CN109609175A - A kind of descending-bed reactor lighter hydrocarbons catalysis conversion method and its device - Google Patents
A kind of descending-bed reactor lighter hydrocarbons catalysis conversion method and its device Download PDFInfo
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- CN109609175A CN109609175A CN201910093273.8A CN201910093273A CN109609175A CN 109609175 A CN109609175 A CN 109609175A CN 201910093273 A CN201910093273 A CN 201910093273A CN 109609175 A CN109609175 A CN 109609175A
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 122
- 238000000034 method Methods 0.000 title claims abstract description 55
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 28
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 28
- 238000006555 catalytic reaction Methods 0.000 title claims abstract description 13
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 161
- 239000003054 catalyst Substances 0.000 claims abstract description 102
- 230000001172 regenerating effect Effects 0.000 claims abstract description 83
- 238000011069 regeneration method Methods 0.000 claims abstract description 32
- 230000008929 regeneration Effects 0.000 claims abstract description 31
- 239000000203 mixture Substances 0.000 claims abstract description 25
- 239000000571 coke Substances 0.000 claims abstract description 23
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 20
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 16
- 238000011084 recovery Methods 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 52
- 238000002156 mixing Methods 0.000 claims description 48
- 239000003502 gasoline Substances 0.000 claims description 41
- 239000007787 solid Substances 0.000 claims description 20
- 230000008569 process Effects 0.000 claims description 18
- 230000003197 catalytic effect Effects 0.000 claims description 16
- 239000012492 regenerant Substances 0.000 claims description 12
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 9
- 239000005977 Ethylene Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 9
- 238000005336 cracking Methods 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 7
- 238000013461 design Methods 0.000 claims description 6
- 239000002283 diesel fuel Substances 0.000 claims description 6
- 239000000446 fuel Substances 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims description 6
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 claims description 5
- 238000005457 optimization Methods 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 2
- 239000003546 flue gas Substances 0.000 claims description 2
- 238000002347 injection Methods 0.000 claims description 2
- 239000007924 injection Substances 0.000 claims description 2
- 239000003915 liquefied petroleum gas Substances 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 claims description 2
- 239000011555 saturated liquid Substances 0.000 claims description 2
- 238000010025 steaming Methods 0.000 claims description 2
- 238000005243 fluidization Methods 0.000 claims 1
- 239000004575 stone Substances 0.000 claims 1
- 239000000047 product Substances 0.000 description 24
- 150000001336 alkenes Chemical class 0.000 description 23
- 239000002994 raw material Substances 0.000 description 17
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 15
- 230000000694 effects Effects 0.000 description 12
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 12
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 12
- 230000003139 buffering effect Effects 0.000 description 11
- 238000000926 separation method Methods 0.000 description 9
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 7
- 238000009826 distribution Methods 0.000 description 7
- 229910052799 carbon Inorganic materials 0.000 description 6
- -1 ethylene, propylene Chemical group 0.000 description 6
- 230000035611 feeding Effects 0.000 description 6
- 230000001965 increasing effect Effects 0.000 description 6
- 230000004044 response Effects 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 238000009835 boiling Methods 0.000 description 5
- 230000035484 reaction time Effects 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000005899 aromatization reaction Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- 238000004227 thermal cracking Methods 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 3
- 238000005194 fractionation Methods 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 238000006317 isomerization reaction Methods 0.000 description 3
- 239000012263 liquid product Substances 0.000 description 3
- 230000005012 migration Effects 0.000 description 3
- 238000013508 migration Methods 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 239000010457 zeolite Substances 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000001273 butane Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 239000003317 industrial substance Substances 0.000 description 2
- 230000000977 initiatory effect Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 241000839426 Chlamydia virus Chp1 Species 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000007233 catalytic pyrolysis Methods 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 239000007809 chemical reaction catalyst Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 239000013058 crude material Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 238000007616 round robin method Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of descending-bed reactor lighter hydrocarbons catalysis conversion method and its device, its specific embodiment is as follows: 1) light hydrocarbon feedstocks and the low-temp recovery agent from regenerative agent cooler enter descending-bed reactor arrival end after preheating (or not preheating), it flows downward along reactor and the reaction such as catalytic cracking occurs, the mixture of reaction oil gas and catalyst comes downwards to reactor end and carries out quick separating, realizes the quick separating of catalyst and oil gas.Prevailing operating conditions are as follows: reaction temperature is 520~680oC, reaction pressure is 0.11~0.4MPa, and time of contact 0.05~2 second, oil ratio was 6~50.2) spent agent isolated is after spent agent stripper stripping, and into regenerator coke burning regeneration, regeneration temperature is controlled at 630-730 DEG C.3) regenerative agent from regenerator enters regenerative agent cooler and is cooled to 200-720 DEG C, until descending-bed reactor is recycled.
Description
Technical field
The invention belongs to the catalysis conversion methods of light hydrocarbon, in particular to utilize the side of descending-bed reactor volume increase alkene
Method.
Background technique
Ethylene and propylene are important basic petrochemical raw material, and light olefin is split mainly from steam in global range at present
Solve device and catalytic cracking (cracking) device.Although on steam cracking device by reduce cracking severity can with propylene enhancing,
But it will cause the decline of feed stock conversion and light olefin total recovery (ethylene, propylene+butadiene).
US6106697 discloses one kind and carries out catalytic cracking reaction as raw material, using two-stage reactor using wax oil or residual oil
Selectivity production C2-C4The method of alkene.Wax oil or residual oil raw material are in the first stage reactor, under the conditions of Conventional catalytic cracking
The different boiling ranges product for carrying out catalytic cracking reaction generation including gasoline fraction is contacted with macro-porous zeolite catalyst；First is anti-
In the second reactor, progress is contacted with central hole zeolite catalyst, and further reaction generates C to the gasoline fraction for answering device to generate2-C4Alkene
Hydrocarbon.
CN1403540A discloses the catalysis conversion method of a kind of preparing ethylene and propylene.This method is by the hydrocarbon ils after preheating
Raw material A injects dilute phase reaction zone, contacts, reacts with the catalyst containing five-membered ring silica-rich zeolite, and reaction stream enters close opposite
Area is answered, and contacts, react with injection hydrocarbon oil crude material B therein.When the use of vacuum gas oil (VGO) being raw material, ethylene yield is
16.05 heavy %, productivity of propylene are 20.76 heavy %, and butylene yield is 11.21 heavy %.
