CN104725176B - A kind of method that by catalytic cracking or cracking process, C 4 olefin is changed into propylene - Google Patents

A kind of method that by catalytic cracking or cracking process, C 4 olefin is changed into propylene Download PDF

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Publication number
CN104725176B
CN104725176B CN201510125761.4A CN201510125761A CN104725176B CN 104725176 B CN104725176 B CN 104725176B CN 201510125761 A CN201510125761 A CN 201510125761A CN 104725176 B CN104725176 B CN 104725176B
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reaction
reactor
alcohol
cracking
tower
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CN104725176A (en
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赵辉
杨朝合
马安
田亮
山红红
朱亮
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China University of Petroleum East China
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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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Abstract

The present invention discloses a kind of method that C 4 olefin is changed into propylene by catalytic cracking or cracking process, and this technical method is: 1) after etherificate, carbon four is directly entered reactor, first with water generation hydration reaction, generates corresponding alcohol.2) commonly being distilled by reactor outlet material, tower top obtains alkane, obtains corresponding alcohol at the bottom of tower.3) materials at bottom of tower is as the raw material of cracking propylene enhancing, reenters catalytic cracking riser reactor and carries out cracking reaction.The present invention is added by employing does not affects subsequent reactions and without the mass separation agent (water) separated, strengthening alkane olefin separation process, then in the case of without quality separating medium is separated, the olefin component of high reaction activity is carried out high selective reprocessing, thus a difficult problem for the high efficiency separation of alkane and alkene during solving traditional handicraft, thus realize the target by freshening propylene enhancing.This technique may utilize original device, in the case of investment is little, improves alkene utilization rate.

Description

A kind of method that by catalytic cracking or cracking process, C 4 olefin is changed into propylene
Technical field
The present invention relates to a kind of method that by catalytic cracking or cracking process, C 4 olefin is changed into propylene.Belong to Efficiently utilize field in liquefied gas deep processing and petroleum resources, be especially suitable for using catalytic cracking unit by-product Mixing carbon four produces propylene.
Background technology
Propylene is important petrochemical materials, along with continually developing of propylene downstream derivative thing new varieties, in recent years Carry out propylene in great demand.At present, the propylene of China 54% derives from the steam cracking of Petroleum, and 42% propylene is Catalytic cracking unit by-product.Contrasting with in world wide, China's catalytic cracking by-product propylene occupies an important position. Domestic catalytic cracking unit is many, and adaptability to raw material is strong, and it is the hugest that catalytic cracking process produces propylene potentiality.Borrow Co-catalysis cracking unit, is that propylene is raising carbon four resource utilization, improves economy by C 4 olefin Efficient Conversion One important channel of benefit.
CN102372608A discloses a kind of Application way mixing carbon four, and in this technique, after ether, carbon four extracts Taking rectification, obtain mixed butanes and mixed butene, mixed butene produces the raw material of propylene as cracking reaction.This In method, extracting rectifying process uses extraction tower and the double-column process of stripper combination, the extract after regeneration Looping back extraction tower, technology controlling and process is complicated；Select acetonitrile relatively big as toxicity during extractant, labor protection condition Harsh；Often process 1 ton of carbon four and produce 300～400kg containing ethane nitrile wastewater, seriously polluted.
CN102603454A discloses a kind of method mixing carbon four separating treatment.According to this process, mixed After conjunction carbon four is by conventional distillation method abjection carbon three, carbon five component, enter by iso-butane extraction tower, normal butane Extraction tower and the extracting rectifying device of stripper composition, obtain high-purity isobutane, normal butane and butylene product. Butylene product can be used for freshening, and cracking produces propylene.This technique separation process needs 5 towers to complete altogether, extraction Column plate reaches 70～100 pieces；The extractant regenerated through stripper divides two-way to be recycled into iso-butane tower, normal butane tower, Extraction rectification technique is complicated, is difficult to operation；When using morpholine/N-N-formyl morpholine N mixed liquor as extractant, vapour Carry bottom temperature higher, easily cause extractant coking loss, and extractant price is higher；Investment, operating cost The highest.
