CN103880584A - Method for combined production of p-xylene - Google Patents
Method for combined production of p-xylene Download PDFInfo
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- CN103880584A CN103880584A CN201210553097.XA CN201210553097A CN103880584A CN 103880584 A CN103880584 A CN 103880584A CN 201210553097 A CN201210553097 A CN 201210553097A CN 103880584 A CN103880584 A CN 103880584A
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Abstract
The invention relates to a method for combined production of p-xylene, and mainly solves the technical problems that conventional aromatic combination plant is long in flow, large in investment, rigor in reaction raw material requirement, low in recovery utilization rate of heavy components, and high in energy consumption in the prior art. According to the method, products with six or more carbons and coming from a reforming apparatus and hydrogen are mixed and enter a catalytic hydrogenation unit for generating a mixture of benzene, toluene, C8 arenes, C9 arenes and C10 arenes; the mixture enters a benzene tower for separation, a high-purity benzene product is obtained at the benzene tower top; tower bottoms of the benzene tower is sent to a toluene tower for separation, toluene obtained at the tower top is sent to a disproportionation and transalkylation reactor, and toluene tower bottoms are obtained from the tower kettle; the toluene tower bottoms enter a xylene tower for separation, xylene obtained at the tower top enters an absorption and separation unit, and compositions with nine or more carbons are obtained from the tower kettle; and the compositions with nine or more carbons enter a heavy arene tower for separation, and C9 arenes are obtained at the tower top. The technical scheme relatively well solves the above technical scheme and is application to industrial production of xylene.
Description
Technical field
The present invention relates to a kind of method of combination producing p-Xylol, say more specifically by catalytic hydrogenation unit, disproportionation are combined with transalkylation, p-Xylol adsorption separation unit and isomerization of C-8 aromatics unit, produce the method that obtains highly purified benzaldehyde product and p-Xylol product.
Background technology
P-Xylol is one of main basic organic of petrochemical industry, has purposes widely in numerous chemical production field such as chemical fibre, synthetic resins, agricultural chemicals, medicine, plastics.Typical p-Xylol (PX) production equipment generally includes petroleum naphtha catalytic reforming, dimethylbenzene fractionation, Aromatics Extractive Project, toluene disproportionation and transalkylation, fractionation by adsorption, isomerization totally six unit.Aromatics Extractive Project needs the solvent extraction apparatus of a set of complexity, and extraction solvent needs to supplement into continuously in extraction procedure process, and this extractive process expense has occupied the very big ratio of aromatic hydrocarbons cost.Though industrialized disproportionation and transalkylation can recycle a small amount of carbon ten and above component at present, Chinese patent CN1340489A points out in disproportionation and transalkylation charging, carbon ten and above component hydrocarbon are 0 ~ 20%, but most heavy constituent hydrocarbon cannot be recycled.
Chinese patent CN101348405B proposes to utilize the efficient dual-function catalyst of binder free Zeolite support carried noble metal to be converted into light aromatics and light paraffins for hydrocarbon raw material, by this process, heavy arene in raw material, through dealkylation and non-aromatics hydrocracking reaction, generates the BTX light aromatics of high added value.U.S. Patent No. 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. Patent No. 3,849,290 and 3,950,241 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. Patent No. 5,865,986 and No.6,001,241 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 that traditional Aromatic Hydrocarbon United Plant long flow path, investment are large, reaction raw materials requirement harshness, heavy constituent recovery utilization rate is low, energy consumption is high problem.The invention provides a kind of method of combination producing p-Xylol, by by the combination of the separating unit of catalytic hydrogenation unit, disproportionation and transalkylation, p-Xylol and isomerization of C-8 aromatics unit, production obtains the method for highly purified benzaldehyde product and p-Xylol product, larger simplification the flow process of traditional Aromatic Hydrocarbon United Plant, solved preferably above-mentioned technical problem.It is simple that the method has separating technology, and without solvent extraction process, energy consumption is low, and heavy arene and non-aromatics obtain the advantage of high value added utilization.
