CN102344831A - Petroleum hydrocarbon catalytic conversion method - Google Patents
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- CN102344831A CN102344831A CN2010102399215A CN201010239921A CN102344831A CN 102344831 A CN102344831 A CN 102344831A CN 2010102399215 A CN2010102399215 A CN 2010102399215A CN 201010239921 A CN201010239921 A CN 201010239921A CN 102344831 A CN102344831 A CN 102344831A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention discloses a petroleum hydrocarbon catalytic conversion method. The petroleum hydrocarbon catalytic conversion method comprises the following steps that raw oil contacts a mesoporous zeolite-rich catalyst in a first reaction zone of a reactor and undergo a cracking reaction; a reactant flow and a part of the raw oil are fed into a second reaction zone of the reactor and further undergo a cracking reaction; reaction oil gas and a catalyst needing to be regenerated are separated out, wherein the catalyst needing to be regenerated is subjected to steam stripping and burning regeneration and then is fed back to the reactor; the reaction oil gas is subjected to separation to form a desired ethane product, propylene and aromatic hydrocarbon-rich catalytic gasoline; the aromatic hydrocarbon-rich catalytic gasoline is subjected to selective hydrogenation and then is fed into a aromatic hydrocarbon extraction device to produce a desired light aromatic hydrocarbon product by separation; and the extract oil obtained by the previous step is fed back to the first reaction zone of the reactor. Through petroleum hydrocarbon catalytic conversion method, an ethene yield is 22.43 wt%; a propylene yield is 33.22 wt%; and a benzene-toluene-xylene mixture yield is 25.28 wt%.
Description
Technical field
The present invention provides a kind of petroleum hydrocarbon catalytic conversion method on the basis of existing technology, particularly heavy feed stock is converted into low-carbon alkenes such as ethene and propylene, produces light aromatic hydrocarbons simultaneously, thereby realizes the efficient method of utilizing of petroleum resources.
Background technology
Ethene is one of most important basic material of petrochemical industry, through vinyl polymerization, with the alkylation of benzene and with the addition reaction of water, oxygen, halogen, can obtain a series of extremely valuable derivatives.World Ethylene industry continues keeping the situation of stable development.Estimate 2007～2012 years, the world will increase 3,878 ten thousand tons/year of ethene abilities newly, and average growth rate per annum reaches 5.6%, will reach 162,670,000 tons/year to world Ethylene throughput in 2012.At present, about in the world 98% ethene comes from the tube furnace steam cracking technology, and in the ethylene production raw material, petroleum naphtha accounts for 46%, and ethane accounts for 34%.
Propylene is one of most important alkene, and consumption is only second to ethene.World's production of propylene ability was about 8,348 ten thousand tons in 2007, and global propylene demand growth speed will reach 4.9% in 2006～2011 years, and global propylene demand will reach 8,834 ten thousand tons by 2011.The derivative of the maximum consumption of propylene is a polypropylene, accounts for 61% of global propylene consumption.2005, about 62% propylene in the whole world was from the coproduction of preparing ethylene by steam cracking, and 34% propylene also has 4% propylene from dehydrogenating propane and ethene-butylene metathesis reaction from plant catalytic cracking unit by-product.
Adopt prior steam cracking ethylene preparation, propylene route; Bigger to chemical industry lighter hydrocarbons demands such as lighter hydrocarbons, petroleum naphthas; Estimate to need in 2010 530000 tons/year of chemical industry light oils; The year two thousand twenty needs 700,000 tons/year of chemical industry light oils; And domestic crude oil is generally laid particular stress on; Chemical industry light oil is difficult to satisfy the demand of ethene, propylene feedstocks; Under the insufficient situation of petroleum resources; The variation of ethene, propylene feedstocks and heaviness have become ethene, propylene industrial development trend, and the exploitation of mink cell focus system ethene and propylene technology also will be opened up a new raw material approach to ethene, propylene industry.