CN101928195A discloses the method for a kind of carbon four comprehensive utilization.Mixing carbon four is passed through and urges by this technique Changing rectification and produce MTBE, after ether, carbon four carries out conventional distillation operation after separating methanol processes: after ether, carbon four draws Entering the first rectifying column, tower top isolates iso-butane, and materials at bottom of tower enters Second distillation column, Second distillation column tower top Isolated high purity butene-1, at the bottom of tower, 2-butylene concentration is also improved.Use the exemplary device of this technology, Two rectifiying plate numbers the most up to 200 pieces, often separate 1 ton of carbon four and consume steam 3.8 tons.Equipment investment, operation Expensive, energy consumption is high.
CN102071054A discloses a kind of method of heavy crude and lighter hydrocarbons co-catalysis cracking, and this technique can Being introduced by carbon after ether four in catalytic cracking riser reactor and carry out freshening, normal butylenes is propylene.But this work Skill, owing to containing fractional saturation alkane in freshening lighter hydrocarbons, causes system loading relatively big, and olefin conversion is low, process Energy consumption is higher.
A kind of method that CN101381272A discloses methanol and C 4 olefin two-step method prepares ethylene and propylene. According to this process, first methanol, dimethyl ether are carried out etherification reaction with carbon four and above alkene, then will be anti- Answer outlet material to carry out cracking reaction and produce ethylene, propylene.But this technique is mainly by methanol-to-olefins and carbon Four cracking produce the coupling of two kinds of alkene reaction, reach to make full use of heat, reduce the purpose of reaction temperature.Work The separation process of alkane and alkene it is not directed to, if it is anti-to use catalytic cracking unit to carry out cracking during skill Should, still it is difficult to solve alkane in system, accumulates the problem that device load is big, energy consumption is high caused.It addition, During this patent is described, uses dimethyl ether that carbon four and above alkene are etherified and (generate methyl alkane Base ether also has methanol), then product is carried out the process of freshening, or using methanol decomposition alkene as whole The steps necessary of course of reaction.
The technological process of the catalytic pyrolysis producing more propylene technology of the more employing in current domestic refinery: catalytic cracking unit The liquefied gas of output, after gas separation unit removing C2, C3, C5, enters ether-based device, without isobutene. Ether after carbon four or rich in alkene petroleum benzin without alkane/olefin separate, directly back within catalysis and split Gasifying device carries out freshening.But constantly accumulate in system due to alkane, in ultimately resulting in system, carry out the alkene of freshening Hydrocarbon content is relatively low.So this process needs carbon four relatively low for some olefin content is discharged system, carbon in the program Four utilization rates are relatively low, and system loading is big, and process energy consumption is high.
Above-mentioned technique relates to mix butane, the separation problem of alkene, current carbon four separating technology master mostly Conventional distillation technology to be had and extraction and distillation technology.When carbon four is processed by the method using conventional distillation, Owing to each component boiling point of butylene in carbon four, butane is close, conventional distillation method separates that to there is reflux ratio big, tower Plate number is many, and energy consumption is high, the problem that operation investment cost is high.Butylene yield is there is when using extraction and distillation technology Low；Flow process is complicated, operating difficulties；Separate in product butylene and be mixed with extractant；Solvent is than big, and extractant uses The problems such as amount is big.
In sum, after exploitation ether, carbon four is converted in the technical process of propylene, improves alkene utilization rate and carries High device benefit aspect needs to coordinate to consider.
Summary of the invention
It is an object of the invention to provide one to pass through catalytic cracking on the basis of existing technology or cracking process will C 4 olefin changes into the method for propylene, and lacking mainly for the most C 4 olefins as liquefied gas as fuel has The recovery separation Application way of effect, it is provided that it is corresponding that alkene in carbon four or other lighter hydrocarbons is reacted generation by one with water Alcohol so that be easily isolated between alkane and alkene, then introduces catalytic cracking riser reactor by alcohol and splits Solve reaction, the method for producing more propylene.The method Propylene Selectivity is high, energy consumption is low, can increase substantially the carbon fourth class The economy of lighter hydrocarbons propylene enhancing technique.
