CN102268286A - C4 hydrocarbon catalytic splitting and heavy oil catalytic cracking combined technology and device - Google Patents
C4 hydrocarbon catalytic splitting and heavy oil catalytic cracking combined technology and device Download PDFInfo
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- CN102268286A CN102268286A CN2010101887743A CN201010188774A CN102268286A CN 102268286 A CN102268286 A CN 102268286A CN 2010101887743 A CN2010101887743 A CN 2010101887743A CN 201010188774 A CN201010188774 A CN 201010188774A CN 102268286 A CN102268286 A CN 102268286A
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- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 98
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 68
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 47
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 47
- 239000000295 fuel oil Substances 0.000 title claims abstract description 41
- 238000005516 engineering process Methods 0.000 title abstract description 20
- 230000003197 catalytic effect Effects 0.000 title abstract description 9
- 239000003054 catalyst Substances 0.000 claims abstract description 80
- 238000006243 chemical reaction Methods 0.000 claims abstract description 68
- 238000011069 regeneration method Methods 0.000 claims abstract description 24
- 230000008929 regeneration Effects 0.000 claims abstract description 23
- 239000003921 oil Substances 0.000 claims description 43
- 238000000034 method Methods 0.000 claims description 41
- 238000007233 catalytic pyrolysis Methods 0.000 claims description 17
- 238000004231 fluid catalytic cracking Methods 0.000 claims description 13
- 239000003795 chemical substances by application Substances 0.000 claims description 12
- 238000009826 distribution Methods 0.000 claims description 10
- 238000007086 side reaction Methods 0.000 claims description 6
- 230000008676 import Effects 0.000 claims description 5
- 238000004230 steam cracking Methods 0.000 claims description 5
- 239000000376 reactant Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 230000035484 reaction time Effects 0.000 claims description 3
- 238000001311 chemical methods and process Methods 0.000 claims description 2
- 238000007670 refining Methods 0.000 claims description 2
- 150000001336 alkenes Chemical class 0.000 claims 1
- HQQADJVZYDDRJT-UHFFFAOYSA-N ethene;prop-1-ene Chemical group C=C.CC=C HQQADJVZYDDRJT-UHFFFAOYSA-N 0.000 abstract 1
- 238000004064 recycling Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 23
- 238000005336 cracking Methods 0.000 description 20
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 16
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 14
- 229910021536 Zeolite Inorganic materials 0.000 description 5
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 5
- 239000002808 molecular sieve Substances 0.000 description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 239000010457 zeolite Substances 0.000 description 5
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 4
- 238000005243 fluidization Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 229910052698 phosphorus Inorganic materials 0.000 description 4
- 239000011574 phosphorus Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 239000005977 Ethylene Substances 0.000 description 3
- 238000010168 coupling process Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000002708 enhancing effect Effects 0.000 description 3
- 239000002010 green coke Substances 0.000 description 3
- 229910052761 rare earth metal Inorganic materials 0.000 description 3
- 150000002910 rare earth metals Chemical class 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- CZXDHMZKNAOPHQ-VOTSOKGWSA-N [(5e)-10-propyltrideca-5,9-dienyl] acetate Chemical compound CCCC(CCC)=CCC\C=C\CCCCOC(C)=O CZXDHMZKNAOPHQ-VOTSOKGWSA-N 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910021417 amorphous silicon Inorganic materials 0.000 description 1
- 238000005844 autocatalytic reaction Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 229910001657 ferrierite group Inorganic materials 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000002075 main ingredient Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 235000012976 tarts Nutrition 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a C4 hydrocarbon catalytic splitting and heavy oil catalytic cracking combined technology and a device. The C4 hydrocarbon catalytic splitting and heavy oil catalytic cracking combined technology and the device are characterized mainly in that C4 hydrocarbon catalytic splitting and a heavy oil catalytic cracking reaction reclaiming technology are combined; an ancillary regenerator is arranged in a dense section of a main regenerator; a C4 hydrocarbon catalytic splitting catalyst needing to be regenerated enters into the ancillary regenerator, is mixed with a high temperature catalytic cracking semi-regenerated catalyst entering into the ancillary regenerator and undergoes a regeneration reaction; and a large proportion of a regenerated catalytic cracking catalyst returns back to the main regenerator and a regenerated C4 splitting catalyst and a small quantity of the regenerated catalytic cracking catalyst enter into a C4 hydrocarbon catalytic splitting reactor for recycling. Through the C4 hydrocarbon catalytic splitting and heavy oil catalytic cracking combined technology and the device, excess heat from a heavy oil catalytic cracking device is utilized for a C4 hydrocarbon catalytic splitting reaction process which does not get enough heat, thus a yield of ethylene propylene is increased.
