前苏联专利SU890971A3 Method of producing xylene isomers

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专利摘要:
Mixtures of C8 aromatic hydrocarbons are contacted in liquid phase with acid zeolite ZSM-5, zeolite ZSM-12 or ZSM-21. The xylene content is thereby isomerized and the ethyl benzene content of the charge is converted in a manner which facilitates separation of the conversion products from the stream of isomerization products.
公开号:SU890971A3
申请号:SU742049507
申请日:1974-07-24
公开日:1981-12-15
发明作者:Отто Хааг Вернер；Гарольд Ольсон Дэвид
申请人:Мобил Ойл Корпорейшн (Фирма)；
IPC主号:

专利说明:

(54) METHOD OBTAINED BY ISOMERS BY XYL

It is related to methods for producing xylene isomers and can be used in the petrochemical industry.
Xylenes are contained in fractions 5 of distillate of coal tar, oil reforming products and fusible pyrolysis products in a mixture with other hydrocarbons having a close boiling point. Aromatic components 10 are easily separated from non-aromatic, for example, by solvent extraction. As a result of distillation, a fraction containing mainly C-aromatic hydrocarbons is obtained. It is possible to separate 0-Xi-18 LOL from other S-aromatic hydrocarbons by fractionated distillation, p-xylene by fractional or fractional crystallization.20
Typically, p-xylene is obtained from mixtures of C-aromatic compounds Cg, derived from raw materials such as naphtha, in particular from reforming products, usually by extraction method 25
solvents. In tab. 1 shows the characteristic of Cg-aromatic hydrocarbons contained in such mixtures.
Table
136,170,8676
Ethylbenzene-95
138,330,8626
p-Xylene13.28
139,10,8645
m-xylene-47.95
144,440,8824
o-Xylene-25,16
The main sources of C-aromatic carbonaceous hydrocarbons are fractions resulting from the reforming of naphtha and the distillation of the pyrolysis process. Aromatic hydrocarbons: derived from these fractions, 3 widely differ in composition and usually contain 10-32 wt.% Ethylbenzene, the rest is xylenes: up to about 50 wt.% Meta-, 25 wt.% Para- and orthoxylene. xylene isomers by contacting arabic hydrocarbons with an isomerization catalyst in the presence of hydrogen. A catalyst containing platinum is usually used as a catalyst, and p-xylene SP is obtained as the main isomer. The calculated thermodynamic equilibrium for aromatic C isomers under the process conditions at 454.44 ° C in l, wt%: ethylbenzene 8.5; “- xl lol 22.0; m-xylene 48.0; o-xylene 21; When the temperature rises by 10, the equilibrium concentration of ethylbenzene increases by 1 wt.%, o-xylene does not change, and for n- and m-xylenes, o decreases by 0.5 wt.%. The contacting process is characterized by the following data: Pressure in the reactor, kg / cm 12.30-15.82 Temperature at the reactor inlet, s 443.33-482.22 Reaction heat None Liquid-hour volumetric rate, rev / h 0.6- 1.6 The number of reactors in the system1 The thickness of the catalyst bed, m 3,353-4,57 The density of the catalyst, g / cm 0,608 Re circulation, mol of hydrogen per mole of hydrocarbon feedstock 7.0-14.0 Maximum pressure drop in the catalyst: , kg / cm 1.406 Thus, together with the aromatic hydrocarbons supplied, a significant amount of hydrogen C is introduced. increasing the productivity of the process is necessary to reduce the hydrogen circus l tion, the drive to higher boiling NIJ catalyst aging rate. Aging of the catalyst occurs as a result of deposition of carbonaceous materials on the catalyst, which necessitates its regeneration by burning off coke with a decrease in the catalyst's II activity. The reaction is started at 454.44 ° C and increased temperature in order to maintain the isomerization level to 482.22 ° C. The ethylbenzene present in the feedstock is partially removed before contacting the catalyst with the catalyst. When conducting contact, tilbenzene passes through ethyl cyclohexane to dimethyl cyclohexanes, which, in turn, equilibrate with the transfer of xylenes. The competing reactions are the diproportionation of ethylenezol to benzene and diethylbenzene, the hydrocracking of ethylbenzene to ethane and benzene, and the hydrocracking of alkylcyclohexanes. The degree of approximation of the ethylbenzene content to the equilibrium concentration in a mixture of Cg-aromatic hydrocarbons depends on the duration of the contacting process. The equilibrium content of ethylbenzene is greatly