For reaching above-mentioned target, the invention provides the side of a kind of C 4 olefin height selective reprocessing propylene enhancing Method, concrete grammar is:
1) hydration reaction: the mixing C 4 materials containing alkene enters filling hydration reaction catalysis with water after mixing The reactor of agent, reaction temperature 30～200 DEG C, absolute pressure 0.3～6MPa, mass space velocity is 0.1～10h-1, water: Olefin molar feed ratio is to carry out hydration reaction under the conditions of 0.1～10:1, generates corresponding alcohol.Reactor outlet thing Material enters step 2)；
2) separation process: from step 1) mainly contain the reactor outlet material of alkane, alcohol, water, enter Entering Dealkylater, only need to carry out conventional distillation, tower top obtains mixed alkanes, and materials at bottom of tower enters into step 3)；
3) cracking reaction: from step 2) mainly containing alcohol, the dealkylate materials at bottom of tower of unreacted water enter and urge Change in cracking riser reactor, reaction temperature 350～650 DEG C, absolute pressure 0.08～0.4MPa, reactant with Catalyst contacts and reacts, and generates the low-carbon alkene comprising propylene.
Described step 1) hydration reaction use reactor be tubular reactor, fixed bed reactors or catalysis essence Evaporating tower, could be arranged to a reactor or multiple tandem reactor, unreacting material also can reenter water Conjunction reactor cycles is reacted.
Hydration reaction catalyst is ion-exchange resin catalyst or its modified product, strong acidic ion liquid, dense Sulphuric acid, carried heteropoly acid, Y type molecular sieve or its modified product, ZSM molecular sieve or its modified product, SAPO One or more in molecular sieve or its modified product.All types of catalyst can be used alone, it is also possible to passes through Bonding or the mode blended are combined as mixed catalyst.
Containing alkane, alcohol in the outlet material of hydration reactor, it is also possible to there is unreacted water etc..
Described step 2) separation process only need to use simple conventional distillation to operate, can realize alkane and alcohol, The separation of water etc., dealkylate tower top isolates alkane, and materials at bottom of tower is mainly made up of alcohol and unreacted methanol.
Main material boiling point (standard atmosphere pressure) in table 1, Dealkylater
Component Water Sec-butyl alcohol Normal butane Iso-butane
Boiling point DEG C 100 99.5 -0.5 -11.72
In system, each typical material boiling point understands as shown in Table 1, and alkane and alcohol boiling-point difference are relatively big (more than 90 DEG C), Much larger than boiling-point difference (shown in table 2) between alkane, alkene in carbon four component, separate between component easily, relatively The process energy consumptions such as extraction and distillation technology are low, simple to operate.
Main material boiling point (standard atmosphere pressure) in table 2, mixing carbon four
Component Iso-butane Isobutene. Normal butane Butene-1 C-butene-2 S-butene-2
Boiling point DEG C -11.72 -6.9 -0.5 -6.2 3.72 0.88
The water reacted the most completely in material after removing alkane, without separating with alcohol, can enter together with alcohol and urge Change in cracking riser reactor and carry out cracking reaction.
Described step 3) catalytic cracking reaction process carries out in catalytic cracking riser reactor, Dealkylater In substrate material alcohol, water etc. enter riser reactor position may be located at heavy charge oil-in top, under Square or identical height, wherein preferred lower section.Heavy crude hydro carbons reacts in the same space with alcohol, reaches Improve the target of propene yield.
At least one in following of catalytic cracking reaction used catalyst: Y type molecular sieve or its modified product Product, ZSM-5 molecular sieve or its modified product, SAPO molecular sieve or its modified product.All types of catalyst can To be used alone, it is also possible to be combined as mixed catalyst by the way of bonding or blending.
The key point of the present invention is: by C 4 materials and water are carried out hydration reaction so that alkene therein Component generates corresponding alcohol, the feature utilizing the alcohol generated to differ greatly with boiling point of alkanes, is entered with alcohol by alkane Row separates, so that it is guaranteed that do not contain the inert components such as alkane in the material of freshening propylene enhancing.Due to by lighter hydrocarbons During freshening, alkane isolates system in time, available purity higher alkane material, therefore can reduce and urge Change cracking unit load, reduce energy consumption；Improve lighter hydrocarbons and produce the production capacity of propylene.Therefore the method Propylene Selectivity Height, energy consumption are low, and the economy of carbon fourth class lighter hydrocarbons propylene enhancing production technology can be greatly improved.