Description
Technical field
The invention belongs to the catalyzed conversion field of petroleum hydrocarbon, specifically, relate to heavy oil catalytic cracking process and C
4The COMBINED PROCESS of hydrocarbon catalytic pyrolysis process particularly relates to a kind of pair of reaction double catalyst regeneration system and efficiently makes up fluidized catalytic reaction technology and device.
Background technology
Propylene is one of important petrochemical complex basic material.In recent years, the demand to propylene in the world wide increases day by day, and the source of propylene mainly contains: the by product of ethylene plant's steam cracking (accounting for 68%), catalytic cracking by product (accounting for 29%), dehydrogenating propane etc. (3%).The main raw material of steam cracking is a petroleum naphtha, has the problem that there is lack of raw materials; And the conventional yield of the propylene of fluidized catalytic cracker by-product has only 3%～6%, and therefore, the method that traditional ethene coproduction and refinery reclaim propylene has been difficult to satisfy its growing demand.
On the other hand, China C
4The hydro carbons resource is abundanter.But at present to C
4The utilization ratio of hydro carbons is also lower, and as the industrial chemicals, major part is used as industry and domestic fuel except that partly.Along with improving constantly of China's ethylene production and crude capacity, the C that steam cracking device and catalytic cracking unit are a large amount of with by-product
4Hydrocarbon; In addition China " smooth implementation of West-east Gas plan, acting as a fuel, (main ingredient is C to the liquefied gas that uses
4Hydro carbons) will seriously devalue, this will bring huge impact and challenge to petroleum chemical enterprise.
C in recent years grew up
4Hydrocarbon catalytic cracking system propylene technology is for making full use of C
4Resource and propylene enhancing provide a valid approach.C
4The main utilization of hydrocarbon catalytic cracking system propylene reaction has unique shape selectivity and tart ZSM-5 molecular sieve catalyst, with C
4The hydro carbons highly selective is converted into propylene.The domestic and international at present C that develops
4Hydrocarbon catalytic cracking is produced propylene technology fixed-bed process and fluidized-bed process, and the representational technology of fixed-bed process has the Propylur technology of Lurgi company, the OCP technology of Uop Inc., the Omega technology of company of Asahi Chemical Industry; The technology of fluidized-bed process has the MOI technology of KBR Corporation's Super flex technology and Exxon/Mobil company.
In the fixed-bed process, reaction process and catalyst regeneration process are intermittently carried out in same reactor in turn, and for heat being provided for reaction process and catalyst regeneration process, need to set up heating unit in the reactor, therefore, there is the shortcoming of conversion unit complex structure and production poor continuity in fixed-bed process.
With respect to fixed-bed process, advantage such as fluidized-bed process has that the raw material treatment capacity is big, gas-solid full contact, reaction regeneration can carry out continuously, thus receive much concern.Studies show that fluidized-bed C
4The temperature of reaction of hydrocarbon catalytic cracking reaction process is mostly at 450～650 ℃, and be endothermic process, because process green coke amount lower (about 1.5～2.0%), be difficult to keep corresponding temperature of reaction and regeneration and burn needed regeneration temperature, during these technological process isolated operations, all need take the concurrent heating measure.
On the other hand, conventional heavy oil catalytic cracking process is because the raw material slag-mixing amount is increasing, and the green coke amount is up to 8～10%.For conventional catalytic cracking unit, under the situation that operating parameterss such as temperature of reaction, reaction heat and regeneration temperature are determined, the green coke amount of maintenance process heat balance operation is about 6%, and therefore, the heat of conventional catalytic cracking process is superfluous.If with C
4Hydrocarbon catalytic cracking propylene enhancing technology and conventional heavy oil catalytic cracking process effectively are coupled, and the superfluous heat that utilizes heavy oil catalytic cracking process is as C
4The origin of heat of hydrocarbon catalytic cracking technological process with the more shared large-scale general facilities facilities of catalytic cracking unit, can improve C simultaneously greatly
4The competitive edge of hydrocarbon catalytic cracking propylene enhancing technology.
