CN100336790C - Process for preparing p-xylene - Google Patents
Process for preparing p-xylene Download PDFInfo
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- CN100336790C CN100336790C CNB2004100527158A CN200410052715A CN100336790C CN 100336790 C CN100336790 C CN 100336790C CN B2004100527158 A CNB2004100527158 A CN B2004100527158A CN 200410052715 A CN200410052715 A CN 200410052715A CN 100336790 C CN100336790 C CN 100336790C
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- xylol
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- benzene
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- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 238000004519 manufacturing process Methods 0.000 title abstract description 11
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 90
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims abstract description 81
- 238000006243 chemical reaction Methods 0.000 claims abstract description 31
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 29
- 238000010555 transalkylation reaction Methods 0.000 claims abstract description 13
- 229930195733 hydrocarbon Natural products 0.000 claims description 33
- 239000004215 Carbon black (E152) Substances 0.000 claims description 32
- 150000002430 hydrocarbons Chemical class 0.000 claims description 32
- 238000000034 method Methods 0.000 claims description 30
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 26
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims description 25
- 238000000605 extraction Methods 0.000 claims description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 10
- 125000000217 alkyl group Chemical group 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 9
- 239000002808 molecular sieve Substances 0.000 claims description 8
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 8
- 241000282326 Felis catus Species 0.000 claims description 7
- 229910052739 hydrogen Inorganic materials 0.000 claims description 7
- 239000001257 hydrogen Substances 0.000 claims description 7
- 238000006317 isomerization reaction Methods 0.000 claims description 6
- 238000001179 sorption measurement Methods 0.000 claims description 6
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 5
- 229910021536 Zeolite Inorganic materials 0.000 claims description 5
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 5
- 238000005194 fractionation Methods 0.000 claims description 5
- 229910052750 molybdenum Inorganic materials 0.000 claims description 5
- 239000011733 molybdenum Substances 0.000 claims description 5
- 239000010457 zeolite Substances 0.000 claims description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 4
- OKTJSMMVPCPJKN-BJUDXGSMSA-N carbon-11 Chemical compound [11C] OKTJSMMVPCPJKN-BJUDXGSMSA-N 0.000 claims description 3
- 125000000118 dimethyl group Chemical group [H]C([H])([H])* 0.000 claims description 3
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 229910052680 mordenite Inorganic materials 0.000 claims description 2
- 238000012216 screening Methods 0.000 claims 1
- 239000002994 raw material Substances 0.000 abstract description 24
- 239000006227 byproduct Substances 0.000 abstract description 5
- 239000000463 material Substances 0.000 abstract description 4
- 238000009776 industrial production Methods 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 19
- 238000000926 separation method Methods 0.000 description 7
- PQNFLJBBNBOBRQ-UHFFFAOYSA-N indane Chemical compound C1=CC=C2CCCC2=C1 PQNFLJBBNBOBRQ-UHFFFAOYSA-N 0.000 description 6
- 239000008096 xylene Substances 0.000 description 6
- 238000007323 disproportionation reaction Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 125000003118 aryl group Chemical group 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 2
- HUMNYLRZRPPJDN-UHFFFAOYSA-N benzaldehyde Chemical compound O=CC1=CC=CC=C1 HUMNYLRZRPPJDN-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- -1 still Substances 0.000 description 2
- 239000003905 agrochemical Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000006900 dealkylation reaction Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- QNGNSVIICDLXHT-UHFFFAOYSA-N para-ethylbenzaldehyde Natural products CCC1=CC=C(C=O)C=C1 QNGNSVIICDLXHT-UHFFFAOYSA-N 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 230000008707 rearrangement Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The present invention relates to a method for producing p-xylene, which mainly solves problems existing in the prior art that a large quantity of benzene as a byproduct is produced in the production of the p-xylene, and the content of the heavy aromatics of C10 or higher in raw materials is low. The present invention adopts the technical scheme that benzene, toluene and the aromatic hydrocarbon of C9 or higher are used for a transalkylation reaction to produce the material flow of the aromatic hydrocarbon of C8, then the p-xylene is separated, and the unreacted benzene, the unreacted toluene and the unreacted aromatic hydrocarbon of C9A or higher are circulated to the fed material of the reaction. Therefore, the problems in the prior art are solved well, and the present invention can be used for the industrial production of the p-xylene.
Description
Technical field
The present invention relates to be used to produce the method for p-Xylol.Particularly about passing through benzene (Ben), toluene (Tol) and carbon nine and above aromatic hydrocarbons (C thereof
9 +A) aromatic hydrocarbons transalkylation reaction generates C8 aronmatic (C
8A) back obtains the method for p-Xylol.