From the point of view of the above-mentioned prior art, catalytic cracking reaction device generallys use double lifting leg, riser+bed reactor shape
Formula.But in view of riser reactor feature itself and defect, as catalyst back-mixing is serious, the radial density of catalyst of axis is distributed not
The reasons such as uniformity, receive certain restrictions in terms of low-carbon olefines high-output.
CN1162514C proposes a kind of catalytic cracking reaction device that gas-solid cocurrent flow descending is coupled with uplink, uses first
The reaction process of uplink after downlink, and by being arranged or being not provided with two kinds of gas-solid quick disconnector in downlink conversion zone exit
Structure type improves the yield of gasoline and liquefied gas, reduces the production quantity of dry gas and coke；Or carry out selective hydrogen migration and different
Structureization reaction, improves the content of isohydrocarbon and aromatic hydrocarbon in gasoline, reduces olefin(e) centent.
From the point of view of current status of implementation and the data delivered, using the technology of duo-lift tube reactor form, third
The maximum output of alkene is 18m% or so, and using down pipe, riser+bed reactor productivity of propylene is about 24m% or so.
Riser reactor and descending-bed reactor respectively have the advantage of oneself.Riser reactor has catalyst concn
The advantages that height, gas-solid contact area is larger, and gas-solid contact is high-efficient, but due to gas-solid cocurrent against gravitational field flow, riser
Inner shaft Radial Flow it is uneven, catalyst slide back-mixing it is larger, residence time destribution is uneven.Descending-bed reactor is gas-solid
Cocurrent is flowed along gravitational field, and Radial Flow is more uniform, catalyst without axial backmixing, the radial distribution of granule density and speed compared with
The riser of upstriker has clear improvement, and particularly suitable super short contact time (reaction) time (will usually shorten 1-3 compared with riser
Again), the catalytic conversion reaction of super large oil ratio (usually to increase 1-3 times compared with riser), as the Deep catalytic of residual oil turns
Change, catalytic pyrolysis, gasoline catalytic cracking alkene etc. can make full use of the initial activity of catalyst, improve light oil yield, drop
The generation of low dry gas and coke.
In riser catalytic cracking reaction process, the raw material after preheating connects with the high-temperature regenerated catalyst from regenerator
It touches, vaporize and reacted, the reaction time is about at 2~3 seconds.Studies have shown that the catalyst activity at leg outlet only has
1/3 or so of initial activity, reaction carry out 1 second or so, the activity decline 50% or so of catalyst.Due to promoting tube reaction mistake
The coke laydown generated in journey declines the activity of catalyst sharply, catalytic action is big on catalyst surface and activated centre
To weaken, heat cracking reaction increases, and generates more dry gas and coke.
Therefore, research both domestic and external generally concentrate on the exploitation entrance structure of descending-bed reactor, gas-solid quick separating with
And the catalyst etc. of coupling riser reactor and exploitation high activity, to strengthen raw material and catalyst in the mixed of arrival end
It closes, improves the total conversion and selectivity of reaction.CN 1113689C discloses a kind of gas-solid and flow folding type fast fluidized bed is anti-
Answer device；CN 1162514C discloses a kind of catalytic cracking reaction device that gas-solid cocurrent flow descending is coupled with uplink.
Studies have shown that improving catalyst concn in descending-bed reactor, down-flow fluidized bed using ECT catalytic conversion reaction process can be improved
Conversion ratio and reaction selectivity, to obtain higher purpose product yield.But the technical side of oil ratio how is not improved
The report of case or the research and development achievement of measure.
Efficiency and regeneration effect are burnt in fact, to improve, is typically employed to higher regeneration temperature (such as 700-730
DEG C), thusAgainRaw catalyst (abbreviation regenerative agent) temperature is all very high, much higher than needed for descending-bed reactor system thermal balance
Regenerative agent temperature；That is, oil ratio is significantly increased, the temperature of regenerative agent must be just reduced, could be maintained in this way
The heat balance of reaction system.Meanwhile the ultrashort reaction time also has to guarantee by super large oil ratio；Otherwise, if passed through
Reaction temperature is improved to realize the high conversion under the ultrashort reaction time, will certainly just aggravate the non-ideal reaction such as thermal cracking, from
And the decline of the purpose of will lead to the increasing of coke and dry gas yied, gasoline and light olefin product yield.
The purpose of the present invention is using cold renewal agent round-robin method, realize under the premise of guaranteeing good regeneration effect
High agent-oil ratio operation, is lowered into the temperature of the regenerative agent of descending-bed reactor, and the heat for breaking descending-bed reactor system is flat
Weighing apparatus limitation improves catalyst concn in descending-bed reactor to improve the internal circulating load of catalyst, improves catalyst activity and work
Property in calculation, promote catalyzed conversion, hydrogen migration, isomerization, the ideal responses such as aromatisation, reduce the non-ideal reactions such as thermal cracking,
Reaction selectivity is improved, so that the yield of the purpose of improving gasoline and light olefin product, reduces the yield of coke and gas.
It is another object of the present invention to enter the regenerative agent temperature of descending-bed reactor by adjusting, optimization down-flow fluidized bed using ECT is realized
The purpose of reactor reaction temperature optimizes the temperature point of descending-bed reactor with suitable reaction temperature and suitable oil ratio
Cloth optimizes reaction depth and product distribution, to further improve reaction selectivity, reduces the yield of coke and gas,
The yield of the purpose of improving gasoline and light olefin product.
Summary of the invention
The technical problem to be solved by the present invention is to use regenerative agent cooling technology, break the heat balance of descending-bed reactor system
Limitation really realizes high agent-oil ratio operation, improves catalyst concn and catalyst activity in descending-bed reactor；Simultaneously using suitable
Suitable reaction temperature (0-50 DEG C relatively low), optimizes the Temperature Distribution of descending-bed reactor, realizes the optimal control of reaction depth,
To improve reaction selectivity, light olefins and the gasoline yields such as propylene are improved, improves the arene content in gasoline, is reduced in gasoline
Olefin(e) centent, while reducing coke and dry gas yied.