CN1624078A discloses a kind of dual catalyst system, coupled process of regenerating, utilizes the special-purpose catalyst of pyritous catalytic cracking regenerated catalyst heating novel process process and make its regeneration in secondary revivifier; CN1626623A discloses a kind of pair of reaction-regeneration system multiple-effect coupling fluidized catalytic reaction processing method, and the high-temperature flue gas of catalytic cracking regenerator is introduced the special-purpose catalyst of secondary revivifier heating novel process process and made its regeneration; But CN1624078A and CN1626623A technology all need be set up and be used for the secondary revivifier of special-purpose catalyst regenerated, cause facility investment to increase, and floor space are big.CN1935349A discloses a kind of gas-solid fluidization Coupling device and has utilized this equipment to carry out the mixing of big-difference particle multistage, heat exchange, reaction, fractionated coupling process, but equipment is comparatively complicated.USP7491315 discloses a kind of duo-lift tube reactor C
4The processing method of cracking and heavy oil cracking, but the USP7491315 technology is because C
4Cracking and heavy oil cracking are adopted with a kind of catalyzer, and the selectivity of second propylene is lower.
Summary of the invention
The object of the present invention is to provide a kind of C
4The combination process of hydrocarbon catalytic pyrolysis and heavy oil fluid catalytic cracking and device are the C of shortage of heat with the superfluous heat with heavy oil catalytically cracking equipment
4Hydrocarbon catalytic cracking reaction process is used, increasing output of ethylene and propylene.The present invention also provides and has been used for C
4The device of the combination process of hydrocarbon catalytic pyrolysis and heavy oil fluid catalytic cracking.Main reactor of the present invention is conventional heavy oil catalytically cracking equipment, and the conventional heavy oil catalytically cracking equipment is set up another independent C that is used for
4The fluidizing reactor of hydrocarbon catalytic cracking reaction, two cover fluidization reaction units adopt special catalyzer separately, C simultaneously
4The hydrocarbon catalytic cracking catalyst has notable difference with catalytic cracking catalyst on rerum naturas such as size-grade distribution, density and/or shape.
The invention provides a kind of C
4The combination process of hydrocarbon catalytic pyrolysis and heavy oil fluid catalytic cracking is characterized in that comprising the steps:
Heavy raw oil enters the heavy oil fluid catalytic cracking riser reactor, with the catalytic cracking regenerated catalyst contact reacts of coming autonomous revivifier, reactant flow is carried out separating of spent catalytic cracking catalyst and main reaction oil gas, isolated spent catalytic cracking catalyst is regenerated through the laggard close phase section of becoming owner of revivifier of stripping, part catalytic cracking half regenerated catalyst in the close phase section of main revivifier enters secondary revivifier, return the heavy oil fluid catalytic cracking riser reactor after the other parts regeneration and recycle, isolated main reaction oil gas enters fractionating system to be separated.
C
4Hydrocarbon feed oil enters C
4Hydrocarbon catalytic cracking reaction device carries out contact reacts with catalytic cracking catalyst from secondary revivifier, and this pair revivifier is arranged in the close phase section of main revivifier, and what reactant flow was carried out catalytic pyrolysis reclaimable catalyst and side reaction oil gas separates isolated C
4Hydrocarbon catalytic pyrolysis reclaimable catalyst enters secondary revivifier, and regenerates after catalytic cracking half regenerated catalyst that enters secondary revivifier mixes, and the most of catalytic cracking catalyst after the regeneration is got back to main revivifier, the C after the regeneration
4The hydrocarbon catalytic cracking catalyst enters C with a small amount of catalytic cracking catalyst
4Hydrocarbon catalytic cracking reaction device recycles, and isolated side reaction oil gas mixes with main reaction oil gas or enters fractionating system separately.
The present invention is further characterized in that: the reaction conditions in the heavy oil fluid catalytic cracking riser reactor is: temperature of reaction is 460～560 ℃, and agent weight of oil ratio is 2～10, and the reaction times is 1.0～6.0s, and reaction pressure is 0.1～0.4MPa.
The present invention is further characterized in that: the reaction conditions in the catalytic cracking reaction device is: temperature of reaction is 450～750 ℃, water vapor and C
4The weight ratio of hydrocarbon feed oil is 0.01～1, and weight hourly space velocity is 1～150hr
-1, reaction pressure is 0.03～0.4MPa, C
4Hydrocarbon catalytic cracking catalyst and C
4The weight ratio of hydrocarbon feed oil is 2～150: 1.
