CN104611002A - Liquid-state petroleum hydrocarbon cracking method with characteristic of propylene yield increase and aromatic hydrocarbon yield increase - Google Patents

Liquid-state petroleum hydrocarbon cracking method with characteristic of propylene yield increase and aromatic hydrocarbon yield increase Download PDF

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CN104611002A
CN104611002A CN201310541181.4A CN201310541181A CN104611002A CN 104611002 A CN104611002 A CN 104611002A CN 201310541181 A CN201310541181 A CN 201310541181A CN 104611002 A CN104611002 A CN 104611002A
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petroleum hydrocarbon
cracking
liquid
product
steam heat
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CN104611002B (en
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吉媛媛
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Sinopec Beijing Research Institute of Chemical Industry
China Petroleum and Chemical Corp
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Sinopec Beijing Research Institute of Chemical Industry
China Petroleum and Chemical Corp
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Abstract

The present invention relates to a liquid-state petroleum hydrocarbon cracking method, which comprises: before steam thermal-cracking, carrying out catalytic cracking on a petroleum hydrocarbon; carrying out aromatic hydrocarbon extraction on the liquid-phase product of the catalytic cracking; and carrying out steam thermal-cracking on the obtained aromatic hydrocarbon extraction product. Compared with the industrial conventional method for directly carrying out steam cracking on the petroleum hydrocarbon, the method of the present invention has the following characteristics that: the catalytic cracking reactor and the aromatic hydrocarbon extraction device are added in front of the steam cracking device, wherein the petroleum hydrocarbon is subjected to the catalytic cracking, condensation separation is performed to obtain the gas-phase product and the liquid-phase product, and the steam thermal-cracking is further performed after the liquid-phase product is subjected to the partial aromatic hydrocarbon extraction; and the purposes of propylene yield increase and aromatic hydrocarbon yield increase are achieved on the base of the assurance of the high ethylene yield.

Description

A kind of liquid condition petroleum hydrocarbon cleavage method improving propylene and aromatics yield
Technical field
The present invention relates to a kind of liquid condition petroleum hydrocarbon cleavage method, more particularly, relate to a kind of liquid condition petroleum hydrocarbon cleavage method improving propylene and aromatics yield.
Background technology
At present, the production of low-carbon alkene (ethene, propylene and butylene) mainly adopts tube furnace steam heat cracking process in the world, and the ethylene yield that method obtains thus exceedes 99% of ethene ultimate production.The materials such as a certain amount of propylene, divinyl and aromatic hydrocarbons can also be obtained simultaneously.Along with the growth that market requires propylene, research and the production of " for the purpose of propylene product " day by day increase.In recent years, along with market is to the increase gradually of propylene demand, occur as dehydrogenating propane, preparing propylene from methanol and C4 conversion of olefines etc. prepare the method for propylene.These methods use together with naphtha steam pyrolysis technology, for market provides required ethene, propylene and divinyl.But these technology also exist raw material supply quantity not sufficient, or product kind can not meet the phenomenon of market demand.
In addition, along with the development and utilization of shale gas, the raw materials for production of ethene gradually by oil to gas transition; Because the cost of shale gas is lower than petroleum naphtha, the economy of therefore producing ethene by petroleum naphtha by steam heat cracking technology is subject to serious challenge.Contend with the method for being produced ethene by shale gas on cost to make the method for being produced ethene by petroleum hydrocarbon, ensure certain economy, steam cracking liquid condition petroleum hydrocarbon technique needs the yield reducing low value-added product methane, improves the yield of propylene and C6 ~ C8 aromatic hydrocarbons.