The present invention provides a kind of regenerative agent of the descending-bed reactor lighter hydrocarbons catalysis conversion method from regenerator through regenerative agent
Cooler cool after enter descending-bed reactor, with light hydrocarbon feedstocks arrival end mixing, contact, in descending-bed reactor
The catalytic conversion reaction of lighter hydrocarbons is carried out, cocurrent flow descending to descending-bed reactor end carries out quick separating；That isolates to be generated urges
Agent (abbreviation spent agent) enters regenerator coke burning regeneration after stripping, and the catalyst after regeneration is after regenerative agent cooler is cooling
Descending-bed reactor is returned to be recycled.
Its specific embodiment is as follows:
1) light hydrocarbon feedstocks after preheating (or not preheating) and the low-temp recovery agent from regenerative agent cooler enter down-flow fluidized bed using ECT
Reactor inlet end, flows downward along reactor and reacts, and the mixture of reaction oil gas and catalyst comes downwards to reactor end
End carries out quick separating, realizes the quick separating of catalyst and oil gas.Prevailing operating conditions are as follows: reaction temperature is 520~680
DEG C (preferably 560~660 DEG C, best 580~630 DEG C), reaction pressure are 0.11~0.4MPa, and time of contact is 0.05~2 second
(preferably 0.1~1.5 second), catalyst and raw material weight ratio (oil ratio) are 8~60 (preferably 10~50, best 16-50).
2) spent agent isolated is after spent agent stripper stripping, into regenerator coke burning regeneration, regeneration temperature control
At 630~800 DEG C (preferably 630-730 DEG C, best 650~730 DEG C).
3) regenerative agent from regenerator enters regenerative agent cooler and is cooled to 200-720 DEG C, regenerative agent (letter after cooling
Claim cold renewal agent) enter the recycling of descending-bed reactor arrival end；Or setting thermal regenerant is (i.e. from regenerator without cold
But regenerative agent) it bypasses, a part of thermal regenerant enters descending-bed reactor arrival end after mixing with above-mentioned cold renewal agent and recycles
It uses.
Further, the reaction temperature of above-mentioned descending-bed reactor mainly pass through adjust oil ratio (i.e. it is above-mentioned it is cold again
Control element such as slide valve, plug valve etc. is set in raw agent delivery pipe), or/and it is main by adjusting cold renewal agent or mixed regeneration agent
Temperature controlled, so that it is kept at optimum value.
Enter the temperature of the regenerative agent of above-mentioned descending-bed reactor by adjusting, realizes and adjust descending-bed reactor reaction temperature
The purpose of degree, and then using suitable reaction temperature and suitable oil ratio, optimize the Temperature Distribution of descending-bed reactor, optimizes
Reaction depth and product distribution reduce the yield of coke and gas to further improve reaction selectivity, improve gasoline
And the yield of the purpose of light olefin product.
The cold renewal agent temperature is regenerated by adjusting to enter the fluidizing agent flow of regenerative agent cooler and/or return
The flow and/or other parameters of the cold catalyst of device are controlled.The fluidizing agent can be air, steam or other gas
Body either their mixture, take thermal medium can be water, steam, air or other gases, various oil products etc. either it
Mixture.
The temperature of the mixed regeneration agent into descending-bed reactor can pass through the ratio of the above-mentioned cold and hot regenerative agent of adjusting
Example and be independently controlled.
The cold renewal agent temperature into descending-bed reactor mainly passes through adjusting fluidizing agent and/or takes thermal medium
Flow or/and other parameters controlled；Or cold regenerated catalyst temperature mainly passes through adjusting fluidizing agent and/or takes heat
The flow or/and other parameters of the cold catalyst of medium and/or return regenerator are controlled.Therefore, descending-bed reactor
Independent control can be obtained in oil ratio (weight ratio of regenerated catalyst and raw material) and reaction temperature.
Certainly any specific implementation to present inventive concept can not also be constituted there are many other control equipment and control method
The limitation of mode.
Method and device thereof of the invention can also be arranged catalyst in the downstream of the regenerative agent cooler and mix buffering
Space, the mixing of intensifying regenerating agent eliminate the non-homogeneous radial temperature difference generated with Non-Uniform Flow that conducts heat (so that regenerative agent temperature
Degree reaches balanced), to meet the temperature controlled requirement of downstream reaction, improve the temperature controlled accuracy of downstream reaction and flexibly
Property.Meanwhile the density of regenerative agent also can be improved, the motive force of regenerant recycle system is improved, to overcome oil ratio increase to cause
Circulatory system resistance increase, realize high agent-oil ratio operation.
The mixing cushion space is operated using low speed dense-phase fluidized bed, superficial gas velocity (fluidizing agent flow and equipment
The ratio between void tower cross section) be less than 0.3m/s (preferably 0.0001~0.1999m/s).
The fluidizing agent of the catalyst mixing cushion space can be air, steam or other gases either they
Mixture (preferably steam) reduces the non-hydrocarbon gases content such as nitrogen in dry gas to reduce the air capacity of recycling catalyst entrainment,
Dry gas calorific value is improved, the power consumption of rich gas compressor is reduced.Those of ordinary skill in the art are to its specific structure, connecting-type
Formula, operation and control process are perfectly clear, and do not constitute the limitation to any specific embodiment of present inventive concept.
The above-mentioned regenerative agent cooler being connected with reactor can be set outside regenerator, also can be set in regeneration
Inside device.Above-mentioned regenerative agent cooler can be linked as with regenerator, descending-bed reactor and/or catalyst mixing cushion space
One, can also be coupled by delivery pipe.Those of ordinary skill in the art to its specific structure, linked vector graph, operation and
Control process is perfectly clear, and does not constitute the limitation to any specific embodiment of present inventive concept.
Catalyst cooler is mature industry equipment, and various structure types can be used (such as in method and device thereof of the invention
Up flow type, downflow system etc.), various specific connection structures (such as inner circulating tube, Y type, U-shaped outer can also be used in catalyst transport channel
Convey (circulation) pipe etc.), it is arranged or does not set degassing (balance) pipe, those of ordinary skill in the art are to its specific structure, connecting-type
Formula, operation and control process are perfectly clear, and do not constitute the limitation to any specific embodiment of present inventive concept.