influenced by the partial pressure of hydrogen, and the temperature change is insignificant. The loss of ethylbenzene due to the transition into substances of a different molecular weight depends on the degree of approximation to equilibrium. Compounds formed from ethylbenzene include naphthenes C, benzene resulting from cracking, benzene and aromatics C resulting from the disproportionation of a compound of a different molecular weight, most of the compounds Cd. Cf hydrocarbons and lighter hydrocarbon by-products are also formed. Isomerization of xylenes is more selective than isomerization of ethylbenzene, and therefore, with different composition of the raw materials, the degree of equilibrium can fluctuate over a considerable interval of starts. The loss of xylene due to the transfer to products of a different molecular weight depends on the duration of the contact. By-products include naphthenes, toluene, Cg and C5 aromatics, and lighter hydrocracking products. Ethylbenzene causes a relatively rapid drop in catalyst activity and this effect is proportional to its concentration in the feedstock. Thus, when carrying out this method, it is necessary to use hydrogen, an expensive catalyst 58. During the process, by-products are also formed, xylene is lost. There is also known a method for producing xylene isomers by contacting Cd-aromatic hydrocarbons with an aluminosilicate catalyst, such as mordenite, fujazite, etc. The closest to the invention is a method for producing xylene ol isomers by contacting a mixture of Cg-aromatic hydrocarbons containing ethylbenzenes and xylenes with a catalyst based on a ZSM type zeolite, in particular ZSM-4. The process is carried out in the absence of hydrogen, a temperature of 121.1-367.8 ° C, a pressure of up to 140.6 kg / cm3. The disadvantage of this method is that the ethylbenzene contained in the raw material does not undergo transformations. The purpose of the invention is to improve the quality of the target product. The goal has been achieved by the method of producing isomers cc: tol by contacting a mixture of Cd-aromatic hydrocarbons 5 containing ethylbenzenes and xylenes in the cd phase using a catalyst-zeolite ZSM-5 or zeolite ZSM-21 in acidic form at a temperature of 260-348.9 C and an overpressure . A distinctive feature of the method is the use of ZSM-5, or ZSM-2 or ZSM-12 zeolites in acid form at the indicated temperature as a catalyst. The process is carried out at a pressure of up to 70.3 kg / cm and a bulk feed rate of 0.5-13 dOh. In addition, the catalyst contains an alumina-type binder. ZSM-5 type ZSM-2I zeolites in acid form (in H-form) are catalysts for the isomerization of C aromatics, which are not only very active and selective when shifting methyl groups in xylenes, but also cause the conversion of benzene. In particular, there is a significant disproportionation of ethyl benzene with a slight disproportionation of xylenes. Pa drawing presents a schematic diagram of the process. A mixture of 1 C-aromatic hydrocarbons, obtained as a result of the extraction of the platforming products of naphtha, is fed to the distillation in column 2, in which partial separation of the ethyl benzene is carried out. The latter is presented in the form of a head-on line 3. It is possible to carry out the process without the use of a column 2. The bottom line of coloins 2 consists of xylenes and ethylbenzene. Kubovas residue is withdrawn through line 4 and mixed with recycled xylene, which is fed through line 5. Semi-1% of the mixture is fed into the splitting column 6. The bottom product of the column is withdrawn through line 7. This product is composed of aromatic derivatives of Cd, obtained 1xx as a result of disproportionation of ztilbenzene and side reactions of xylene transalkylation. It is possible to carry out the process to obtain a bottom column product containing o-xylene. In this case, the bottom product is sent to a distillation to separate the o-xylene from the aromatic compounds Cq (iia shown). The head fractions fraction of the cleavage column 6 are directed along line 8 to the p-xylene separation devices. In the scheme presented, p-xylene is isolated by fractional crystallization in a crystallizer 9, including the formation of OAla and filtration of p-xylene crystals from the liquid phase. It is possible to use other p-xylene extraction