EP305720A2 discloses a kind of hydrocarbon conversion processes of producing low-carbon alkene, and raw material is petroleum fractions, residual oil or the crude oil of different boiling ranges, in fluidized-bed or moving-burden bed reactor, uses solid acid catalyst, at 500～650 ℃ of temperature, pressure 1.5 * 10
5～3 * 10
5Pa, weight hourly space velocity 0.2～2.0h
-1, agent-oil ratio 2～12 condition under carry out catalytic conversion reaction, reacted catalyzer Returning reactor internal recycle behind coke burning regeneration uses.The overall yield of this method propylene and butylene can reach about 40 heavy %, and wherein productivity of propylene is up to 26.34 heavy %.
WO00/31215A1 discloses a kind of catalyst cracking method of producing alkene, and this method adopts ZSM-5 and/or ZSM-11 zeolite to do active component, is the catalyzer of matrix with a large amount of inert substances, is raw material with vacuum gas oil (VGO), and productivity of propylene is lower than 20 heavy %.
US 2002/0003103A1 discloses a kind of catalytic cracking process that increases productivity of propylene.At least the part gasoline product is introduced in second riser tube and is carried out cracking reaction again; And in the catalyst composition that is adopted except that containing macropore USY zeolite; The mineral binder bond component that also contains mesopore zeolites such as ZSM-5 and have cracking performance; Phosphorous in the mineral binder bond component wherein, its P/Al ratio is 0.1～10.
US 5009769 discloses a kind of cracking hydrocarbon method and has adopted duo-lift tube reactor cracking hydrocarbon raw material of different nature.Wax oil and residual oil inject first riser tube, cracking under agent-oil ratio 5～10, the condition of 1～4 second residence time; Straight-run spirit, straight run intermediate oil and catalysis heavy petrol inject second riser tube, cracking under agent-oil ratio 3～12, the condition of 1～5 second residence time, two terminal entering in the same settling vessel of riser tube, and shared follow-up fractionating system.
US 4422925 discloses the method that multiple hydro carbons with different cracking performances contacts and transforms with hot regenerated catalyst; The described hydro carbons of this method contains a kind of gas alkane raw material and a kind of liquid hydrocarbon raw material at least; This method has different cracking performances according to different hydrocarbon molecules; Adopt a plurality of reaction zones to carry out cracking reaction, with voluminous low-molecular olefine.
Light aromatic hydrocarbons (benzene, toluene and xylenes are called for short BTX) also is a kind of important Organic Chemicals, and output and scale are only second to ethene and propylene, and its derivative is widely used in Chemicals and fine chemicals such as producing chemical fibre, plastics and rubber.Light aromatic hydrocarbons production mainly comes from reformed gasoline and cracking of ethylene gasoline device.It is predicted; Satisfy following demand growth; In the period of 2006～2015; The whole world need increase the purified petroleum benzin production capacity of about 1,600 ten thousand tons of/year p-Xylol and 1,400 ten thousand tons/year newly, estimates the following market growth demand that possibly can't satisfy purified petroleum benzin and p-Xylol with the by-product of these devices as the source.
CN101362963A discloses a kind of catalysis conversion method of preparing aromatic hydrocarbons and light olefins, and the hydrocarbon raw material of different cracking performances contacts with catalytic cracking catalyst, at 450～750 ℃, weight hourly space velocity 0.1～800h
-1, reaction pressure 0.1～1.0MPa, catalytic cracking catalyst and raw material weight ratio 1～150; The weight ratio of water vapor and raw material is under 0.05～1.0 condition; In fluidized-bed reactor, carry out cracking reaction; Separate reclaimable catalyst and reaction oil gas; Reclaimable catalyst is Returning reactor after regenerating; Separating reaction oil gas; Obtain purpose product low-carbon alkene, aromatic hydrocarbons and cracked raw material again; This method is produced low-carbon alkenes such as propylene to greatest extent from heavy feed stock; Wherein productivity of propylene is more than the 40 heavy %, simultaneously aromatic hydrocarbons such as coproduction toluene and xylenes.
