CN103772123A - Method for increasing yield of BTX aromatics - Google Patents
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Abstract
The invention relates to a method for increasing yield of BTX aromatics, and mainly solves the problem that in the prior art, the utilization value of heavy aromatics and non-aromatics is low. According to the invention, heavy components containing polycyclic aromatic compound or carbons higher than or equal to six containing are mixed with hydrogen, the mixture enters a fixed bed reactor containing a catalyst, so that dealkylation and alkyl shifting reactions are performed on heavy aromatics, isomerization reaction is performed on light aromatics, and hydrocracking and aromatisation reactions are performed on heavy non-aromatics; the obtained BTX-rich reaction products continuously pass through a vapour liquid separator, a stripping column, a benzene column, a toluene column, and a dimethyl benzene column; the products of liquefied gas, benzene, toluene, and dimethyl benzene are obtained. The technical scheme excellently solves the problem, and can be applied to the industrial production of aromatics.
Description
Technical field
The present invention relates to a kind of method of the BTX of volume increase aromatic hydrocarbons.
Background technology
BTX is important organic chemical industry's basic material of petrochemical complex.BTX, B is that benzene, T are toluene, X is dimethylbenzene.Along with global economic growth, BTX aromatic hydrocarbons will continue to keep market growth from now on.The Main Resources of producing aromatic hydrocarbons has catalytic reforming to generate oil, understands gasoline and coal tar.In pyrolysis gasoline, aromaticity content, up to 60%, is the important source material of preparing aromatic hydrocarbon.Because International Crude Oil is for a long time in high position concussion, China's ethylene cracking material source diversification in recent years also has the trend that becomes heavy gradually, will cause the increase of production of by-product pyrolysis gasoline, for volume increase BTX aromatic hydrocarbons provides raw material assurance.
Heavy arene comprises the C of steam cracking device and refinery continuous reformer by-product
9above aromatic hydrocarbons, is mainly C
9and C
10aromatic hydrocarbons, is the reformation heavy arene of valuable petrochemical complex resource, especially catforming process by-product, accounts for 4% left and right of oil refining process catalytic reforming charging.Reformation heavy aromatics contains alkene, good stability, further deep processing and utilization hardly.Continuous reformer heavy aromatics can generate the aromatic hydrocarbons such as benzene, toluene and dimethylbenzene (BTX) by transalkylation or dealkylation, also has considerable part to enter heavy aromatics comprehensive utilization generating apparatus and processes.
Industrial is generally that the reformate that reforming process is made and the pyrolysis gasoline being obtained by naphtha cracking carry out solvent extraction and separate BTX aromatic hydrocarbons and non-aromatics, this process is according to aromatic hydrocarbons, the polarity difference of non-aromatics in use solvent, reaches the object of separate targets aromatic hydrocarbons.Although solvent extraction BTX can obtain the BTX aromatic hydrocarbons of higher degree, but need the solvent extraction apparatus of a set of complexity, and extraction solvent needs to supplement into continuously in extraction procedure process, solvent extraction method is favourable from obtaining highly purified aromatic hydrocarbon mixing, but from the extra solvent extraction equipment of needs and disadvantageous in the time that equipment needs in service drop into solvent continuously, therefore solvent extraction process has occupied the very big ratio of producing BTX aromatic hydrocarbons cost.From lightweight aromatic product, in product, contain a large amount of toluene, lower with heavy arene and non-aromatic utility value after separating, the value of benzene and dimethylbenzene is higher by contrast.
U.S. Pat 3,729,409 non-aromaticss that propose to mix with aromatic hydrocarbons are reacted and are changed into low-carbon alkanes by hydrocracking under the existence of catalyzer, can from non-aromatics, isolate aromatic hydrocarbons by vapour-liquid separator.In addition, U.S. Pat 3,849,290 and US3,950,241 have also proposed a kind ofly under the existence of ZSM-5 type zeolite, to change into gaseous component to increase aromaticity content in liquid composition to prepare the method for high-quality ethereal oil component through hydrocracking reaction by the straight chain hydrocarbon component that makes to mix with aromatic hydrocarbons.U.S. Pat 5,865,986 and US6,001,241 has further disclosed a kind of naphtha fraction upgrade method, by catalyst based at partial reaction mesolite, to increase the output of aromatic hydrocarbons.