The present invention is further characterized in that: the regeneration temperature in the secondary revivifier is 550～750 ℃, and the time of burning is 1.0～20min, and superficial gas velocity is 0.5～2.5m/s, and pressure is 0.1～0.4Mpa.
The invention provides a kind of C
4The device of hydrocarbon catalytic pyrolysis and heavy oil fluid catalytic cracking combination process, this device comprise heavy oil catalytic cracking reaction device, main revivifier, C
4Hydrocarbon catalytic cracking reaction device and secondary revivifier, it is characterized in that: secondary revivifier is arranged at the close phase section of main revivifier, comprise vertically disposed cylindrical shell, the bottom of cylindrical shell is a lower cover, the side of cylindrical shell is provided with the catalyst for heavy oil catalytic cracking import, the inside of cylindrical shell is provided with the back taper gas distribution grid, and the top of gas distribution grid is with the fluidized bed body lower end closed of secondary revivifier, and the bottom connects C
4Hydrocarbon catalytic cracking catalyst outlet pipe, gas distribution grid, C
4The part cylindrical shell of hydrocarbon catalytic cracking catalyst outlet pipe, gas-solid fluidized bed body and lower cover surround a closed space, and the cylindrical shell of this closed space correspondence is provided with the fluidizing agent inlet tube that is used to introduce fluidizing agent.
C of the present invention
4C in the hydrocarbon feed oil
4Olefin(e) centent is greater than 50 weight %, described C
4Hydrocarbon feed oil is from the C of autocatalysis cracking unit
4Cut also can be the C from other catalytic cracking unit and steam cracking device
4Cut can also be the C that other oil refining and/or chemical process are produced
4Cut.
The present invention compared with prior art has following effect:
1, the present invention is the C of shortage of heat with the superfluous heat of heavy oil catalytically cracking equipment
4The hydrocarbon catalytic cracking reaction process is used, and utilizes other general facilities devices of heavy oil catalytically cracking equipment; The Btu utilization mode is reasonable, the regeneration efficiency height.
2, present device is simple, floor space is little, less investment.
3, second of the present invention, propene yield height, selectivity is good.
The present invention is described in detail below in conjunction with the drawings and specific embodiments, but do not limit the scope of the invention.
Accompanying drawing and description of drawings
Accompanying drawing is a kind of process flow sheet of the present invention.
Among the figure: 1-heavy oil catalytically cracking equipment, 2-heavy raw oil, 3-riser reactor, 4-gas-solid separating device, 5-master's turboseparator, 6-main reaction oil gas, 7-master's settling vessel, 8-master's stripping stage, the close phase of 9-master's revivifier, 10-master's revivifier, the secondary revivifier of 11-, 12-cylindrical shell, 13-C
4The catalyst for cracking outlet pipe, the import of 14-catalyst for heavy oil catalytic cracking, the 15-gas distribution grid, the 16-lower cover, 17-fluidizing agent inlet tube, the 18-fluidizing agent, 19-inclined tube to be generated, the 20-regenerator sloped tube, 21-catalyzer standpipe, 22-promotes steam, 23-C
4Hydrocarbon catalytic cracking reaction device, 24-catalytic cracking reaction bed, 25-C
4Hydrocarbon feed oil, the secondary stripping stage of 26-, 27-stripped vapor, the secondary settling section of 28-, 30-side reaction oil gas.
Embodiment
As shown in the figure, the heavy raw oil 2 that contains atomizing steam enters the riser reactor 3 of heavy oil catalytically cracking equipment 1 from the bottom, with the high-temperature catalytic cracking regenerated catalyst that comes autonomous revivifier 10 be 460～560 ℃ in temperature of reaction, the heavy raw oil preheating temperature is 150～300 ℃, agent-oil ratio (weight ratio of riser reactor 3 catalytic cracking catalysts and heavy raw oil) is 2～10, catalyst activity is 50～70, reaction times is 1.0～6.0s, reaction pressure is to contact under the condition of 0.1～0.4MPa, gasification, mix and reaction, oil gas, water vapour passes through riser reactor 3 with catalyzer, the main cyclonic separator 5 that enters gas-solid separating device 4 and main settling vessel 7 successively separates, isolated main reaction oil gas 6 advances fractionating system, isolated reclaimable catalyst enters main settling vessel 7 and main stripping stage 8 successively, regenerate through the laggard close phase section 9 of main revivifier of becoming owner of revivifier 10 of stripping, the regenerated catalyst after the regeneration recycles.
