CN109957421A - Combination method of catalytic cracking and light hydrocarbon deep processing - Google Patents
Combination method of catalytic cracking and light hydrocarbon deep processing Download PDFInfo
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- CN109957421A CN109957421A CN201711419457.6A CN201711419457A CN109957421A CN 109957421 A CN109957421 A CN 109957421A CN 201711419457 A CN201711419457 A CN 201711419457A CN 109957421 A CN109957421 A CN 109957421A
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- lighter hydrocarbons
- catalytic cracking
- deep processing
- riser
- combined method
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 229
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 229
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 94
- 238000012545 processing Methods 0.000 title claims abstract description 72
- 238000000034 method Methods 0.000 title claims abstract description 56
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 18
- 239000003054 catalyst Substances 0.000 claims abstract description 54
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 claims abstract description 37
- 238000006266 etherification reaction Methods 0.000 claims abstract description 29
- -1 polypropylene Polymers 0.000 claims abstract description 21
- 239000004743 Polypropylene Substances 0.000 claims abstract description 16
- 229920001155 polypropylene Polymers 0.000 claims abstract description 16
- 238000000926 separation method Methods 0.000 claims abstract description 10
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 78
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 78
- 238000006243 chemical reaction Methods 0.000 claims description 33
- 239000000295 fuel oil Substances 0.000 claims description 26
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 claims description 20
- 150000001336 alkenes Chemical class 0.000 claims description 18
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 claims description 14
- 238000002156 mixing Methods 0.000 claims description 14
- 229910021536 Zeolite Inorganic materials 0.000 claims description 13
- 125000000217 alkyl group Chemical group 0.000 claims description 13
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 13
- 239000010457 zeolite Substances 0.000 claims description 13
- 238000005336 cracking Methods 0.000 claims description 12
- 239000001282 iso-butane Substances 0.000 claims description 10
- 235000013847 iso-butane Nutrition 0.000 claims description 10
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 claims description 10
- 238000002309 gasification Methods 0.000 claims description 9
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 8
- 238000006555 catalytic reaction Methods 0.000 claims description 8
- 229910052761 rare earth metal Inorganic materials 0.000 claims description 6
- 150000002910 rare earth metals Chemical class 0.000 claims description 6
- BKOOMYPCSUNDGP-UHFFFAOYSA-N 2-methylbut-2-ene Chemical group CC=C(C)C BKOOMYPCSUNDGP-UHFFFAOYSA-N 0.000 claims description 5
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 5
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 5
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 5
- WWUVJRULCWHUSA-UHFFFAOYSA-N 2-methyl-1-pentene Chemical group CCCC(C)=C WWUVJRULCWHUSA-UHFFFAOYSA-N 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 239000001294 propane Substances 0.000 claims description 4
- 239000004411 aluminium Substances 0.000 claims description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 3
- 229910052782 aluminium Inorganic materials 0.000 claims description 3
- 229910021417 amorphous silicon Inorganic materials 0.000 claims description 3
- 230000008929 regeneration Effects 0.000 claims description 3
- 238000011069 regeneration method Methods 0.000 claims description 3
- 238000009835 boiling Methods 0.000 claims description 2
- 230000008676 import Effects 0.000 claims description 2
- 238000010025 steaming Methods 0.000 claims description 2
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims 1
- 229910052710 silicon Inorganic materials 0.000 claims 1
- 239000010703 silicon Substances 0.000 claims 1
- 239000004575 stone Substances 0.000 claims 1
- 230000029936 alkylation Effects 0.000 abstract description 3
- 238000005804 alkylation reaction Methods 0.000 abstract description 2
- 230000003197 catalytic effect Effects 0.000 description 45
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 33
- 239000007789 gas Substances 0.000 description 24
- 238000005516 engineering process Methods 0.000 description 16
- 239000003795 chemical substances by application Substances 0.000 description 11
- 238000003808 methanol extraction Methods 0.000 description 11
- 239000003921 oil Substances 0.000 description 11
- 230000008569 process Effects 0.000 description 11
- 239000002994 raw material Substances 0.000 description 11
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 9
- 229910052799 carbon Inorganic materials 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- 238000005457 optimization Methods 0.000 description 7
- 238000013461 design Methods 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 238000006317 isomerization reaction Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 238000009826 distribution Methods 0.000 description 5
- 238000011160 research Methods 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 230000001172 regenerating effect Effects 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- 230000001737 promoting effect Effects 0.000 description 3
- 238000011084 recovery Methods 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
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000003209 petroleum derivative Substances 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000012958 reprocessing Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- JFWIOFGVMQJBNT-UHFFFAOYSA-N 2-methoxy-2-methylhexane Chemical compound CCCCC(C)(C)OC JFWIOFGVMQJBNT-UHFFFAOYSA-N 0.000 description 1
- WYLQOLGJMFRRLX-UHFFFAOYSA-N 2-methoxy-2-methylpentane Chemical compound CCCC(C)(C)OC WYLQOLGJMFRRLX-UHFFFAOYSA-N 0.000 description 1
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 206010019332 Heat exhaustion Diseases 0.000 description 1
- 206010019345 Heat stroke Diseases 0.000 description 1
- 241000446313 Lamella Species 0.000 description 1
- 241001608711 Melo Species 0.000 description 1
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 238000009412 basement excavation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 238000003442 catalytic alkylation reaction Methods 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 150000002170 ethers Chemical class 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 239000002010 green coke Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 125000001972 isopentyl group Chemical group [H]C([H])([H])C([H])(C([H])([H])[H])C([H])([H])C([H])([H])* 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- HVZJRWJGKQPSFL-UHFFFAOYSA-N tert-Amyl methyl ether Chemical compound CCC(C)(C)OC HVZJRWJGKQPSFL-UHFFFAOYSA-N 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 238000002207 thermal evaporation Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002918 waste heat Substances 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
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
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 invention provides a combined method of catalytic cracking and light hydrocarbon deep processing. Step 1, establishing a light hydrocarbon collection system: establishing a C3-C6 light hydrocarbon collecting system through newly-built connecting pipelines at the separation system or the outflow pipeline position of one or more light hydrocarbon deep processing devices in a polypropylene device, an MTBE device, an alkylation device and a light gasoline etherification device, and collecting one or more partially or completely unreacted C3-C6 light hydrocarbons; step 2, pretreating the collected C3-C6 light hydrocarbon: C3-C6 light hydrocarbons collected in the step 1 are introduced into a dividing wall type heat exchanger or a boiler to be completely gasified; and 3, introducing the completely gasified C3-C6 light hydrocarbon in the step 2 into a catalytic cracking device independently or after being mixed with steam, contacting with a hot regenerated catalyst, and partially reacting in a catalytic cracking reactor to generate active light hydrocarbon required by a light hydrocarbon deep processing device matched with a refinery enterprise. The method can improve the yield of the product of the light hydrocarbon deep processing device.
