CN103435432A - Method for preparing ethylene and propylene by taking naphtha as raw material - Google Patents
Method for preparing ethylene and propylene by taking naphtha as raw material Download PDFInfo
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- CN103435432A CN103435432A CN2013103103433A CN201310310343A CN103435432A CN 103435432 A CN103435432 A CN 103435432A CN 2013103103433 A CN2013103103433 A CN 2013103103433A CN 201310310343 A CN201310310343 A CN 201310310343A CN 103435432 A CN103435432 A CN 103435432A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The invention belongs to the technical field for producing ethylene and propylene, and particularly relates to a method for preparing ethylene and propylene by taking naphtha as the raw material. The method for preparing ethylene and propylene by taking naphtha as the raw material comprises the following steps: (1) preparation of a composite catalyst; (2) catalyzed cracking; and (3) separation of products. The method for preparing ethylene and propylene by taking naphtha as the raw material has simple steps and reasonable design, and helps to substantially improve conversion rate of naphtha and yields of ethylene and propylene.
Description
Technical field
The invention belongs to the technical field of producing ethylene, propylene, be specifically related to a kind of method of petroleum naphtha as the raw materials for ethylene production propylene of take.
Background technology
The low-carbon alkene such as ethene, propylene, as the important foundation raw material of petrochemical complex, plays a part very important in petrochemical industry.In the production technology of numerous hydrocarbon crackings ethene processed, the pyrolysis in tubular furnace method is occupied an leading position in ethylene yield.Yet, along with the increase of acryloyl derivative demand, the propone output obtained by the pyrolysis method coproduction can not meet on domestic and international market the needs growing to propylene.In addition, also there is energy consumption in the steam heat cracking technique and the problem such as facility investment is too high, the cracking stock range of choice is narrower, environmental pollution is more serious.The steam cracking reaction temperature is high, and energy consumption is large, needs expensive high temperature alloy steel, and the operational cycle is short, and the boiler tube life-span is low, discharges a large amount of carbon monoxide, and yield is lower, has restricted further developing of ethylene industry.
Catalytic pyrolysis is under the condition existed at catalyzer, petroleum hydrocarbon is carried out to the process of the low-carbon alkenes such as cracking ethene, propylene.Compare with conventional steam heat cracking technique, not only can reduce temperature of reaction, obtain high selectivity of light olefin, and be easier to regulate the distribution of product composition.Affect the factor of catalytic pyrolysis except raw material composition, operational condition and reaction unit, catalyzer is the key factor in the catalytic pyrolysis technology, the catalyzer adopted in cracking process will guarantee that the yield of low-carbon alkene is higher, the by products such as hydrogen, methane, coke are lower, also will possess satisfactory stability and mechanical wear intensity simultaneously.
The core of catalytic pyrolysis is reactor, is divided into fixed fluidized-bed reactor, circulating fluid bed reactor and fixed-bed reactor etc.Wherein, fixed fluidized-bed reactor is widely used in catalytic cracking and catalytic pyrolysis with its simple structure and good turndown ratio.Now widespread use be traditional fixed fluidized-bed reactor, when being applied to heavy oil and naphtha catalytic cracking, have the easy coking of inside reactor and affect that reaction is normally carried out, catalyst fluidization weak effect and the defect such as the reactor reaction effect is undesirable.Traditional fixed fluidized-bed reactor main part can be divided into conversion zone and expanding reach from bottom to top.Reactor adopts the chuck heating, the feed-pipe feed imported from top, and reactor bottom is have certain radian semi-circular, by the catalyzer dismounting pipe dismounting catalyzer of reactor bottom.Traditional reactor is larger due to reactor two ends heat radiations, and focus concentrates on the reactor middle part, easily causes reacting dilute phase section excess Temperature and deepens the cracking degree, and the coking of aggravation reactor, increase the deep pyrolytic product as CO and CO