Korea S SK patent CN127892C, by similar approach, is prepared into liquefied petroleum gas (LPG) and light aromatics by the upgrading such as reformate and pyrolysis gasoline.
Summary of the invention
Technical problem to be solved by this invention is for low aromatic hydrocarbons mixture in prior art, conventional solvent extracting sepn process exists and only simply BTX aromatic hydrocarbons is separated, the low problem of a large amount of toluene and heavy arene and non-aromatic utility value in light aromatics product, the method of new volume increase BTX a kind of is provided, the method has hydrocarbon raw material and separates simple, product added value is high, avoids solvent extraction process, the advantage that non-aromatics utility value is high.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method of increasing production BTX aromatic hydrocarbons, comprises the following steps successively:
A) heavy arene and non-aromatics raw material react through purifying, after hyperthermic treatment, mixes with hydrogen, enter the fixed-bed reactor that catalyzer is housed, and generate the aromatic product that contains benzene,toluene,xylene;
B) aromatic product is divided into gas phase and liquid phase through condensation, and gas-phase product comprises low-carbon alkanes and hydrogen, and liquid product comprises a small amount of non-aromatics;
C) liquid product enters stripping tower middle part, obtains liquefied gas from return tank of top of the tower, and tower reactor obtains carbon six and above material;
D) described carbon six and above material enter benzene tower, and after separating, tower top obtains benzaldehyde product, and tower reactor obtains carbon seven and above material; Wherein, benzaldehyde product is divided into two strands, and first strand of benzene that accounts for 0～100% weight returns in the fixed-bed reactor in step a), and second strand accounts for the benzene extraction of 0～100% weight;
E) described carbon seven and above material enter toluene tower middle part, and tower top obtains toluene product, and tower reactor obtains carbon eight and above material; Wherein, toluene product is divided into two strands, and first strand of toluene that accounts for 0～100% weight returns in the fixed-bed reactor in step a), and second strand accounts for the toluene extraction of 0～100% weight;
F) described carbon eight and above material enter benzenol hydrorefining middle part, and tower top obtains Mixed XYLENE product, and tower reactor obtains carbon nine and above cut; Wherein, carbon nine and above cut are divided into two strands, and first strand of carbon nine and above cut that accounts for 0～100% weight returns in the fixed-bed reactor in step a), and second strand accounts for carbon nine and the above cut extraction of 0～100% weight.
In technique scheme, preferred technical scheme, heavy arene and non-aromatics raw material are from the by-product carbon six of cracker and above component, or carbon six and the above heavy component mixture containing more aromatic ring or the many rings that come from devices such as reformation, catalytic cracking, gasoline hydrogenations; After purifying treatment, in heavy arene and non-aromatics raw material, sulphur weight content is less than 200ppm, and alkene or diolefin weight content are less than 20%; In catalyzer, contain at least one in metal or the oxide compound that is selected from Cu, Sn, Pb, Zn and Fe; Reactor is the fixed bed adiabatic reactor of single hop or multi-stage type; In reactor feed, hydrogen dividing potential drop preferable range is 0.25 ~ 2.5 MPa, and temperature of reaction preferable range is 200 ~ 500 ℃, and liquid phase weight space velocity preferable range is 0.1 ~ 10h
-1; Stripping tower top working pressure preferable range is 0.0～1.0MPa, more preferably scope 0.5 ~ 1.0MPa, and tower top service temperature preferable range is 60～200 ℃, more preferably scope is 120～200 ℃; Benzene column overhead working pressure preferable range is 0.0～0.5MPa, and more preferably scope is 0.0 ~ 0.2MPa, and tower top service temperature preferable range is 80～160 ℃, and more preferably scope is 80～120 ℃; Toluene tower tower top working pressure preferable range is 0.0～0.5MPa, and more preferably scope is 0.0 ~ 0.2MPa (g), and service temperature more preferably scope is 110～200 ℃, and more preferably scope is 110～155 ℃; Benzenol hydrorefining tower top working pressure preferable range is 0～0.5MPa, and more preferably scope is 0.0 ~ 0.2MPa, and service temperature preferable range is 140～220 ℃, and more preferably scope is 140～190 ℃.
