CN1067040C - Toluene disproportionation and alkyl transfering process - Google Patents
Toluene disproportionation and alkyl transfering process Download PDFInfo
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- CN1067040C CN1067040C CN97106716A CN97106716A CN1067040C CN 1067040 C CN1067040 C CN 1067040C CN 97106716 A CN97106716 A CN 97106716A CN 97106716 A CN97106716 A CN 97106716A CN 1067040 C CN1067040 C CN 1067040C
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- toluene
- aromatic hydrocarbons
- toluene disproportionation
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- disproportionation
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Abstract
The present invention relates to a process for producing benzene and C8 arene by using methylbenzene, C9 arene and C10 arene through methylbenzene disproportionation and an alkyl transfer reaction. Under the condition of hydroforming, the reactions are carried out on a zeolite catalyst containing bismuth oxide, and the reaction distillate is a mixture of C6 to C10 arene and paraffin below C5. After the separation of the distillate, benzene and C8 A are discharged, the methylbenzene is cycled, and a C9 A material flow and heavy aromatic overhead liquor are converged and enter a reaction zone. The present invention has the characteristics of no loss of the C9 A raw material, high allowable indane content of the technology, and high C10 A utilization rate; the present invention can be used for industrial production.
Description
The present invention relates to toluene disproportionation and alkyl transfering process, specifically relate to toluene disproportionation and toluene and C
9Or above aromatic hydrocarbons alkyl transfering process.
In petroleum cuts reformation and cracking process, can obtain a large amount of benzene,toluene,xylenes and C
9Aroamtic hydrocarbon raw materials such as A.According to different boiling ranges petroleum cuts and working method, toluene and C
9A (C
9Aromatic hydrocarbons) content generally accounts for 40～50% of aromatic hydrocarbons gross weight.
In recent years, because the development of plastics, synthon and China Synthetic Rubber Industry, very fast to the demand growth of benzene and dimethylbenzene, its commercially available price is also than toluene and C
9A is much higher.In order to make full use of aromatic hydrocarbon resource, adopt the aromatic hydrocarbons of low value to increase production benzene and dimethylbenzene with higher utility value.Up to the present, a lot of countries are arranged to using toluene and C
9A produces benzene and dimethylbenzene has carried out number of research projects, and has obtained certain achievement.
Usually this technology is under hydro condition, with toluene and C
9A is a raw material, uses fixed-bed reactor, and reaction generates C in the presence of mordenite catalyst
6～C
10Aromatic hydrocarbons and C
1～C
5Alkane and a small amount of C
11Hydrocarbon.Toluene in the reaction effluent and C
9A circulates fresh toluene and the fresh C external with the battery limit (BL) after separating
9A converges as reactor feed.Owing to be subjected to the restriction of catalyst performance, the C of device own
10A (C
10Aromatic hydrocarbons) do not circulate, discharge out-of-bounds by the tower still, and the fresh C that out-of-bounds comes
9Strict control IND (indane) content wherein is lower than 0.3% to guarantee the IND content in the reactor aromatic feed among the A.Because boiling point and the C of IND
9The boiling point of the trimethylbenzene among the A (TMB) is very approaching, provides the disproportionation device fresh C
9The C of the heavy aromatics column overhead of A
9The content of IND need be lower than 1.0% usually among the A, could satisfy this processing requirement, has so just caused about 5～15% C
9A discharges at the bottom of the heavy aromatics Tata and can not make full use of.
Transalkylation catalyst, reaction mass composition and reaction conditions have been described among the USP2795629,3551510,3701813 and 3729521.The catalyzer patent that is used for alkyl transfering process has USP2795629,3780122 and 3849340.In fact above patent can not make full use of C owing to be subjected to the influence of catalyst performance
9A and above aromatic hydrocarbons, the yield of purpose product is all lower, and its material consumption, energy consumption are very big on the industrial application device, and economic and technical norms are uneconomical.
The exploitation of a petrochemical process and to improve be because succeeding in developing with improving constantly of its performance of associated catalysts promotes after all.Improve disproportionation device processing toluene and C in order to adapt to
9The ability of A, reduce device energy consumption and material consumption, reach the working condition requirement of scale economics, developed the catalyst for toluene disproportionation and transalkylation of high-speed high conversion both at home and abroad in succession about company and unit.But along with the raising of catalyzer transformation efficiency, the C of generation
10The amount of above heavy aromatics is also higher, thereby has caused the decline of purpose selectivity of product.