CN100487080C discloses a kind of chemical industry type oil refining method of producing low-carbon alkene and aromatic hydrocarbons; Stock oil with contact in the catalytic cracking reaction device through regenerated catalytic cracking catalyst, water vapor; Under weight ratio 0.05～0.6 condition of weight ratio 5～50, water vapor and the stock oil of 500～700 ℃ of temperature of reaction, pressure 0.15～0.4MPa, catalytic cracking catalyst and stock oil, react; Separate reclaimable catalyst and reaction oil gas, reclaimable catalyst is Returning reactor after regenerating; Separating reaction oil gas obtains purpose product low-carbon alkene and aromatic hydrocarbons.This method is produced low-carbon alkenes such as propylene, ethene to greatest extent from heavy feed stock, wherein the productive rate of propylene surpasses 30 heavy %, light aromatic hydrocarbons such as the BTX of coproduction simultaneously.
CN101362669A discloses a kind of catalysis conversion method of producing ethene, propylene and aromatic hydrocarbons, contacts with catalytic cracking catalyst with raw material at the hydro carbons of different cracking performances, at temperature 550-800 ℃, weight hourly space velocity 0.1～800h
-1, reaction pressure 0.10～1.0MPa, catalytic cracking catalyst and raw material weight ratio 10～150; The weight ratio of water vapor and raw material is under 0.15～1.0 condition; In fluidized-bed reactor, carry out cracking reaction; Separate reclaimable catalyst and reaction oil gas; Reclaimable catalyst is Returning reactor after regenerating; Separating reaction oil gas obtains purpose product low-carbon alkene and aromatic hydrocarbons through separation; Wherein 160～260 ℃ of cuts return catalytic pyrolysis as recycle stock, and ethane, propane, butane get into steam cracking and further produce ethene, propylene.Ethene and productivity of propylene weigh more than the % 20, simultaneously aromatic hydrocarbons such as coproduction toluene and xylenes.
Above-mentioned prior art exists two aspects not enough: the one, when producing low-carbon alkene, underuse arene underwater content in the gasoline; The 2nd, the technology of producing low-carbon alkene and light aromatic hydrocarbons fails to make full use of the hydro carbons resource, and also there are bigger room for promotion in especially light aromatics yield and quality.In order to satisfy the demand of industrial chemicals such as growing low-carbon alkene and aromatic hydrocarbons, be necessary to develop and a kind of heavy feed stock be converted into the catalysis conversion method of ethene, propylene and light aromatic hydrocarbons to greatest extent, thereby realize the efficient utilization of petroleum resources.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of catalysis conversion method that heavy feed stock is converted into ethene, propylene and BTX.
The technical scheme of petroleum hydrocarbon catalytic conversion method provided by the invention is following: this method is carried out in the reactor that comprises two reaction zones.
Stock oil contacts with the catalyzer that is rich in mesopore zeolite in first reaction zone of reactor, is 600～750 ℃, weight hourly space velocity 100～200h in temperature of reaction
-1, pressure 0.10～1.0MPa, catalyzer and stock oil the weight ratio of weight ratio 30～150 (hereinafter to be referred as agent-oil ratio), water vapor and raw material be to carry out cracking reaction under 0.05～1.0 the condition; Reactant flow and part material oil get into second reaction zone of reactor, at 450～600 ℃ of temperature of reaction, weight hourly space velocity 0.1～100h
-1, pressure 0.10～1.0MPa, catalyzer and stock oil weight ratio 1～30; The weight ratio of water vapor and stock oil is that cracking reaction further takes place under 0.05～1.0 the condition; Separate reclaimable catalyst and reaction oil gas; Reclaimable catalyst Returning reactor behind stripping, coke burning regeneration wherein; The product that reaction oil gas obtains comprising purpose product ethene, propylene and is rich in the catalytic gasoline of aromatic hydrocarbons through separation; Catalytic gasoline is after selective hydrogenation; Get into the aromatic extraction unit separation and obtain the light aromatic hydrocarbons of purpose product, and extract first reaction zone of oily Returning reactor out.
Said stock oil is selected from or comprises petroleum hydrocarbon and/or other mineral oil; Wherein petroleum hydrocarbon is selected from one or more in vacuum gas oil, atmospheric gas oil, coker gas oil, deasphalted oil, vacuum residuum, the long residuum, and other mineral oil is selected from one or more in liquefied coal coil, tar sand oil, the shale oil.