Preferred technical scheme, the benzene that first strand of benzene column overhead preferably accounts for 10～90% weight, before sending into fixed-bed reactor, mixes with heavy arene and non-aromatics raw material after purifying treatment; First strand of toluene tower tower top preferably accounts for the toluene of 10～80% weight, before sending into fixed-bed reactor, mixes with heavy arene and non-aromatics raw material after purifying treatment; Carbon nine and above cut that first strand of benzenol hydrorefining tower reactor preferably accounts for 0～70% weight, before sending into fixed-bed reactor, mix with heavy arene and non-aromatics raw material after purifying treatment.Preferred technical scheme, in step d), first strand of benzene that accounts for 20～80% weight returns in the fixed-bed reactor in step a), and second strand accounts for the benzene extraction of 20～80% weight; In step e), first strand of toluene that accounts for 25～75% weight returns in the fixed-bed reactor in step a), and second strand accounts for the toluene extraction of 25～75% weight; In step f), first strand of carbon nine and above cut that accounts for 30～70% weight returns in the fixed-bed reactor in step a), and second strand accounts for carbon nine and the above cut extraction of 30～70% weight.
In technical scheme of the present invention, the gaseous product of reaction can be isolated hydrogen and low-carbon alkanes by further processing, and hydrogen can Returning reacting system recycle, and low-carbon alkanes can be used as ethylene cracker produces the raw material of ethene or propylene; The non-aromatic hydrocracking reaction of heavy is a high thermopositive reaction, can the self-sufficiency of realization response heat, and energy consumption is low; Dimethylbenzene tower reactor heavy composition can be used as the blend component of high-quality vehicle fuel; Recycle benzene, toluene or the above component of carbon nine not only can be taken away reaction heat and reduce bed temperature rise, and can optimize and revise aromatic hydrocarbon product ratio, therefore can be according to material condition and the flexible adjusting process project of product requirement.Adopt technical scheme of the present invention, in the product obtaining, benzene reduces 3.4 tons/hour, and toluene increases by 5.9 tons/hour, and dimethylbenzene increases by 1.7 tons/hour, and ethylbenzene reduces 3.1 tons/hour, has improved added value of product, has obtained significant technique effect.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of volume increase BTX aromatic hydrocarbons.
In Fig. 1, I is reaction member, and II is product separation device, III stripping tower, and IV is benzene tower, and V is toluene tower, and VI is benzenol hydrorefining.1 is fresh feed, and 2 is recycle benzene raw material, and 3 is circulation methylbenzene raw material, 4 is cyclic carbon nine and above component raw material, and 5 is reaction product, and 6 is reactant gases product, 7 is reaction liquid product, and 8 is LPG, and 9 is the charging of benzene tower, 10 is benzaldehyde product, 11 is toluene tower charging, and 12 is toluene product, and 13 is benzenol hydrorefining charging, 14 is dimethylbenzene product, and 15 is the extraction of dimethylbenzene tower reactor.
In the technical process of the volume increase BTX aromatic hydrocarbons shown in Fig. 1, fresh feed 1 and recycle feed 2, 3, 4 enter reaction member I, reaction product 5 enters product separation device II and carries out vapor-liquid separation, the reaction solution 7 separating enters stripping tower III, obtain LPG at stripping tower tower top, benzene tower charging 9 comes from stripping tower reactor, benzene tower IV overhead extraction benzene, part recycle benzene 2 Returning reacting systems, 10 extraction of part benzaldehyde product, toluene tower V tower top obtains toluene, part toluene 3 Returning reacting systems, 12 extraction of part toluene product, benzenol hydrorefining VI tower top obtains Mixed XYLENE, tower reactor to carbon nine and above component, part cyclic carbon nine and above component 4 Returning reacting systems, part heavy constituent 15 tower reactors are discharged.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
With C
6and the miscellany of above component is raw material (wherein benzene content is 24.4 tons/hour, and toluene level is 9.3 tons/hour, and xylene content is 2.1 tons/hour, and ethyl-benzene level is 3.6 tons/hour), adopt the volume increase of Fig. 1 Technology BTX, wherein benzene, toluene, C
9 +all do not circulate.Reaction member, reaction pressure 2.8 MPa, 350 ℃ of temperature of reaction, hydrogen dividing potential drop 1.4 MPa; Stripping tower is 44 layers of valve tray, and tower top working pressure is 0.7MPa, and dephlegmator of top of the tower control temperature is 40 ℃, discharges non-condensable gas, and wherein ethane volumetric molar concentration is 47.1%, and propane volumetric molar concentration is 39.9%, other lighter hydrocarbons 13.0mol%.Benzene tower adopts 55 layers of valve tray, and tower top working pressure is 0.05MPa, and tower top obtains the benzaldehyde product that 21 tons of/hour purity are 99.95wt%.Toluene tower adopts 55 layers of valve tray, and tower top working pressure is 0.05MPa, and tower top obtains the toluene product that 15.2 tons of/hour purity are 99.9wt%.Benzenol hydrorefining adopts 80 layers of valve tray, and tower top working pressure is 0.05MPa, and tower top obtains the dimethylbenzene product that 4.3 tons of/hour purity are 87.7wt%, and wherein ethyl-benzene level is 12.3 wt%.Therefore, adopt this Technology, in the product obtaining, benzene reduces 3.4 tons/hour, and toluene increases by 5.9 tons/hour, and dimethylbenzene increases by 1.7 tons/hour, and ethylbenzene reduces 3.1 tons/hour, has improved added value of product.