Light hydrocarbon feedstocks of the present invention are oil plant or the various olefin-containings of petrochemical plant or saturated liquid light hydrocarbon, packet
Include the mixture of any one or more than one arbitrary proportion in liquefied petroleum gas, light oil etc.；The liquid light hydrocarbon can
To be the main C rich in butylene, amylene4、C5The mixture of fraction either their arbitrary proportion；The light oil can be
Gasoline fraction includes catalytically cracked gasoline, pressure gasoline, visbreaking gasoline, coker gasoline, cracking ethylene preparation gasoline, straight run vapour
One of gasoline including oil, condensate, two kinds, a variety of and its arbitrary proportion blend gasolines, can be full distillation gasoline
As initial boiling point to 220 DEG C or so fraction or in which part narrow fraction such as initial boiling point to 80 DEG C fraction；The light oil is also
Can be fraction of diesel oil, including catalytic cracking diesel oil, can be full fraction diesel oil oil such as initial boiling point to 365 DEG C or so fraction or
The fraction of narrow fraction such as initial boiling point in part therein to 300 DEG C.
For the preference temperature for guaranteeing catalyst coke burning regeneration, the thermal balance of reaction-regeneration system is maintained, can also be taken down
One of column measure, two or more are used alone or in combination:
1) can be injected to regenerator flammable solid, in liquid fuel or gaseous fuel any one, two kinds, it is a variety of and its mixed
Close object；
2) it can be exchanged heat with the main wind (Air for burning coke) into regenerator with regenerated flue gas, or taking as regenerative agent cooler
Thermal medium and regenerative agent exchange heat, and temperature when main wind to be entered to regenerator improves 160-650 DEG C (preferably 200-520 DEG C)；
3) main wind can be heated to one of solid, liquid or gaseous fuel, two kinds, a variety of and its mixture
200-1800 DEG C (preferably 600-1500 DEG C) enters regenerator.
Catalysis conversion method of the invention can individually be implemented, and use can also be coupled with riser reactor, such as: can adopt
Gas-solid cocurrent disclosed in the gas-solid disclosed in CN 1113689C and flow folding type fast fluidized bed reaction unit, CN 1162514C
The catalytic cracking reaction device etc. that downlink is coupled with uplink.
Various reaction regeneration patterns can be used in method and device thereof of the invention, and the first regenerator, the second regeneration is such as arranged
Device etc., those of ordinary skill in the art are perfectly clear to a combination thereof pattern, operation and control process, do not constitute to present inventive concept
Any specific embodiment limitation.
Using method and device thereof of the invention, the separation of reaction product and the regeneration of catalyst according to a conventional method into
Row, spent agent carry out coke burning regeneration, general regeneration temperature control under Conventional catalytic reforming catalyst regeneration condition in a regenerator
System is at 630~800 DEG C (preferably 630-730 DEG C, best 650~730 DEG C).
Method and device thereof of the invention can use any catalytic converting catalyst and auxiliary agent industrially used, including
Producing more propylene ZSM catalyst, overtemperature molecular sieve catalyst etc..
Fluidized catalytic process for transforming and device are mature industry process, those of ordinary skill in the art to a combination thereof pattern,
Operation and control process are perfectly clear, to its operating condition (such as feeding temperature, reaction temperature, reaction pressure, time of contact, agent
Oil than etc.) and the selection of catalyst be also perfectly clear, do not constitute the limitation to any specific embodiment of present inventive concept.
It has the following advantages compared with prior art:
Catalysis conversion method of the invention uses cold renewal agent circulating technology, has broken the heat balance in reactor and has reacted again
The heat balance of raw system, makes it possible high agent-oil ratio, so as to optimize the operating condition of descending-bed reactor (such as: can adopt
With ultrashort reaction time and bigger oil ratio), under suitable (relatively low) reaction temperature, effectively realize reaction depth
Optimal control greatly promotes the ideal responses such as catalyzed conversion (cracking), inhibits the non-ideal reactions such as thermal cracking, to improve anti-
It should selectivity.
1. increasing catalyst circulation amount, the coking rate (i.e. the carbon of regenerative agent and spent agent is poor) of catalyst is reduced, is mentioned
The number of active center of unit catalyst in high descending-bed reactor.
2. increasing catalyst circulation amount, the concentration of catalyst in descending-bed reactor is improved, increases finish contact
Area improves finish contact effect；The catalyst active center's number for increasing the contact of unit raw material simultaneously, is greatly facilitated and urges
Change the ideal responses such as cracking, hydrogen migration, isomerization, aromatisation.
3. increasing catalyst circulation amount, the entrance temperature difference in descending-bed reactor is greatly reduced, and optimizes downlink
The temperature distribution state of bed reactor, restrained effectively the non-ideal reaction such as thermal cracking.
4. recycling using low-temp recovery agent, hydro-thermal of the regenerative agent during transportation (to before descending-bed reactor) is alleviated
Inactivation improves regenerated catalyst activity, reduces catalyst consumption.
5. the present invention is recycled using low-temp recovery agent, feeding temperature can be improved, improve finish and contact effect, with high activity
Catalyst and high agent-oil ratio and suitable reaction temperature synergistic effect, substantially reducing undesirable product, (such as coke is gentle
Body etc.) yield while, the purpose of greatling improve gasoline and light olefin 2-3 percentage points of yield of product, improve gasoline
Octane number 0.5-2.0 unit, to improve the economy of the technology.
6. catalyst mixing cushion space is arranged, the mixing of fortifying catalytic agent makes regenerative agent temperature reach balanced, uniformly steady
It is fixed, improve the temperature controlled accuracy of downstream reaction and flexibility.
Meanwhile the density and buffer capacity of regenerative agent are also effectively improved, the motive force of regenerant recycle system is improved,
To improve safety, reliability, stability, controllability and the flexibility of operation, realize reaction temperature optimal control and
The optimal control of reaction depth.
7. fluidizing agent uses steam, the air of recycling catalyst entrainment is eliminated, the nonhydrocarbons such as nitrogen in dry gas are eliminated
Class gas improves dry gas calorific value, reduces the power consumption of rich gas compressor, reduces the equipment size of gas separate section
And consumption.