Said catalyzer comprises zeolite, inorganic oxide and optional clay, and each component accounts for total catalyst weight respectively: zeolite 1～50 heavy %, inorganic oxide 5～99 heavy %, clay 0～70 heavy %.Its mesolite is selected from mesopore zeolite and optional large pore zeolite as active ingredient, and mesopore zeolite accounts for 50～100 heavy % of zeolite gross weight, and preferred 70～100 heavy %, large pore zeolite account for 0～50 heavy % of zeolite gross weight, preferred 0～30 heavy %.Mesopore zeolite is selected from ZSM series zeolite and/or ZRP zeolite; Also can carry out modification with transition metals such as non-metallic elements such as phosphorus and/or iron, cobalt, nickel to above-mentioned mesopore zeolite; The more detailed description of relevant ZRP is referring to US5; 232; 675, the ZSM series zeolite is selected from one or more among the zeolite of ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38, ZSM-48 and other similar structures, and the more detailed description of relevant ZSM-5 is referring to US3; 702,886.Large pore zeolite is selected from one or more in this group zeolite that the ultra steady Y that is obtained by Rare Earth Y (REY), rare earth hydrogen Y (REHY), different methods, high silicon Y constitute.
Inorganic oxide is selected from silicon-dioxide (SiO as caking agent
2) and/or aluminium sesquioxide (Al
2O
3).
Clay is selected from kaolin and/or halloysite as matrix (being carrier).
Said reactor be selected from riser tube, etc. one or more the combination in the fluidized-bed, isodiametric fluidized-bed, upstriker transfer limes, downstriker transfer limes of linear speed; Or with the two or more combinations of a kind of reactor; Said combination comprises series connection or/and parallelly connected, and wherein riser tube is the isodiametric riser tube of routine or the riser tube of various forms reducing.Wherein the gas speed of fluidized-bed is 0.1～2 meter per second, and the gas speed of riser tube is 2～30 meter per seconds (disregarding catalyzer).
Preferred forms of the present invention is to carry out in a kind of reducing riser reactor, about the more detailed description of this reactor referring to CN1237477A.
In order to increase the agent-oil ratio of second reaction zone, improve the catalytic activity of catalyzer, can pass through supplemental heat or cold regenerated catalyst, half regenerated catalyst, reclaimable catalyst, live catalyst.Refrigerative regenerated catalyst and refrigerative half regenerated catalyst are that reclaimable catalyst obtains through two-stage regeneration and one section regeneration postcooling respectively; The regenerated catalyst carbon content is below the 0.1 heavy %; Be preferably below the 0.05 heavy %; Half regenerated catalyst carbon content is 0.1～0.9 heavy %, and preferably carbon content is 0.15～0.7 heavy %; The reclaimable catalyst carbon content is more than the 0.9 heavy %, and preferably carbon content is 0.9～1.2 heavy %.
Reaction oil gas also comprises dry gas, C3-4 alkane (being propane and butane), C4 alkene, diesel oil, slurry oil etc. through the product that separation obtains comprising purpose product ethene, propylene and is rich in the catalytic gasoline of aromatic hydrocarbons in the product.Wherein first reaction zone that C4 alkene can Returning reactor is or/and the further cracking of second reaction zone.
The catalytic gasoline selective hydrogenation is under there is situation in hydrogen, contacts with selective hydrogenation catalyst, at hydrogen dividing potential drop 1.2～8.0MPa (absolute pressure), 150～400 ℃ of temperature of reaction, hydrogen to oil volume ratio 150～600Nm
3/ m
3, volume space velocity 1～20h
-1React under the condition, the selective hydrogenation gasoline that obtains is as the raw material of aromatic extraction unit.Said selective hydrogenation catalyst is to be that active ingredient, activated alumina are the non-precious metal catalyst of carrier with Ni-W, Co-Ni-W, Ni-Mo or Co-Mo, requires this catalyzer to possess that high to take off diene active and desulphurizing activated.