Description
Technical field
The present invention relates to the combined methods of a kind of catalytic cracking and lighter hydrocarbons deep processing, belong to technical field of petrochemical industry.
Background technique
Petrochemical Enterprises are in order to increase economic efficiency, the lighter hydrocarbons of C3~C7 fraction produced to devices such as catalytic cracking, coking
Deep processing is carried out, further isolated propylene enters polypropylene plant, while isolated richness to gas separation unit separation C3 component
Containing propylene oxide stream, dehydrogenating propane device is sold or entered to the general liquefied gas component that imports；The isolated C 4 fraction of gas separation unit
Sequentially enter MTBE device and alkyl plant, in MTBE device by isobutene conversion be MTBE, alkyl plant will be different
Butane and remaining butylene are converted into high-octane alkylate oil according to the molar ratio of 1:1；After C 4 fraction enters MTBE device
Methyl ethyl ketone plant can be entered back into, is methyl ethyl ketone by remaining chain butenc；C5~C7 light gasoline fraction enters Etherification of Light FCC Gasoline dress
Set, can make in catalytic gasoline can active olefin after ether, be such as to represent isoamyl with 2-methyl-1-butene alkene, 2- methyl-2-butene
Alkene is to represent dissident's alkene with 2- Methyl-1-pentene etc., and ether corresponding with alcohols reaction generation can reduce catalytic gasoline alkene and contain
10~15 percentage points of amount.The as active lighter hydrocarbons of hydro carbons for generating high value purpose product can be reacted in lighter hydrocarbons deep processing device,
Such as the propylene of polypropylene plant, the isobutene of MTBE device, the iso-butane and butylene of alkyl plant, the positive fourth of methyl ethyl ketone plant
Alkene etc..Petrochemical Enterprises generally define, the refinery of C3~C7 lighter hydrocarbons deep processing matched with devices leading with catalytic cracking unit
The liquefied gas component of low value can not only be processed polypropylene, the MTBE, first and second for generating high value by integral combined process
Ketone, alkylate oil and etherified benzine improve light hydrocarbon product value, while can also further decrease gasoline to a certain extent
The olefin(e) centent of blend component.
The lighter hydrocarbons deep processing type of device and scale that different Petrochemical Enterprises are equipped with are differences, generally there is polypropylene, MTBE, alkane
After base, light petrol ether, it is one or more of in methyl ethyl ketone plant, it is also different with catalysis accessory processing ability.From lighter hydrocarbons depth
The unreacted lighter hydrocarbons that processing unit (plant) comes out, C3~C4 component undersells generally as liquefied gas, light petrol component generally regardless of
Gasoline reconciliation pond, which is directly entered, from light petrol after i.e. ether removes reconciliation gasoline product.Existing Petrochemical Enterprises not yet consider
Faucet, including each C3~C6 lighter hydrocarbons deep processing device carry out complex optimum as a whole.
By the study found that flow out that unreacted lighter hydrocarbons logistics still contains from lighter hydrocarbons deep processing device largely can be further
The hydro carbons of catalytic cracking reaction.The reactivities such as alkene cracking with higher, isomerization are generally believed, such as in MTBE device
Still there are also 30%~60% alkene, mainly other three kinds of isobutene in the unreacted C4 of methanol extraction column overhead extraction
Isomer；Also contain 25~50% in the part unreacted light petrol that the methanol extraction column overhead of Etherification of Light FCC Gasoline is extracted out
The alkene of (percentage by volume), including unconverted C5~C7 active olefin and non-reactive olefin.To how promoting this some olefin
The research further converted is mainly concentrated in etherificate overall technology equipped with optional light hydrocarbon isomerization module, and (such as CDTECH's is light
Etherification technology of gasoline), but it is again in need light petrol is gasified again to 400 DEG C or so, reenter the isomery of super regeneration
Change reactor, complicated for operation, energy consumption is high, do not select in the existing Petrochemical Enterprises choice of technology or isomerization module or
The utilization of capacity is very low.It is rich in normal butane, iso-butane in the output of the lighter hydrocarbons deep processing device such as alkyl plant, methyl ethyl ketone plant, simultaneously
Also the stream stock containing a great deal of butylene, existing Petrochemical Enterprises are undersold after generally collecting as liquefied gas.
It is also a research hotspot that lighter hydrocarbons, which enter catalytic cracking unit to react again,.Wherein in order to improve gasoline quality, reduce
Content of olefin in gasoline and raising liquefied gas yield, disclose the technical measures for largely taking catalytic gasoline freshening, allusion quotation both at home and abroad
There are two types of types: (1) by gasoline reprocessing to original weight oil riser, usually injecting the upstream of raw material oil spray nozzle, such as
USP5043522 and USP5846403, which is disclosed, injects feedstock oil feed nozzle upstream for catalytically cracked gasoline, utilizes high temperature, height
Active regenerated catalyst carries out catalyzed conversion to it；CN1160746A also discloses a kind of by direct steaming gasoline, coker gasoline etc.