8. descending-bed reactor catalytic conversion process of the invention, the adjusting phase of the operating conditions such as reaction temperature, oil ratio
It is more flexible to independence, it can be adjusted flexibly according to raw material type and market situation, to realize different product distributions.Such as:
1) lower reaction temperature can be used, produce low alkene high-knock rating gasoline.
At this point, reaction temperature can lower (such as 520-530 DEG C), promote catalytic cracking, isomerization, aromatisation etc. ideal anti-
It answers, produces low alkene high-knock rating gasoline.
2) higher reaction temperature, the light olefins such as high output of ethylene, propylene can be used, while producing the industrial chemicals such as aromatic hydrocarbons.
When needing voluminous light olefin and aromatic hydrocarbons, reaction temperature again can very high (such as 560-650 DEG C, preferably 580-630
DEG C), account for the reactions such as cracking of olefins and aromatisation leading, the light olefins such as high output of ethylene, propylene, while producing high arene content
Gasoline reconciliation component, and then Aromatics Extractive Project can be passed through and produce the industrial chemicals such as aromatic hydrocarbons.
Detailed description of the invention
Attached drawing 1-3: for the canonical schema of descending-bed reactor catalytic convention design of the invention.
The invention will now be described in detail with reference to the accompanying drawings, and attached drawing is drawn in order to illustrate the present invention, does not constitute to this hair
The limitation of any specific embodiment of bright design.
Attached drawing 1 is the schematic block follow diagram of descending-bed reactor catalytic convention design of the invention.
As shown in Fig. 1: catalysis conversion method and its device of the invention includes descending-bed reactor arrival end 1, downlink
Bed reactor 2, fast separation device 3, spent agent stripper 4, regenerator 5, regenerative agent cooler 6, catalyst mixing buffering are empty
Between 7, second-stage separator 8.
Mixing section in descending-bed reactor 2 is entered after the preheated heating of light hydrocarbon feedstocks, at the same time, by 5 mistake of regenerator
The high temperature catalyst come, cools through regenerative agent cooler 6, then mixed through downstream (or lower part) catalyst mixing cushion space 7
Close after buffering temperature reaches equilibrium, into descending-bed reactor arrival end 1 it is uniformly distributed after, enter in descending-bed reactor 2 and with
Feedstock oil mixing after atomization；Gas-particle two-phase Rapid contact and after being sufficiently mixed in mixing section, cocurrent is along reactor 2 to flowing down
It is dynamic, while carrying out generation catalytic conversion reaction.The mixture cocurrent flow descending of reaction product and catalyst is last to descending-bed reactor
End fast gas-solid separator 3 (is not drawn catalyst and product oil gas quick separating or high-temperature product oil gas by chilling in figure
Out, to avoid the generation of secondary response), then enter second-stage separator 8 (such as cyclone separator) further Removal of catalyst
After enter back into downstream fractionation or separation system is further separated, thus gas products required for obtaining and liquid product.
Prevailing operating conditions are as follows: reaction temperature is 520~680 DEG C of (preferably 560~660 DEG C, best 580~630 DEG C), reaction pressures
For 0.11~0.4MPa, time of contact is 0.05~2 second (preferably 0.1~1.5 second), catalyst and raw material weight ratio (oil ratio)
For 8~60 (preferably 10~50, best 16-50).
The spent agent isolated carries out coke burning regeneration, regeneration temperature after the stripping of spent agent stripper 4, into regenerator 5
Control is at 630-730 DEG C (preferably 650-730 DEG C).
Regenerative agent from regenerator 5 enters regenerative agent cooler 6 and is cooled to 200-720 DEG C of directly return down-flow fluidized bed using ECT reaction
Device 2 is recycled；Or the cold renewal agent of 6 lower part of regenerative agent cooler or bottom is left, then through catalyst mixing cushion space 7
After mixing buffering makes its temperature equalization, returns to descending-bed reactor 2 and be recycled.
It is cooling in the regenerative agent for the target for realizing the optimal control of reaction temperature and the optimal control of reaction depth
Catalyst mixing cushion space 7 is arranged in the downstream of device 6, and the mixing of intensifying regenerating agent makes to regenerate before entering descending-bed reactor 2
Agent temperature reaches balanced, to meet the temperature controlled requirement of downstream reaction.It saves space to realize and reduces investment outlay, catalyst is mixed
Closing cushion space 7 can also use and 6 isodiametric integral structure (as shown in Fig. 3) of regenerative agent cooler.Catalyst is mixed
It closes cushion space 7 to operate using low speed dense-phase fluidized bed, superficial gas velocity is less than 0.3m/s (preferably 0.0001~0.1999m/
s)。
Attached drawing 2 is a kind of regenerated flow diagram of coaxial-type of descending-bed reactor catalytic convention design of the invention.
As shown in Fig. 2: catalysis conversion method and its device of the invention includes descending-bed reactor arrival end 1, downlink
Bed reactor 2, fast separation device 3, spent agent stripper 4, regenerator 5, regenerative agent cooler 6, catalyst mixing buffering are empty
Between 7 (can not also set), second-stage separator 8 and settler 9.
Regenerator 5 is connected by regenerative agent delivery pipe with regenerative agent cooler 6, and cold renewal agent is catalyzed through downstream (or lower part)
After the mixing buffering of agent mixing cushion space 7, it is connected by cold renewal agent delivery pipe 10 with descending-bed reactor arrival end 1.It leaves
The cold renewal agent temperature of regenerative agent cooler 6 is controlled by adjusting fluidizing agent 35 (including air, steam etc.) flow.Control
Valve 21 processed is the specific control element for controlling the flow of cold regenerated catalyst for convenience and being arranged.Pumped (conveying) medium 32 can be steaming
Vapour or other gases or their mixture (preferably steam).
Enter the regenerative agent temperature of descending-bed reactor for convenience of control, it can be with settable thermal regenerant shunt valve (packet
Include control valve) (being not drawn into figure) be directly connected with catalyst mixing cushion space 7, and cold renewal agent mixes herein with thermal regenerant
After so that its temperature is reached balanced.