USP4341914 has at first proposed to use C on the basis of above-mentioned technology
10A round-robin alkyl transfering process suppresses C
10The generation of hydrocarbon, thus purpose product benzene and C improved
8The selectivity of A, its technical process as shown in Figure 1.
Fig. 1 is for carrying out C
10A round-robin process flow diagram.
1 is benzenol hydrorefining among Fig. 1, and 2 is the heavy aromatics tower, and 3 is toluene disproportionation and transalkylation reaction zone, and 4 is the benzene tower, and 5 is toluene tower, and 6 is benzenol hydrorefining, and 8 for being rich in C
8A (C
8Aromatic hydrocarbons) raw material charging, 9 is the fresh feed toluene feed, and 10 are circulation toluene, and 11 is the benzene discharging, and 12 is C
8The A discharging.
In fact above-mentioned technology go out first Disengagement zone, and reaction zone and second Disengagement zone form. First Disengagement zone comprises benzenol hydrorefining 1 and 2 liang of Tower Systems of heavy aromatics tower; Reaction zone comprises reactor, high pressure knockout drum and stripper; Second Disengagement zone is made up of benzene tower 4, toluene tower 5 and benzenol hydrorefining 6 three towers. Its characteristics are: (1) can carry out part and all circulations of product benzene, improves C8The productive rate of A; (2) utilize C10The circulation of A improves C8The productive rate of A. Yet, when after the circulation of carrying out benzene with the decrease reaction raw materials in the conversion ratio of toluene, thereby make above-mentioned technology only be suitable for high C9The reaction raw materials of A concentration (〉=50%). Generally, C in the reaction raw materials9The concentration of A is the concentration that is lower than toluene, and therefore, the circulation of benzene should not be adopted for most factories. In addition, owing to be subjected to the restriction of catalyst service condition, must strict control raw material C8Indane among the A is brought reactor into, namely must the strict control first fractionation zone heavy aromatics tower 2 cat head C9Indane content＜1% among the A, thus with the indane more than 50% from its tower reactor with C10Hydrocarbon is discharged out-of-bounds, because indane and C9The boiling point of TMB among the A (trimethylbenzene) is very approaching, can cause 5～15% C in control heavy aromatics column overhead indane content9A is with C10Hydrocarbon is discharged out-of-bounds from tower reactor. Therefore, this technology has just partly been utilized the C that transalkylation itself generates10Hydrocarbon, and raw material C8C among the A10Hydrocarbon can't obtain utilizing, and C8Part C in the A raw material9A is with C10Hydrocarbon is discharged out-of-bounds.
The objective of the invention is the strict demand C that exists in the above-mentioned document in order to overcome
9Indane content can not surpass 1% in the charging of A raw material, need lose 5～15% C for separating indane
9A raw material, and C
10Hydrocarbon also can not get the shortcoming than good utilisation, and a kind of toluene disproportionation and transalkylation novel process are provided, and this technology has permission indane content height in the raw material charging, C
9The free of losses of A raw material, C
10The characteristics that the A raw material availability is high.
The objective of the invention is to realize: a kind of toluene disproportionation and alkyl transfering process by following technical scheme.May further comprise the steps:
A) contain indane, C
8, C
9, C
10And C
11Aroamtic hydrocarbon raw material separates in first disengaging zone of being made up of first, second two knockout towers earlier, isolates C at the first knockout tower cat head
8Aromatic hydrocarbons material, tower still material enter second knockout tower to be separated, and the second knockout tower cat head is isolated indane, C
9And C
10Aromatic hydrocarbons, wherein indane is 0～5% by weight percentage, C
10Aromatic hydrocarbons is 0～50%, and the tower still is discharged C
11Aromatic hydrocarbons;
B) the above-mentioned second knockout tower cat head material and toluene material being entered with the bismuth oxide zeolite is the toluene disproportionation and the transalkylation reaction zone of catalyzer, generates under alkylation conditions and is rich in C
6And C
8The toluene disproportionation of aromatic hydrocarbons and transalkylation reaction zone logistics;
C) above-mentioned toluene disproportionation is separated in second disengaging zone with the transalkylation reaction zone logistics, isolates C
6Aromatic hydrocarbons, toluene, do not contain the C of o-Xylol
8Aromatic hydrocarbons and contain C
10The heavy aromatics of aromatic hydrocarbons.