Be provided for C in the close phase section 9 of the main revivifier of catalytic cracking master revivifier 10
4The secondary revivifier 11 of hydrocarbon catalytic cracking catalyst regenerated; This pair revivifier 11 comprises vertically disposed cylindrical shell 12, the bottom of cylindrical shell 12 is a lower cover 16, and the side is provided with catalyst for heavy oil catalytic cracking import 14, and the inside of cylindrical shell 12 is provided with back taper gas distribution grid 15, its top is with the fluidized bed body lower end closed of secondary revivifier 11, and the bottom connects C
4Catalyst for cracking outlet pipe 13 makes gas distribution grid 15, C
4Catalyst for cracking outlet pipe 13 surrounds a closed space with the part cylindrical shell and the lower cover 16 of fluidized bed body, and the cylindrical shell of this closed space correspondence is provided with the fluidizing agent inlet tube 17 that is used to introduce fluidizing agent 18.
The C that contains atomizing steam
4Hydrocarbon feed oil 25 enters C by shower nozzle
4The bottom of the catalytic cracking reaction bed 24 of hydrocarbon catalytic cracking reaction device 23 contacts, gasifies, mixes and react with catalytic cracking catalyst.Reaction conditions in the catalytic cracking reaction bed 24 is: temperature of reaction is 450～750 ℃, water vapor and C
4The weight ratio of hydrocarbon feed oil is 0.01～1, and weight hourly space velocity is 1～150hr
-1, reaction pressure is 0.03～0.4MPa, catalyzer and C
4The weight ratio of hydrocarbon feed oil is 2～150: 1.Reacted catalytic pyrolysis reclaimable catalyst enters C
4The secondary stripping stage 26 of hydrocarbon catalytic cracking reactor 23 carries out counter current contact with the stripped vapor of introducing 27, goes out catalytic pyrolysis reclaimable catalyst entrained oil gas with stripping.It is secondary revivifier 11 that catalytic pyrolysis reclaimable catalyst behind the stripping enters the fluidization regenerating unit by the inclined tube of newly establishing to be generated 19.Reacted oil gas enters C successively
4The secondary settling section 28 of hydrocarbon catalytic cracking reaction device 23 separates with the catalyzer that carries with secondary cyclonic separator 29, and side reaction oil gas 30 complete and catalyst separating leaves C
4Behind the hydrocarbon catalytic cracking reaction device 23, mix with main reaction oil gas 6 or enter fractionating system separately.
Enter the catalytic pyrolysis reclaimable catalyst of secondary revivifier 11, mix with the high temperature half regeneration catalyzing cracking catalyst that enters secondary revivifier 11 by catalyst for heavy oil catalytic cracking import 14, so that high temperature half regeneration catalyzing cracking catalyst provides heat for the catalytic pyrolysis reclaimable catalyst, two kinds of catalyzer mix under the fluidisation of the fluidizing agent of introducing by fluidizing agent inlet tube 17 (as air) 18, conduct heat, and it is 550～750 ℃ in temperature, the time of burning is 1.0～20min, superficial gas velocity is 0.5～2.5m/s, pressure is to burn reaction under the condition of 0.1～0.4Mpa, regenerated flue gas and most of catalytic cracking catalyst are got back to former catalytic cracking master revivifier 10 from the top of secondary revivifier 11, bottom at secondary revivifier 11, controlling flow wind transmission amount is by the effect of gravity catalytic cracking catalyst and C that rerum natura is different
4Catalyst for cracking separates, the C behind the high temperature regeneration
4Catalyst for cracking and a spot of conventional catalytic cracking catalyst are from the C of secondary revivifier 11 bottoms
4Catalyst for cracking outlet pipe 13 is discharged, and guides to the C that sets up through regenerator sloped tube 20
4The catalyzer standpipe 21 of hydrocarbon catalytic cracking reaction device 23 rises to C by promoting steam 22 by catalyzer standpipe 21 again
4Form catalytic cracking reaction bed 24 in the hydrocarbon catalytic cracking reactor 23, the last spout of catalyzer standpipe 21 is at the top of catalytic cracking reaction bed 24.