Catalyzer is Hydrogen adhesiveless ZSM-5 zeolite (SiO
2/ Al
2o
3mol ratio is 90) go up load in the Pt of catalyst weight per-cent 0.17% and 0.50% Pb.
[embodiment 2]
With the non-aromatic cracking C of the height after secondary hydrogenation
9 +for raw material (toluene level is 3.1 tons/hour), adopt the volume increase of Fig. 1 Technology BTX, wherein benzene, toluene, C
9 +all do not circulate.Reaction member, reaction pressure 2.8 MPa, 340 ℃ of temperature of reaction, hydrogen dividing potential drop 1.14 MPa; Stripping tower is 44 layers of valve tray, and tower top working pressure is 0.7MPa, and dephlegmator of top of the tower control temperature is 40 ℃, discharges non-condensable gas, and wherein ethane volumetric molar concentration is 23.3%, and propane volumetric molar concentration is 63.3%, other lighter hydrocarbons 13.4mol%.Benzene tower adopts 55 layers of valve tray, and tower top working pressure is 0.05MPa, and tower top obtains the benzaldehyde product that 8.4 tons of/hour purity are 99.95wt%.Toluene tower adopts 55 layers of valve tray, and tower top working pressure is 0.05MPa, and tower top obtains the toluene product that 14.2 tons of/hour purity are 99.9wt%.Benzenol hydrorefining adopts 80 layers of valve tray, and tower top working pressure is 0.05MPa, and tower top obtains the Mixed XYLENE product that 6.8 tons of/hour purity are 99.7wt%.Therefore, adopt this Technology, in the product obtaining, benzene increases by 8.4 tons/hour, and toluene increases by 11.1 tons/hour, and dimethylbenzene increases by 6.8 tons/hour, has improved added value of product.
Catalyzer is Hydrogen adhesive-free mordenite (SiO
2/ Al
2o
3mol ratio is 30) go up load in the Pt of weight percent of catalyst 0.06% and 0.08% Pb.
[embodiment 3]
With reformation C
9 +for raw material, (benzene content is 0 ton/hour, and toluene level is 30.5 tons/hour, and xylene content is 42.3 tons/hour, C
9 +aromaticity content is 504.5 tons/hour), adopt the volume increase of Fig. 1 Technology BTX, wherein benzene, toluene, C
9 +all do not circulate.Reaction member, reaction pressure 2.6 MPa, 320 ℃ of temperature of reaction, hydrogen dividing potential drop 1.04 MPa; Stripping tower is 44 layers of valve tray, and tower top working pressure is 0.7MPa, and dephlegmator of top of the tower control temperature is 40 ℃, discharges non-condensable gas, and wherein ethane volumetric molar concentration is 18.3%, and propane volumetric molar concentration is 63.3%, other lighter hydrocarbons 18.4mol%.Benzene tower adopts 55 layers of valve tray, and tower top working pressure is 0.05MPa, and tower top obtains the benzaldehyde product that 53.7 tons of/hour purity are 99.95wt%.Toluene tower adopts 55 layers of valve tray, and tower top working pressure is 0.05MPa, and tower top obtains the toluene product that 160.7 tons of/hour purity are 99.9wt%.Benzenol hydrorefining adopts 80 layers of valve tray, and tower top working pressure is 0.05MPa, and tower top obtains the Mixed XYLENE product that 130.8 tons of/hour purity are 99.7wt%.Therefore, adopt this Technology, in the product obtaining, benzene increases by 53.7 tons/hour, and toluene increases by 130.2 tons/hour, and dimethylbenzene increases by 88.5 tons/hour, has improved added value of product.