The used extraction solvent of aromatic extraction unit is selected from one or more in tetramethylene sulfone, N-Methyl pyrrolidone, diethylene glycol ether, triethylene glycol ether, TEG, dimethyl sulfoxide (DMSO) and the N-formyl morpholine ether.The extractive process solvent recovery cycle is used.Extraction temperature is 40～120 ℃, and the volume ratio between the raw material of solvent and aromatic extraction unit is 0.5～5.0.Extracting oil out is purpose product B TX, and raffinating oil is non-aromatic hydrocarbons as one of raw material of catalytic pyrolysis.
Method such as separating ethene, propylene is identical with the method that those of ordinary skills know from reaction product; The method of from the catalytic gasoline of reaction oil gas, separating light aromatic hydrocarbons is that the solvent extracting is identical with the method for aromatics separation from steam cracking or reformed gasoline that those of ordinary skills know.
This technical scheme organically combines technologies such as catalytic pyrolysis, catalytic gasoline selective hydrogenation and the extracting of catalytic gasoline aromatic hydrocarbons, produces low-carbon alkene and light aromatic hydrocarbons such as ethene, propylene to greatest extent from the lower heavy feed stock of hydrogen richness.The present invention compared with prior art has following technique effect:
1, ethene, productivity of propylene and selectivity increase, and the therein ethylene productive rate can be up to 22.43 heavy %, and productivity of propylene is up to 33.22 heavy %.
2, the BTX productive rate is up to about 25.28 heavy %, and wherein the benzene productive rate is 4.46 heavy %, and the toluene productive rate is 12.82 heavy %, and the xylenes productive rate is 8.00 heavy %.
3, C4 alkene and/or aromatic hydrocarbons are raffinated oil and are mixed with stock oil, have improved the stock oil atomizing effect, and under the situation that the reaction severity reduces, the heavy oil productive rate reduces significantly.
4, other component productive rate reduces significantly in the dry gas.
Adopt method provided by the invention; The refinery can produce ethene, propylene and light aromatic hydrocarbons to greatest extent from heavy feed stock; Thereby realize the technological breakthrough of refinery's notion; Change to chemical industry type from traditional fuel type and fuel-lubricated oil type refinery production model; Make the refinery from single oil refining to industrial chemicals and production development of high added value derived product and extension; Both solve the petrochemical material problem of shortage, improved the economic benefit of refinery again.
Description of drawings
Accompanying drawing is the basic procedure synoptic diagram with catalysis conversion method of the present invention.
Embodiment
Further specify method provided by the present invention below in conjunction with accompanying drawing, but therefore the present invention does not receive any restriction.
Accompanying drawing is the basic procedure synoptic diagram with catalysis conversion method of the present invention.
Its technical process is following:
Promoting medium is in advance got into by reducing riser reactor 2 bottoms through pipeline 1; From the regenerated catalyst of pipeline 16 in the castering action lower edge riser that the promotes medium in advance accelerated motion that makes progress; C4 alkene and/or aromatic hydrocarbons are raffinated oil and are mixed after pipeline 3 and bottom from the first reaction zone I of the atomizing steam injecting lift pipe 2 of pipeline 4 with raw material; Mix with the existing logistics of riser reactor; Cracking reaction takes place in feedstock oil on the catalyst of heat; And upwards accelerated motion, be mixed into the second reaction zone II with the part material oil that injects through pipeline 5 and atomizing steam cracking reaction takes place from pipeline 6.The cyclonic separator that the reaction product oil gas that generates and the reclaimable catalyst of inactivation get in the settling vessel 8 through pipeline 7, the realization reclaimable catalyst separates with reaction product oil gas, and reaction product oil gas gets into collection chamber 9, and catalyst fines returns settling vessel by dipleg.Reclaimable catalyst flows to stripping stage 10 in the settling vessel, contacts with steam from pipeline 11.The reaction product oil gas that stripping goes out from reclaimable catalyst gets into collection chamber 9 behind cyclonic separator.Reclaimable catalyst behind the stripping gets into revivifier 13 through inclined tube 12, and main air gets into revivifier through pipeline 14, and the coke on the burning-off reclaimable catalyst makes the reclaimable catalyst regeneration of inactivation, and flue gas gets into the cigarette machine through pipeline 15.Catalyzer after the regeneration gets into riser tube through inclined tube 16.