Background technology
P-Xylol is one of main basic organic of petrochemical industry, in numerous chemical production field such as chemical fibre, synthetic resins, agricultural chemicals, medicine, plastics purposes is widely arranged.Typical p-Xylol (pX) production method is that the dimethylbenzene that contains ethylbenzene of the thermodynamic(al)equilibrium that generates from the petroleum naphtha catalytic reforming is to separate or molecular sieve simulated moving bed adsorption separation (abbreviation fractionation by adsorption) technology by multistage cryogenic crystallization the C8 aronmatic, and p-Xylol is separated from the close with it isomer mixture of boiling point.And, often take C for the processing of the dimethylbenzene of an ortho position and a position
8A isomerization (abbreviation isomerization) technology makes it isomery and turns to p-Xylol.In order to increase production p-Xylol, utilize toluene disproportionation or toluene and carbon nine and above aromatic hydrocarbons (C thereof
9 +A) disproportionation and transalkylation reaction generate benzene and C
8A, thereby volume increase C
8A is the operational path that effectively increases production p-Xylol.
Up to now, in the world more typically, also the technology relevant with toluene disproportionation of comparative maturity has sixties Mo industrialized Tatoray tradition toluene disproportionation process, the MTDP of late nineteen eighties release and S-TDT technology and the TransPlus technology of releasing in recent years.
The reactor feed of typical Tatoray technology is with toluene and C9 aromatic (C
9A) be reaction raw materials, C
10 +The content of hydrocarbon (carbon ten and above hydrocarbon thereof) must strict control.In order to improve the economic benefit of device, cut down the consumption of energy and material consumption, people have carried out further research and optimization to Tatoray technology, mainly be devoted to its core technology---Study of Catalyst, improve the indicators of overall performance of catalyzer, as improving the molecular-weight average of weight space velocity, prolongation catalyst operation and increase aromatic hydrocarbons reaction raw materials.The raising of molecular-weight average helps increasing C
8A, but when the heavy aromatics too high levels, in order to keep certain transformation efficiency, promptly keep catalyst activity must cause the especially aggravation of hydro-dealkylation reaction of side reaction, thereby makes in the reaction product benzaldehyde product on the high side, causes product C
8A/Ben is on the low side, and the aromatic hydrocarbons loss is bigger, handles equal raw material, the C that obtains
8A is on the low side, the Ben amount is on the high side.
Document based on Tatoray technology has USP4341914, Chinese patent 98110859.8, USP2795629, USP3551510, Chinese patent 97106719.8 etc.In US4341914 technology, though with the portion C in the reaction product
10A is with circulation C
9A returns reaction zone (logistics 18), the C that has partly utilized reaction itself to generate
10A comes to generate in the inhibited reaction process more substantial C
10 +Hydrocarbon, still, raw material C
8 +C among the A
10 +Hydrocarbon but can't obtain utilizing, and C
8 +Portion C in the A raw material
9A is with C
10 +Hydrocarbon is discharged out-of-bounds (logistics 19) at heavy aromatics Tata still.Because the restriction of catalyst performance, this technology also has exacting terms in the selection of raw material, require heavy aromatics tower (tower 2) cat head effluent---C
9Indane (IND) content in the A logistics (logistics 7) must be lower than below 1%, thereby has caused aforesaid C
9The loss of A and the C that just partly utilizes reaction self to generate
10A, and raw material C
8 +C among the A
10 +Hydrocarbon but can't obtain utilizing.
In the technical process of Chinese patent 98110859.8,, have high indane content, high C in the raw material of permission though this technology has overcome many drawbacks of above-mentioned patent
10 +Advantages such as hydrocarbon content, but still a large amount of benzene of by-product.
Summary of the invention
Technical problem to be solved by this invention is carbon ten and the low problem of above heavy aromatics content thereof in a large amount of benzene of by-product, the raw material when exist producing p-Xylol in the conventional art, and a kind of new method that is used to produce p-Xylol is provided.This method has that separation process is simple, and plant energy consumption is low, can significantly increase production the characteristics of p-Xylol throughput.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method that is used to produce p-Xylol may further comprise the steps:
A) benzene that out-of-bounds comes, toluene and C
9A and above aromatic hydrocarbons thereof enter the alkyl transfering process unit that contains the molybdenum molecular sieve catalyst, carry out the aromatic hydrocarbons transalkylation reaction under hydro condition, and the reaction back generates to contain mixes the dimethylbenzene logistics;
B) the mixing dimethylbenzene logistics that contains that reaction generates goes the fractionation by adsorption isomerization unit to produce p-Xylol, unreacted benzene, toluene and C
9A and above aromatic hydrocarbons thereof are circulated in the alkyl transfering process unit feed;
Wherein said fractionation by adsorption isomerization unit comprises the benzenol hydrorefining and the deheptanizer of separating mixed dimethyl logistics.