Low-quality gasoline injecting lift tube reaction lower part, contacts it preferentially with regenerated catalyst；(2) individual gasoline rising pipe is used
Freshening gasoline, as CN1069054A and USP3784463 uses the catalytic cracking unit with duo-lift tube reactor to be reacted
, the low-quality gasoline including catalytic cracked naphtha is injected into gasoline rising pipe reactor, utilizes high temperature, high agent-oil ratio
Reaction condition realize to the catalytic reforming of low-quality gasoline, to improve liquefied gas yield and octane number.Research both at home and abroad
Person (CORMA A, MELO F V, et al.Applied Catalysis A:General, 2004,265:195-206.) discovery,
When needing high low-carbon alkene (ethylene, propylene, butylene) yield, more excellent using the first freshening mode product distribution, this is
Due to declining the temperature of reaction system after heavy oil feedstock injection, oil, agent reaction time are shortened, gasoline is terminated in time and exists
Excessive fragmentation under hot environment generates the reaction of dry gas.It, can be in traditional single riser using independent riser freshening gasoline
Gasoline reprocessing reactor is added on the basis of reactor, can be interfered with each other during the reaction to avoid weight raw material, is realized different
The subregion of raw material reacts, adjustable to the freshening reaction depth of gasoline.Domestic and international researcher is lighter almost without comparison gasoline
C3~C 4 fraction liquefied gas enters the research reacted again in catalytic cracking commercial plant；Enter the industry of catalytic cracking unit simultaneously
Generally using high pressure liquid phase lighter hydrocarbons by dedicated lighter hydrocarbons nozzle material-feeding in, into the regeneration catalyzing of riser inside and heat
Agent contact, Quick-gasifying expansion may cause " heat collapses " to catalyst and become more short grained catalyst fines, cause to be catalyzed
Device agent consumption increases, and cold liquid phase hydro carbons absorbs big calorimetric in gasification and causes hydro carbons periphery local temperature low, thus
The conversion ratio of lighter hydrocarbons declines, and cannot reach lighter hydrocarbons and enter the reaction depth design reacted again in catalytic unit.Such as Daqing Refinery public affairs
(Wang Wei, Weiqiang, Xu Zhanwu, wait RECYCLING TECHNIQUES FOR FCC GASOLINE, 2002,32 (3): oil refining design 24~28) is adopted for department
Enter pre-lift steam pipe line with cold liquid phase gasoline cross-line, cause mixing temperature too low, catalyst breakage aggravation causes to be catalyzed
Damage is run in agent.
The purity problem of the unreacted lighter hydrocarbons flowed out from lighter hydrocarbons deep processing device is also investigated, for example lighter hydrocarbons contain after ether
There is a certain amount of methanol.CN86101079A is disclosed using methanol as the method for reactant catalytic cracking together with petroleum hydrocarbon,
Reactant is contacted with fine grain ZSM-5 catalyst, so that exothermic the reaction of methanol conversion and the catalytic cracking reaction of heat absorption are big
Heat balance in cause." petrochemical industry, 2009,38 (3): it is mixed that 267-272 " has studied methanol and catalytic gasoline on small riser
Refining changes Quality Research, the results showed that methanol and FCC gasoline are kneaded while improving quality of gasoline, be conducive to increase production cracked gas with
Improve liquid yield.But methanol conversion and catalytic cracking of petroleum hydrocarbon coupling reaction are by process conditions, catalyst activity and choosing
The limitation of selecting property, methanol conversion and olefine selective be not high.CN200610091074.6 and CN200810117095.X are disclosed
Catalyst containing silicoaluminophosphamolecular molecular sieve composition, it has been investigated that oxygenatedchemicals can in lower temperature, carbon deposition catalyst
It is converted into low-carbon alkene, conversion ratio is higher, but this method needs replacing the catalyst of existing catalytic unit, and to riser
It is individually transformed settler part.
Summary of the invention
The main purpose of the present invention is to provide the combined methods of a kind of catalytic cracking and lighter hydrocarbons deep processing, existing to overcome
The low problem of lighter hydrocarbons deep processing device product yield in technology.
To achieve the goals above, the present invention provides the combined method of a kind of catalytic cracking and lighter hydrocarbons deep processing, the party
Method includes the following steps:
Step 1, establish a lighter hydrocarbons collection system: the polypropylene plant that is configured in existing Petrochemical Enterprises, MTBE device,
The separation system or device of one or more of alkyl plant, Etherification of Light FCC Gasoline device lighter hydrocarbons deep processing device flow out pipeline
C3~C6 lighter hydrocarbons collection system is established by newly-built connecting pipe in position, collects the part or complete of wherein one or several strands
Portion's unreacted C3~C6 lighter hydrocarbons；
Step 2, C3~C6 lighter hydrocarbons of collection are pre-processed: C3~C6 lighter hydrocarbons that step 1 is collected is passed through dividing wall type
Heat exchanger or boiler make it be gasified totally, and the pressure of lighter hydrocarbons is greater than 0.5MPa after gasification, and temperature need to meet lighter hydrocarbons after gasification simultaneously
Temperature is greater than 20 DEG C greater than 160 DEG C, the degree of superheat；
Step 3, C3~C6 lighter hydrocarbons after step 2 is gasified totally individually or after mixing with vapor are passed through catalytic cracking dress
It sets, is contacted with the regenerated catalyst of heat, react the matched lighter hydrocarbons of generation Petrochemical Enterprises in catalyst cracker inner part and add deeply
Tooling sets required active lighter hydrocarbons.
The combined method of catalytic cracking of the present invention and lighter hydrocarbons deep processing, wherein polypropylene plant described in step 1,
The raw material of one or more of MTBE device, alkyl plant, Etherification of Light FCC Gasoline device is preferably derived from catalytic cracking reaction
Device.
The combined method of catalytic cracking of the present invention and lighter hydrocarbons deep processing, wherein activity lighter hydrocarbons described in step 3 are preferred
It is passed through one of the polypropylene plant that existing Petrochemical Enterprises are configured, MTBE device, alkyl plant, Etherification of Light FCC Gasoline device
Or it is handled in several lighter hydrocarbons deep processing devices.
