CN104355959A - Production process for producing benzene aromatic hydrocarbons from coking crude benzene - Google Patents
Production process for producing benzene aromatic hydrocarbons from coking crude benzene Download PDFInfo
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- CN104355959A CN104355959A CN201410617946.2A CN201410617946A CN104355959A CN 104355959 A CN104355959 A CN 104355959A CN 201410617946 A CN201410617946 A CN 201410617946A CN 104355959 A CN104355959 A CN 104355959A
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Abstract
The invention discloses a production process for producing benzene aromatic hydrocarbons from coking crude benzene. The production process of the benzene aromatic hydrocarbons comprises the units of preliminary separation of raw materials, hydrogenation refining, extractive distillation, aromatic hydrocarbon refining and xylene distillation, wherein the supplementary hydrogen needed by the reaction in the hydrogenation refining unit is provided by the outside; the reformate is pre-distilled to separate out heavy components containing xylene and above and light components containing benzene, methylbenzene and non-aromatic hydrocarbons, the heavy components are subjected to rectification to obtain petroleum-grade mixed xylene, and the light components are subjected to extractive distillation by use of N-formylmorpholine to separate out the non-aromatic hydrocarbons and a rich solvent containing benzene and methylbenzene; the rich solvent is further rectified to obtain petroleum-grade benzene and nitration-grade methylbenzene, respectively; nitration-grade methylbenzene is subjected to extractive distillation by use of N-formylmorpholine to obtain petroleum-grade methylbenzene; the mixed oil of crude benzene and other hydrocarbon oil is subjected to a hydrogenation reaction with hydrogen in a reactor filled with a hydrogenation catalyst under the following reaction conditions: a temperature within the range of 285-370 DEG C, hydrogen pressure within the range of 3.0-9.0MPa, a liquid space velocity of 5-6 hours, and a hydrogen-oil ratio of (1500-1600) to 1; the hydrogenation catalyst can be a molybdenum-nickel-tungsten-phosphorus catalyst, a molybdenum-nickel catalyst or a molybdenum-cobalt catalyst. The process is high in yield.
Description
Technical field
The present invention relates to the production technique that a kind of coking crude benzene produces benzene aromatic hydrocarbon.
Background technology
Current coking crude benzene (abbreviation crude benzol) refining commercial run has two kinds: one to be acid wash, and two is hydrogenation methods.Acid wash is comparatively ripe, but its purification degree of depth is inadequate, and the benzene rate of recovery is low, its fatal defects be produce in process many to environment extremely harmful and reluctant higher boiling sulfur compound and acidic polymer, and to be difficult to the waste sulfate that utilizes, severe contamination environment in a large number; Hydrogenation method can obtain high-quality benzene or benzene-type products, and its shortcoming is that facility investment is large, and tooling cost is high, and in hydrogenation process, some useful components in crude benzol generate hydrogen sulfide as thiophene is decomposed and cannot recycle.Environment-friendly type method for refining carbonization crude benzole (CN1686977A) adopts the technique of extracting rectifying, high-quality benzene can be obtained, also recyclable thiophene simultaneously, its shortcoming be account for the toluene of crude benzol 15-18%, xylene fraction refined not yet fully, with regard to the triphen process that coked crude benzene refining reclaims most worthy, the method waits perfect.