In the technique scheme, the isolated toluene in second disengaging zone is capable of circulation as the charging of reaction zone raw material, and isolated benzene also can partly loop back reaction zone, is beneficial to improve C
8The productive rate of A, but because can reduce the transformation efficiency of toluene in the reaction raw materials simultaneously, therefore also can not circulate, directly as product, discharge out-of-bounds; The isolated C that contains
10The heavy aromatics of aromatic hydrocarbons can be isolated second knockout tower that enters first disengaging zone behind the o-Xylol more earlier, perhaps without separating second knockout tower that directly enters first disengaging zone.In the raw material that enters toluene disproportionation and transalkylation reaction zone, toluene and C
9The part by weight of A aromatic hydrocarbons is 90/10～10/90, and the used zeolite of reaction zone is mordenite, ZSM-5 zeolite or β zeolite, and its preferred version is a mordenite.
Key of the present invention has been to use the zeolite catalyst of bismuth oxide, make the reactivity worth of catalyzer improve greatly, reduced the restriction of catalyzer, made the content of indane in the raw material allow to reach 0～5% (weight), therefore at C indane content in the reaction raw materials
8Bring a small amount of indane that comes in the A raw material into and just need not its major part to be removed C when so also just having avoided the separation indane by the heavy aromatics tower
9The loss of A raw material.Same because used the zeolite catalyst of bismuth oxide, make this catalyzer have C simultaneously
10The function of aromatic hydrogenation dealkylation, thereby C
10Aromatic hydrocarbons itself just can be used as raw material and circulates, and need not from heavy aromatics tower still to discharge out-of-bounds, has improved C
10The utilization ratio of A has obtained effect preferably.
Fig. 2 is toluene disproportionation of the present invention and alkyl transfering process schematic diagram.
This technology comprises that equally first Disengagement zone, second Disengagement zone and toluene disproportionation and transalkylation reaction zone 3 three parts form among Fig. 2. First Disengagement zone is made up of benzenol hydrorefining 1 and heavy aromatics tower 2. Second Disengagement zone is made up of benzene tower 4, toluene tower 5 and benzenol hydrorefining 6 and/or ortho-xylene column 7. Reaction zone comprises reactor, high pressure knockout drum and stripper. The effluent of reaction zone (contains C6～C
10Aromatic hydrocarbons, and C11Hydrocarbon) at first enters benzene tower 4, the benzaldehyde product of isolating benzene 11 drains into out-of-bounds or partly is recycled into reaction zone, the tower bottoms of benzene tower 4 enters toluene tower 5, as the reaction zone toluene feed, the tower bottoms of toluene tower 5 enters in the benzenol hydrorefining 6 the toluene cycle stock 10 that cat head is extracted after fresh toluene material 9 converges. Extract the cat head C of ethylbenzene, meta-xylene, paraxylene mixture 13 and benzenol hydrorefining 1 in this column overhead8A liquid 12 converges rear discharge out-of-bounds. The still liquid of benzenol hydrorefining 6 can (be rich in C with the tower bottoms of benzenol hydrorefining 19A, indane) enter together heavy aromatics tower 2 after converging, perhaps after isolating ortho-xylene material 14, ortho-xylene column 7 converges with the tower bottoms of benzenol hydrorefining 1 more earlier, enter together then heavy aromatics tower 2. In the heavy aromatics tower; Cat head is extracted and is contained C9A、C
10The feed liquid 15 of hydrocarbon and whole indanes is as reaction zone feeds, and tower bottoms is for being rich in C11Hydrocarbon stream 16 is discharged out-of-bounds. C in the clean liquid of this technology heavy aromatics column overhead10Hydrocarbon comprises C10A、C
10Cyclic hydrocarbon and C10Hydrocarbon with condensed rings.
The present invention is further elaborated below by embodiment.[embodiment 1～4]
Carry out toluene and be rich in C with fixed-bed reactor
9The disproportionation of the raw material of A and transalkylation reaction performance are investigated, reactor inside diameter φ 25mm, length 1000mm, stainless steel.The equal up and down filling φ 3mm granulated glass sphere of beds plays air-flow and distributes and supporting role the mordenite catalyst of filling 20g bismuth oxide-containing in the reactor.Aroamtic hydrocarbon raw material (toluene and C
9A) with after hydrogen mixes pass through beds from top to bottom, toluene disproportionation and transalkylation reaction take place, generate benzene and C
8A, and a spot of C
5Following non-aromatics and C
10Hydrocarbon.
Raw material toluene and C
9A derives from petrochemical complex Aromatic Hydrocarbon United Plant, H
2Be electrolysis hydrogen, through dehydrating processing, reaction result is listed in the table 1.