The combined method of catalytic cracking of the present invention and lighter hydrocarbons deep processing, wherein step 2 is complete in the step 3
C3~C6 lighter hydrocarbons after gasification individually or after mix with vapor are passed through catalytic cracking unit, refer to C3~C6 lighter hydrocarbons it is independent or with
The lighter hydrocarbons feed nozzle of individual lighter hydrocarbons riser reactor lower part in catalytic cracking unit, Huo Zhetong are passed through after vapor mixing
Enter the lighter hydrocarbons feed nozzle of the heavy oil feed nozzle lower part of heavy oil riser in catalytic cracking unit, or is passed through heavy oil riser
Pre-lift jet chimney or dry gas pre-lifting pipeline enter back into heavy oil riser pre lift zone after mixing with steam.
The combined method of catalytic cracking of the present invention and lighter hydrocarbons deep processing, wherein in the catalytic cracking unit
Riser uses expanding interior expanding containing the expanding riser of vertical tranporter structure or bottom without expanding riser or bottom
The expanding riser of riser or middle part.
The combined method of catalytic cracking of the present invention and lighter hydrocarbons deep processing, wherein the collected unreacted C3~
C6 lighter hydrocarbons are preferably enriched in propane, normal butane, iso-butane, butylene, middle one or more of lighter hydrocarbons logistics of light petrol after ether.
The combined method of catalytic cracking of the present invention and lighter hydrocarbons deep processing, wherein described from MTBE device and/or light
It include methanol in the unreacted C3~C6 lighter hydrocarbons recycled in gasoline etherification device.
The combined method of catalytic cracking of the present invention and lighter hydrocarbons deep processing, wherein in the step 3, be passed through catalysis
The weight of C3~C6 lighter hydrocarbons after being gasified totally in cracking unit preferably accounts for the 0 of the heavy oil weight being passed through in the catalytic cracking unit
~40%.
The combined method of catalytic cracking of the present invention and lighter hydrocarbons deep processing, wherein in the step 3, C3~C6 is light
The Contact Temperature of the regenerated catalyst of hydrocarbon and heat is preferably 640~700 DEG C, and the outlet temperature of the lighter hydrocarbons riser is 580
~670 DEG C；The outlet temperature of the heavy oil riser is 500~560 DEG C.
The combined method of catalytic cracking of the present invention and lighter hydrocarbons deep processing, wherein the regenerated catalyst is catalysis
Cracking catalyst, the active component of the catalytic cracking catalyst be selected from Y or HY type zeolite with or without rare earth, with or without
One of ultrastable, silicoaluminophosphate zeolite, ZSM-5 zeolite and silica-rich zeolite with five-membered ring structure of rare earth or
Several or described catalytic cracking catalyst is amorphous silicon aluminium catalyst.
The combined method of catalytic cracking of the present invention and lighter hydrocarbons deep processing, wherein in the catalytic cracking catalyst
Preferably comprise account for catalytic cracking catalyst weight ratio 5%~40% five-membered ring structure zeolite.
Beneficial effects of the present invention:
The combined method of catalytic cracking provided by the invention and lighter hydrocarbons deep processing optimizes intermediate reaction object in different device
Between flow direction to optimizing integral product structure, and part operation unit can be cut off, save device operation energy consumption.It such as takes ether
Lighter hydrocarbons enter catalytic unit freshening afterwards, and olefin isomerization in lighter hydrocarbons after ether is realized in catalytic unit, can save ether-based device
Isomerization unit；A small amount of methanol need not be separated and return catalytic unit freshening by lighter hydrocarbons after ether, thus after ether device methanol
Extraction tower and methanol distillation column can also be cut off, and methanol enters the yield and selectivity that low-carbon alkene can be improved in catalytic unit freshening,
Optimize catalytic unit product distribution；In equivalent fixture scale, because lighter hydrocarbons recycle between catalytic unit and ether-based device,
Raw material of etherification can be greatly improved, etherification product yield is improved.
In addition, since the unreacted lighter hydrocarbons separated in lighter hydrocarbons deep processing device are returned to catalytic cracking unit by the present invention
It is reacted, generates active lighter hydrocarbons and continue lighter hydrocarbons deep process, improve the yield of the product of lighter hydrocarbons deep processing device.
Detailed description of the invention
Fig. 1 is the catalytic unit and MTBE device group technology schematic diagram of the embodiment of the present invention 1；
Fig. 2 is the catalytic unit and Etherification of Light FCC Gasoline device group technology schematic diagram of the embodiment of the present invention 2；
Fig. 3 is the catalytic unit and ether-based device group technology schematic diagram of the embodiment of the present invention 3；
Fig. 4 is the devices group technology schematic diagrames such as catalytic unit and MTBE, the methyl ethyl ketone of the embodiment of the present invention 4；
Fig. 5 is that the present invention establishes catalytic unit in Petrochemical Enterprises and lighter hydrocarbons deep processing device is combined the signal of technique
Figure.
Specific embodiment
Elaborate below to the embodiment of the present invention: embodiment carries out reality under the premise of the technical scheme of the present invention
It applies, gives detailed embodiment and process, but protection scope of the present invention is not limited to following embodiments, the following example
Middle test method without specific conditions, usually according to normal condition.
The present invention provides the combined methods of a kind of catalytic cracking and lighter hydrocarbons deep processing.Specifically, being incited somebody to action about a kind of
The produced lighter hydrocarbons of catalytic cracking unit are passed through lighter hydrocarbons deep processing device and are reacted, and the unreacted lighter hydrocarbons in part pass through lighter hydrocarbons recovery
The appropriate location of Returning catalyticing cracking device reactor is reacted again after system and pretreatment, and the product after reaction is passed through again
Lighter hydrocarbons deep processing device is handled.The active lighter hydrocarbons yield of lighter hydrocarbons deep processing device can be improved in the present invention, while can be certain
Degree reduces olefin(e) centent in gained gasoline blend component.
Lighter hydrocarbons within the scope of unreacted C3~C6 of lighter hydrocarbons deep processing device recycling are urged in 620 DEG C or more, catalytic cracking
There is quite high conversion ratio, a series of thermal cracking, oligomeric cracking, hydrogen can occur for lighter hydrocarbons under reaction condition existing for agent
Transfer, isomerization etc. are reacted, and the lighter hydrocarbons ratio lacked in lighter hydrocarbons deep processing device raw material in the product after reaction is substantially increased.Such as
The content of isobutene is almost nil in C4 after ether, and after carrying out above-mentioned reaction, isobutene, which can rise to, accounts for entire butenes ratio
40% or more；Propane, iso-butane, normal butane etc. are under high-temperature catalytic cracking conditions, it may have considerable conversion ratio and ethylene, third
The yield of alkene, butylene.