In the product that the cracking of liquid condition petroleum hydrocarbon steam heat obtains, the yield of ethene and propylene is about 45%, and the yield of low value-added methane is about 15%, and propylene and ethylene ratio are less than 0.6.Meanwhile, because petroleum hydrocarbon steam thermal cracking temperature is 780 ~ 840 DEG C, react at such high temperatures, product, by thermal control, causes producing the low methane of a large amount of added value, and low-carbon alkene aggregates into ring simultaneously, high-carbon aromaticity content increases, and C6 ~ C8 aromaticity content that in product, added value is high reduces.Cause the effective rate of utilization of petroleum liquid hydrocarbon feed low like this, products distribution can not regulate.Therefore need a kind of liquid condition petroleum hydrocarbon cleavage method, the yield of propylene and C6 ~ C8 aromatic hydrocarbons in steam heat split product can be improved.
Summary of the invention
For reducing the methane content in liquid condition petroleum hydrocarbon split product, improving the yield by liquid condition petroleum hydrocarbon preparing propone and C6 ~ C8 aromatic hydrocarbons, ensureing the yield of ethene of higher level simultaneously, the invention provides a kind of liquid condition petroleum hydrocarbon cleavage method.
For achieving the above object, technical scheme of the present invention is as follows:
Improve a liquid condition petroleum hydrocarbon cleavage method for propylene and aromatics yield, the method comprises carries out catalytic pyrolysis by petroleum hydrocarbon, and the liquid product of catalytic pyrolysis is carried out Aromatics Extractive Project, and then liquid product remaining after gained Aromatics Extractive Project is carried out steam heat cracking.
In a specific embodiment, described method can comprise the following steps:
(1) liquid condition petroleum hydrocarbon and water for the treatment of cracking being introduced preheater, is gas through preheater heating and gasifying;
The source of described petroleum hydrocarbon comprises the lighter hydrocarbons of gas plant, as carbonatoms is more than or equal to the butane etc. of four, and the converted products of refinery, as refinery gas, petroleum naphtha, diesel oil, heavy oil, residual oil etc., and refinery secondary processing oil, as coking hydrogenated oil, hydrogenation tail oil etc.
(2) the thermal evaporation gas that obtains in advance is sent into catalytic cracking reaction device, under the effect of catalyzer, carry out the catalytic cracking reaction of low cracking degree.Described catalytic cracking reaction is undertaken by existing catalytic cracking reaction device, and as fixed-bed reactor or fluidized-bed reactor, catalyst cupport is in reactor.
In a specific embodiment, the temperature of reaction of described catalytic pyrolysis is 450-700 DEG C, and reaction pressure is 0.001-0.3MPa, and weight space velocity is 1-20h -1, the mass ratio of water and petroleum hydrocarbon is 0.1:1-1:1.Preferable reaction temperature is 550-650 DEG C, and the weight space velocity of petroleum hydrocarbon is 2-10h -1, the mass ratio of water and petroleum hydrocarbon is 0.2:1-0.7:1.
In a specific embodiment, the catalyzer used in catalytic cracking reaction is made up of type ZSM 5 molecular sieve, tackiness agent and modified component.Wherein, the content of ZSM-5 molecular sieve is 20-80wt%, and tackiness agent is 20-70wt%, and modified component is 0.1-10wt%, and the content of preferred ZSM-5 molecular sieve is 40-70wt%, and tackiness agent is 25-55wt%, and modified component is 1-5wt%.Wherein tackiness agent is by SiO 2and/or Al 2o 3composition, modified component is made up of P and La series elements, and described phosphoric is selected from phosphoric acid and/or phosphoric acid salt, and La series elements is selected from its water-soluble salt.The element of modified component is introduced by pickling process, ion exchange method or mechanical mixing, and the shaping of catalyzer can adopt the ordinary methods such as extruded moulding.
(3) product of catalytic pyrolysis is carried out condensation, be separated and obtain gas phase and liquid product; Liquid product is carried out Aromatics Extractive Project, makes the content of aromatic hydrocarbons in remaining liquid product be reduced to below 10wt%, be preferably 4-8wt%.Described Aromatics Extractive Project is undertaken by the method for extracting rectifying aromatics separation from hydrocarbon mixture that utilizes of routine, as recorded in CN99107785.7, from hydrocarbon mixture, isolate benzene cut by prefractionation, benzene cut is passed into the bottom of extractive distillation column, solvent passes into from tower top.The rich solvent being rich in aromatic hydrocarbons of being discharged the bottom of extractive distillation column passes into solvent recovery tower, and overhead fraction obtains BTX aromatics after condensation, and the lean solvent of discharging at the bottom of tower is reintroduced back to the top recycle of extractive distillation column.