The used catalyst for heavy oil catalytic cracking of the present invention is conventional catalyst for heavy oil catalytic cracking, as amorphous silicon aluminium catalyzer or molecular sieve catalyst, wherein, the active ingredient of molecular sieve catalyst is to contain or do not contain Y type or HY type zeolite, the ultrastable Y that contains or do not contain rare earth and/or phosphorus, the ZSM-5 series zeolite of rare earth and/or phosphorus or have in the supersiliceous zeolite, β zeolite, ferrierite of five-membered ring structure one or more.
The C that the present invention is used
4Catalytic cracking catalyst is the type of the selecting molecular sieve catalyst of ZSM-5 series, its particle size range is 150～2000 μ m, wherein the ZSM-5 molecular sieve be modified molecular screen and not modified molecular screen all can, the used modifying element of modified zsm-5 zeolite is a phosphorus, or phosphorus and be selected from one or more metals in IIA family metal and the rare earth metal.
Claims (8)
1. C
4The combination process of hydrocarbon catalytic pyrolysis and heavy oil fluid catalytic cracking is characterized in that:
Heavy raw oil enters the heavy oil fluid catalytic cracking riser reactor, with the catalytic cracking regenerated catalyst contact reacts of coming autonomous revivifier, reactant flow is carried out separating of spent catalytic cracking catalyst and main reaction oil gas, isolated spent catalytic cracking catalyst is regenerated through the laggard close phase section of becoming owner of revivifier of stripping, part catalytic cracking half regenerated catalyst in the close phase section of main revivifier enters secondary revivifier, return the heavy oil fluid catalytic cracking riser reactor after the other parts regeneration and recycle, isolated main reaction oil gas enters fractionating system to be separated;
C
4Hydrocarbon feed oil enters C
4Hydrocarbon catalytic cracking reaction device carries out contact reacts with catalytic cracking catalyst from secondary revivifier, and this pair revivifier is arranged in the close phase section of main revivifier, and what reactant flow was carried out catalytic pyrolysis reclaimable catalyst and side reaction oil gas separates isolated C
4Hydrocarbon catalytic pyrolysis reclaimable catalyst enters secondary revivifier, and regenerates after catalytic cracking half regenerated catalyst that enters secondary revivifier mixes, and the most of catalytic cracking catalyst after the regeneration is got back to main revivifier, the C after the regeneration
4The hydrocarbon catalytic cracking catalyst enters C with a small amount of catalytic cracking catalyst
4Hydrocarbon catalytic cracking reaction device recycles, and isolated side reaction oil gas mixes with main reaction oil gas or enters fractionating system separately.
2. combination process according to claim 1, it is characterized in that: the reaction conditions in the described heavy oil fluid catalytic cracking riser reactor is: temperature of reaction is 460～560 ℃, agent weight of oil ratio is 2～10, and the reaction times is 1.0～6.0s, and reaction pressure is 0.1～0.4MPa.
3. combination process according to claim 1 is characterized in that: described C
4Reaction conditions in the hydrocarbon catalytic cracking reaction device is: temperature of reaction is 450～750 ℃, water vapor and C
4The weight ratio of hydrocarbon feed oil is 0.01～1, and weight hourly space velocity is 1～150hr
-1, reaction pressure is 0.03～0.4MPa, C
4Hydrocarbon catalytic cracking catalyst and C
4The weight ratio of hydrocarbon feed oil is 2～150: 1.
4. combination process according to claim 1 is characterized in that: the regeneration temperature in the described secondary revivifier is 550～750 ℃, and the time of burning is 1.0～20min, and superficial gas velocity is 0.5～2.5m/s, and pressure is 0.1～0.4Mpa.
5. combination process according to claim 1 is characterized in that: described C
4The particle size range of hydrocarbon catalytic cracking catalyst is 150～2000 μ m.
6. combination process according to claim 1 is characterized in that: described C
4Hydrocarbon feed oil is the C from self device, other catalytic cracking unit or steam cracking device
4Cut, or the C of other oil refining and/or chemical process production
4Cut.
7. according to claim 1 or 6 described combination procesies, it is characterized in that: described C
4C in the hydrocarbon feed oil
4The content of alkene is greater than 50 weight %.