The present invention provides the combined method of a kind of catalytic cracking and lighter hydrocarbons deep processing, which comprises catalytic cracking institute
C3~the C4 and/or light petrol of production pass through respectively enter after pretreatment of raw material polypropylene plant that existing Petrochemical Enterprises are configured,
Reacted in the lighter hydrocarbons deep processing device such as alkyl plant, MTBE and/or Etherification of Light FCC Gasoline device, recycle unreacted C3~
C6 lighter hydrocarbons, return catalytic unit reacts again after being heated the pretreatment such as gasification, to improve the energy of catalytic cracking unit production
The yield of the reactive active lighter hydrocarbons such as propylene, iso-butane, butylene enough as lighter hydrocarbons deep processing device raw material.To realization pair
The lighter hydrocarbons deep process such as catalytic cracking and alkylation carries out complex optimum, forms group technology.The present invention can be to refinery
Under the premise of the technology of enterprise, catalyst do big adjustment, the treating capacity of existing Petrochemical Enterprises lighter hydrocarbons deep processing device is improved
And product yield, raising polypropylene, alkylate oil, methyl ethyl ketone, methyl tertiary butyl ether(MTBE) (MTBE) and tert amyl methyl ether(TAME) (TAME),
The etherification products yield such as methyl- tert hexyl ether (MTHEXE), methyl- tert heptyl ether (MTHEPE), while can reduce to a certain degree
Olefin(e) centent in gasoline blend component.The product distribution that Petrochemical Enterprises can significantly be optimized using the present invention improves high value production
Product yield, increases economic efficiency.
The present invention selects on the basis of carrying out comprehensive accounting optimization to catalytic cracking and C3~C6 lighter hydrocarbons deep processing device
The lighter hydrocarbons logistics reacted again into catalytic unit, recycling unreacted C3~C6 lighter hydrocarbons enter unreacted lighter hydrocarbons and collect and pre-
Processing system refers to the lighter hydrocarbons deep processing such as the polypropylene configured from Petrochemical Enterprises, alkylation, MTBE and/or Etherification of Light FCC Gasoline
The some or all of unreacted lighter hydrocarbons of one or several strands of separation system intermediate stream or the device outflow of device collect into
Enter the collection of unreacted lighter hydrocarbons and pretreatment system.The selection principle of lighter hydrocarbons logistics fully considers the production of lighter hydrocarbons high-temperature catalytic cracking
Object distribution and the factors such as product and poor, the local market situation of cost of material.Therefore the present invention can be according to market, sufficiently excavation catalysis
The potentiality of device and lighter hydrocarbons deep processing device carry out relatively flexible adjustment to it, thus voluminous Petrochemical Enterprises lighter hydrocarbons deep processing dress
The reactive active lighter hydrocarbons yield such as machinable propylene, isobutene, iso-butane, butylene is set, and then produces cost performance in market
High or in short supply product improves the profitability under complicated turn of the market of Petrochemical Enterprises.
The present invention by the unreacted lighter hydrocarbons of recycling enter catalytic cracking unit react again (freshening) can use it is following several
Freshening mode, i.e. C3~C6 lighter hydrocarbons individually or with individual lighter hydrocarbons freshening is passed through in catalytic cracking unit after vapor mixing are reacted
Device bottom, be perhaps passed through the heavy oil feed nozzle lower part of heavy oil riser in catalytic cracking unit lighter hydrocarbons feed nozzle or
Be passed through catalyst cracker pre-lift jet chimney or dry gas pre-lifting pipeline mixed with steam after enter back into riser and mention in advance
Rise section.The present invention, which emphasizes to enter lighter hydrocarbons, simultaneously is introduced into dividing wall type heat exchanger before catalytic cracking unit reactor (shell-and-tube changes
Hot device, lamella heat exchanger etc.), the equipment such as waste heat boiler or conventional boiler can also be used be gasified totally, heat source can be
The middle part of fractionating column or bottom cycle oil or steam or high-temperature flue gas or the combustion heat etc..The pressure of gas in injecting lift pipe
Power must be greater than 0.5MPa, and the dew-point temperature of vapor is 152 DEG C under this pressure, the dew point of light petrol component C5~C6 90~
150℃；To guarantee that lighter hydrocarbons can smoothly enter into riser reactor, while avoiding causing in lighter hydrocarbons and vapor heat transfer process
Lighter hydrocarbons or vapor regelation are at liquid, and the lighter hydrocarbons in injecting lift pipe need to meet simultaneously following two condition: (1) after gasifying
Lighter hydrocarbons pressure is greater than 0.5MPa；(2) lighter hydrocarbons temperature is greater than 160 DEG C after gasifying, while considering that lighter hydrocarbons may there are also heavier components
Gasoline, lighter hydrocarbons feed pressure may more high factor, therefore it is required that the light hydrocarbon temperature actually fed is on dew-point temperature
20 DEG C, i.e. the degree of superheat of lighter hydrocarbons is 20 DEG C；Above-mentioned two condition will meet simultaneously.Lighter hydrocarbons of the present invention may further enter into pre- mention
Liter jet chimney or dry gas pre-lifting pipeline enter back into promotion bottom of the tube after mixing with steam.Catalytic cracking of the present invention mentions
The expanding interior expanding riser containing vertical tranporter structure of common pre-lift structure or bottom can be used in riser reaction, or
The expanding riser in middle part.Using technical measures of the invention, emphasize the mixed gas of lighter hydrocarbons or lighter hydrocarbons and vapor sufficiently mistake
It is thermal evaporation, and can be used as a step lift gas for promoting the regenerated catalyst of the heat to come from regenerator conveying；In this process
In, lighter hydrocarbons can be sufficiently mixed with the regenerated catalyst of heat and uniformly contact, and lighter hydrocarbons can also be heated to high temperature faster, exchange heat
There is no liquid phase to occur that catalyst heat is avoided to collapse in the process.The lighter hydrocarbons heating temperature of this technology implementation process can be
160~500 DEG C, preferably 200~400 DEG C.It is smaller to the transformation of existing catalytic cracking unit using technical measures of the invention, one
As only need to establish the heat exchanger or heating furnace of the lighter hydrocarbons collection conduit of Petrochemical Enterprises, lighter hydrocarbons heating, and the lighter hydrocarbons after overheat are connected
Access the appropriate pipeline of catalytic unit or gas nozzle；Slave dry gas pre-lifting pipeline of the invention is passed through overheat light hydrocarbon gas
When retrofit scheme, or even it can be completed in the state that catalytic unit is not stopped work.When catalytic unit processing scheme change or it is subsequent
The factors such as fractionation, aerostatic press, Vapor recovery unit, gas separation also can be convenient by limited time and cut out the solution of the present invention, do not influence
The normal operating of device.