(4) liquid product remaining after Aromatics Extractive Project is sent into steam heat pyrolyzer, carry out the steam heat scission reaction of high cracking degree.
In a specific embodiment, the pyrolyzer that steam heat cracking can adopt reactor and process furnace to combine together carries out.Petroleum hydrocarbon and water liquid flow through in radiating furnace tube, and heat is passed to material in pipe through the tube wall of radiating furnace tube by stack gas, the furnace wall radiation heating of the outer thermal-flame by fuel combustion of pipe, generation, and scission reaction is carried out under high temperature in pipe, catalyst-free in pipe.Simultaneously for reducing petroleum hydrocarbon dividing potential drop, mostly adopting the mode adding dilution steam generation (as diluting water) to impel reaction to carry out towards the direction of cracking petroleum hydrocarbon at present, being therefore called steam heat cracking.
In a specific embodiment, the temperature of reaction of described steam heat cracking is 780-860 DEG C, and the residence time is 0.1-0.3s, and the mass ratio of water and petroleum hydrocarbon is 0.3:1-0.6:1.Preferable reaction temperature is 820-850 DEG C, and the residence time is 0.2-0.3s, and the mass ratio of water and petroleum hydrocarbon is 0.4:1-0.6:1.Because the water introduced in step (1) has entered in gas-phase product when step (3), therefore need to input water vapour in steam heat pyrolyzer, ensured the mass ratio of water and petroleum hydrocarbon.
(5) product of steam heat cracking is carried out condensation, be separated and obtain gas phase and liquid product.
Gas phase separation and liquid phase separation can adopt the conventional equipment in existing steam heat cracking technology to carry out.The gas-phase product that the gas-phase product obtain described catalytic pyrolysis and steam heat cracking obtain carries out gas phase separation, obtains the mixture comprising ethene, propylene and C4 hydro carbons; Steam heat cracking liquid product as requested, can carry out liquid phase separation, obtains the oil product of aromatic hydrocarbons and different fractions.
The invention provides a kind of liquid condition petroleum hydrocarbon cleavage method improving propylene and aromatics yield, compared with the direct method of petroleum hydrocarbon being carried out to steam cracking of industrial routine, described method is by first carrying out catalytic pyrolysis to petroleum hydrocarbon, condensation separation obtains gas phase and liquid product, carries out steam heat cracking further after then carrying out part Aromatics Extractive Project to liquid product.On the basis ensureing higher yield of ethene, reach the object improving propylene and aromatics yield.Specifically on the ethene identical with steam heat cracking+propene yield basis, propene yield improves more than 5 percentage points; Aromatics yield improves more than 3 percentage points; Methane yield reduces by more than 3 percentage points.There is the advantage that technique is simple, reaction conditions is gentle, with low cost.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the liquid condition petroleum hydrocarbon cleavage method of raising propylene of the present invention and aromatics yield.
Embodiment
In the present invention, described air speed is the feed throughput in the unit time, on unit catalyst.If inlet amount and catalytic amount all calculate with weight unit, be called weight space velocity.
As shown in Figure 1, first the liquid condition petroleum hydrocarbon and water for the treatment of cracking are introduced preheater, in preheater, carry out preheating vaporization and mix, then the thermal evaporation gas that obtains in advance being sent into catalytic cracking reaction device, under the effect of catalyzer, carry out the catalytic cracking reaction of low cracking degree.The effluent of catalytic cracking reaction device is separated into gas phase and liquid product through condensing works 1.Gas-phase product flows out from condensing works 1 top and enters gas phase separation device; Liquid product flows out and enters aromatic extraction unit and carry out Aromatics Extractive Project bottom condensing works 1, aromaticity content is reduced to a certain degree, enters steam heat pyrolyzer and carry out steam heat scission reaction.The effluent of steam heat pyrolyzer, through condensing works 2, is again separated and obtains gas phase and liquid product.The gas-phase product of the steam heat cracking that condensing works 2 top is flowed out enters gas phase separation device; The steam heat cracking liquid product flowed out bottom condensing works 2 enters liquid phase separating device and is separated.By the gas-phase product of catalytic pyrolysis and steam heat cracking gained after gas phase separation device, obtain ethene, propylene and C4 hydrocarbon product.Steam heat cracking liquid product as required, can enter liquid phase separating device, obtains the oil product of aromatic hydrocarbons and different fractions.