Catalyzer is Hydrogen adhesive-free mordenite (SiO
2/ Al
2o
3mol ratio is 30) go up load in the Pt of weight percent of catalyst 0.06% and 0.08% Pb.
[embodiment 4]
With reformation C
9 +for raw material, (benzene content is 10 tons/hour, and toluene level is 30.5 tons/hour, and xylene content is 42.3 tons/hour, C
9 +aromaticity content is 504.5 tons/hour), adopt the volume increase of Fig. 1 Technology BTX, wherein benzene, toluene, C
9 +all do not circulate.Reaction member, reaction pressure 2.6 MPa, 320 ℃ of temperature of reaction, hydrogen dividing potential drop 1.04 MPa; Stripping tower is 44 layers of valve tray, and tower top working pressure is 0.7MPa, and dephlegmator of top of the tower control temperature is 40 ℃, discharges non-condensable gas, and wherein ethane volumetric molar concentration is 18.3%, and propane volumetric molar concentration is 63.3%, other lighter hydrocarbons 18.4mol%.Benzene tower adopts 55 layers of valve tray, and tower top working pressure is 0.05MPa, and tower top obtains the benzaldehyde product that 53.7 tons of/hour purity are 99.95wt%.Toluene tower adopts 55 layers of valve tray, and tower top working pressure is 0.05MPa, and tower top obtains the toluene product that 160.7 tons of/hour purity are 99.9wt%.Benzenol hydrorefining adopts 80 layers of valve tray, and tower top working pressure is 0.05MPa, and tower top obtains the Mixed XYLENE product that 130.8 tons of/hour purity are 99.7wt%.Therefore, adopt this Technology, in the product obtaining, benzene increases by 63.7 tons/hour, and toluene increases by 134.2 tons/hour, and dimethylbenzene increases by 98.5 tons/hour, has improved added value of product.
Catalyzer is Hydrogen adhesive-free mordenite (SiO
2/ Al
2o
3mol ratio is 40) go up load in the Pt of weight percent of catalyst 0.06% and 0.08% Pb.
Wherein, carbon six and above material enter benzene tower, and after separating, tower top obtains benzaldehyde product, and tower reactor obtains carbon seven and above material; Wherein, benzaldehyde product is divided into two strands, and first strand of benzene that accounts for 20% weight returns in fixed-bed reactor, and second strand accounts for the benzene extraction of 80% weight; Described carbon seven and above material enter toluene tower middle part, and tower top obtains toluene product, and tower reactor obtains carbon eight and above material; Wherein, toluene product is divided into two strands, and first strand of toluene that accounts for 30% weight returns in fixed-bed reactor, and second strand accounts for the toluene extraction of 70% weight; Described carbon eight and above material enter benzenol hydrorefining middle part, and tower top obtains Mixed XYLENE product, and tower reactor obtains carbon nine and above cut; Wherein, carbon nine and above cut are divided into two strands, and first strand of carbon nine and above cut that accounts for 60% weight returns in fixed-bed reactor, and second strand accounts for carbon nine and the above cut extraction of 40% weight.
[comparative example 1]
Adopt embodiment 1 identical raw material and catalyzer, adopt Technology as shown in Figure 1,16.5 tons/hour of toluene wherein circulate.Adopt the process conditions identical with embodiment 1, in the non-condensable gas that stripping tower top obtains, ethane volumetric molar concentration is 40.9%, and propane volumetric molar concentration is 47.3%, other lighter hydrocarbons 11.8mol%; Benzene tower top obtains the benzaldehyde product that 25 tons of/hour purity are 99.95wt%; The toluene product that 7.5 tons of/hour purity of toluene overhead extraction are 99.9wt%; Benzenol hydrorefining tower top obtains the dimethylbenzene product that 7.6 tons of/hour purity are 87.7wt%, and wherein ethyl-benzene level is 12.3 wt%.Compare embodiment 1, in the product obtaining, benzene increases by 4 tons/hour, and toluene reduces 7.7 tons/hour, and dimethylbenzene increases by 2.9 tons/hour, and ethylbenzene increases by 0.4 ton/hour.Therefore, adopt this Technology, by circulation toluene, adjusted product composition, reduced toluene output, improved the output of dimethylbenzene.