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 combination producing p-Xylol, comprises the following steps successively:
A) from the above product of carbon six of reformer and the mixed catalytic hydrogenation unit that enters of hydrogen, comprise the reaction of non-aromatics cracking, the de-alkyl of heavy aromatics, transalkylation, generate the mixture I of benzene, toluene, C8 aronmatic, C9 aromatic, C10 aromartic;
B) described mixture enters the separation of benzene tower, obtains benzaldehyde product at the tower top of benzene tower;
C) tower bottoms of benzene tower is sent into toluene tower separation, and the toluene that tower top obtains is delivered to disproportionation and transalkylation reactor, and tower reactor obtains toluene tower tower bottoms;
D) toluene tower tower bottoms enters benzenol hydrorefining separation, and the dimethylbenzene that tower top obtains enters adsorption separation unit, and tower reactor obtains carbon nine and above component;
E) carbon nine and above component enter the separation of heavy aromatics tower, and the above component of carbon ten obtaining at the bottom of heavy aromatics tower is returned to a) catalytic hydrogenation unit of step, and heavy aromatics column overhead obtains the mixture II containing C10 aromartic and C9 aromatic;
F) described mixture II and from toluene that c) step is come, enter disproportionation and transalkylation together with hydrogen, there is disproportionation and transalkylation reaction, the hydrogen that reaction generates returns to a) step and carries out catalytic hydrogenation reaction, and the mixture III of reaction generation benzene and C8 aronmatic enters b) the benzene tower of step and separates;
G) enter p-Xylol adsorption separation unit from the dimethylbenzene that d) step is come, obtain p-Xylol product and the C8 aronmatic containing p-Xylol;
H) the described C8 aronmatic from g) step is come enters isomerization of C-8 aromatics unit, and the Mixed XYLENE obtaining returns to e) the heavy aromatics tower of step and separates.
In technique scheme, preferred technical scheme, f) hydrogen of step reaction discharge enters catalytic hydrogenation unit, turnover catalytic hydrogenation reaction as a) hydrogen of step; F) benzene that step reaction generates and the mixture of C8 aronmatic with together with mixture that a) step generates, send into benzene tower and separate; H) together with the carbon nine that the Mixed XYLENE of step generates with d) step and above component, send into the separation of heavy aromatics tower; In the carbon six of reformer and above product, sulphur weight content is less than 200ppm, and alkene or diolefin weight content are less than 20%; Catalytic hydrogenation unit is used molecular sieve catalyst, and catalyzer contains at least one metal or its oxide compound that are selected from platinum, molybdenum or magnesium, and its consumption by weight percentage preferable range is 0.001 ~ 5%; Catalytic hydrogenation unit: reaction pressure preferable range is 0.1 ~ 5MPa, temperature of reaction preferable range is 100 ~ 600 ℃, and hydrogen hydrocarbon mol ratio preferable range is 0.1 ~ 10, and liquid weight air speed preferable range is 0.5 ~ 10h
-1; The catalyzer that disproportionation and transalkylation are used contains at least one molecular sieve being selected from beta-zeolite, mordenite, ZSM-5 or MCM-22, the metal of bismuth-containing or its oxide compound in catalyzer, its consumption by weight percentage preferable range is 0.005 ~ 5%; Disproportionation and transalkylation: reaction pressure preferable range is 0.5 ~ 5MPa, temperature of reaction preferable range is 200 ~ 600 ℃, and hydrogen hydrocarbon mol ratio preferable range is 0.5 ~ 10, and liquid weight air speed preferable range is 0.8 ~ 10h
-1; Disproportionation is reacted the hydrogen purity preferable range of discharging with transalkylation be 70 ~ 90mol%; Benzaldehyde product purity is>=99.9wt%; P-xylene separation unit adopts adsorption separation technology; P-Xylol product concentration is>=99.8wt%; Isomerization of C-8 aromatics unit: reaction pressure preferable range is 0.5 ~ 6MPa, temperature of reaction preferable range is 300 ~ 500 ℃, hydrogen hydrocarbon mol ratio preferable range 0.5 ~ 25, liquid weight air speed preferable range is 0.5 ~ 10h
-1; Carbon ten and above component are divided into two strands, and one that wherein preferably accounts for 80 ~ 100wt% returns to catalytic hydroprocessing unit, and a stock-traders' know-how heavy aromatics tower top that accounts for 0 ~ 20wt% enters disproportionation and transalkylation generation disproportionation reaction.