Embodiment 1
Catalyzer used consists of: ZSM-5 molecular sieve 60wt%, P element 5wt%, La element 1wt%, Al 2o 334wt%.ZSM-5 molecular sieve and Al 2o 3extruded moulding, introduces modifying element by pickling process.
The inlet amount of petroleum naphtha is 100g, consists of: normal paraffin 30.92wt%, isoparaffin 28.63wt%, naphthenic hydrocarbon 31.25wt%, aromatic hydrocarbons 8.09wt%.
By petroleum naphtha and water heat vaporized respectively through preheater, enter catalytic cracking reaction device.Temperature of reaction be 580 DEG C, weight space velocity is 4h -1, water and petroleum naphtha mass ratio be carry out catalytic pyrolysis under the condition of 0.3:1.The distribution of catalytic cracking reaction device effluent is in table 1.
Table 1 catalytic cracking reaction device effluent distributes
Catalytic pyrolysis effluent enters condensing works 1, and condensation is also separated into gas phase and liquid product.Gas-phase product enters gas phase separation device, is separated and obtains methane, ethene, propylene, ethane, propane, C4 hydrocarbon.The liquid product obtained mainly carbonatoms is more than or equal to the hydrocarbons (C5+) of 5, liquid product is passed into aromatic extraction unit, extracting part aromatic hydrocarbons wherein, the content making to enter aromatic hydrocarbons in the petroleum naphtha of steam heat pyrolyzer is 6wt%, extracts C6 ~ C8 aromatic hydrocarbons of 13.99 grams thus.The liquid product remaining 57.05 grams enters steam heat pyrolyzer.
The best steam heat cracking condition of petroleum naphtha is selected to react: temperature of reaction is 840 DEG C, the mass ratio of residence time 0.22s, water and petroleum naphtha is 0.5:1.The distribution of steam heat pyrolyzer effluent is in table 2.
Table 2 steam heat pyrolyzer effluent distributes
By the product of steam heat pyrolyzer through condensing works 2, be separated and obtain gas phase and liquid product.Gas-phase product enters gas phase separation device, and steam heat cracking c5+liquid product enters liquid phase separating device.Extracting accounts for C6 ~ C8 aromatic hydrocarbons of liquid product 40wt% weight, and residue C5+ uses as oil product.The final product distribution that raw material petroleum naphtha obtains through method provided by the invention in table 3, C6 ~ C8 aromatic hydrocarbons be wherein adding of obtaining of twice extracting and.
Table 3 final product distribution (% by weight)
Comparative example 1
Steam heat scission reaction is carried out in steam heat pyrolyzer.Select the best crack reacting condition of petroleum naphtha: 840 DEG C, 0.125MPa, residence time 0.24s, the mass ratio of water and petroleum naphtha is 0.5:1.Extracting accounts for C6 ~ C8 aromatic hydrocarbons of liquid product 40% weight, and residue C5+ uses as oil product.Final product distribution is in table 3.
Because propane can to obtain the propylene of 80% through dehydrogenating propane device.Therefore the propane obtained in embodiment 1 can make the propene yield of embodiment 1 become 23.25% after dehydrogenating propane.Embodiment 1 and comparative example 1 are contrasted by table 3, known liquid condition petroleum hydrocarbon cleavage method provided by the invention has following characteristics:
(1) ethene+propene yield is close, but propene yield improves nearly 9 percentage points;
(2) aromatics yield improves nearly 8 percentage points;
(3) C5+ oil product and C6 ~ C8 aromatic hydrocarbons sum almost do not change;
(4) methane yield reduces nearly 4 percentage points;
(5) divinyl reduces nearly 2 percentage points, but the no change of C4 total amount.