2yield.In traditional reactor, after gasifying by preheater, reaction mass stretched into the feed-pipe supply of reactor bottom by top.Reactor bottom is have certain radian semi-circular.After gas feed reaches certain linear speed, the impellent made progress makes catalyst fluidization.This design is when the cracking of application high-temperature catalytic, reactant gas is identical with the temperature of reaction of reactor in the feed-pipe that stretches into the reactor part, now the generation of coking will occur and follow in high temperature pyrolysis in feed-pipe, and the slight fluctuations of the inevitable reactor internal pressure brought because of operation, make catalyzer be easy to enter the reaction feed pipe, these reasons very easily cause in reaction process the reaction-ure feeding pipe blocked and reaction can't normally be carried out.Usually after reaction is carried out 2 hours, because coking increases, reaction pressure starts to increase, and operational condition starts to worsen.Therefore, when the traditional fixed fluidized bed device reaction of application, operational condition is as harsher as the control requirement of temperature, pressure and feed time etc., needs the control of strict charging proportioning, temperature and pressure, otherwise the reaction feed pipe is easy to stop up, and reaction can't normally be carried out.The semicircular design of reactor bottom makes structure of reactor simply and is easy to processing, but the fluid effect of catalyzer is determined by the flow velocity of semicircular radian and feed gas, can't regulate flexibly, limited reactor the scope of applicable reaction type, raw material and processing condition, simultaneous reactions device bottom air-flow condition complexity, be easy to produce the phenomenon that channel etc. affects catalyst fluidization, affect catalytic performance.
Summary of the invention
The object of the invention is to for the defect of above-mentioned existence and a kind of method that petroleum naphtha is the raw materials for ethylene production propylene of take is provided, step is simple, reasonable in design, has greatly improved the transformation efficiency of petroleum naphtha and the yield of ethylene, propylene.
Technical scheme of the present invention is: a kind ofly take the method that petroleum naphtha is the raw materials for ethylene production propylene, comprise the following steps:
(1) preparation of composite catalyst: after ZSM-5 molecular sieve, RE-USY molecular sieve, cakingagent, the distilled water taken is mixed, carry out crystallization, filtration, washing, drying, roasting, make composite catalyst, wherein the weight part ratio of ZSM-5 molecular sieve and RE-USY molecular sieve is (1～3): 1;
(2) catalytic pyrolysis: deionized water and petroleum naphtha are inputted to the raw material preheating gasifier by volume pump respectively, carry out the preheating gasification under 200～230 ℃ of conditions, then the deionized water after gasification and petroleum naphtha are entered to reactor by the bottom of fixed fluidized-bed reactor and carry out catalytic cracking reaction, wherein catalyst loading is 3～5g petroleum naphtha/g catalyzer hour, the weight part ratio of deionized water and petroleum naphtha is (1～3): 1, temperature of reaction is 600～680 ℃, reaction pressure is 0.05～0.5MPa, and the reaction mass air speed is 1～3 hour
-1;
(3) separation of product: reaction product after catalytic pyrolysis is delivered to condenser and carry out condensation, then deliver to water-and-oil separator, the ethylene, propylene gaseous product is isolated by water-and-oil separator top.
In described step (1), the temperature of crystallization is 120～140 ℃, crystallization time 20～50 hours; 450～600 ℃ of maturing temperatures, roasting time 4～7 hours.
In described step (1), cakingagent is polynite, and wherein the weight part ratio of polynite and RE-USY molecular sieve is 1:(2～4).
In described step (1), the weight part ratio of ZSM-5 molecular sieve and RE-USY molecular sieve is 1:1.
Fixed fluidized-bed reactor in described step (2) is respectively collection chamber from bottom to top, reacts close phase section, reacts dilute phase section and expanding reach.
The close phase section of the reaction of the fixed fluidized-bed reactor in described step (2), reaction dilute phase section and expanding reach are equipped with heating installation.
Fixed fluidized-bed reactor inside in described step (2) is equipped with thermoscope.
Fixed fluidized-bed reactor expanding reach top in described step (2) is provided with catalyst filter, reaction discharge nozzle and catalyzer mounting or dismounting pipe.