Unreacted C3~C6 lighter hydrocarbons of the present invention enter the freshening amount of catalytic unit, to enter the heavy oil amount of catalytic unit
On the basis of be 0~40 (weight) %, the catalytic unit lighter hydrocarbons and regenerated catalyst agent Contact Temperature after freshening lighter hydrocarbons are 640~
700 DEG C, the outlet temperature of catalytic unit riser is 500~560 DEG C.
Some unreacted methanol can be contained in the lighter hydrocarbons collected after ether-based device of the invention.In etherification reaction mistake
Cheng Zhong, in order to recycle unreacted methanol, usually by from the mixture of lighter hydrocarbons and methanol after the ether that etherificate fractionator overhead obtains,
Methanol is extracted to separate lighter hydrocarbons after ether with water into methanol extraction tower, and the mixture of first alcohol and water also needs methanol to return
It receives tower to be separated, energy consumption is very high.Methanol injection catalytic cracking unit is realized methanol conversion and petroleum by the present invention simultaneously
The catalytic cracking of hydrocarbon couples.The present invention passes through the study found that quantity of methyl alcohol is relatively fewer contained by lighter hydrocarbons after ether, can be without isolation
Catalytic unit freshening is returned to, into lighter hydrocarbons freshening position of the invention, since reaction severity is relatively high, methanol is almost complete
Full conversion；To the selection of catalytic cracking catalyst also without particular/special requirement.
Group of the invention, which is combined into, guarantees merchantable gasoline boiling range, according to lighter hydrocarbons freshening after the ether of methanol extraction tower top, then ether
Lighter hydrocarbons a part enters catalytic cracking unit freshening afterwards, and a part throws away device；According to etherificate separation tower top with light after ether
When mixed raw material freshening based on hydrocarbon, supplemented by a small amount of methanol, then the part light petrol of catalytic cracking unit and/or mixing carbon four are gone
Ether-based device, part light petrol and/or mixing carbon four throw away Association Technology Devices.
Signified etherification technology of the invention is general MTBE and catalytic light gasoline etherification technology, and it is proprietary to be not specific to a certain item
Etherification technology, generally comprise etherification reaction unit, realize product separation etherificate fractionating column and methanol extraction tower, Methanol Recovery
Tower, coupling technique only need to by be etherified fractionator overhead based on lighter hydrocarbons after ether, the material containing a small amount of methanol return catalysis dress
It sets；Lighter hydrocarbons after the ether of methanol extraction tower top can also be returned to catalytic unit.
Catalytic unit of the invention can be carried out improving a little on the basis of existing catalytic unit and be can be realized, if be equipped with single
Only riser can inject the raw material containing unreacted lighter hydrocarbons in independent riser；It, will not if only one riser
Reaction lighter hydrocarbons preferentially enter promotion bottom of the tube, since the cracking that lighter hydrocarbons are first contacted and absorbed heat with the regenerated catalyst of high temperature is anti-
It answers, the temperature of catalyst can be reduced, therefore lighter hydrocarbons are reacted with regenerated catalyst, green coke is seldom on catalyst, i.e., catalyst retains
Most of activity.Lighter hydrocarbons freshening improves the oil ratio of heavy oil and catalyst to a certain extent, reduces the finish contact temperature difference, has
Conducive to the optimization of catalyst article distribution.Due to requiring the lighter hydrocarbons into riser reactor to be gasified totally, lighter hydrocarbons of the present invention
Enter riser bottom after can mixing by pre-lift jet chimney or dry gas pre-lifting pipeline with steam.
Catalytic cracking unit of the invention does not have particular/special requirement to catalyst, is suitable for all types of catalytic cracking and is catalyzed
Agent, active component are selected from Y or HY type zeolite, the ultrastable with or without rare earth, silicoaluminophosphate with or without rare earth
Molecular sieve, ZSM-5 series zeolite or with one of other methods silica-rich zeolite with five-membered ring structure obtained, two kinds or
Three kinds of catalyst and amorphous silicon aluminium catalyst.When catalytic unit optimization operation, original catalyst can be used, it can also
Five-membered ring structure using containing selecting the catalyst of type molecular sieve, preferably in active component containing weight ratio 5%~40%
The catalyst of zeolite.
Embodiment of the method for the invention that the following is further explained with reference to the attached drawings on experimental provision and commercial plant and
Feature.
Lighter hydrocarbons deep processing device in Fig. 5 includes polypropylene plant, MTBE device, alkyl plant, Etherification of Light FCC Gasoline dress
It sets, can also be increased and decreased according to the actual state of enterprise.Enterprise, can be according to market, light hydrogen cracking in actual moving process
Characteristic, device operational circumstances are selected to be adjusted flexibly the type and quantity into the freshening lighter hydrocarbons of catalytic unit.Implementation specific as follows
Example.