Embodiment 2
Catalyst weight consists of: ZSM-5 molecular sieve 70%, P element 4.5%, La element 1.5%, Al 2o 312%, SiO 212%.ZSM-5 molecular sieve and Al 2o 3extruded moulding, introduces modifying element by pickling process.Petroleum naphtha and technical process are with embodiment 1.
By petroleum naphtha and water heat vaporized respectively through preheater, enter catalytic cracking reaction device.Temperature of reaction be 550 DEG C, weight space velocity is 2h -1, water and petroleum naphtha mass ratio be carry out catalytic pyrolysis under the condition of 0.3:1.The distribution of catalytic cracking reaction device effluent is in table 4.
Table 4 catalytic cracking reaction device effluent distributes
Catalytic pyrolysis effluent enters condensing works 1, and condensation is also separated into gas phase and liquid product.Gas-phase product enters gas phase separation device, is separated and obtains methane, ethene, propylene, ethane, propane, C4 hydrocarbon.The liquid product obtained mainly carbonatoms is more than or equal to the hydrocarbons (C5+) of 5, liquid product is passed into aromatic extraction unit, extracting part aromatic hydrocarbons wherein, the content making to enter aromatic hydrocarbons in the petroleum naphtha of steam heat pyrolyzer is 6wt%, extracts C6 ~ C8 aromatic hydrocarbons of 10.65 grams thus.The liquid product remaining 61.14 grams enters steam heat pyrolyzer.
The best steam heat cracking condition of petroleum naphtha is selected to react: temperature of reaction is 840 DEG C, the mass ratio of 0.125MPa, residence time 0.24s, water and petroleum naphtha is 0.5:1.The distribution of steam heat pyrolyzer effluent is in table 2.
By the product of steam heat pyrolyzer through condensing works 2, be separated and obtain gas phase and liquid product.Gas-phase product enters gas phase separation device, and steam heat cracking c5+liquid product enters liquid phase separating device.Extracting accounts for C6 ~ C8 aromatic hydrocarbons of liquid product 40wt% weight, and residue C5+ uses as oil product.The final product distribution that raw material petroleum naphtha obtains through method provided by the invention in table 5, C6 ~ C8 aromatic hydrocarbons be wherein adding of obtaining of twice extracting and.
Table 5 final product distribution (% by weight)
Propane, after dehydrogenating propane device, makes the propene yield of embodiment 2 reach 22.385%.Like this, embodiment 1 and comparative example 1 are contrasted by table 5, known liquid condition petroleum hydrocarbon cleavage method provided by the invention has following characteristics:
(1) ethene+propene yield is close, and propene yield improves 7 percentage points;
(2) C6 ~ C8 aromatics yield improves 5 percentage points;
(3) C5+ oil product and C6 ~ C8 aromatic hydrocarbons sum reduce by 2 percentage points;
(4) methane yield reduces nearly 4 percentage points;
(5) divinyl reduces nearly 2 percentage points, and C4 total amount improves 3 percentage points.
Embodiment 3
Catalyst weight consists of: ZSM-5 molecular sieve 66%, P element 3%, La element 2%, Al 2o 310%, SiO 219%.ZSM-5 molecular sieve and Al 2o 3extruded moulding, introduces modifying element by pickling process.
Treat that the liquid condition petroleum hydrocarbon of cracking is hydrogenation tail oil, its weight consists of: paraffinic hydrocarbons 70.0%, a naphthenic hydrocarbon 13.1%, bicyclic alkane 9.0%, three naphthenic hydrocarbon 3.1%, Fourth Ring alkane 2.0%, five rings alkane 0.7%, alkylbenzene 2.1%.Cleavage method is with embodiment 1.