In technical scheme of the present invention, hydrogen feed also can be used as the hydrogen feed of catalytic hydrogenation unit after disproportionation has been reacted with transalkylation; Toluene in catalytic hydrogenation unit reaction product and carbon nine products can be used as the raw material of disproportionation and transalkylation; A small amount of carbon ten components of system enter disproportionation and transalkylation as reaction raw materials through heavy aromatics tower top, carbon ten components of the overwhelming majority are as the charging of catalytic hydrogenation unit, carbon ten component utilization ratios are high, without discharging out-of-bounds from heavy aromatics tower reactor, obtained good technique effect.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the method for combination producing p-Xylol of the present invention.
In Fig. 1, I is catalytic hydrogenation unit, and II is disproportionation and transalkylation, III benzene tower, and IV is toluene tower, and V is benzenol hydrorefining, and VI is heavy aromatics tower, and VII is p-Xylol adsorption separation unit, VIII is isomerization of C-8 aromatics unit.1 is carbon six and the above component raw material of reformer unit, 2 is discharge hydrogen, 3 lighter hydrocarbons for catalytic hydrogenation unit generation, 4 carbon six and above components for catalytic hydrogenation unit generation, 5 is that disproportionation and transalkylation generate gently, 6 is hydrogen, 7 is carbon six and the above component that disproportionation and transalkylation generate, 8 is benzaldehyde product, 9 is toluene tower charging, 10 is toluene, 11 is toluene tower bottoms, 12 is dimethylbenzene, 13 is the charging of heavy aromatics tower, 14 is carbon nine components containing a small amount of C10 aromartic, 15 is heavy aromatics tower reactor carbon ten and above component, 16 is p-Xylol product, 17 isomerization chargings, 18 is isomerization unit product, 19 is the hydrogen compared with low-purity.
In the technical process of the production p-Xylol shown in Fig. 1, fresh feed 1, recycle feed 15 with enter catalytic hydrogenation unit I compared with low-purity hydrogen 19, fresh hydrogen 6, toluene 10 enters disproportionation and transalkylation I together with containing carbon nine components 14 of a small amount of C10 aromartic, that discharges enters catalytic hydrogenation unit II compared with low-purity hydrogen 19, unit I and II obtain product 3 and 5 gently, the liquid-phase reaction product 4 and 7 that unit I and II obtain respectively enters the benzene tower III of rectification cell more successively, toluene tower IV, benzenol hydrorefining V separates with heavy aromatics tower VI, obtain high-purity benzene product 8 on benzene tower III top, toluene tower IV is pushed up the toluene 10 obtaining and is returned to disproportionation and transalkylation II, the dimethylbenzene 12 of benzenol hydrorefining VI tower top enters p-Xylol adsorption separation unit VII, carbon nine components 14 containing a small amount of C10 aromartic that heavy aromatics tower VII tower top obtains are returned to disproportionation and transalkylation II, carbon ten and above component 15 that heavy aromatics tower VII tower reactor obtains turn back to catalytic hydrogenation unit, adsorption separation unit VII obtains high purity p-Xylol product 16, o-Xylol and m-xylene 17 are sent into isomerization of C-8 aromatics unit VIII, Mixed XYLENE 18 is sent into benzenol hydrorefining V and is separated.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
With reformation C
6 +for raw material, raw material composition is as shown in table 1.