The collection chamber top of the fixed fluidized-bed reactor in described step (2) is provided with gas distribution grid.
Beneficial effect of the present invention is: in the method for the invention, composite catalyst consists of the Primary Catalysts ZSM-5 molecular sieve with microvoid structure and promotor RE-USY molecular sieve and cakingagent with meso-hole structure, formed the hole continuous structure of funnel type after ZSM-5 molecular sieve and RE-USY molecular sieve mixing moulding, the Gradient distribution of its pore passage structure and two diacid reasonably combined, produce useful synergistic effect and make this catalyzer make the transformation efficiency of petroleum naphtha and the hydrocarbon-selective of ethylene, propylene improve.Simultaneously the present invention adopts composite catalyst that chemical method prepares to be beneficial to synthesize the composite catalyst with different pore passage structures and Acidity, and the interaction between component and component is more strong.
The method of the invention fixed fluidized-bed reactor focus used concentrates on the close phase section of reactor, and thermograde raises with beds and progressively descends, and is conducive to reaction and carries out the highest section of catalyst concn.Adjusted within the specific limits as requested because reactor adopts the layout of three-phase section independent heating can make reaction bed temperature distribute, therefore, can be optimized catalyzed reaction technique.This reactor still shows good performance at the temperature higher than 650 ℃, catalyst fluidization is effective, bed temperature is evenly distributed, fixed fluidized-bed reactor of the present invention, reaction-ure conversion-age and product yield are higher, ethene and propylene total recovery are more than 50%, comparing the traditional reactor of application has improved more than 7 percentage points, and in whole reaction process, scission reaction is not subject to larger impact because of coking, illustrate that this reactor performance is reliable and stable, and changed traditional feeding manner, reaction feed enters reactor from reactor bottom after preheating, the feed-pipe feed that can avoid like this reactant gases to import from top by traditional way, and cause reactant gases because reaching cracking temperature, heat scission reaction to occur in feed-pipe, not there will be and cause the phenomenon of stopping up feed-pipe after the product coking because the feed-pipe aperture is little, guarantee normally carrying out of catalytic cracking reaction.And adopt this feeding manner, can make charging fully mixed in preheater.Preheating temperature is controlled effectively, guarantees that feeding temperature is not subject to reaction temperatures affect.At the collection chamber top, gas distribution grid is set, can effectively makes feed gas be evenly distributed, make catalyzer in comparatively ideal fluidized state, occur with channel and the turbulent flow phenomenon of avoiding catalyzer in reaction process, can obviously improve reaction conditions.
In sum, of the present inventionly take petroleum naphtha as the method steps of raw materials for ethylene production propylene is simple, reasonable in design, greatly improved the transformation efficiency of petroleum naphtha and the yield of ethylene, propylene.
The accompanying drawing explanation
The structural representation that Fig. 1 is fixed fluidized-bed reactor in the specific embodiment of the invention.
Wherein, 1 is collection chamber, and 2 is the close phase section of reaction, and 3 is reaction dilute phase section, and 4 is expanding reach, and 5 is heating installation, and 6 is thermoscope, and 7 is catalyst filter, and 8 is the reaction discharge nozzle, and 9 is catalyzer mounting or dismounting pipe, and 10 is gas distribution grid.
Embodiment
Below by embodiment, the present invention will be described in detail.