Reaction product oil gas in the collection chamber 9 gets into follow-up separation system 18 through main oil gas piping 17, and separation obtains the catalytic pyrolysis dry gas and draws through pipeline 19, obtains one of purpose product-ethene through further separating; Separate the propane and the butane that obtain and draw through pipeline 20, propylene is drawn the two-propylene that obtains the purpose product through pipeline 21; The C 4 olefin that separation obtains is drawn through pipeline 3 and/or pipeline 5 through pipeline 22 and is returned riser tube cracking again; Diesel oil is drawn through pipeline 24 and is returned riser tube 2; Slurry oil is drawn through pipeline 25; The aromatic type gasoline that is rich in of catalytic pyrolysis C5～180 ℃ is drawn out to selective hydrogenation unit 26 through pipeline 23; Isolating light constituent draws through pipeline 27; Gasoline gets into aromatic hydrocarbons extracting unit 29 through pipeline 28 behind the hydrogenation; Aromatic hydrocarbons is raffinated oil and is drawn through pipeline 30; Mix through pipeline 3 and the first reaction zone I that returns riser reactor 2 with heavy feed stock, extraction oil is that three-aromatic hydrocarbons pipeline 31 of purpose product is drawn as purpose product B TX.
The following examples will further illustrate present method, but therefore not limit present method.
Used raw material is VGO among the embodiment, and its character is as shown in table 1.Used extraction solvent is a tetramethylene sulfone among the embodiment.The used selective hydrogenation catalyst trade mark is RSDS-1 among the embodiment, is produced by Sinopec catalyzer branch office.
Catalytic cracking catalyst preparation method used among the embodiment is summarized as follows:
1) with 20gNH
4Cl is dissolved in the 1000g water, and (Qilu Petrochemical company catalyst plant is produced, SiO in this solution, to add 100g (butt) crystallization product ZRP-1 zeolite
2/ Al
2O
3=30, content of rare earth RE
2O
3=2.0 heavy %), behind 90 ℃ of exchange 0.5h, cross and filter filter cake; Add 4.0gH
3PO
4(concentration 85%) and 4.5gFe (NO
3)
3Be dissolved in the 90g water, dry with the filter cake hybrid infusion; Then handle at 550 ℃ of roasting temperatures and obtained phosphorous and MFI structure mesopore zeolite iron in 2 hours, its elementary analytical chemistry consists of
0.1Na
2O·5.1Al
2O
3·2.4P
2O
5·1.5Fe
2O
3·3.8RE
2O
3·88.1SiO
2。
2) with 250kg decationized Y sieve water with 75.4kg halloysite (Suzhou china clay company Industrial products; Solid content 71.6 heavy %) making beating; Add 54.8kg pseudo-boehmite (Shandong Aluminum Plant's Industrial products, solid content 63 heavy %) again, its PH is transferred to 2～4 with hydrochloric acid; Stir; Under 60～70 ℃, left standstill aging 1 hour, keeping PH is 2～4, cools the temperature to below 60 ℃; Add 41.5kg aluminium colloidal sol (Qilu Petrochemical company catalyst plant product, Al
2O
3Content is 21.7 heavy %), stirred 40 minutes, obtain mixed serum.
3) the MFI structure mesopore zeolite (butt is 22.5kg) and DASY zeolite (the Qilu Petrochemical company catalyst plant Industrial products of the phosphorous and iron that step 1) is prepared; Lattice constant is 2.445～2.448nm; Butt is 2.0kg) join step 2) in the mixed serum that obtains; Stir; Spray drying forming; With ammonium dihydrogen phosphate (phosphorus content be 1 heavy %) washing, the flush away Na that dissociates
+, being drying to obtain the catalytic cracking catalyst sample, phosphorous MFI structure mesopore zeolite, 2 heavy %DASY zeolites, the 28 heavy % pseudo-boehmites, 7 with iron of 18 heavy % that consist of of this catalyzer weigh % aluminium colloidal sol and surplus kaolin.