In recent years, along with the development of national economy, the demand of national STRENGTH ON COKE increases fast, causes the output of the resource-type byproducts such as coking crude benzene to improve constantly.Owing to containing some unsaturated hydrocarbons and sulfur-bearing organic compounds containing nitrogen in coking crude benzene, as straight-chain paraffin mercaptan, aromatic base mercaptan, thioether, thiophene, dibenzothiophene, benzo-thiophene, pyridine etc., directly cannot use as organic synthesis raw material, only have and can use after above-mentioned impurity removal.The traditional removing impurities method of coking crude benzene is acid wash, although the method can part remove sulfocompound (mainly thiophene) in crude benzol and some other impurity.But aromatic hydroxy compound loss comparatively large (10% ~ 20%) in the course of processing; By-product refuse acid tar and residue there is no effective governance approach, cause environmental pollution; End product quality and grade oil product quality variance are comparatively large, and use has larger limitation; Added value is low, and economic benefit is relatively poor.Developed country eliminates this method already.At present, comparatively advanced removing impurities method is coking crude benzene hydrogenation element process for refining, and the product of this explained hereafter can reach the requirement of grade oil aromatics quality, product application wide scope, and environmental protection effect is given prominence to, and can effectively promote coal chemical industry product structure.Its principle is: by hydrogenation, unsaturated hydrocarbons compounds is changed into saturated alkane and alkane derivative, and nitrogenous, organic compounds containing sulfur are converted into inorganic sulfur, inorganic nitrogen compound, thus reaches the object of purification.First this technique researched and developed and industrialization by developed country.Take American technology as Litol method and the pyroprocess of representative, be characterized in that hydrogenation reaction temperature 600 DEG C ~ 630 DEG C and reaction pressure 6.0MPa are very high, also high to equipment requirements, manufacture difficulty and investment be comparatively large, to operate operation process danger relatively high; Take Germany technology as K.K method and the low temperature process of representative, it is refining by the initial gross separation of crude benzol raw material, hydrogenation element, fore-distillation, extractive distillation, refining aromatic hydrocarbons, distillation xylene unit form, hydrogenation element refined unit is divided into again reactive moieties and steady component.Reactive moieties adopts pre-hydrogenation and the reaction of main hydrogenation secondary hydrogenation, and the hydrogen make-up needed for reaction is provided by the external world.Be characterized in that reaction conditions is gentleer, temperature of reaction 320 DEG C ~ 380 DEG C, reaction pressure 3.0MPa ~ 3.5MPa, invest relatively low, processing safety is high.Comparatively speaking, low temperature process is comparatively ideal processing method.But this kind of low temperature process hydrogenation is temperature required still will reach 320 DEG C ~ 380 DEG C, and benzene can be converted into the hexanaphthene that second pyrolysis very easily occurs at such a temperature, aromatic hydroxy compound loss is comparatively large, reduces aromatic hydrocarbons retention.
Benzene,toluene,xylene is all important organic chemical industry's basic raw material, and they mainly come from petroleum refining process.Crude benzol is from the raw gas of coking of coal, reclaim a kind of benzoline obtained, and main component is mononuclear aromatics.Benzene,toluene,xylene content in crude benzol accounts for more than 90%, wherein benzene account for 70%, toluene 8% ~ 25%, dimethylbenzene 2% ~ 5%.The benzene,toluene,xylene obtained from crude benzol can be used for the deficiency making up benzene series produce market.
At present, mainly contain two kinds by the method for preparing benzene aromatic hydrocarbon by crude benzene: one is vitriol oil acid wash, another kind is shortening method.Acid wash technical process is simple, flexible operation, equipment are simple, material is easy to get, but can only sulfocompound in partial removal crude benzol and impurity, in the course of processing, aromatic hydroxy compound purity is not high, loss is comparatively large, and processing by-product refuse acid tar and residue can cause serious environmental pollution.This method is prohibited from using in some developed countries, and major part producer of China is still in this method of employing.
Since the 1950's, American and Britain, moral, Fa Deng state succeed in developing crude benzol shortening element essence method for making in succession.The sixties in 20th century, Hu get Li Air Products Company of the U.S. succeeds in developing high temperature crude benzole hydrogenation element process for refining (Litol method) purified petroleum benzin processed, this technique is refined and dealkylation by hydrogenation element under high temperature (600 ~ 630 DEG C), high pressure (5.7 ~ 6.0MPa), producing purity is 99.9%, the purified petroleum benzin product of S < 0.5ppm, benzaldehyde product yield reaches 114%.To the eighties in 20th century, the U.S. and Germany succeed in developing again low temperature hydrogenation element purification techniques in crude benzol (sulfolane process and KK method) in succession, this technique is the refining and extractive distillation by hydrogenation element under middle low temperature (320 ~ 380 DEG C), middle pressure (3.5 ~ 3.7MPa), produce benzene, toluene and xylene product, product purity >=99.9%, S < 0.5ppm, yield is about 98%.The aromatic hydrocarbon product purity obtained by hydrogenation element essence method for making is high, and S content is low, and yield is high, non-environmental-pollution.But these three kinds of crude benzole hydrogenation techniques also exist a unavoidable defect, namely have part aromatic hydrocarbons to be hydrogenated into naphthenic hydrocarbon or alkane in crude benzol, thus cause aromatic hydrocarbons to lose large, aromatic hydrocarbon product yield is low.