8. C
4The device of hydrocarbon catalytic pyrolysis and heavy oil fluid catalytic cracking combination process, this device comprise heavy oil catalytic cracking reaction device, main revivifier, C
4Hydrocarbon catalytic cracking reaction device and secondary revivifier, it is characterized in that: secondary revivifier is arranged in the close phase section of main revivifier, comprise vertically disposed cylindrical shell, the bottom of cylindrical shell is a lower cover, the side of cylindrical shell is provided with the catalyst for heavy oil catalytic cracking import, the inside of cylindrical shell is provided with the back taper gas distribution grid, and the top of gas distribution grid is with the fluidized bed body lower end closed of secondary revivifier, and the bottom connects C
4Hydrocarbon catalytic cracking catalyst outlet pipe, gas distribution grid, C
4The part cylindrical shell of hydrocarbon catalytic cracking catalyst outlet pipe, fluidized bed body and lower cover surround a closed space, and the cylindrical shell of this closed space correspondence is provided with the fluidizing agent inlet tube that is used to introduce fluidizing agent.
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|---|---|---|---|
| CN2010101887743A CN102268286A (en) | 2010-06-02 | 2010-06-02 | C4 hydrocarbon catalytic splitting and heavy oil catalytic cracking combined technology and device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101887743A CN102268286A (en) | 2010-06-02 | 2010-06-02 | C4 hydrocarbon catalytic splitting and heavy oil catalytic cracking combined technology and device |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103509589A (en) * | 2012-06-26 | 2014-01-15 | 中国石油化工股份有限公司 | Light hydrocarbon oil catalytic conversion method |
| CN104419457A (en) * | 2013-09-09 | 2015-03-18 | 中石化洛阳工程有限公司 | Catalytic cracking method and device employing double lift pipes |
| CN104419458A (en) * | 2013-09-09 | 2015-03-18 | 中石化洛阳工程有限公司 | Catalytic cracking method and device |
| CN106147832A (en) * | 2015-04-20 | 2016-11-23 | 中国石化工程建设有限公司 | A kind of catalytic cracking selective reaction regeneration technology |
| CN114262624A (en) * | 2021-12-09 | 2022-04-01 | 中国石油大学(北京) | A method and device for coupling fluidized bed catalytic cracking with two-component particle catalyst |
| CN114606020A (en) * | 2020-12-09 | 2022-06-10 | 中国石油化工股份有限公司 | Ethylene and propylene production system and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103509589A (en) * | 2012-06-26 | 2014-01-15 | 中国石油化工股份有限公司 | Light hydrocarbon oil catalytic conversion method |
| CN103509589B (en) * | 2012-06-26 | 2015-07-29 | 中国石油化工股份有限公司 | A kind of Light hydrocarbon oil catalytic conversion method |
| CN104419457A (en) * | 2013-09-09 | 2015-03-18 | 中石化洛阳工程有限公司 | Catalytic cracking method and device employing double lift pipes |
| CN104419458A (en) * | 2013-09-09 | 2015-03-18 | 中石化洛阳工程有限公司 | Catalytic cracking method and device |
| CN104419457B (en) * | 2013-09-09 | 2016-05-11 | 中石化洛阳工程有限公司 | A kind of double lift pipe catalytic cracking method and device |
| CN104419458B (en) * | 2013-09-09 | 2016-06-08 | 中石化洛阳工程有限公司 | A kind of catalyst cracking method and device |
| CN106147832A (en) * | 2015-04-20 | 2016-11-23 | 中国石化工程建设有限公司 | A kind of catalytic cracking selective reaction regeneration technology |
| CN106147832B (en) * | 2015-04-20 | 2017-11-14 | 中国石化工程建设有限公司 | A kind of catalytic cracking selective reaction regeneration technology |
| CN114606020A (en) * | 2020-12-09 | 2022-06-10 | 中国石油化工股份有限公司 | Ethylene and propylene production system and method |
| CN114606020B (en) * | 2020-12-09 | 2024-01-12 | 中国石油化工股份有限公司 | Ethylene and propylene production system and method |
| CN114262624A (en) * | 2021-12-09 | 2022-04-01 | 中国石油大学(北京) | A method and device for coupling fluidized bed catalytic cracking with two-component particle catalyst |
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Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant after: China Petrochemical Group Corp. Co-applicant after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant before: China Petrochemical Group Corp. Co-applicant before: Luoyang Petrochemical Engineering Co., China Petrochemical Group |
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