Molecular sieve preferred version in the technique scheme in the employed molecular sieve catalyst is selected from mordenite, β zeolite or omega zeolite; The unitary operational condition of alkyl transfering process: reaction pressure is 1～4MPa, and temperature of reaction is 300～480 ℃, and hydrogen/hydrocarbon mol ratio is 0.5～10, and weight space velocity is 0.8～8 hour
-1In the separation process of xylol logistics, the isolating C of deheptanizer cat head
7And following hydrocarbon is circulated in the alkyl transfering process unit feed tower still C
8And above aromatic hydrocarbons enters benzenol hydrorefining.The benzenol hydrorefining of separating mixed dimethyl logistics, its cat head extraction C8 aronmatic logistics, carbon nine and C10 aromartic logistics are rich in the line extraction of tower bottom side, extraction of tower still or not extraction carbon 11 and above hydrocarbon (C thereof
11 +Hydrocarbon).
Dimethylbenzene Tata still produced quantity described in the such scheme is means of control technique unit raw material molecular-weight average of the present invention.In the normal running, not extraction of tower still C
11 +Hydrocarbon is to increase production more pX (p-Xylol); Have only when catalyzer be in the latter stage in operational cycle and be difficult to synchronous situation of factory's turnaround under, can be by the extraction portion C
11 +Hydrocarbon reducing the raw material molecular-weight average of this technique unit, thereby reduces the severity of reaction, makes this unitary operation not influence the turnaround plans of factory.
As can be seen, such operational path makes the aromatic hydrocarbons of carbon more than six all be transformed into the Mixed XYLENE of high added value, has simplified separation process effectively, has fully reduced the energy consumption material consumption of aromatic device.
Principal reaction involved in the technology of the present invention comprises:
In technology of the present invention, the aromatic hydrocarbons transalkylation reaction is different with traditional transalkylation notion, and it is with benzene, toluene and carbon nine and above aromatic hydrocarbons (C thereof
9 +A) be raw material, reaction generates C
8A.Because benzene and heavy aromatics be also as producing the raw material of Mixed XYLENE, thereby under the constant situation of reformation scale, just can improve the throughput of p-Xylol significantly.Therefore in the inventive method with benzene, toluene and C
9 +A is that raw material is produced p-Xylol, because in the technology of the present invention, benzene and C
10And above aromatic hydrocarbons need not be separated from reaction effluent, thereby simplified separation process significantly, can save the necessary stripping tower of typical Tatoray technology separating reaction effluent, benzene tower and heavy aromatics tower, only need to make toluene tower into deheptanizer, and the reservation benzenol hydrorefining gets final product.Five original tower separation systems are simplified to two tower separation systems, therefore, have reduced the energy consumption of device significantly, reduced production cost effectively.Simultaneously because benzene and all C
10And above heavy aromatics can be used as reaction raw materials, for Aromatic Hydrocarbon United Plant, under the constant situation of rearrangement capability, just can increase production p-Xylol throughput significantly, obtained better technical effect.
Description of drawings
Fig. 1 is the technical process of US4341914.
Fig. 2 is the technical process of Chinese patent 98110859.8.
Fig. 3 is used to produce the alkyl transfering process flow process of p-Xylol for the present invention.
Among Fig. 1,1 is benzenol hydrorefining I, and 2 is the heavy aromatics tower, and 3 is reaction zone, and 4 is the benzene tower, and 5 is toluene tower, and 6 is benzenol hydrorefining II, and 7 is C
9A, 8 is C
8 +The A raw material, 9 and 10 is toluene, and 11 is benzene, and 12 and 13 is C
8A, 17 and 19 for being rich in C
10 +Hydrocarbon stream, 18 for being rich in C
9The A logistics.
1 is benzenol hydrorefining I among Fig. 2, and 2 is the heavy aromatics tower, and 3 is reaction zone, and 4 is the benzene tower, and 5 is toluene tower, and 6 is benzenol hydrorefining II, and 7 is ortho-xylene column, and 8 is C
8 +The A raw material, 9 is fresh toluene, 12 and 13 is C
8A, 14 for being rich in C
9The A logistics, 15 is carbon 11 and above hydrocarbon (C thereof
11 +Hydrocarbon), 16 are circulation toluene, and 17 is benzene, and 19 is o-Xylol, and 20 for containing or do not contain the C of o-Xylol
9 +A.This technology has overcome many drawbacks of above-mentioned patent, has high indane content, high C in the raw material of permission
10 +Advantages such as hydrocarbon content, but still a large amount of benzene of by-product.