Embodiment 1
Present embodiments provide a kind of process that catalytic cracking is combined with ether-based device, shown in Figure 1, this reality
The commercial plant that the heavy oil catalytically cracking equipment in example is 2,500,000 tons/year of certain Petrochemical Enterprises is applied, ether-based device is that design produces 8 per year
The MTBE device of ten thousand tons of MTBE.In experimentation by lighter hydrocarbons after the ether of methanol extraction tower top after heat exchanger heats with promoted steam
Together into the pre-lift steam pipework of the promotion bottom of the tube of catalytic unit, the steam after gasification alternatively falls the pre- of equal volume
Promote steam；The top extraction of the etherificate knockout tower based on lighter hydrocarbons after ether, supplemented by a small amount of methanol has also been investigated in experiment simultaneously
Lighter hydrocarbons mixed raw material enters the promotion bottom of the tube of catalytic unit after heat exchanger heats together with promotion steam.
The freshening amount of lighter hydrocarbons is 5~200,000 tons/year after ether, and freshening lighter hydrocarbons are preferentially anti-with regenerated catalyst in promotion bottom of the tube
It answers, lighter hydrocarbons and regenerative agent Contact Temperature are 640~700 DEG C, and the outlet temperature of catalytic unit riser is 500~540 DEG C.Table 1
List in embodiment 1 two embodiments as a result, lighter hydrocarbons are obtained from methanol extraction tower top after the ether that wherein scheme 1 uses,
And what scheme 2 used extracts out from the top of etherificate knockout tower.
1 catalytic unit of table and MTBE Combinatorial Optimization embodiment
Embodiment 2
Present embodiments provide the combined technical method of a kind of catalytic cracking and etherificate, shown in Figure 2, the present embodiment
In heavy oil catalytically cracking equipment be 2,500,000 tons/year of certain Petrochemical Enterprises commercial plant, ether-based device be design 500,000 tons of light vapour
Oily ether-based device.In experimentation by lighter hydrocarbons after the ether of methanol extraction tower top by after heat exchanger heating and gasifying from heavy oil riser
Heavy oil feed nozzle below lighter hydrocarbons feed nozzle enter promotion bottom of the tube.
After ether the freshening amount of light petrol be 15~300,000 tons/year, freshening lighter hydrocarbons pass through be located at promoted bottom of the tube lighter hydrocarbons into
Material nozzle is preferentially reacted with regenerated catalyst, and lighter hydrocarbons and regenerative agent Contact Temperature are 640~700 DEG C, catalytic unit riser
Outlet temperature is 500~540 DEG C.Table 2 lists an embodiment result in embodiment 2.
2 catalytic unit of table and Etherification of Light FCC Gasoline device Combinatorial Optimization embodiment
Embodiment 3
Present embodiments provide the combined technical method of a kind of catalytic cracking and etherificate, shown in Figure 3, the present embodiment
In heavy oil catalytically cracking equipment be 2,500,000 tons/year of certain Petrochemical Enterprises commercial plant, ether-based device be design produce per year 80,000 tons
The MTBE device of MTBE and it is designed as 500,000 tons of Etherification of Light FCC Gasoline devices.It will be after two kinds of ethers of methanol extraction tower top in experimentation
After lighter hydrocarbons mixing by after heat exchanger heating and gasifying from the lighter hydrocarbons feed nozzle below the heavy oil feed nozzle of heavy oil riser into
Enter to promote bottom of the tube.
C4 and the freshening amount for light petrol after ether are respectively 5~200,000 tons/year and 15~300,000 tons/year after ether, after mixing
Freshening lighter hydrocarbons preferentially react with regenerated catalyst promoting bottom of the tube, lighter hydrocarbons and regenerative agent Contact Temperature are 640~700 DEG C,
The outlet temperature of catalytic unit riser is 500~540 DEG C.Table 3 lists an embodiment result in embodiment 3.
3 catalytic unit of table and MTBE, Etherification of Light FCC Gasoline device Combinatorial Optimization embodiment
Embodiment 4
The devices group technologies such as a kind of catalytic cracking and MTBE, methyl ethyl ketone are present embodiments provided, it is shown in Figure 4,
Heavy oil catalytically cracking equipment in the present embodiment is the commercial plant of 600,000 tons/year of certain Petrochemical Enterprises, and ether-based device is design year
It produces the MTBE device of 50,000 tons of MTBE and is designed as producing 40000 tons of methyl ethyl ketone plants per year.By catalytic unit and subsequent lighter hydrocarbons deep processing
The working ability of device limits, and that plans 60,000 tons/year of the separator being fed for methyl ethyl ketone plant is rich in iso-butane (content
For 90w%) the heated gasification of logistics by importing pre-lift steam pipe line after dry gas pre-lifting pipeline with pre-lift steam one
Block enters promotion bottom of the tube.
Freshening amount rich in iso-butane logistics is respectively 3~80,000 tons/year, and heating and gasifying passes through dry gas and riser pipeline
Enter promotion bottom of the tube with steam miscella is promoted, preferentially reacted with regenerated catalyst, lighter hydrocarbons and regenerative agent Contact Temperature are 640
~700 DEG C, the outlet temperature of catalytic unit riser is 500~540 DEG C.Table 4 lists an embodiment knot in embodiment 4
Fruit.
4 catalytic unit of table and MTBE, methyl ethyl ketone plant Combinatorial Optimization embodiment
It can be seen that compared with prior art that (i.e. unreacted lighter hydrocarbons are not collected in lighter hydrocarbons deep processing device by table 1-4
It is passed through catalytic cracking unit and carries out freshening), using method of the invention, the yield of the active lighter hydrocarbons of catalytic cracking unit production has
Increased, the yield of the target product of lighter hydrocarbons deep processing device is also correspondinglyd increase.
Certainly, the present invention can also have other various embodiments, without deviating from the spirit and substance of the present invention, ripe
Various corresponding changes and modifications, but these corresponding changes and modifications can be made according to the present invention by knowing those skilled in the art
It all should belong to the protection scope of the claims in the present invention.