Though hydrogenation technique can obtain the benzene series product of high-quality, but it is complicated that its shortcoming is Technology, facility investment is large, energy consumption is high, and also there is a unavoidable defect in above-mentioned crude benzole hydrogenation element process for refining, namely have part aromatic hydrocarbons to be hydrogenated into naphthenic hydrocarbon or alkane in crude benzol, thus cause aromatic hydrocarbons to lose large, aromatic hydrocarbon product yield is low.
The textural defect that the purification apparatus of existing coking crude benzene exists is: in whole separation system, each tower all arranges the facilities such as heating, overhead condensation at the bottom of tower, therefore needs to consume a large amount of heat energy and recirculated cooling water.Also the technique (as German Patent 4586986) had adopts pressurized operation at preheating rectifying tower, then with the high-temperature steam of this column overhead thermal source as other tower, though like this can be energy-conservation, but because the working pressure of pre-rectifying tower is large, temperature is high, causes facility investment to increase considerably, and needs high temperature heat source, need significantly to increase investment construction high temperature heating medium system, thus production cost is still higher.
Chinese patent CN1948244A discloses a kind of technique by coking benzene hydrogenation desulfurization denitrogenation producing refined benzene, mainly comprises coking benzene pre-treatment rectification step, three grades of desulfurized steps, purification step etc.Chinese patent CN101486623A discloses a kind of crude benzole hydrogenation element process for purification, coking crude benzene raw material after pretreatment, pre-hydrotreating reaction and main hydrogenation reaction is carried out after de-weight of reducing pressure, gaseous phase materials after hydrogenation reaction enters hp flash drum, isolate hydrogen-rich gas, liquid phase enters stabilizer tower and removes low boiling hydrocarbon, finally enters aromatic extraction unit, extracting obtains highly purified triphen, there is the problem that catalyst for pre-hydrogenation bed pressure drop raises.Chinese patent CN101519338A discloses a kind of coking crude benzene hydrogenation element process for refining, and, fore-distillation refining by raw material initial gross separation, hydrogenation element, extractive distillation, refining aromatic hydrocarbons, dimethylbenzene distill unit and forms; This invention can reduce aromatic hydrocarbons loss to a certain extent, and quality product can reach the quality of petroleum benzene.But no matter be external hydrogen addition technology or domestic hydrogen addition technology, all do not have to remove pyridines material de-weight is independent afterwards, and in the charging of conventional hydro device in coking of coal crude benzol pyridine compounds and their content high, these compounds are basic nitrogen compounds, seriously inhibit thiophenes hydrodesulfurization reaction, is the maximum inhibition of hydrodesulfurization reaction.They are vied each other by hydrogenation approach in catalyst active center, and denitrification reaction is slower than desulphurization reaction, and the time that nitride is trapped in active centre is longer than sulfide, therefore can reduce desulfurization rate, and substantially reduce the work-ing life of hydrogenation catalyst.As can be seen here, the pyridine compounds and their that pre-treatment removes in hydrogenating materials is very necessary, and the denitrfying agent provided with ZL94115190.5 or other acidic components denitrfying agent and denitrfying agent have larger solubleness with pyridine compounds and their in crude benzol than in oil product, their residual meetings in crude benzol are adsorbed on catalyst surface, reduce the surfactivity of expensive hydrogenation catalyst.
Summary of the invention
The object of the invention is to propose the production technique that a kind of coking crude benzene produces benzene aromatic hydrocarbon.
For reaching this object, the present invention by the following technical solutions:
Coking crude benzene produces the production technique of benzene aromatic hydrocarbon, and, extractive distillation refining by raw material initial gross separation, hydrogenation element, refining aromatic hydrocarbons, distillation xylene unit form, the hydrogen make-up that hydrogenation element is refined needed for unit process is provided by the external world, reformate is through fore-distillation, separate the heavy constituent of dimethylbenzene and above component and contain benzene, the light constituent of toluene and non-aromatics, the former sends to rectifying and obtains grade oil xylol, the latter is with the extractive distillation of N-N-formyl morpholine N-, isolate non-aromatics and contain benzene, the rich solvent of toluene, rich solvent is again through rectifying, obtain grade oil benzene and nitration grade toluene respectively, nitration grade toluene obtains grade oil toluene through the extractive distillation of N-N-formyl morpholine N-, it is characterized in that: the mixing oil of crude benzol and other hydrocarbon ils and hydrogen, in the reactor that hydrogenation catalyst is housed, hydrogenation reaction occurs, reaction conditions is: temperature 285-370, hydrogen pressure 3.0-9.0MPa, liquid air speed 5-6h, hydrogen-oil ratio 1500-1600:1, hydrogenation catalyst can select molybdenum nickel tungsten phosphorus series catalysts, molybdenum nickel catalyst or molybdenum cobalt series catalyst.