systems, for example, selective sorption, HIGH PURE x-xylene is withdrawn through line 10. A drip of aromatic compounds of Cd with a reduced content of p-xylene is withdrawn from the crystallizer through line 1) a catalytic isomerization unit 13; where it contacts, under reaction conditions, with a zeolite of the type ZSM-5 or ZSM-21 in an acid form. The main reaction in the isomerization apparatus 13 is the shift of the methyl groups in the xylene molecules towards the equilibrium concentrations of the three xylenes. In addition to the isomerization of xylene, secondary editions of transalkyloroobs are formed to form benzene, toluene, polyethylbenzenes, polymethylbenzenes, ethyltoluenes and ethylxylene. An important reaction is the disproportionation of ethylbenzene to form benzene and polyethylbenzenes. The isomerizate obtained in the apparatus 13- for isomerization is sent via line 14 through the heat exchanger 15 to the column 16 for stripping. Light isomerized fractions (benzene, toluene, and gaseous and normal hydrocarbons are removed from the top of column 16 through line 17, and the bottom product of line 5 is sent to blend with raw materials.
-Receive transfer catalyst used in zeolite H-form (acid form by calcination}, which translates characteristic for these zeolites tetraalkylammonium cations into protons by decomposition of ammonium cations substituted. Additional protons and various cations metallovmogut displaced by sodium cations present in the zeolite and mainly at obrazuyuschimis exchange.
Used ceo: pins should be drowned in a binder material to obtain tablets or granules of a given size and resistance to abrasion Alumina is used as a binder. Preferably, the catalyst consists of tablets containing 35% by weight of alumina and 65% by weight of a zeolite of the type ZSM-5 or ZSM-21 in the H-form.
2 ethylbenzene
benzene + diethylbenzene
2 xylene
toluene + trimethylbenzene
Transalkylation proceeds at the following rate constants:
benzene + ethylxylene
Ethylbenzene + Xylene Toluene + Ethyltoluene Xylene + Ethylbenzene
Thus, ethylbenzene is converted to a greater extent by disproportionation to benzene and ethylbenzene, and to a lesser extent by transalkylation with xylenes.
HSSE SP 2 SSeSSS 2I2: S SSS22-. -7P xylene conversion,%
They can be isolated and used in pure form or as valuable high-octane components of motor fuel.
The severity of the process conditions should be optimally chosen. Thus, this isomerization method is carried out in the liquid phase at a temperature of from 260 to 348.9 ° C under pressure sufficient to liquefy the charge. Pressure above 70.3 kg / cm is undesirable.
The volumetric rate varies in the range from 0.5 to 10 volumes of feed material per volume of catalyst per hour {liquid hourly volumetric rate). The temperature and space velocity are adjusted so as to provide the necessary conditions for the required degree of xylene isomerization and the conversion of ethylbenzene without excessive loss of by-products. Thus, the temperature in the lower part of the temperature range usually corresponds to low volume velocities.
When used as catalysts for zeolites such as ZSM-5 and ZSM-2, disproportionation and transalkylation of ethylbenzene to xylenes occurs selectively.
The rate constants of disproportionation reactions at 287.8-315.6 C are as follows:
Relative constant j: ia; growth
125
Relative speed constant
16.8 3.6
The corresponding conversion steps of ethylbenzene and xylene by transalkylation depend on the composition of the feedstock. For typical feedstocks containing 10-25% ethylbenzenes, the following relationship occurs:
In order to cause the conversion of a sufficient amount of ethylbenzene to 55 of its running into the recycled stream. The optimal degree of conversion depends on the composition of the feedstock, on the method of removing p-xylene (for example crystallization or removing the put sorbdium) and on whether o-xylene is also removed. The degree of n rotation of ethylbenzene is the elimination of zs with the equation DEV R-uXYL, where EB is the amount of ethylbenzene, which is one pass in the transformation; AXYL amount of rotating xylene + amount per ton of xylene removed per pass; R is the ratio of ethylbenzene / KS lol in fresh raw materials. Below is data illustrating the use of the indicated equated in a process in which p-xylene is recovered by sorption extraction of raw materials having R 0.25, Ethyl benzo xylene Fresh raw materials, wt.