Technical process as shown in Figure 1.Fresh reformation C
6 +raw material 100t/h and circulation heavy aromatics tower tower reactor material 10.3t/h, that comes with disproportionation and transalkylation enters catalytic hydrogenation unit compared with low-purity hydrogen (hydrogen purity is 80mol%) and reacts, fresh hydrogen 6.34t/h(hydrogen purity is 93mol%), circulation toluene enters disproportionation and transalkylation together with containing carbon nine components of a small amount of C10 aromartic, two reaction members are discharged on a small quantity product gently, liquid-phase reaction product enters the benzene tower of rectification cell more successively, toluene tower, benzenol hydrorefining separates with heavy aromatics tower, benzene overhead extraction high-purity benzene product (benzene purity is 99.9wt%), the toluene 26.4t/h that toluene tower top obtains returns to disproportionation and transalkylation, the dimethylbenzene 125.8t/h of benzenol hydrorefining tower top enters p-Xylol adsorption separation unit, carbon nine components containing a small amount of C10 aromartic that heavy aromatics column overhead obtains are returned to disproportionation and transalkylation, carbon ten and above component 10.3t/h that heavy aromatics tower tower reactor obtains turn back to catalytic hydrogenation unit, adsorption separation unit obtains high purity p-Xylol product (dimethylbenzene purity is 99.8wt%), o-Xylol and m-xylene are sent into isomerization of C-8 aromatics unit, Mixed XYLENE is sent into benzenol hydrorefining and is separated.
Catalytic hydrogenation unit adopts fixed-bed reactor, the Pt for load weight ratio meter 0.04% of filling and 0.13% Pb Hydrogen adhesiveless ZSM-5 zeolite catalyst in reactor.Disproportionation and transalkylation adopt fixed-bed reactor, the beta-zeolite catalyzer that in reactor, filling bismuth-containing is 0.05%.The main operational condition of each reaction member refers to table 2.The process conditions of the each tower of distillation system refers to table 3.
Table 1
Table 2
Table 3
[embodiment 2]
With reformation C
9 +for raw material, raw material composition is as shown in table 4.
Technical process as shown in Figure 1.Fresh reformation C
9 +raw material 100t/h and circulation heavy aromatics tower tower reactor material 13.9t/h, that comes with disproportionation and transalkylation enters catalytic hydrogenation unit compared with low-purity hydrogen (hydrogen purity is 80mol%) and reacts, fresh hydrogen 8.46t/h(hydrogen purity is 93mol%), circulation toluene enters disproportionation and transalkylation together with containing carbon nine components of a small amount of C10 aromartic, two reaction members are discharged on a small quantity product gently, liquid-phase reaction product enters the benzene tower of rectification cell more successively, toluene tower, benzenol hydrorefining separates with heavy aromatics tower, benzene overhead extraction high-purity benzene product (benzene purity is 99.9wt%), the toluene 28.0t/h that toluene tower top obtains returns to disproportionation and transalkylation, the dimethylbenzene 155.4t/h of benzenol hydrorefining tower top enters p-Xylol adsorption separation unit, carbon nine components containing a small amount of C10 aromartic that heavy aromatics column overhead obtains are returned to disproportionation and transalkylation, carbon ten and above component 13.9t/h that heavy aromatics tower tower reactor obtains turn back to catalytic hydrogenation unit, adsorption separation unit obtains high purity p-Xylol product (dimethylbenzene purity is 99.8wt%), o-Xylol and m-xylene are sent into isomerization of C-8 aromatics unit, Mixed XYLENE is sent into benzenol hydrorefining and is separated.
Catalytic hydrogenation unit adopts fixed-bed reactor, the Pt for load weight ratio meter 0.04% of filling and 0.13% Pb Hydrogen adhesiveless ZSM-5 zeolite catalyst in reactor.Disproportionation and transalkylation adopt fixed-bed reactor, the beta-zeolite catalyzer that in reactor, filling bismuth-containing is 0.05%.The main operational condition of each reaction member refers to table 5.The process conditions of the each tower of distillation system refers to table 6.