1 is the raw hydrogen, benzene, toluene and the C that out-of-bounds come among Fig. 3
9And above aromatic hydrocarbons, 2 aromatic hydrocarbons transalkylation reaction of the present invention unit, 3 is deheptanizer, and 4 is benzenol hydrorefining, and 5 is round-robin C
7And following hydrocarbon, 6 is C
8And above hydrocarbon, 7 are the product Mixed XYLENE of technology of the present invention, i.e. C
8Aromatic hydrocarbons, 8 is C
9And above aromatic hydrocarbons, 9 is C
11And above aromatic hydrocarbons.From benzene, toluene and the C that out-of-bounds comes
9And isolated C in above aromatic hydrocarbons 1 and the reaction effluent
7And following hydrocarbon and C
9And above hydrocarbon and hydrogen enters aromatic hydrocarbons transalkylation reaction of the present invention unit 2 after mixing and carries out the aromatic hydrocarbons transalkylation reaction, generates Mixed XYLENE, and reaction effluent separates through deheptanizer, the isolated C of cat head
7And following hydrocarbon 5 is circulated in the reaction feed, and extraction is rich in C at the bottom of the tower
8 +Benzenol hydrorefining 4 is advanced in A logistics 6, the Mixed XYLENE logistics 7 of cat head extraction, and C is rich in the line extraction of tower bottom side
9A logistics 8 is circulated in the reaction feed, tower still C
11 +Hydrocarbon 9 is by extraction or not extraction.
The invention will be further elaborated below by embodiment.
Embodiment
[embodiment 1～7]
Under the hydro condition, in fixed-bed reactor, carry out benzene, toluene and C
9 +A transalkylation reaction performance is investigated.25 millimeters of reactor inside diameter φ, 1000 millimeters of length, stainless steel.The equal up and down 3 millimeters granulated glass spherees of filling φ of beds play air-flow and distribute and supporting role, and filling 20 grams contain the molecular sieve catalyst of molybdenum 4% weight in the reactor.Aroamtic hydrocarbon raw material with after hydrogen mixes from top to bottom by beds, carry out benzene, toluene and C
9 +The transalkylation reaction of A generates C
8A, i.e. Mixed XYLENE.
Benzene feedstock, toluene and C
9 +A derives from petrochemical complex Aromatic Hydrocarbon United Plant, H
2Be electrolysis hydrogen, through dehydrating processing, reaction result is listed in the table 1.
Table 1 benzene, toluene and C9 aromatic transalkylation reaction raw material and product compositional analysis (1～7)
| | 1 | 2 | 3 | 4 | 5 | 6 | 7 | |
| The molecular sieve temperature of reaction, ℃ reaction pressure, the MPa weight space velocity, hour -1Hydrogen hydrocarbon mol ratio | A 325 1.5 0.8 3 | B 345 1.5 1.3 2 | B 400 4 4.5 8.5 | A 420 4 6 10 | A 430 4 6 4 | A 390 2.5 3.5 5 | B 450 4 8 8.5 | |
| Reaction raw materials is formed weight % | NA Ben Tol C 8A C 9A IND C 10 +The hydrocarbon ∑ | 0.01 73.98 0.01 0.06 19.13 0.61 6.20 100.00 | 0.01 39.00 35.00 0.06 19.13 0.61 6.19 100.00 | 0.10 19.00 55.00 0.06 19.13 0.61 6.10 100.00 | 0.1 14.07 60 0.09 19.03 0.61 6.10 100 | 0.16 12.49 61.52 0.09 19.03 0.61 6.10 100.00 | 0.01 50.91 0.01 0.26 34.22 1.56 13.03 100.00 | 0.10 19.10 32.13 0.06 34.26 1.31 13.03 99.99 |
| Reaction product is formed weight % | NA Ben Tol C 8A C 9A C 10 +The hydrocarbon ∑ | 2.51 49.57 25.72 13.11 5.86 3.23 100.00 | 4.01 29.71 30.00 26.59 6.06 3.62 99.99 | 5.51 16.48 32.90 33.60 7.21 4.31 100.01 | 5.34 13.02 34.9 33.7 8.03 5.01 100 | 5.39 12.57 35.12 33.60 8.13 5.20 100.01 | 6.09 30.52 29.05 17.43 9.57 7.34 100.00 | 6.51 16.48 22.90 42.60 7.21 4.31 100.01 |
Annotate: the A representative contains the molybdenum filament geolyte; The B representative contains molybdenum β zeolite; NA is a non-aromatics, C
10 +Hydrocarbon is carbon ten and above hydrocarbon thereof.