Embodiment
Embodiment 1
Coking crude benzene produces the production technique of benzene aromatic hydrocarbon, and, extractive distillation refining by raw material initial gross separation, hydrogenation element, refining aromatic hydrocarbons, distillation xylene unit form, the hydrogen make-up that hydrogenation element is refined needed for unit process is provided by the external world, reformate is through fore-distillation, separate the heavy constituent of dimethylbenzene and above component and contain benzene, the light constituent of toluene and non-aromatics, the former sends to rectifying and obtains grade oil xylol, the latter is with the extractive distillation of N-N-formyl morpholine N-, isolate non-aromatics and contain benzene, the rich solvent of toluene, rich solvent is again through rectifying, obtain grade oil benzene and nitration grade toluene respectively, nitration grade toluene obtains grade oil toluene through the extractive distillation of N-N-formyl morpholine N-, it is characterized in that: the mixing oil of crude benzol and other hydrocarbon ils and hydrogen, in the reactor that hydrogenation catalyst is housed, hydrogenation reaction occurs, reaction conditions is: temperature 280 DEG C, hydrogen pressure 2.0MPa, liquid air speed 0.5h, hydrogen-oil ratio 200: 1, hydrogenation catalyst can select molybdenum nickel tungsten phosphorus series catalysts, molybdenum nickel catalyst or molybdenum cobalt series catalyst.
Embodiment 2
Coking crude benzene produces the production technique of benzene aromatic hydrocarbon, and, extractive distillation refining by raw material initial gross separation, hydrogenation element, refining aromatic hydrocarbons, distillation xylene unit form, the hydrogen make-up that hydrogenation element is refined needed for unit process is provided by the external world, reformate is through fore-distillation, separate the heavy constituent of dimethylbenzene and above component and contain benzene, the light constituent of toluene and non-aromatics, the former sends to rectifying and obtains grade oil xylol, the latter is with the extractive distillation of N-N-formyl morpholine N-, isolate non-aromatics and contain benzene, the rich solvent of toluene, rich solvent is again through rectifying, obtain grade oil benzene and nitration grade toluene respectively, nitration grade toluene obtains grade oil toluene through the extractive distillation of N-N-formyl morpholine N-, it is characterized in that: the mixing oil of crude benzol and other hydrocarbon ils and hydrogen, in the reactor that hydrogenation catalyst is housed, hydrogenation reaction occurs, reaction conditions is: temperature 280 DEG C, hydrogen pressure 2.0MPa, liquid air speed 4.0h, hydrogen-oil ratio 1500: 1, hydrogenation catalyst can select molybdenum nickel tungsten phosphorus series catalysts, molybdenum nickel catalyst or molybdenum cobalt series catalyst.
Embodiment 3
Coking crude benzene produces the production technique of benzene aromatic hydrocarbon, and, extractive distillation refining by raw material initial gross separation, hydrogenation element, refining aromatic hydrocarbons, distillation xylene unit form, the hydrogen make-up that hydrogenation element is refined needed for unit process is provided by the external world, reformate is through fore-distillation, separate the heavy constituent of dimethylbenzene and above component and contain benzene, the light constituent of toluene and non-aromatics, the former sends to rectifying and obtains grade oil xylol, the latter is with the extractive distillation of N-N-formyl morpholine N-, isolate non-aromatics and contain benzene, the rich solvent of toluene, rich solvent is again through rectifying, obtain grade oil benzene and nitration grade toluene respectively, nitration grade toluene obtains grade oil toluene through the extractive distillation of N-N-formyl morpholine N-, it is characterized in that: the mixing oil of crude benzol and other hydrocarbon ils and hydrogen, in the reactor that hydrogenation catalyst is housed, hydrogenation reaction occurs, reaction conditions is: temperature 380 DEG C, hydrogen pressure 10.0MPa, liquid air speed 4.0h, hydrogen-oil ratio 1500: 1, hydrogenation catalyst can select molybdenum nickel tungsten phosphorus series catalysts, molybdenum nickel catalyst or molybdenum cobalt series catalyst.