Table 4
Table 5
Table 6
Claims (10)
1. a method for combination producing p-Xylol, comprises the following steps successively:
A) from the above product of carbon six of reformer and the mixed catalytic hydrogenation unit that enters of hydrogen, comprise the reaction of non-aromatics cracking, the de-alkyl of heavy aromatics, transalkylation, generate the mixture I of benzene, toluene, C8 aronmatic, C9 aromatic, C10 aromartic;
B) described mixture enters the separation of benzene tower, obtains benzaldehyde product at the tower top of benzene tower;
C) tower bottoms of benzene tower is sent into toluene tower separation, and the toluene that tower top obtains is delivered to disproportionation and transalkylation reactor, and tower reactor obtains toluene tower tower bottoms;
D) toluene tower tower bottoms enters benzenol hydrorefining separation, and the dimethylbenzene that tower top obtains enters adsorption separation unit, and tower reactor obtains carbon nine and above component;
E) carbon nine and above component enter the separation of heavy aromatics tower, and the above component of carbon ten obtaining at the bottom of heavy aromatics tower is returned to a) catalytic hydrogenation unit of step, and heavy aromatics column overhead obtains the mixture II containing C10 aromartic and C9 aromatic;
F) described mixture II and from toluene that c) step is come, enter disproportionation and transalkylation together with hydrogen, there is disproportionation and transalkylation reaction, the hydrogen that reaction generates returns to a) step and carries out catalytic hydrogenation reaction, and the mixture III of reaction generation benzene and C8 aronmatic enters b) the benzene tower of step and separates;
G) enter p-Xylol adsorption separation unit from the dimethylbenzene that d) step is come, obtain p-Xylol product and the C8 aronmatic containing p-Xylol;
H) the described C8 aronmatic from g) step is come enters isomerization of C-8 aromatics unit, and the Mixed XYLENE obtaining returns to e) the heavy aromatics tower of step and separates.
2. the method for combination producing p-Xylol according to claim 1, the hydrogen that it is characterized in that f) step reaction by-product enters catalytic hydrogenation unit, turnover catalytic hydrogenation reaction as a) hydrogen of step; F) benzene that step reaction generates and the mixture of C8 aronmatic with together with mixture that a) step generates, send into benzene tower and separate; H) together with the carbon nine that the Mixed XYLENE of step generates with d) step and above component, send into the separation of heavy aromatics tower.
3. the method for combination producing p-Xylol according to claim 1, is characterized in that in the carbon six of reformer and above product, sulphur weight content is less than 200ppm, and alkene or diolefin weight content are less than 20%.
4. the method for combination producing p-Xylol according to claim 1, it is characterized in that catalytic hydrogenation unit is used molecular sieve catalyst, catalyzer contains at least one metal or its oxide compound that are selected from platinum, molybdenum or magnesium, and its consumption counts 0.001 ~ 5% with catalyst weight per-cent.
5. the method for combination producing p-Xylol according to claim 1, it is characterized in that the catalyzer that disproportionation and transalkylation are used contains at least one molecular sieve being selected from beta-zeolite, mordenite, ZSM-5 or MCM-22, the metal of bismuth-containing or its oxide compound in catalyzer, its consumption is 0.005 ~ 5% by weight percentage.
6. the method for combination producing p-Xylol according to claim 1, is characterized in that the operational condition of catalytic hydrogenation unit is as follows: reaction pressure is 0.1 ~ 5MPa, and temperature of reaction is 100 ~ 600 ℃, hydrogen hydrocarbon mol ratio 0.1 ~ 10, and liquid weight air speed is 0.5 ~ 10h
-1; The operational condition of disproportionation and transalkylation is as follows: reaction pressure is 0.5 ~ 5MPa, and temperature of reaction is 200 ~ 600 ℃, hydrogen hydrocarbon mol ratio 0.5 ~ 10, and liquid weight air speed is 0.8 ~ 10h
-1.
7. the method for combination producing p-Xylol according to claim 1, is characterized in that in f) step that disproportionation is reacted the hydrogen purity producing with transalkylation be 70 ~ 90mol%; B) in step benzaldehyde product purity for being greater than 99.9wt%; G) in step, p-Xylol product concentration is >=99.8wt%.