The data processing calculation formula is as follows:
Table 1 toluene be rich in C
9The raw material reaction result of A
* annotate: liquid yield is meant the weight (gram) of the reaction liquid product that every gram reaction raw materials obtains after reaction.
| | 1 | 2 | 3 | 4 |
| Temperature of reaction, ℃ reaction pressure, MPa WHSV, hr -1Hydrogen hydrocarbon mol ratio | 300 2.0 0.8 1 | 380 3.0 2.0 - 5 | 420 3.0 3.0 10 | 480 4.0 4.5 15 |
| Raw material is formed, %:C 1～C 5Non-aromatics benzene toluene C 8A C 9Non-aromatics C 9A C 10The hydrocarbon indane | / 0.27 90.30 1.31 / 5.41 2.51 0.20 | / / 58.30 1.10 1.00 35.02 3.50 1.08 | / / 40.30 0.70 1.07 49.80 5.90 2.23 | / / 10.50 0.50 1.10 70.40 13.50 4.00 |
| The reaction liquid product is formed, %:C 1～C 5Non-aromatics benzene toluene ethylbenzene paraxylene meta-xylene ortho-xylene ∑ C8A C 9Non-aromatics C 9A indane C 10 +Hydrocarbon | 0.52 17.42 52.37 1.21 5.58 12.33 5.05 24.17 2.51 / 2.92 | 1.04 9.26 52.37 1.86 7.76 17.15 7.03 33.80 0.11 14.56 0.05 4.26 | 1.20 9.26 36.92 1.74 7.55 16.68 6.83 32.80 0.12 20.51 0.05 8.66 | 1.33 3.26 20.24 1.47 6.80 15.02 6.15 29.44 0.12 34.02 0.05 11.54 |
| Liquid yield *, (weight) | 0.9657 | 0.9616 | 0.9585 | 0.9550 |
According to data and the product liquid weight of table 1 embodiment 2, the reaction result that calculates embodiment 2 is:
Toluene conversion: 39.10%
C
9A transformation efficiency: 60.02%
Indane transformation efficiency: 95.55%
C
9Non-aromatics transformation efficiency: 89.42%
Generate benzene selective: 20.32%
Generate C
8A selectivity: 74.63%
The purity of o-Xylol: 98.46%
From table 1 data as can be seen, because the change of raw material proportion of composing and the variation of reaction conditions, the ratio of each material is not quite similar in the reaction product, but reaction back benzene amount and C
8The A amount all significantly increases, and shows that reaction has generated benzene and C
8A.From the calculation result of table 1 data and embodiment 2, the C of the higher concentration of bringing in the raw material
9Non-aromatics and indane its concentration after reacting reduces significantly, illustrates that the used catalyzer of the present invention has good conversion C
9The ability of non-aromatics and indane.Therefore the production of o-Xylol is arranged on the separation process of reaction effluent of toluene disproportionation and transalkylation and can produces high-quality o-Xylol (purity 〉=98% weight).From embodiment, as can be seen, allow the indane of high density and the C of high density in the reaction raw materials
10Hydrocarbon exists, thereby has guaranteed can extract all C in the heavy aromatics column overhead in industrial production
9A, indane and part even whole C
10Hydrocarbon has made full use of C
9The A resource.Simultaneously owing to C in the raw material
10The existence of hydrocarbon can suppress C to a certain extent
9The disproportionation reaction of A, thus C impelled
9A and toluene carry out transalkylation and generate C
8A has improved C
8The selectivity of A.
Therefore technology of the present invention can be produced highly purified o-Xylol product, consumes identical reaction raw materials, and the present invention can produce more C
8A.
Claims (4)
1, a kind of toluene disproportionation and alkyl transfering process may further comprise the steps:
A) contain indane, C
8, C
9, C
10And C
11Aroamtic hydrocarbon raw material separates in first disengaging zone of being made up of first, second two knockout towers earlier, isolates C at the first knockout tower cat head
8Aromatic hydrocarbons material, tower still material enter second knockout tower to be separated, and the second knockout tower cat head is isolated indane, C
9And C
10Aromatic hydrocarbons, wherein indane is 0～5% by weight percentage, C
10Aromatic hydrocarbons is 0～50%, and the tower still is discharged C
11Aromatic hydrocarbons;
B) the above-mentioned second knockout tower cat head material and toluene material being entered with the mordenite of bismuth oxide-containing is the toluene disproportionation and the transalkylation reaction zone of catalyzer, generates under alkylation conditions and is rich in C
6And C
8The toluene disproportionation of aromatic hydrocarbons and transalkylation reaction zone logistics;
C) above-mentioned toluene disproportionation is separated in second disengaging zone with the transalkylation reaction zone logistics, isolates C
6Aromatic hydrocarbons, toluene, do not contain the C of o-Xylol
8Aromatic hydrocarbons and contain C
10The heavy aromatics of aromatic hydrocarbons wherein contains C
10The heavy aromatics of aromatic hydrocarbons enters second knockout tower of first disengaging zone.