Certainly any specific implementation to present inventive concept can not also be constituted there are many other control equipment and control method
The limitation of mode.
Light hydrocarbon feedstocks and regenerative agent are mixed into descending-bed reactor, are reacted under catalyticing conversioning condition, main to grasp
It is as follows to make condition: reaction temperature is 460~680 DEG C of (preferably 480~660 DEG C, best 490~630 DEG C), reaction pressures 0.11
~0.4MPa, time of contact are 0.05~2 second (preferably 0.1~1.5 second), catalyst and raw material weight ratio (oil ratio) be 6~
50 (preferably 8~40).
The mixture cocurrent flow descending of reaction oil gas and catalyst will be urged to 2 end fast separation device 3 of descending-bed reactor
Agent and product oil gas quick separating or high-temperature product oil gas (are not drawn into, to avoid the hair of secondary response by chilling in figure
It is raw), downstream fractionation or separation are entered back into after then entering second-stage separator 8 (such as cyclone separator) further Removal of catalyst
System is further separated, thus gas products required for obtaining and liquid product.
Spent agent is entered after the spent agent stripper 4 of settler 9 strips by spent agent delivery pipe 7 and control valve 20
Regenerator 5, coke burning regeneration in the presence of main wind 38 (oxygen-containing gas includes air etc.).Regenerative agent is drawn by 5 lower part of regenerator,
Into regenerative agent cooler 6, cold renewal agent is recycled through delivery pipe 11 (or mixing with thermal regenerant) and (also can be set another
Road catalyst transport returns to regenerator).(it is of course also possible to external warmer be separately provided according to process requirement, to realize multiplexing
Flexible operating under condition).
Regenerative agent from regenerator 5 enters regenerative agent cooler 6 and is cooled to 200-720 DEG C.Leave regenerative agent cooler 6
The cold renewal agent of lower part or bottom, then after the mixing buffering of catalyst mixing cushion space 7 makes its temperature equalization, return to down-flow fluidized bed using ECT
Reactor 2 is recycled.Fluidizing agent 32 can be air, steam or other gases or their mixture (preferably steams
Vapour).Thermal medium 37 is taken to can be water, steam, air or other gases, various oil products etc. or their mixture.
To realize the optimal control of reaction temperature and the optimal control of reaction depth, under the regenerative agent cooler
Trip setting catalyst mixing cushion space 7, the mixing of intensifying regenerating agent make regenerative agent temperature before entering descending-bed reactor 2
Reach balanced, to meet the temperature controlled requirement of downstream reaction.It saves space to realize and reduces investment outlay, catalyst mixing buffering
Space 7 may be designed in and 6 isodiametric integral structure (as shown in Figure 3) of regenerative agent cooler.Catalyst mixing buffering
Space 7 is operated using low speed dense-phase fluidized bed, and superficial gas velocity is less than 0.3m/s (preferably 0.0001~0.1999m/s).
Attached drawing 3 is a kind of regenerated flow diagram of fast bed of descending-bed reactor catalytic convention design of the invention.
As shown in Fig. 3: catalysis conversion method and its device of the invention includes descending-bed reactor arrival end 1, downlink
Bed reactor 2, fast separation device 3, spent agent stripper 4, regenerator 5, regenerative agent cooler 6, catalyst mixing buffering are empty
Between 7, second-stage separator 8 and settler 9.
Regenerator 5 is connected by regenerative agent delivery pipe with regenerative agent cooler 6, and regenerative agent is cooling through regenerative agent cooler 6
Cooling, then through downstream (or lower part) catalyst mixing cushion space 7 mixing buffer so that its temperature is reached equilibrium after, by it is cold again
Raw agent delivery pipe 10 is connected with descending-bed reactor arrival end 1.The cold renewal agent temperature for leaving regenerative agent cooler 6 passes through adjusting
The flow of fluidizing agent 35 (including air, steam etc.) is controlled.Control valve 21 is the stream for controlling cold renewal agent for convenience
The specific control element measured and be arranged.
Enter the regenerative agent temperature of descending-bed reactor 2 for convenience of control, it can be with settable thermal regenerant shunt valve (packet
Control valve is included, is not drawn into figure) directly it is connected with regenerative agent mixing cushion space 7, cold renewal agent mixes herein with thermal regenerant
After so that its temperature is reached balanced.
Certainly any specific implementation to present inventive concept can not also be constituted there are many other control equipment and control method
The limitation of mode.
Above-mentioned catalyst cooler can be linked together with regenerator, down-flow fluidized bed using ECT, can also be coupled by pipeline.
Light hydrocarbon feedstocks and regenerative agent are mixed into descending-bed reactor, are reacted under catalyticing conversioning condition, main to grasp
It is as follows to make condition: reaction temperature is 460~680 DEG C of (preferably 480~660 DEG C, best 490~630 DEG C), reaction pressures 0.11
~0.4MPa, 0.05~2 second time of contact (preferably 0.1~1.5 second), catalyst and raw material weight ratio (oil ratio) are 6~50
(preferably 8~40).
The mixture cocurrent flow descending of reaction oil gas and catalyst will be urged to 2 end fast separation device 3 of descending-bed reactor
Agent and product oil gas quick separating or high-temperature product oil gas (are not drawn into, to avoid the hair of secondary response by chilling in figure
It is raw), downstream fractionation or separation are entered back into after then entering second-stage separator 8 (such as cyclone separator) further Removal of catalyst
System is further separated, thus gas products required for obtaining and liquid product.
The spent agent isolated is after the stripping of spent agent stripper 4, (in figure not by spent agent delivery pipe 13 and control valve
Draw) enter burning tank 5A, through quickly being burnt in the presence of main wind 38A (oxygen-containing gas includes air etc.), be delivered up to
The further coke burning regeneration of regenerator 5,5 bottom of regenerator supplement Secondary Air 38B (oxygen-containing gas includes air etc.).Regenerative agent is by again
Raw 5 lower part of device is drawn, and into regenerative agent cooler 6, cold renewal agent is recycled through delivery pipe 11 (or mixing with thermal regenerant),
Another way returns to regenerator (it is of course also possible to individually set according to process requirement through delivery pipe 12 (can not also set delivery pipe 12)
External warmer is set, to realize the flexible operating under multi-state).