% 80 20 Extracted p-xylene, wt.% 18.4 Trans-xylated xylenes, weight% 1.3 Total xylene extracted 19.7 Required conversion degree of ethylbenzene-, 25x19.7-4.92 The degree of conversion of ethylbenzene required is regulated in a relatively wide range of conditions and conditions of the process, in particular temperature and volume. speed.The process is conducted in temperature of 260-348 x ,, blowing pressure conditions. 1 is sufficient to ensure the conditions of the liquid phase, 11.25-36.56 kg / cm, respectively, or higher, ZHOLOS about 0.5-10, preferably 1-5, catalysts of the type HZSM-5 or HZSM-21. The ratio of ethylbenzene / xylene (R) in the recycled stream can be the same as in fresh raw materials. It is possible to further reduce the xylene losses caused by transalkylation and increase the yield of p-xylene, maintaining a higher R value in the recycle stream than in fresh feedstocks. This can be achieved at start-up by adding a certain amount of ethylbenzene to the feed during the first few hours of operation, it is also easy to choose less stringent start-up conditions that would allow the ethylbenzene content in the recycled stream to be at a given level. This technique is preferable in the processing of raw materials with low ethylbenzene content. The advantages of the proposed method are illustrated below. R in fresh feedstock 0.111 0.1.11 0.111 R in recycle, 111-0.293 0.488 flow stream The final yield of p-xylene (% of xylene in feedstock; 92.4 97.0 98.4 Example 1. HZSh-5 is used as a catalyst (b5% zeolite, 35% binder AloGj.l, activated by rushing 6 dry air per 1 cm of catalyst at a temperature of 25 to 538 s, then for 3 hours at 538 ° C. The raw material used contains 16.2% ethyl benzene, 61, 2% m-xyloa and 22.6% o-xylene (m-xylene / o-xiol-2, 7). Table 2 shows the operating conditions of the process and its results. The process is carried out at a pressure of 42.19 kg / cmH
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Example 2. When using raw materials containing 16% ethylbenzene, 62% m xylene and 22% o-xylene and an HZSM-21 catalyst, the degree of conversion of β-p-xylene close to the equilibrium is reached at 248.9 sec. 12 kg / cm (liquid phase}. Xylene loss due to disproportionation is less than 0.3%. HZSM-21 zeolite is used with silica / alumina ratio equal to 29. Before use, the zeolite is calcined in air, raising the temperature from room temperature to 537 8 ° C and incubated for 10 hours at 537.8 ° C.
In tab. Table 3 lists the process conditions and analyzes of products obtained using raw materials containing 15.5% ethylbenzene, 62% m-1 silol, and 22.5% o-xylene. The process pressure is 28.12 kg / cm.
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权利要求:
Claims (3)
[1]
rvl 21 Example 3. HZSM-12 without binding is used as a catalyst. The raw materials used contain 15% ethylbenzene, 2.2% p-xylene, 61.3% m-xylene and 21.5% o-xylene. The process proceeds as Claim 1. The method for producing xylene isomers by contacting a mixture of Cg-apomatic hydrocarbons containing methylbenzenes and xylenes in the liquid phase with a catalyst based on zeolite of the ZSM type at elevated temperatures and pressures, is characterized in that the quality of the product, as catalyzed 90971 isomerization of xylene and the conversion of ethylbeisol. In tab. 4 shows the operating conditions of the process and its results. In this case, four experiments were conducted. Table 4 of the mash uses zeolite ZSM-5 or ZSM-21 or ZSM-12 in an acid form, the 50 process is carried out at 260-348 ,. 2. The method according to claim 1, which is also distinguished by the fact that the process is carried out at a pressure of up to 70.3 kg / cm, a volumetric flow rate of the liquid feed is 0.5-U. 3. The method according to p. 1, I differ u and with the fact that used
23
Catalysate p contains a binder of the type gloryumena.
Sources of information taken into account in the examination
one . Patent CIIJA N 3078318, cl. 260-668, published in 1963.
/
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.2
890971
24
[2]
2. US patent number 3377400, cl. 260-668, published 1968.
[3]
3. US Patent No. 357 & 723,
cl. 260-672, publ. 1971 (prototype).
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类似技术:

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同族专利:

公开号 | 公开日

CA1026384A|1978-02-14|

PL94144B1|1977-07-30|

CS189668B2|1979-04-30|

ES428167A1|1976-07-16|

JPS5053335A|1975-05-12|

BE819848A|1975-03-12|

AR224491A1|1981-12-15|

DD113741A5|1975-06-20|

NL7412093A|1975-03-17|

DD113741B3|1986-06-11|

NL173846C|1984-03-16|

US3856871A|1974-12-24|

IT1021337B|1978-01-30|

DE2441516C3|1979-12-13|

FR2243919B1|1979-08-03|

GB1444702A|1976-08-04|

DE2441516B2|1979-04-26|

DE2441516A1|1975-03-20|

ZA743917B|1976-01-28|

JPS5341657B2|1978-11-06|

IN142292B|1977-06-18|

FR2243919A1|1975-04-11|

NL173846B|1983-10-17|

RO71348A|1982-02-01|

引用文献:

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US3281483A|1963-08-15|1966-10-25|Shell Oil Co|Disproportionation of alkyl aromatic hydrocarbons in the presence of hydrogen mordenite|

US3790471A|1969-10-10|1974-02-05|Mobil Oil Corp|Conversion with zsm-5 family of crystalline aluminosilicate zeolites|

US3646236A|1970-03-27|1972-02-29|Engelhard Min & Chem|Disproportionation of toluene with a platinum-rhenium-solid oxide catalyst|

US3691247A|1970-09-28|1972-09-12|Phillips Petroleum Co|Selectively removing monoalkylbenzenes from mixtures thereof with dialkylbenzenes|

US3751504A|1972-05-12|1973-08-07|Mobil Oil Corp|Vapor-phase alkylation in presence of crystalline aluminosilicate catalyst with separate transalkylation|

US3756942A|1972-05-17|1973-09-04|Mobil Oil Corp|Process for the production of aromatic compounds|

US3761389A|1972-08-28|1973-09-25|Mobil Oil Corp|Process of converting aliphatics to aromatics|US4101596A|1977-01-10|1978-07-18|Mobil Oil Company|Low pressure xylene isomerization|

US4101595A|1977-05-02|1978-07-18|Mobil Oil Corporation|Conversion of ethyl benzene to para xylene|

US4163028A|1977-07-22|1979-07-31|Mobil Oil Corporation|Xylene isomerization|

US4159283A|1978-04-07|1979-06-26|Mobil Oil Corporation|Isomerization process|

US4245130A|1978-06-02|1981-01-13|The British Petroleum Company Limited|Isomerization of alkyl aromatics using a gallium containing aluminosilicate catalyst|

US4159282A|1978-06-09|1979-06-26|Mobil Oil Corporation|Xylene isomerization|

US4188282A|1978-06-12|1980-02-12|Mobile Oil Corporation|Manufacture of benzene, toluene and xylene|

US4218573A|1978-06-12|1980-08-19|Mobil Oil Corporation|Xylene isomerization|

US4224141A|1979-05-21|1980-09-23|Mobil Oil Corporation|Manufacture of aromatic compounds|

US4236996A|1979-05-25|1980-12-02|Mobil Oil Corporation|Xylene isomerization|

US4283584A|1980-04-14|1981-08-11|Mobil Oil Corporation|Manufacture of aromatic compounds|

US4409413A|1980-06-23|1983-10-11|Toray Industries, Incorporated|Conversion of xylenes containing ethyl benzene|

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US20050143615A1|2003-12-30|2005-06-30|Bogdan Paula L.|Process and bimetallic catalyst for C8 alkylaromatic isomerization|

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法律状态:

优先权:

申请号 | 申请日 | 专利标题

US00397038A|US3856871A|1973-09-13|1973-09-13|Xylene isomerization|

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