Embodiment
This embodiment makes an experiment according to the flow process of accompanying drawing; Stock oil A is directly as the raw material of catalytic pyrolysis; On the middle-scale device by riser reactor, make an experiment, aromatic hydrocarbons is raffinated oil and stock oil is mixed into first reaction zone I bottom, at 640 ℃ of temperature of reaction, weight hourly space velocity 180h
-1, the weight ratio 60 of catalytic cracking catalyst and stock oil, the weight ratio of water vapor and stock oil are to carry out cracking reaction under 0.20 condition; At the second reaction zone II, reactant flow oil gas mixes the back at 540 ℃ of temperature of reaction, weight hourly space velocity 30h with C 4 olefin
-1The weight ratio 30 of catalytic cracking catalyst and stock oil; Water vapor and stock oil weight ratio are that cracking reaction further takes place under 0.15 condition; Reaction product oil gas separates at settling vessel with catalyzer to be generated; Product cuts by boiling range in separation system; Thereby obtain ethene, propylene and be rich in product such as aromatic type gasoline, the gasoline that is rich in aromatic hydrocarbons gets into the selective hydrogenation unit, at hydrogen dividing potential drop 1.6MPa, 270 ℃ of temperature of reaction, hydrogen to oil volume ratio 350, volume space velocity 4.0h
-1Reaction conditions under carry out hydrogenation; Gasoline behind the hydrogenation gets into the extracting unit through the tetramethylene sulfone extracting; Extraction temperature is 100 ℃; The volume ratio of the gasoline behind solvent and the hydrogenation is 3.0; Tell and raffinate oil (being mainly stable hydrocarbon) and extract oil (light aromatic hydrocarbons BTX) out, raffinate oil and return first reaction zone bottom and mixes further production ethene and propylene with stock oil.Operational condition and product distribute and list in table 3.
Can find out that from table 3 ethylene yield can reach 22.43 heavy %, productivity of propylene can reach 33.22 heavy %; The benzene productive rate is 4.46 heavy %; The toluene productive rate is 12.82 heavy %, and the xylenes productive rate is 8.00 heavy %, and coke yield only is 5.67 heavy %, and the slurry oil productive rate is 4.78 heavy %.
Table 1
| The stock oil numbering | A |
| Stock oil character | |
| Density (20 ℃), g/cm 3 | 0.9083 |
| Sulphur content, ppm | 3700 |
| Nitrogen content, ppm | 2600 |
| Aromatic hydrocarbons, heavy % | 24.7 |
| C, heavy % | 87.25 |
| H, heavy % | 12.75 |
| Boiling range (ASTM D-1160), ℃ | |
| IBP | 251 |
| 10％ | 362 |
| 30％ | 408 |
| 50％ | 437 |
| 70％ | 464 |
| 90％ | 510 |
| 95％ | 529 |
Table 2
| The catalytic pyrolysis unit | |
| The riser tube temperature out, ℃ | 530 |
| Riser reaction zone II | |
| Temperature of reaction, ℃ | 540 |
| Weight hourly space velocity, |
30 |
| Agent- |
30 |
| The weight ratio of water vapor/raw material | 0.15 |
| Riser reaction zone I | |
| Temperature of reaction, ℃ | 640 |
| Agent-oil ratio | 60 |
| Weight hourly space velocity, h -1 | 180 |
| The weight ratio of water vapor/raw material | 0.20 |
| Aromatic hydrocarbons extracting unit | |
| Temperature, ℃ | 100 |
| The solvent volume ratio | 3.0 |
| The selective hydrogenation unit | |
| The hydrogen dividing potential drop, MPa | 1.6 |
| Temperature of reaction, ℃ | 270 |
| Hydrogen to oil volume ratio | 350 |
| Volume space velocity, h -1 | 4.0 |
| Product distributes, heavy % | |
| Hydrogen+methane | 3.71 |
| Ethene | 22.43 |
| Propylene | 33.22 |
| Propane+butane | 4.91 |
| Benzene | 4.46 |
| Toluene | 12.82 |
| Xylenes | 8.00 |
| Slurry oil | 4.78 |
| Coke | 5.67 |
Claims (10)
1. a petroleum hydrocarbon catalytic conversion method is characterized in that stock oil contacts with the catalyzer that is rich in mesopore zeolite in first reaction zone of reactor, is 600～750 ℃, weight hourly space velocity 100～200h in temperature of reaction