Regenerative agent from regenerator 5 enters regenerative agent cooler 6 and is cooled to 200-720 DEG C.Leave regenerative agent cooler 6
The cold renewal agent of lower part or bottom, then after the mixing buffering of catalyst mixing cushion space 7 makes its temperature equalization, return to down-flow fluidized bed using ECT
Reactor 2 is recycled.Fluidizing agent 39 can be air, steam or other gases or their mixture (preferably steams
Vapour).Thermal medium 37 is taken to can be water, steam, air or other gases, various oil products etc. or their mixture.Conveying
Medium 36 can be air, steam or other gases or their mixture.
To realize the optimal control of reaction temperature and the optimal control of reaction depth, in the regenerative agent cooler 6
Catalyst mixing cushion space 7 is arranged in downstream, and the mixing of intensifying regenerating agent makes regenerative agent temperature before entering descending-bed reactor 2
Degree reaches balanced, to meet the temperature controlled requirement of downstream reaction.It saves space to realize and reduces investment outlay, catalyst mixing is slow
Space 7 is rushed to use with regenerative agent cooler 6 as isodiametric integral structure.Catalyst mixing cushion space 7 is close using low speed
Phase fluidized bed process, superficial gas velocity are less than 0.3m/s (preferably 0.0001~0.1999m/s).
Specific embodiment
Example 1
For example 1, the raw material of descending-bed reactor is catalytically cracked gasoline, and descending-bed reactor need to be oily using 30 super large agent
Than being just able to achieve optimization reaction temperature profile, improving reaction selectivity, improve propylene and yield of gasoline, improve the virtue in gasoline
Hydrocarbon content and octane number reduce the purpose of the olefin(e) centent in gasoline.
This example is using the prior art and process conditions of the invention shown in Fig. 2 or process flow shown in Fig. 3, table 1
And the molecular sieve catalyst (CHP-1) of producing more propylene, gasoline stocks and test result are listed in table 2.
Shown in table 2 the result shows that, due to the limitation of descending-bed reactor heat balance, prior art B use into
At 400 DEG C of material temperature degree, the oil ratio under thermal balance only has 12.1.So low oil ratio will seriously affect descending-bed reactor
Conversion ratio and selectivity.At 40 DEG C of option A feeding temperature, although can improve oil ratio to 25.9, this will seriously affect dress
Set low the recycling and utilization of warm.
Table 2 the result shows that, compared with prior art, the present invention high added value productivity of propylene improve 1.2 percentage points,
Coke dry gas yied is suitable, and total light receipts are suitable；Aromatic Hydrocarbon in Gasoline content reduces by 3.7 percentage points, and olefin(e) centent reduces by 3 percentages
Point, octane number (RON) improve 0.8 unit.Meanwhile table 4 shows that the present invention can also maximum journey because using 400 DEG C of high-temperature feedings
Improve pre- heat recovery efficiency in degree ground.
These all illustrate that gasoline catalyzing method for transformation of the invention has significant beneficial effect.
1 prior art of table and process conditions of the invention
2 prior art of table and comparison of test results of the invention
Example 2
For example 2, the raw material of descending-bed reactor is the mixing carbon four rich in alkene.This example uses Fig. 2 or shown in Fig. 3
The prior art shown in process flow, table 3 and process conditions of the invention and ZSM-5 molecular sieve catalyst.
Descending-bed reactor is typically employed to the super large oil ratio greater than 30 and operates, and is just able to achieve optimization reaction temperature point
Cloth improves reaction selectivity, improves the purpose of ethylene, propene yield.However table 3 the result shows that using 400 DEG C of high-temperature feedings,
Due to the limitation of descending-bed reactor heat balance, the oil ratio under prior art thermal balance only has 16.3.So low agent oil
Than the conversion ratio and selectivity that will seriously affect descending-bed reactor
Four feedstock property of mixing carbon and test result that the present invention uses are listed in table 4.Table 4 shows the productivity of propylene of high added value about
47.2%, ethylene yield 10.6% illustrates that four catalysis conversion method of mixing carbon of the invention has significant beneficial effect.
3 prior art of table and process conditions of the invention comparison
| Parameter | The prior art | The present invention |
| Reaction temperature, DEG C | 620 | 620 |
| Feeding temperature, DEG C | 400 | 400 |
| Regeneration temperature, DEG C | 700 | 700 |
| Enter the catalyst temperature of down-flow fluidized bed using ECT, DEG C | 695 | 655 |
| Catalystoil ratio, weight by weight | 16.5 | 30 |
| Reaction time, second | 0.6 | 0.6 |
Table 4 mixes four feedstock property of carbon and test result
| Project | Parameter | The present invention |
| Raw material composition: mol% | ||
| C3+C5: | 0.6 | |
| Butane: | 11.9 | |
| Butylene | 87.5 | |
| It is total | 100 | |
| Product yield: wt% | ||
| < C2 | 15.8 | |
| Wherein ethylene | 10.6 | |
| Propane | 4.3 | |
| Propylene | 47.2 | |
| Butane | 10.3 | |
| Butylene | 11.7 | |
| Liquid+coke+loss | 10.7 | |
| Wherein ethylene+propylene | 57.8 | |
| It is total | 100.0 |
Claims (13)
1. a kind of descending-bed reactor lighter hydrocarbons catalysis conversion method, which is characterized in that the regenerated catalyst from regenerator is through again
Raw agent cooler enters descending-bed reactor after cooling, with light hydrocarbon feedstocks in arrival end mixing, contact, reacted in down-flow fluidized bed using ECT
The catalytic conversion reaction of lighter hydrocarbons is carried out in device, cocurrent flow descending to descending-bed reactor end carries out quick separating；Isolate to
Raw catalyst enters regenerator coke burning regeneration after stripping, and the catalyst after regeneration returns to downlink after regenerative agent cooler is cooling
Bed reactor cycles use.