[comparative example 2]
Adopt identical raw material and the catalyzer of embodiment 1, adopt Technology as shown in Figure 1.Wherein 14.3 tons/hour of recycle benzene.Adopt the process conditions identical with embodiment 1, benzene tower top obtains the benzaldehyde product that 23.4 tons of/hour purity are 99.95wt%; The toluene product that 13.6 tons of/hour purity of toluene overhead extraction are 99.9wt%; Benzenol hydrorefining tower top obtains the dimethylbenzene product that 3.33 tons of/hour purity are 82.2wt%, and wherein ethyl-benzene level is 17.8 wt%.Compare embodiment 1, in the product obtaining, benzene has increased by 2.4 tons/hour, and toluene reduces 1.6 tons/hour, and dimethylbenzene reduces 1.0 tons/hour, and ethylbenzene increases by 0.1 ton/hour.Therefore, adopt this Technology, by recycle benzene, adjusted product composition, increased benzene yield, reduced toluene and dimethylbenzene output.
Claims (10)
1. a method of increasing production BTX aromatic hydrocarbons, comprises the following steps successively:
A) heavy arene and non-aromatics raw material react through purifying, after hyperthermic treatment, mixes with hydrogen, enter the fixed-bed reactor that catalyzer is housed, and generate the aromatic product that contains benzene,toluene,xylene;
B) aromatic product is divided into gas phase and liquid phase through condensation, and gas-phase product comprises low-carbon alkanes and hydrogen, and liquid product comprises non-aromatics;
C) liquid product enters stripping tower middle part, obtains liquefied gas from return tank of top of the tower, and tower reactor obtains carbon six and above material;
D) described carbon six and above material enters benzene tower, and after separating, tower top obtains benzaldehyde product, and tower reactor obtains carbon seven and above material; Wherein, benzaldehyde product is divided into two strands, and first strand of benzene that accounts for 0～100% weight returns in the fixed-bed reactor in step a), and second strand accounts for the benzene extraction of 0～100% weight;
E) described carbon seven and above material enter toluene tower middle part, and tower top obtains toluene product, and tower reactor obtains carbon eight and above material; Wherein, toluene product is divided into two strands, and first strand of toluene that accounts for 0～100% weight returns in the fixed-bed reactor in step a), and second strand accounts for the toluene extraction of 0～100% weight;
F) described carbon eight and above material enter benzenol hydrorefining middle part, and tower top obtains Mixed XYLENE product, and tower reactor obtains carbon nine and above cut; Wherein, carbon nine and above cut are divided into two strands, and first strand of carbon nine and above cut that accounts for 0～100% weight returns in the fixed-bed reactor in step a), and second strand accounts for carbon nine and the above cut extraction of 0～100% weight.
2. the method for volume increase BTX aromatic hydrocarbons according to claim 1, it is characterized in that heavy arene and non-aromatics raw material are the above components of by-product carbon six that is selected from cracker, the above heavy component mixture of carbon six containing aromatic ring or many rings that reformation, catalytic cracking, gasoline hydrogenation device come.
3. the method for volume increase according to claim 1 BTX aromatic hydrocarbons, is characterized in that after purifying treatment in heavy arene and non-aromatics raw material that sulphur weight content is less than 200ppm, and alkene or diolefin weight content are less than 20%.
4. the method for volume increase BTX aromatic hydrocarbons according to claim 1, it is characterized in that containing in described catalyzer at least one in metal or the oxide compound that is selected from Cu, Sn, Pb, Zn and Fe, its consumption is counted and is greater than 0 and be less than or equal to 1% with catalyst weight per-cent.
5. the method for volume increase BTX aromatic hydrocarbons according to claim 1, is characterized in that reactor is the fixed bed adiabatic reactor of single hop or multi-stage type.
6. the method for volume increase BTX aromatic hydrocarbons according to claim 1, is characterized in that in fixed-bed reactor charging, and hydrogen dividing potential drop is 0.25 ~ 2.5 MPa, and temperature of reaction is 200 ~ 500 ℃, and liquid phase weight space velocity is 0.1 ~ 10h
-1.