Claims (13)
1. the combined method of a kind of catalytic cracking and lighter hydrocarbons deep processing, which is characterized in that this method comprises the following steps:
Step 1, a lighter hydrocarbons collection system is established: in polypropylene plant, the MTBE device, alkyl that existing Petrochemical Enterprises are configured
Makeup sets, the separation system of one or several lighter hydrocarbons deep processing devices in Etherification of Light FCC Gasoline device or device outflow pipeline position
It sets, C3~C6 lighter hydrocarbons collection system is established by newly-built connecting pipe, collect wherein one or some or all of several strands
Unreacted C3~C6 lighter hydrocarbons；
Step 2, C3~C6 lighter hydrocarbons of collection are pre-processed: C3~C6 lighter hydrocarbons that step 1 is collected is passed through wall-type heat exchange
Device or boiler make it be gasified totally, and the pressure of C3~C6 lighter hydrocarbons is greater than 0.5MPa after gasification, and temperature need to meet light after gasification simultaneously
Hydrocarbon temperature is greater than 20 DEG C greater than 160 DEG C, the degree of superheat；
Step 3, C3~C6 lighter hydrocarbons after step 2 is gasified totally individually or after mixing with vapor are passed through mentioning for catalytic cracking unit
Riser reactors are contacted with the regenerated catalyst of heat, and it is deep to generate the matched lighter hydrocarbons of Petrochemical Enterprises for reaction in riser reactor
Active lighter hydrocarbons needed for processing unit (plant).
2. the combined method of catalytic cracking according to claim 1 and lighter hydrocarbons deep processing, which is characterized in that the step 3
C3~C6 lighter hydrocarbons after middle step 2 is gasified totally individually or after mixing with vapor are passed through the promotion tube reaction of catalytic cracking unit
Device refers to that C3~C6 lighter hydrocarbons individually or after mixing with vapor are passed through the lighter hydrocarbons promotion of independent lighter hydrocarbons freshening in catalytic cracking unit
The lighter hydrocarbons feed nozzle of pipe lower part；Or be passed through catalytic cracking unit heavy oil riser heavy oil feed nozzle lower part lighter hydrocarbons into
Expect nozzle, or imports pre-lift steaming after being passed through the pre-lift jet chimney or dry gas pre-lifting pipeline of heavy oil promotion bottom of the tube
Steam pipe road is mixed with steam enters back into the pre lift zone that heavy oil promotes bottom of the tube.
3. the combined method of catalytic cracking according to claim 2 and lighter hydrocarbons deep processing, which is characterized in that the catalysis is split
Disguise the heavy oil riser in setting to use without the expanding interior expanding promotion containing vertical tranporter structure of expanding riser or bottom
Pipe or the expanding riser of the expanding riser in bottom or middle part.
4. the combined method of catalytic cracking according to claim 1 and lighter hydrocarbons deep processing, which is characterized in that described in step 1
The original of polypropylene plant, MTBE device, alkyl plant, one or several lighter hydrocarbons deep processing devices in Etherification of Light FCC Gasoline device
Material derives from catalytic cracking unit.
5. the combined method of catalytic cracking according to claim 1 and lighter hydrocarbons deep processing, which is characterized in that collected
Unreacted C3~C6 lighter hydrocarbons include that the separating methanol tower top of propane, normal butane, iso-butane, butylene and Etherification of Light FCC Gasoline device separates
One or more of formed group of light petrol after ether.
6. the combined method of catalytic cracking according to claim 1 and lighter hydrocarbons deep processing, which is characterized in that described in step 3
Active lighter hydrocarbons refer to the polypropylene plant for entering step the 1 existing Petrochemical Enterprises and being configured, MTBE device, alkyl plant,
The lighter hydrocarbons that can be chemically reacted in one or several lighter hydrocarbons deep processing devices in Etherification of Light FCC Gasoline device.
7. the combined method of catalytic cracking according to claim 6 and lighter hydrocarbons deep processing, which is characterized in that described in step 3
Active lighter hydrocarbons refer to the propylene into polypropylene plant, into the isobutene of MTBE device, into the iso-butane of alkyl plant
With chain butylene, into the iso-amylene or dissident's alkene of Etherification of Light FCC Gasoline device.
8. the combined method of catalytic cracking according to claim 7 and lighter hydrocarbons deep processing, which is characterized in that the iso-amylene
For 2-methyl-1-butene alkene and/or 2- methyl-2-butene, dissident's alkene is 2- Methyl-1-pentene.
9. the combined method of catalytic cracking according to claim 1 and lighter hydrocarbons deep processing, which is characterized in that described from MTBE
It include methanol in the unreacted C3~C6 lighter hydrocarbons recycled in device and/or Etherification of Light FCC Gasoline device.
10. the combined method of catalytic cracking according to claim 1 and lighter hydrocarbons deep processing, which is characterized in that the step 3
In, the weight for being passed through C3~C6 lighter hydrocarbons after being gasified totally in catalytic cracking unit accounts for the heavy oil being passed through in the catalytic cracking unit
The 0~40% of weight.
11. the combined method of catalytic cracking according to claim 4 and lighter hydrocarbons deep processing, which is characterized in that the step 3
In, the Contact Temperature of the regenerated catalyst of C3~C6 lighter hydrocarbons and heat is 640~700 DEG C, the outlet temperature of the lighter hydrocarbons riser
Degree is 580~670 DEG C, and the outlet temperature of the heavy oil riser is 500~560 DEG C.
12. the combined method of catalytic cracking according to claim 1 and lighter hydrocarbons deep processing, which is characterized in that the regeneration
Catalyst is catalytic cracking catalyst, and the active component of the catalytic cracking catalyst is selected from Y the or HY type with or without rare earth
Zeolite, the ultrastable with or without rare earth, silicoaluminophosphate zeolite, ZSM-5 zeolite and the high silicon boiling with five-membered ring structure
One or more of stone or the catalytic cracking catalyst are amorphous silicon aluminium catalyst.
13. the combined method of catalytic cracking according to claim 12 and lighter hydrocarbons deep processing, which is characterized in that the catalysis
In Cracking catalyst containing account for catalytic cracking catalyst weight ratio 5%~40% five-membered ring structure zeolite.
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| CN113058508A (en) * | 2021-03-24 | 2021-07-02 | 宁夏瑞科新源化工有限公司 | Device and method for recycling polluted methanol |
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