2. according to the method for claim 1, which is characterized in that the prevailing operating conditions of the descending-bed reactor are as follows:
Reaction temperature is 520~680oC, reaction pressure is 0.11~0.4MPa, and time of contact is 0.05~2 second, oil ratio is 8~
60。
3. according to the method for claim 1, which is characterized in that the specific process is as follows:
1) by preheating or light hydrocarbon feedstocks enter down-flow fluidized bed using ECT with the low-temp recovery agent from regenerative agent cooler and react after not preheating
Device arrival end, flows downward along reactor and reacts, the mixture of reaction oil gas and catalyst come downwards to reactor end into
Row quick separating, realizes the quick separating of catalyst and oil gas, and the following reaction temperature of prevailing operating conditions is 520~680oC, instead
Answering pressure is 0.11~0.4MPa, and time of contact is 0.05~2 second, and oil ratio is 8~60；
2) reclaimable catalyst isolated is after stripper strips, and into regenerator coke burning regeneration, regeneration temperature is controlled in 630-
730℃；
3) regenerative agent from regenerator enters regenerative agent cooler and is cooled to 200-720 DEG C, under regenerative agent after cooling enters
Row bed reactor inlet end is recycled；Or setting thermal regenerant bypasses, a part of thermal regenerant and above-mentioned cold renewal agent are mixed
After conjunction, mixed regeneration agent enters the recycling of descending-bed reactor arrival end.
4. according to method described in claim 2 or 3, which is characterized in that the reaction temperature of the descending-bed reactor be 560~
660oC, reaction pressure are 0.11~0.4MPa, and time of contact is 0.1~1.5 second, and oil ratio is 16 ~ 50.
5. according to the described in any item methods of Claims 1-4, it is characterised in that enter descending-bed reactor again by adjusting
Raw agent temperature realizes optimization descending-bed reactor reaction temperature.
6. according to method described in any one of claim 1 to 5, which is characterized in that in the downstream of the regenerative agent cooler
Catalyst mixing cushion space is set；The catalyst mixing cushion space is operated using low speed dense-phase fluidized bed, apparent gas
Speed is less than 0.3m/s.
7. according to method as claimed in any one of claims 1 to 6, which is characterized in that the reaction temperature of the descending-bed reactor
It is controlled by adjusting oil ratio, or/and by the temperature of adjusting cold renewal agent or mixed regeneration agent.
8. according to method described in claim 5 or 7, which is characterized in that the temperature of the mixed regeneration agent is cold by adjusting
The ratio of hot regenerated catalyst and be independently controlled；Or the cold renewal agent temperature by adjust fluidizing agent and/or
It takes the flow of thermal medium to be controlled, or is urged by adjusting fluidizing agent and/or taking thermal medium and/or return to the cold of regenerator
The flow of agent is controlled.
9. according to the described in any item methods of claim 1 to 8, which is characterized in that the light hydrocarbon feedstocks are oil plant or stone
The various olefin-containings of oiling factory or saturated liquid light hydrocarbon, including in liquefied petroleum gas, light oil etc. any one or it is a kind of with
On arbitrary proportion mixture；The liquid light hydrocarbon is the C containing butylene, amylene4、C5Fraction or their any ratio
The mixture of example；The light oil is gasoline fraction, including direct steaming gasoline, condensate, catalytically cracked gasoline, pressure gasoline,
One of gasoline including visbreaking gasoline, coker gasoline, cracking ethylene preparation gasoline, two kinds, it is a variety of and its arbitrary proportion mixed
Gasoline is closed, is full fraction or part narrow fraction therein；Either fraction of diesel oil, including catalytic cracking diesel oil, are full fractions
Diesel oil or in which part narrow fraction.
10. according to the described in any item methods of claim 1-9, which is characterized in that take one of following measures, two kinds or
It is a variety of to be used alone or in combination:
1) any one into regenerator injection flammable solid, liquid fuel or gaseous fuel, two kinds, a variety of and its mixing
Object；
2) it is exchanged heat with the main wind and regenerated flue gas that enter regenerator, or takes thermal medium and regenerative agent as regenerative agent cooler
Heat exchange, temperature when main wind to be entered to regenerator improve 160-650 oC；
3) main wind is heated to 200- with one of solid, liquid or gaseous fuel, two kinds, a variety of and its mixture
1800 oC enter regenerator.
11. according to the described in any item methods of claims 1 to 10, which is characterized in that this method is individually implemented or described
Descending-bed reactor is coupled with riser reactor, uses gas-solid and flow folding type fast fluidized bed reaction unit or gas-solid cocurrent
The catalytic cracking reaction device that downlink is coupled with uplink.
12. a kind of descending-bed reactor lighter hydrocarbons catalytic convention design, which is characterized in that the device includes descending-bed reactor, fast
Fast separator, spent agent stripper, regenerator, regenerative agent cooler；The descending-bed reactor either gas-solid cocurrent
The catalytic cracking reaction device that collapsible fast fluidization bed reaction device or gas-solid cocurrent flow descending are coupled with uplink.
13. device according to claim 12, which is characterized in that catalyst is arranged in the downstream of the regenerative agent cooler
Mix cushion space.
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|---|---|---|---|---|
| WO2024049983A1 (en) * | 2022-08-31 | 2024-03-07 | T.En Process Technology Inc. | Systems and processes for temperature control in fluidized catalytic cracking |
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| US4514285A (en) * | 1983-03-23 | 1985-04-30 | Texaco Inc. | Catalytic cracking system |
| CN103540345A (en) * | 2012-07-09 | 2014-01-29 | 中国石油化工集团公司 | Catalytic cracking method |
| CN206014776U (en) * | 2016-08-27 | 2017-03-15 | 中石化炼化工程（集团）股份有限公司 | Catalytic cracking unit |
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2019
- 2019-01-30 CN CN201910093273.8A patent/CN109609175A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4514285A (en) * | 1983-03-23 | 1985-04-30 | Texaco Inc. | Catalytic cracking system |
| CN103540345A (en) * | 2012-07-09 | 2014-01-29 | 中国石油化工集团公司 | Catalytic cracking method |
| CN206014776U (en) * | 2016-08-27 | 2017-03-15 | 中石化炼化工程（集团）股份有限公司 | Catalytic cracking unit |
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| WO2024049983A1 (en) * | 2022-08-31 | 2024-03-07 | T.En Process Technology Inc. | Systems and processes for temperature control in fluidized catalytic cracking |
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