Embodiment 1
A kind ofly take the method that petroleum naphtha is the raw materials for ethylene production propylene, comprise the following steps:
(1) preparation of composite catalyst: after ZSM-5 molecular sieve, RE-USY molecular sieve, cakingagent, the distilled water taken is mixed, carry out crystallization, filtration, washing, drying, roasting, make composite catalyst, wherein the weight part ratio of ZSM-5 molecular sieve and RE-USY molecular sieve is 2:1;
(2) catalytic pyrolysis: deionized water and petroleum naphtha are inputted to the raw material preheating gasifier by volume pump respectively, carry out the preheating gasification under 210 ℃ of conditions, then the deionized water after gasification and petroleum naphtha are entered to reactor by the bottom of fixed fluidized-bed reactor and carry out catalytic cracking reaction, wherein catalyst loading is 3g petroleum naphtha/g catalyzer hour, the weight part ratio of deionized water and petroleum naphtha is 2:1, temperature of reaction is 630 ℃, and reaction pressure is 0.08MPa, and the reaction mass air speed is 2 hours
-1;
(3) separation of product: reaction product after catalytic pyrolysis is delivered to condenser and carry out condensation, then deliver to water-and-oil separator, the ethylene, propylene gaseous product is isolated by water-and-oil separator top.
In described step (1), the temperature of crystallization is 120 ℃, crystallization time 20 hours; 450 ℃ of maturing temperatures, roasting time 5 hours.
In described step (1), cakingagent is polynite, and wherein the weight part ratio of polynite and RE-USY molecular sieve is 1:2.
Fixed fluidized-bed reactor in described step (2) is respectively collection chamber 1 from bottom to top, reacts close phase section 2, reacts dilute phase section 3 and expanding reach 4.
The close phase section 2 of the reaction of the fixed fluidized-bed reactor in described step (2), reaction dilute phase section 3 and expanding reach 4 are equipped with heating installation 5.
Fixed fluidized-bed reactor inside in described step (2) is equipped with thermoscope 6.
Fixed fluidized-bed reactor expanding reach top in described step (2) is provided with catalyst filter 7, reaction discharge nozzle 8 and catalyzer mounting or dismounting pipe 9.
Collection chamber 1 top of the fixed fluidized-bed reactor in described step (2) is provided with gas distribution grid 10.
Adopt the method gained of the present embodiment: yield of ethene 43%, propene yield 16%, reaction conversion ratio is that 80%, CO yield is 1.2%, CO
2yield is 0.6%.
Embodiment 2
A kind ofly take the method that petroleum naphtha is the raw materials for ethylene production propylene, comprise the following steps:
(1) preparation of composite catalyst: after ZSM-5 molecular sieve, RE-USY molecular sieve, cakingagent, the distilled water taken is mixed, carry out crystallization, filtration, washing, drying, roasting, make composite catalyst, wherein the weight part ratio of ZSM-5 molecular sieve and RE-USY molecular sieve is 1:1;
(2) catalytic pyrolysis: deionized water and petroleum naphtha are inputted to the raw material preheating gasifier by volume pump respectively, carry out the preheating gasification under 230 ℃ of conditions, then the deionized water after gasification and petroleum naphtha are entered to reactor by the bottom of fixed fluidized-bed reactor and carry out catalytic cracking reaction, wherein catalyst loading is 5g petroleum naphtha/g catalyzer hour, the weight part ratio of deionized water and petroleum naphtha is 3:1, temperature of reaction is 650 ℃, and reaction pressure is 0.5MPa, and the reaction mass air speed is 1 hour
-1;
(3) separation of product: reaction product after catalytic pyrolysis is delivered to condenser and carry out condensation, then deliver to water-and-oil separator, the ethylene, propylene gaseous product is isolated by water-and-oil separator top.
In described step (1), the temperature of crystallization is 140 ℃, crystallization time 50 hours; 500 ℃ of maturing temperatures,
Roasting time 7 hours.
In described step (1), cakingagent is polynite, and wherein the weight part ratio of polynite and RE-USY molecular sieve is 1:3.
Fixed fluidized-bed reactor in described step (2) is respectively collection chamber 1 from bottom to top, reacts close phase section 2, reacts dilute phase section 3 and expanding reach 4.
The close phase section 2 of the reaction of the fixed fluidized-bed reactor in described step (2), reaction dilute phase section 3 and expanding reach 4 are equipped with heating installation 5.
Fixed fluidized-bed reactor inside in described step (2) is equipped with thermoscope 6.