2,, it is characterized in that the raw material charging of the isolated toluene circulation in second disengaging zone as toluene disproportionation and transalkylation reaction zone according to described toluene disproportionation of claim 1 and alkyl transfering process.
3, according to described toluene disproportionation of claim 1 and alkyl transfering process, it is characterized in that containing C
10The heavy aromatics of aromatic hydrocarbons can be isolated second knockout tower that enters first disengaging zone behind the o-Xylol more earlier.
4,, it is characterized in that in the raw material of toluene disproportionation and transalkylation reaction zone toluene and C according to described toluene disproportionation of claim 1 and alkyl transfering process
9The part by weight of aromatic hydrocarbons is 90/10～10/90.
Priority Applications (7)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97106716A CN1067040C (en) | 1997-11-13 | 1997-11-13 | Toluene disproportionation and alkyl transfering process |
| TW087108671A TW482751B (en) | 1997-06-06 | 1998-06-02 | Catalysts and processes for the conversion of aromatic hydrocarbons and uses thereof in the production of aromatic hydrocarbons |
| JP15498298A JP3988847B2 (en) | 1997-06-06 | 1998-06-03 | Catalysts and processes for the conversion of aromatic hydrocarbons and their use in the production of aromatic hydrocarbons |
| KR10-1998-0020839A KR100517593B1 (en) | 1997-06-06 | 1998-06-05 | Catalysts and methods for the conversion of aromatic hydrocarbons and their use in the production of aromatic hydrocarbons |
| US09/090,917 US6500997B2 (en) | 1997-06-06 | 1998-06-05 | Catalysts and processes for the conversion of aromatic hydrocarbons and uses thereof in the production of aromatic hydrocarbons |
| EP98110398A EP0884103B1 (en) | 1997-06-06 | 1998-06-06 | Catalyst based on high-silica zeolite and bismuth and its use for the conversion of aromatic hydrocarbons |
| DE69819816T DE69819816T2 (en) | 1997-06-06 | 1998-06-06 | Catalyst based on bismuth and silica-rich zeolite and its use in the conversion of aromatic hydrocarbons |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97106716A CN1067040C (en) | 1997-11-13 | 1997-11-13 | Toluene disproportionation and alkyl transfering process |
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| Publication Number | Publication Date |
|---|---|
| CN1217312A CN1217312A (en) | 1999-05-26 |
| CN1067040C true CN1067040C (en) | 2001-06-13 |
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ID=5168932
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97106716A Expired - Lifetime CN1067040C (en) | 1997-06-06 | 1997-11-13 | Toluene disproportionation and alkyl transfering process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1067040C (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1323058C (en) * | 2004-04-29 | 2007-06-27 | 中国石油化工股份有限公司 | Improved toluene disproportionation process |
| CN114436736B (en) * | 2020-10-19 | 2024-01-26 | 中国石油化工股份有限公司 | Catalytic reaction system for heavy aromatics conversion and method for catalyzing heavy aromatics conversion |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4275256A (en) * | 1980-02-25 | 1981-06-23 | Mobil Oil Corporation | Shape selective reactions with group VIIA metal modified zeolite catalysts |
| CN1044052A (en) * | 1988-12-22 | 1990-07-25 | 帝国化学工业公司 | Utilize the catalyzed reaction of zeolite |
| US5030787A (en) * | 1990-01-24 | 1991-07-09 | Mobil Oil Corp. | Catalytic disproportionation/transalkylation utilizing a C9+ aromatics feed |
-
1997
- 1997-11-13 CN CN97106716A patent/CN1067040C/en not_active Expired - Lifetime
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4275256A (en) * | 1980-02-25 | 1981-06-23 | Mobil Oil Corporation | Shape selective reactions with group VIIA metal modified zeolite catalysts |
| CN1044052A (en) * | 1988-12-22 | 1990-07-25 | 帝国化学工业公司 | Utilize the catalyzed reaction of zeolite |
| US5030787A (en) * | 1990-01-24 | 1991-07-09 | Mobil Oil Corp. | Catalytic disproportionation/transalkylation utilizing a C9+ aromatics feed |
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|---|---|
| CN1217312A (en) | 1999-05-26 |
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