By hydrogenation tail oil and water heat vaporized respectively through preheater, enter catalytic cracking reaction device.Temperature of reaction be 520 DEG C, weight space velocity is 2h -1, water and hydrogenation tail oil mass ratio be carry out catalytic pyrolysis under the condition of 0.2:1.The distribution of catalytic cracking reaction device effluent is in table 6.
Table 6 catalytic cracking reaction device effluent distributes
Catalytic pyrolysis effluent enters condensing works 1, and condensation is also separated into gas phase and liquid product.Gas-phase product enters gas phase separation device, is separated and obtains methane, ethene, propylene, ethane, propane, C4 hydrocarbon.The liquid product obtained mainly carbonatoms is more than or equal to the hydrocarbons (C5+) of 5, liquid product is passed into aromatic extraction unit, extracting part aromatic hydrocarbons wherein, the content making to enter aromatic hydrocarbons in the petroleum naphtha of steam heat pyrolyzer is 6wt%, extracts C6 ~ C8 aromatic hydrocarbons of 5.77 grams thus.The liquid product remaining 66.02 grams enters steam heat pyrolyzer.
The best steam heat cracking condition of hydrogenation tail oil is selected to react: temperature of reaction is 810 DEG C, the mass ratio of 0.08MPa, residence time 0.23s, water and hydrogenation tail oil is 0.75:1.The distribution of steam heat pyrolyzer effluent is in table 7.
Table 7 steam heat pyrolyzer effluent distributes
By the product of steam heat pyrolyzer through condensing works 2, be separated and obtain gas phase and liquid product.Gas-phase product enters gas phase separation device, and steam heat cracking c5+liquid product enters liquid phase separating device.Extracting accounts for C6 ~ C8 aromatic hydrocarbons of liquid product 30wt% weight, and residue C5+ uses as oil product.The final product distribution that raw material hydrogenation tail oil obtains through method provided by the invention in table 8, C6 ~ C8 aromatic hydrocarbons be wherein adding of obtaining of twice extracting and.
Table 8 final product distribution (% by weight)
Comparative example 2
The steam heat scission reaction of hydrogenation tail oil is carried out in steam heat pyrolyzer.Select best crack reacting condition: temperature of reaction is 810 DEG C, the mass ratio of 0.08MPa, residence time 0.23s, water and hydrogenation tail oil is 0.75:1.Extracting accounts for C6 ~ C8 aromatic hydrocarbons of liquid product 30% weight, and residue C5+ uses as oil product.Final product distribution is in table 8.
The propane that embodiment 3 obtains can make the propene yield of embodiment 3 become 24.57% after dehydrogenating propane.Embodiment 3 and comparative example 2 are contrasted by table 8, known liquid condition petroleum hydrocarbon cleavage method provided by the invention has following characteristics:
(1) ethene+propene yield improves 2 percentage points, and propene yield improves 8 percentage points;
(2) C6 ~ C8 aromatics yield improves 3 percentage points;
(3) methane yield reduces by 3 percentage points;
(4) divinyl reduces by 2 percentage points, and C4 total amount improves 2 percentage points;
(5) C5+ oil product and aromatic hydrocarbons sum reduce by 4 percentage points.
Therefore, use liquid condition petroleum hydrocarbon cleavage method provided by the invention, the ethene in product and propene yield can be improved, especially propene yield.To the C6 ~ C8 aromatic hydrocarbons in product, there is good recovering effect simultaneously.
It should be noted that above-described embodiment only for explaining the present invention, not forming any limitation of the invention.By referring to exemplary embodiments, invention has been described, but to should be understood to word wherein used be descriptive and explanatory vocabulary, instead of limited vocabulary.Can modify the present invention by the scope being defined in the claims in the present invention, and the present invention be revised not deviating from scope and spirit of the present invention.Although the present invention wherein described relates to specific method, material and embodiment, and do not mean that the present invention is limited to particular case disclosed in it, on the contrary, easily extensible of the present invention is to other all methods and applications with identical function.