Fixed fluidized-bed reactor expanding reach top in described step (2) is provided with catalyst filter 7, reaction discharge nozzle 8 and catalyzer mounting or dismounting pipe 9.
Collection chamber 1 top of the fixed fluidized-bed reactor in described step (2) is provided with gas distribution grid 10.
Adopt the method gained of the present embodiment: yield of ethene 46%, propene yield 17%, reaction conversion ratio is that 89%, CO yield is 1.0%, CO
2yield is 0.5%.
Embodiment 3
A kind ofly take the method that petroleum naphtha is the raw materials for ethylene production propylene, comprise the following steps:
(1) preparation of composite catalyst: after ZSM-5 molecular sieve, RE-USY molecular sieve, cakingagent, the distilled water taken is mixed, carry out crystallization, filtration, washing, drying, roasting, make composite catalyst, wherein the weight part ratio of ZSM-5 molecular sieve and RE-USY molecular sieve is 3:1;
(2) catalytic pyrolysis: deionized water and petroleum naphtha are inputted to the raw material preheating gasifier by volume pump respectively, carry out the preheating gasification under 230 ℃ of conditions, then the deionized water after gasification and petroleum naphtha are entered to reactor by the bottom of fixed fluidized-bed reactor and carry out catalytic cracking reaction, wherein catalyst loading is 3g petroleum naphtha/g catalyzer hour, the weight part ratio of deionized water and petroleum naphtha is 1:1, temperature of reaction is 680 ℃, and reaction pressure is 0.5MPa, and the reaction mass air speed is 2 hours
-1;
(3) separation of product: reaction product after catalytic pyrolysis is delivered to condenser and carry out condensation, then deliver to water-and-oil separator, the ethylene, propylene gaseous product is isolated by water-and-oil separator top.
In described step (1), the temperature of crystallization is 135 ℃, crystallization time 35 hours; 540 ℃ of maturing temperatures,
Roasting time 4.5 hours.
In described step (1), cakingagent is polynite, and wherein the weight part ratio of polynite and RE-USY molecular sieve is 1:4.
Fixed fluidized-bed reactor in described step (2) is respectively collection chamber 1 from bottom to top, reacts close phase section 2, reacts dilute phase section 3 and expanding reach 4.
The close phase section 2 of the reaction of the fixed fluidized-bed reactor in described step (2), reaction dilute phase section 3 and expanding reach 4 are equipped with heating installation 5.
Fixed fluidized-bed reactor inside in described step (2) is equipped with thermoscope 6.
Fixed fluidized-bed reactor expanding reach top in described step (2) is provided with catalyst filter 7, reaction discharge nozzle 8 and catalyzer mounting or dismounting pipe 9.
Collection chamber 1 top of the fixed fluidized-bed reactor in described step (2) is provided with gas distribution grid 10.
Adopt the method gained of the present embodiment: yield of ethene 49%, propene yield 16%, reaction conversion ratio is that 88%, CO yield is 1.0%, CO
2yield is 0.8%.
Claims (9)
1. take the method that petroleum naphtha is the raw materials for ethylene production propylene for one kind, comprise the following steps:
(1) preparation of composite catalyst: after ZSM-5 molecular sieve, RE-USY molecular sieve, cakingagent, the distilled water taken is mixed, carry out crystallization, filtration, washing, drying, roasting, make composite catalyst, wherein the weight part ratio of ZSM-5 molecular sieve and RE-USY molecular sieve is (1～3): 1;
(2) catalytic pyrolysis: deionized water and petroleum naphtha are inputted to the raw material preheating gasifier by volume pump respectively, carry out the preheating gasification under 200～230 ℃ of conditions, then the deionized water after gasification and petroleum naphtha are entered to reactor by the bottom of fixed fluidized-bed reactor and carry out catalytic cracking reaction, wherein catalyst loading is 3～5g petroleum naphtha/g catalyzer hour, the weight part ratio of deionized water and petroleum naphtha is (1～3): 1, temperature of reaction is 600～680 ℃, reaction pressure is 0.05～0.5MPa, and the reaction mass air speed is 1～3 hour
-1;
(3) separation of product: reaction product after catalytic pyrolysis is delivered to condenser and carry out condensation, then deliver to water-and-oil separator, the ethylene, propylene gaseous product is isolated by water-and-oil separator top.