Embodiment 3: the purposes of a kind of benzene aromatic hydrocarbon in mechanical workout lapping liquid, is characterized in that emulsifying agent 10, is weight part containing abrasive material 20, distilled water 100, benzene aromatic hydrocarbon 0.01, tensio-active agent 20.
Obviously, the above embodiment of the present invention is only for example of the present invention is clearly described, and is not the restriction to embodiments of the present invention.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here exhaustive without the need to also giving all embodiments.And these belong to spirit institute's apparent change of extending out of the present invention or change and are still among protection scope of the present invention.
Claims (1)
1. coking crude benzene produces the production technique of benzene aromatic hydrocarbon, and, extractive distillation refining by raw material initial gross separation, hydrogenation element, refining aromatic hydrocarbons, distillation xylene unit form, the hydrogen make-up that hydrogenation element is refined needed for unit process is provided by the external world, reformate is through fore-distillation, separate the heavy constituent of dimethylbenzene and above component and contain benzene, the light constituent of toluene and non-aromatics, the former sends to rectifying and obtains grade oil xylol, the latter is with the extractive distillation of N-N-formyl morpholine N-, isolate non-aromatics and contain benzene, the rich solvent of toluene, rich solvent is again through rectifying, obtain grade oil benzene and nitration grade toluene respectively, nitration grade toluene obtains grade oil toluene through the extractive distillation of N-N-formyl morpholine N-, it is characterized in that: the mixing oil of crude benzol and other hydrocarbon ils and hydrogen, in the reactor that hydrogenation catalyst is housed, hydrogenation reaction occurs, reaction conditions is: temperature 285-370 DEG C, hydrogen pressure 3.0-9.0MPa, liquid air speed 5-6h, hydrogen-oil ratio 1500-1600:1, hydrogenation catalyst can select molybdenum nickel tungsten phosphorus series catalysts, molybdenum nickel catalyst or molybdenum cobalt series catalyst, described raw material can be coking crude benzene.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106396926A (en) * | 2016-08-31 | 2017-02-15 | 阜南县阜合种养农民专业合作联合社 | Fertilizer-efficiency-controllable biofertilizer capable of improving heating resistance of plants |
| CN108002974A (en) * | 2017-12-15 | 2018-05-08 | 武汉钢铁有限公司 | The process of refined coking crude benzene |
| CN109261222A (en) * | 2018-11-21 | 2019-01-25 | 贵州理工学院 | A kind of preparation method of the high stability bimetallic hollow core core/shell-type catalyst for the reaction of toluene steam reforming |
| 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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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1900032A (en) * | 2006-07-06 | 2007-01-24 | 湖南长岭石化科技开发有限公司 | Method for producing benzene aromatic hydrocarbon from crude benzole |
| CN102344338A (en) * | 2011-07-18 | 2012-02-08 | 邢台旭阳煤化工有限公司 | Process for upgrading heavy benzene hydrogenation |
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2014
- 2014-11-05 CN CN201410617946.2A patent/CN104355959A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1900032A (en) * | 2006-07-06 | 2007-01-24 | 湖南长岭石化科技开发有限公司 | Method for producing benzene aromatic hydrocarbon from crude benzole |
| CN102344338A (en) * | 2011-07-18 | 2012-02-08 | 邢台旭阳煤化工有限公司 | Process for upgrading heavy benzene hydrogenation |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106396926A (en) * | 2016-08-31 | 2017-02-15 | 阜南县阜合种养农民专业合作联合社 | Fertilizer-efficiency-controllable biofertilizer capable of improving heating resistance of plants |
| CN108002974A (en) * | 2017-12-15 | 2018-05-08 | 武汉钢铁有限公司 | The process of refined coking crude benzene |
| CN109261222A (en) * | 2018-11-21 | 2019-01-25 | 贵州理工学院 | A kind of preparation method of the high stability bimetallic hollow core core/shell-type catalyst for the reaction of toluene steam reforming |
| 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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