8. the method for combination producing p-Xylol according to claim 1, is characterized in that p-xylene separation unit adopts fractionation by adsorption.
9. the method for combination producing p-Xylol according to claim 1, the operational condition that it is characterized in that isomerization of C-8 aromatics unit is as follows: reaction pressure is 0.5 ~ 6MPa, temperature of reaction is 300 ~ 500 ℃, hydrogen hydrocarbon mol ratio 0.5 ~ 25, and liquid weight air speed is 0.5 ~ 10h
-1.
10. the method for combination producing p-Xylol according to claim 1, it is characterized in that carbon ten and above component are divided into two strands, first strand that wherein accounts for 80 ~ 100wt% is returned to catalytic hydroprocessing unit, and the second stock-traders' know-how heavy aromatics tower top that accounts for 0 ~ 20wt% enters disproportionation and transalkylation generation disproportionation reaction.
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| CN106694054A (en) * | 2016-12-16 | 2017-05-24 | 东至绿洲环保化工有限公司 | Load-type resin catalyst for preparing xylene by virtue of selective toluene disproportionation |
| US9708233B2 (en) | 2014-08-15 | 2017-07-18 | Exxonmobil Chemical Patents Inc. | Aromatics production process |
| CN110139915A (en) * | 2017-01-05 | 2019-08-16 | 沙特基础全球技术有限公司 | Waste plastics is by being pyrolyzed the conversion to the high value products of such as benzene and dimethylbenzene |
| CN112824364A (en) * | 2019-11-21 | 2021-05-21 | 中国石化工程建设有限公司 | Process for disproportionating alkylaromatic hydrocarbons |
| CN114716291A (en) * | 2020-12-22 | 2022-07-08 | 中国石油化工股份有限公司 | Process system and process method for producing p-xylene in high yield from mixed aromatics |
| CN115612525A (en) * | 2021-07-14 | 2023-01-17 | 中国石化工程建设有限公司 | Process for producing light hydrocarbon and C8 aromatic hydrocarbon in high yield |
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| US9708233B2 (en) | 2014-08-15 | 2017-07-18 | Exxonmobil Chemical Patents Inc. | Aromatics production process |
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| JP7065372B2 (en) | 2017-01-05 | 2022-05-12 | サビック グローバル テクノロジーズ ベスローテン フェンノートシャップ | Pyrolysis of waste plastic to high value products such as benzene and xylene |
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| US10975313B2 (en) | 2017-01-05 | 2021-04-13 | Sabic Global Technologies B.V. | Conversion of waste plastic through pyrolysis to high value products like benzene and xylenes |
| CN110139915B (en) * | 2017-01-05 | 2021-12-14 | 沙特基础全球技术有限公司 | Conversion of waste plastics by pyrolysis to high value products such as benzene and xylenes |
| CN112824364A (en) * | 2019-11-21 | 2021-05-21 | 中国石化工程建设有限公司 | Process for disproportionating alkylaromatic hydrocarbons |
| CN112824364B (en) * | 2019-11-21 | 2023-01-03 | 中国石化工程建设有限公司 | Process for disproportionating alkyl aromatic hydrocarbon |
| CN114716291A (en) * | 2020-12-22 | 2022-07-08 | 中国石油化工股份有限公司 | Process system and process method for producing p-xylene in high yield from mixed aromatics |
| CN114716291B (en) * | 2020-12-22 | 2024-03-05 | 中国石油化工股份有限公司 | Process system and process method for producing paraxylene by mixed aromatic hydrocarbon |
| CN115612525A (en) * | 2021-07-14 | 2023-01-17 | 中国石化工程建设有限公司 | Process for producing light hydrocarbon and C8 aromatic hydrocarbon in high yield |
| CN115612525B (en) * | 2021-07-14 | 2024-04-16 | 中国石化工程建设有限公司 | Process for producing light hydrocarbon and C8 aromatic hydrocarbon in high yield |
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