Claims (10)

1. one kind is improved the liquid condition petroleum hydrocarbon cleavage method of propylene and aromatics yield, described method comprises carries out catalytic pyrolysis by petroleum hydrocarbon, the liquid product of catalytic pyrolysis is carried out Aromatics Extractive Project, then liquid product remaining after Aromatics Extractive Project is carried out steam heat cracking.
2. method according to claim 1, is characterized in that, catalytic pyrolysis raw material comprises petroleum hydrocarbon and water, and the temperature of reaction of described catalytic pyrolysis is 450-700 DEG C, and reaction pressure is 0.001-0.3MPa, and weight space velocity is 1-20h -1, the mass ratio of water and petroleum hydrocarbon is 0.1:1-1:1.
3. method according to claim 2, is characterized in that, the temperature of reaction of described catalytic pyrolysis is 550-650 DEG C, and weight space velocity is 2-10h -1, the mass ratio of water and petroleum hydrocarbon is 0.2:1-0.7:1.
4. the method according to any one of claim 1-3, is characterized in that, the catalyzer that described catalytic cracking reaction uses is made up of type ZSM 5 molecular sieve, tackiness agent and modified component.
5. method according to claim 4, is characterized in that, described tackiness agent is by SiO 2and/or Al 2o 3composition, modified component is made up of P and La series elements.
6. the method according to claim 4 or 5, is characterized in that, the content of described ZSM-5 molecular sieve is 40-70wt%, and tackiness agent is 25-55wt%, and modified component is 1-5wt%.
7. method according to claim 1, is characterized in that, in liquid product remaining after Aromatics Extractive Project, the content of aromatic hydrocarbons is reduced to below 10wt%, preferred 4-8wt%.
8. method according to claim 1, is characterized in that, the temperature of reaction of described steam heat cracking is 780-860 DEG C, and the residence time is 0.1-0.3s, and the mass ratio of water and petroleum hydrocarbon is 0.3:1-0.6:1.
9. method according to claim 8, is characterized in that, the temperature of reaction of described steam heat cracking is 820-850 DEG C, and the residence time is 0.2-0.3s, and the mass ratio of water and petroleum hydrocarbon is 0.4:1-0.6:1.
10. method according to claim 1, is characterized in that, the gas-phase product that the gas-phase product obtain described catalytic pyrolysis and steam heat cracking obtain carries out gas phase separation, obtains the mixture comprising ethene, propylene and C4 hydro carbons; Steam heat cracking liquid product carries out liquid phase separation, obtains the oil product of aromatic hydrocarbons and different fractions.
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Publication number Priority date Publication date Assignee Title
CN105349179A (en) * 2015-10-28 2016-02-24 中国石油大学(华东) Combined process of heavy petroleum hydrocarbon catalytic cracking and light petroleum hydrocarbon steam cracking
CN109957421A (en) * 2017-12-25 2019-07-02 中国石油天然气股份有限公司 Combination method of catalytic cracking and light hydrocarbon deep processing

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CN102344832A (en) * 2010-07-29 2012-02-08 中国石油化工股份有限公司 Catalytic conversion method for petroleum hydrocarbon

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CN1721510A (en) * 2004-07-14 2006-01-18 中国石油化工股份有限公司 Method and device for preparing low carbon olefine and arene
CN102344832A (en) * 2010-07-29 2012-02-08 中国石油化工股份有限公司 Catalytic conversion method for petroleum hydrocarbon

Cited By (4)

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Publication number Priority date Publication date Assignee Title
CN105349179A (en) * 2015-10-28 2016-02-24 中国石油大学(华东) Combined process of heavy petroleum hydrocarbon catalytic cracking and light petroleum hydrocarbon steam cracking
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CN109957421A (en) * 2017-12-25 2019-07-02 中国石油天然气股份有限公司 Combination method of catalytic cracking and light hydrocarbon deep processing
CN109957421B (en) * 2017-12-25 2021-01-01 中国石油天然气股份有限公司 Combination method of catalytic cracking and light hydrocarbon deep processing

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