole, Des Carburants Et Lubrifiants Et Entreprise De Recherches Et D'activities Petrolieres Elf | Process for manufacturing and separating from petroleum cuts aromatic hydrocarbons of high purity |
| CN1948244A (en) * | 2006-11-13 | 2007-04-18 | 西南化工研究设计院 | Technology of making refined benzene by hydrogenation, desulfur denitrogen of coking benzene |
| CN101519338A (en) * | 2009-02-25 | 2009-09-02 | 中国石油集团工程设计有限责任公司抚顺分公司 | Process for hydrofining coking crude benzene |
-
2010
- 2010-10-25 CN CN2010105176810A patent/CN101967078A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB814784A (en) * | 1956-04-11 | 1959-06-10 | Metallgesellschaft Ag | Process of recovering pure aromatic compounds from crude benzol |
| US3992465A (en) * | 1973-01-10 | 1976-11-16 | Institut Francais Du Petrole, Des Carburants Et Lubrifiants Et Entreprise De Recherches Et D'activities Petrolieres Elf | Process for manufacturing and separating from petroleum cuts aromatic hydrocarbons of high purity |
| CN1948244A (en) * | 2006-11-13 | 2007-04-18 | 西南化工研究设计院 | Technology of making refined benzene by hydrogenation, desulfur denitrogen of coking benzene |
| CN101519338A (en) * | 2009-02-25 | 2009-09-02 | 中国石油集团工程设计有限责任公司抚顺分公司 | Process for hydrofining coking crude benzene |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102320910A (en) * | 2011-06-02 | 2012-01-18 | 湖南长岭石化科技开发有限公司 | Crude benzene hydrogenation method |
| CN102320910B (en) * | 2011-06-02 | 2013-07-10 | 湖南长岭石化科技开发有限公司 | Crude benzene hydrogenation method |
| CN103910596A (en) * | 2013-12-04 | 2014-07-09 | 徐州龙辉化工科技有限公司 | Full fraction crude benzene hydrogenation method and catalyst |
| CN103910596B (en) * | 2013-12-04 | 2016-02-10 | 徐州龙辉化工科技有限公司 | Full cut crude benzene hydrogenation method and catalyzer |
| CN104672043A (en) * | 2015-02-04 | 2015-06-03 | 沾化瑜凯新材料科技有限公司 | Light benzene hydrogenation method |
| CN104974006A (en) * | 2015-06-24 | 2015-10-14 | 武汉科林精细化工有限公司 | Whole fraction crude benzene hydrogenation process |
| CN108002974A (en) * | 2017-12-15 | 2018-05-08 | 武汉钢铁有限公司 | The process of refined coking crude benzene |
| CN111348981A (en) * | 2019-12-24 | 2020-06-30 | 国家能源集团煤焦化有限责任公司 | Crude benzene hydrofining method and device |
| CN112939722A (en) * | 2021-02-03 | 2021-06-11 | 山东汇能新材料科技股份有限公司 | Low-temperature hydrogenation process for crude benzene |
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