-1, pressure 0.10～1.0MPa, catalyzer and stock oil the weight ratio of weight ratio 30～150, water vapor and raw material be to carry out cracking reaction under 0.05～1.0 the condition; Reactant flow and part material oil get into second reaction zone of reactor, at 450～600 ℃ of temperature of reaction, weight hourly space velocity 0.1～100h
-1, pressure 0.10～1.0MPa, catalyzer and stock oil weight ratio 1～30; The weight ratio of water vapor and stock oil is that cracking reaction further takes place under 0.05～1.0 the condition; Separate reclaimable catalyst and reaction oil gas; Reclaimable catalyst Returning reactor behind stripping, coke burning regeneration wherein; The product that reaction oil gas obtains comprising ethene, propylene and is rich in the catalytic gasoline of aromatic hydrocarbons through separation; Catalytic gasoline is after selective hydrogenation; Get into the aromatic extraction unit separation and obtain the light aromatic hydrocarbons of purpose product, and extract first reaction zone of oily Returning reactor out.
2. according to the method for claim 1; It is characterized in that said stock oil is selected from or comprises petroleum hydrocarbon and/or other mineral oil; Wherein petroleum hydrocarbon is selected from one or more in vacuum gas oil, atmospheric gas oil, coker gas oil, deasphalted oil, vacuum residuum, the long residuum, and other mineral oil is selected from one or more in liquefied coal coil, tar sand oil, the shale oil.
3. according to the method for claim 1, it is characterized in that said catalyzer comprises zeolite, inorganic oxide and optional clay, each component accounts for total catalyst weight respectively: zeolite 1～50 heavy %, inorganic oxide 5～99 heavy %, clay 0～70 heavy %.
4. according to the method for claim 3, it is characterized in that said zeolite as active ingredient, be selected from mesopore zeolite and optional large pore zeolite, mesopore zeolite accounts for 50～100 heavy % of zeolite gross weight, and large pore zeolite accounts for 0～50 heavy % of zeolite gross weight.
5. according to the method for claim 1; It is characterized in that said reactor be selected from riser tube, etc. one or more the combination in the fluidized-bed, isodiametric fluidized-bed, upstriker transfer limes, downstriker transfer limes of linear speed; Or with the two or more combinations of a kind of reactor; Said combination comprises series connection or/and parallelly connected, and wherein riser tube is the isodiametric riser tube of routine or the riser tube of various forms reducing.
6. according to the method for claim 1, it is characterized in that also comprising in the product C4 alkene, first reaction zone of C4 alkene Returning reactor is or/and the further cracking of second reaction zone.
7. according to the method for claim 1, it is characterized in that the catalytic gasoline selective hydrogenation is under there is situation in hydrogen, contact with selective hydrogenation catalyst, at hydrogen dividing potential drop 1.2～8.0MPa, 150～400 ℃ of temperature of reaction, hydrogen to oil volume ratio 150～600Nm
3/ m
3, volume space velocity 1～20h
-1React under the condition.
8. according to the method for claim 7, it is characterized in that said selective hydrogenation catalyst is is that active ingredient, activated alumina are the non-precious metal catalyst of carrier with Ni-W, Co-Ni-W, Ni-Mo or Co-Mo.
9. according to the method for claim 1, it is characterized in that the used extraction solvent choosing of aromatic extraction unit
From tetramethylene sulfone, N-Methyl pyrrolidone, diethylene glycol ether, triethylene glycol ether, TEG, diformazan
In base sulfoxide and the N-formyl morpholine ether one or more.
10. according to the method for claim 1, it is characterized in that the aromatic hydrocarbons extraction temperature is 40～120 ℃, the volume ratio between solvent and the aromatics extraction raw material is 0.5～5.0.
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| CN109679686A (en) * | 2017-10-18 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of hydrocarbon cracking method of high output of ethylene and light aromatic hydrocarbons |
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