7. the method for volume increase BTX aromatic hydrocarbons according to claim 1, is characterized in that first strand of benzene column overhead accounts for the benzene of 10～90% weight, before sending into fixed-bed reactor, mixes with heavy arene and non-aromatics raw material after purifying treatment; First strand of toluene tower tower top accounts for the toluene of 10～80% weight, before sending into fixed-bed reactor, mixes with heavy arene and non-aromatics raw material after purifying treatment; Carbon nine and above cut that first strand of benzenol hydrorefining tower reactor accounts for 0～70% weight, before sending into fixed-bed reactor, mix with heavy arene and non-aromatics raw material after purifying treatment.
8. the method for volume increase BTX aromatic hydrocarbons according to claim 1, is characterized in that stripping tower top working pressure is 0.0～1.0MPa, and tower top service temperature is 60～200 ℃; Benzene column overhead working pressure is 0.0～0.5MPa, and tower top service temperature is 80～160 ℃.
9. the method for volume increase BTX aromatic hydrocarbons according to claim 1, is characterized in that toluene tower tower top working pressure is 0.0～0.5MPa, and service temperature is 110～200 ℃; Benzenol hydrorefining tower top working pressure is 0～0.5MPa, and service temperature is 140～220 ℃.
10. the method for volume increase BTX aromatic hydrocarbons according to claim 1, is characterized in that in step d), first strand of benzene that accounts for 20～80% weight returns in the fixed-bed reactor in step a), and second strand accounts for the benzene extraction of 20～80% weight; In step e), first strand of toluene that accounts for 25～75% weight returns in the fixed-bed reactor in step a), and second strand accounts for the toluene extraction of 25～75% weight; In step f), first strand of carbon nine and above cut that accounts for 30～70% weight returns in the fixed-bed reactor in step a), and second strand accounts for carbon nine and the above cut extraction of 30～70% weight.
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| CN106345463A (en) * | 2016-08-26 | 2017-01-25 | 山东恒信科技发展有限公司 | Catalyst for heavy aromatics hydrogenation dealkylation |
| CN106573854A (en) * | 2014-08-06 | 2017-04-19 | Bp北美公司 | Heat integration in disproportionation or transalkylation processes |
| CN110642665A (en) * | 2018-06-27 | 2020-01-03 | 中国石油化工股份有限公司 | C9+Process for producing dimethylbenzene from heavy aromatic hydrocarbon |
| WO2022083725A1 (en) * | 2020-10-22 | 2022-04-28 | 中国石油化工股份有限公司 | Gasoline component processing method and system |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104974791A (en) * | 2014-04-07 | 2015-10-14 | Ifp新能源公司 | Process for production of light olefins and btx |
| CN104974791B (en) * | 2014-04-07 | 2018-11-06 | Ifp 新能源公司 | The method for producing light olefin and BTX |
| CN106573854A (en) * | 2014-08-06 | 2017-04-19 | Bp北美公司 | Heat integration in disproportionation or transalkylation processes |
| CN106573854B (en) * | 2014-08-06 | 2019-07-30 | Bp北美公司 | Heat integration in disproportionation or transalkylation process |
| US10472305B2 (en) | 2014-08-06 | 2019-11-12 | Bp Corporation North America Inc. | Heat integration in disproportionation or transalkylation processes |
| CN104357084A (en) * | 2014-11-11 | 2015-02-18 | 中国海洋石油总公司 | Combined process for conversion of C10+ heavy aromatics to light aromatics |
| CN104357084B (en) * | 2014-11-11 | 2016-08-24 | 中国海洋石油总公司 | A kind of C10+heavy aromatics lighting combined technical method |
| CN106345463A (en) * | 2016-08-26 | 2017-01-25 | 山东恒信科技发展有限公司 | Catalyst for heavy aromatics hydrogenation dealkylation |
| CN110642665A (en) * | 2018-06-27 | 2020-01-03 | 中国石油化工股份有限公司 | C9+Process for producing dimethylbenzene from heavy aromatic hydrocarbon |
| CN110642665B (en) * | 2018-06-27 | 2022-07-08 | 中国石油化工股份有限公司 | C9+Process for producing dimethylbenzene from heavy aromatic hydrocarbon |
| WO2022083725A1 (en) * | 2020-10-22 | 2022-04-28 | 中国石油化工股份有限公司 | Gasoline component processing method and system |
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