From embodiment 1～7 as can be seen: benzene, toluene and C the raw material
9A and C
10 +After reacting, generated C
8A.
By as seen above-mentioned, problems such as carbon ten and above heavy aromatics content thereof is low in a large amount of benzene of by-product, raw material when patent of the present invention has overcome the production p-Xylol that exists in the conventional art, the method that provides a kind of brand-new more economical being used to produce p-Xylol.
Claims (5)
1, a kind of method that is used to produce p-Xylol may further comprise the steps:
A) benzene that out-of-bounds comes, toluene and C
9A and above aromatic hydrocarbons thereof enter the alkyl transfering process unit that contains the molybdenum molecular sieve catalyst, carry out the aromatic hydrocarbons transalkylation reaction under hydro condition, and the reaction back generates to contain mixes the dimethylbenzene logistics;
B) the mixing dimethylbenzene logistics that contains that reaction generates goes the fractionation by adsorption isomerization unit to produce p-Xylol, unreacted benzene, toluene and C
9A and above aromatic hydrocarbons thereof are circulated in the alkyl transfering process unit feed;
Wherein said fractionation by adsorption isomerization unit comprises the benzenol hydrorefining and the deheptanizer of separating mixed dimethyl logistics.
2, according to the described method that is used to produce p-Xylol of claim 1, it is characterized in that the logistics of described benzenol hydrorefining cat head extraction C8 aronmatic, carbon nine and C10 aromartic logistics are rich in the line extraction of tower bottom side, extraction of tower still or not extraction carbon 11 and above hydrocarbon thereof.
3, according to the described method that is used to produce p-Xylol of claim 1, it is characterized in that the unitary operational condition of alkyl transfering process: reaction pressure is 1～4MPa, temperature of reaction is 300～480 ℃, and hydrogen/hydrocarbon mol ratio is 0.5～10, and weight space velocity is 0.8～8 hour
-1
4,, it is characterized in that the isolating C of described deheptanizer cat head according to the described method that is used to produce p-Xylol of claim 1
7And following hydrocarbon is circulated in the alkyl transfering process unit feed tower still C
8And above aromatic hydrocarbons enters benzenol hydrorefining.
5,, it is characterized in that molecular screening in the employed molecular sieve catalyst is from mordenite, β zeolite or omega zeolite according to the described method that is used to produce p-Xylol of claim 1.
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| CNB2004100527158A CN100336790C (en) | 2004-07-12 | 2004-07-12 | Process for preparing p-xylene |
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|---|---|---|---|
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| CN102190553B (en) * | 2010-03-03 | 2014-03-26 | 中国石油化工股份有限公司 | Aromatic hydrocarbon alkyl transfer method for producing benzene and p-xylene |
| CN104109074B (en) * | 2013-04-16 | 2016-08-24 | 中国石油化工股份有限公司 | The combine production method of xylol |
| CN105130728B (en) * | 2015-08-21 | 2018-06-29 | 中石化炼化工程（集团）股份有限公司 | A kind of method and device that dimethylbenzene is prepared using methanol |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1441759A (en) * | 2000-07-10 | 2003-09-10 | Bp北美公司 | Pressure swing adsorption process for separating para-xylene and ethylbenzene from mixed C8 |
| CN1443736A (en) * | 2002-03-13 | 2003-09-24 | 中国石油化工股份有限公司 | Benzene and C9 and more than that arene transalkylation method |
| CN1123629C (en) * | 2000-11-15 | 2003-10-08 | 中国石油化工股份有限公司 | Disproportionation and transalkylation process of toluene and C9 and heavier aromatic hydrocarbons |
-
2004
- 2004-07-12 CN CNB2004100527158A patent/CN100336790C/en not_active Expired - Lifetime
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1441759A (en) * | 2000-07-10 | 2003-09-10 | Bp北美公司 | Pressure swing adsorption process for separating para-xylene and ethylbenzene from mixed C8 |
| CN1123629C (en) * | 2000-11-15 | 2003-10-08 | 中国石油化工股份有限公司 | Disproportionation and transalkylation process of toluene and C9 and heavier aromatic hydrocarbons |
| CN1443736A (en) * | 2002-03-13 | 2003-09-24 | 中国石油化工股份有限公司 | Benzene and C9 and more than that arene transalkylation method |
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