2. take according to claim 1 is described the method that petroleum naphtha is the raw materials for ethylene production propylene, it is characterized in that, in described step (1), the temperature of crystallization is 120～140 ℃, crystallization time 20～50 hours; 450～600 ℃ of maturing temperatures, roasting time 4～7 hours.
3. take according to claim 1 is described the method that petroleum naphtha is the raw materials for ethylene production propylene, it is characterized in that, in described step (1), cakingagent is polynite, and wherein the weight part ratio of polynite and RE-USY molecular sieve is 1:(2～4).
4. take according to claim 1 is described the method that petroleum naphtha is the raw materials for ethylene production propylene, it is characterized in that, in described step (1), the weight part ratio of ZSM-5 molecular sieve and RE-USY molecular sieve is 1:1.
5. the method that the petroleum naphtha of take according to claim 1 is the raw materials for ethylene production propylene, is characterized in that, the fixed fluidized-bed reactor in described step (2) is respectively collection chamber from bottom to top, reacts close phase section, reacts dilute phase section and expanding reach.
6. the method that the petroleum naphtha of take according to claim 5 is the raw materials for ethylene production propylene, is characterized in that, the close phase section of the reaction of the fixed fluidized-bed reactor in described step (2), reaction dilute phase section and expanding reach are equipped with heating installation.
7. the method that the petroleum naphtha of take according to claim 1 is the raw materials for ethylene production propylene is characterized in that the fixed fluidized-bed reactor inside in described step (2) is equipped with thermoscope.
8. the method that the petroleum naphtha of take according to claim 5 is the raw materials for ethylene production propylene, is characterized in that, the fixed fluidized-bed reactor expanding reach top in described step (2) is provided with catalyst filter, reaction discharge nozzle and catalyzer mounting or dismounting pipe.
9. the method that the petroleum naphtha of take according to claim 5 is the raw materials for ethylene production propylene is characterized in that the collection chamber top of the fixed fluidized-bed reactor in described step (2) is provided with gas distribution grid.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105771809A (en) * | 2016-05-03 | 2016-07-20 | 江苏大学 | Semi-continuous microwave catalytic thermal cracking reactor |
| CN108329944A (en) * | 2018-02-08 | 2018-07-27 | 河北精致科技有限公司 | Utilize the method for catalytically cracked gasoline coproduction desulfurization low alkene gasoline and chemical products |
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| CN108329944A (en) * | 2018-02-08 | 2018-07-27 | 河北精致科技有限公司 | Utilize the method for catalytically cracked gasoline coproduction desulfurization low alkene gasoline and chemical products |
| CN108329944B (en) * | 2018-02-08 | 2020-09-22 | 河北精致科技有限公司 | Method for co-producing desulfurized low-olefin gasoline and chemical products by using catalytic cracking gasoline |
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Effective date of registration: 20191113 Address after: 207-3, floor 2, No.19 B, Chegongzhuang West Road, Haidian District, Beijing 100044 Patentee after: Beijing Sino European Institute of science and technology Address before: 250000, building 2, No. 11, Qilihe Road, Licheng District, Shandong, Ji'nan Patentee before: Xinghuo Sci. & Tech. Research Inst., Jinan Dev. Zone |
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Effective date of registration: 20201218 Address after: Room 608, 6 / F, Zhongxing business enterprise development center, Pingshang Town, Lingang Economic Development Zone, Linyi City, Shandong Province Patentee after: Linyi Xinghuo Intellectual Property Service Co.,Ltd. Address before: 207-3, 2nd floor, No.19, Chegongzhuang West Road, Haidian District, Beijing 100044 Patentee before: BEIJING OUMEIZHONG SCIENCE AND TECHNOLOGY Research Institute |
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