Compared with prior art, the invention have the characteristics that
1) present invention carries out hydration reaction, by light olefin by carbon four or other lighter hydrocarbons logistics containing alkene Convert corresponding alcohol so that the difficult olefin/paraffin separated realizes the separation of high selectivity, low energy consumption, and increases production Propylene target.
2) in the inventive method, alcohol is big with boiling point of alkanes difference, only needs conventional distillation can realize alkane/olefin High Selective Separation, is not required to use the complicated technologies such as extracting rectifying, and simple to operate, energy consumption is low, pollution-free.
3) in the inventive method, alkane isolates system in time, improves device capbility, reduces the negative of system Lotus, energy efficient.And isolated alkane purity is high, and carbon four utilization of resources is abundant.
4) this method can significantly improve to mix selectivity and the product that carbon four is the process of raw material production propylene Rate.
Accompanying drawing explanation
Fig. 1 is the method that C 4 olefin is changed into propylene by catalytic cracking or cracking process of the present invention Principle flow chart.
Fig. 2 is catalytic cracking or the technological process of cracking process processing carbon four component propylene enhancing of comparative example 1 Figure.
In figure: 1, catalytic cracking (or cracking) device, 2, gas separation unit, 3, MTBE device, 4, water Close reaction unit, 5, Dealkylater, 6, dry gas, gasoline, diesel oil etc., 7, liquefied gas, 8, propylene, 9, Mixing carbon four, 10, MTBE, 11, mixing carbon four without isobutene., 12, water, 13, reactor outlet Material, 14, be not involved in the low-carbon alkanes of etherification reaction, 15, the alcohol of freshening, 16, raw oil.
Describe the present invention in detail below by accompanying drawing, but do not limit the scope of the invention.
Detailed description of the invention
Below by specific embodiment, illustrate the effect of the present invention further, but embodiment is not limiting as this Bright scope.
As it is shown in figure 1, heavy oil feedstock (logistics 16) enters, and cracking occurs in riser catalytic cracking reactor Reaction, the gasoline of generation, diesel oil and dry gas as product (logistics 6) separating device of catalytic cracking unit, Liquefied gas (logistics 7) enters into gas separation unit (module 2), obtains propylene product (logistics 8) and mixing carbon Four (logistics 9), after mixing carbon four logistics (logistics 9) converts in MTBE device (module 3), MTBE product (logistics 10) and the mixing carbon four (logistics 11) without isobutene., logistics 11 can be obtained Mix with water (logistics 12), introduced into the reactor (mould equipped with acid cation exchange resin catalyst Block 4), reaction temperature 70～180 DEG C, react gauge pressure 0.5～6MPa, reaction velocity 0.5～3h-1It is hydrated Reaction, wherein water is 0.5～3:1 with the raw materials components mole ratio of butylene, generates sec-butyl alcohol.Reactor outlet material (thing Stream 13) enter Dealkylater (module 5), the alkane in mixed material is distillated (logistics 14) at tower top, Residue materials at bottom of tower (logistics 15) enters the catalytic cracking riser reaction containing ZSM-5 molecular sieve catalyst In device (module 1), reaction temperature 400～600 DEG C, gauge pressure 0～0.1MPa, catalyst contacts with reaction mass Under the conditions of time was less than 0.2 second, carry out cracking reaction, produce propylene.
Embodiment 1
Fixed bed catalytic reactor (Fig. 1 of the acid cation exchange resin catalyst of 200ml will be filled with Middle module 4), it is heated to 120 DEG C.Water (logistics 12) and the mixture (thing containing butane and butene-1 Stream 11) press water/alkene mol ratio 1:1, mass space velocity is 3h-1, enter hydration reactor (module 4 in Fig. 1), Carrying out contacting with hydration reaction catalyst and carry out hydration reaction, temperature 120 DEG C, hydration reactor outlet obtains water Sec-butyl alcohol after conjunction and the mixture (logistics 13) of butane.Hydration reactor is exported the product liquid obtained, Carrying out rectification separation (module 5), tower top obtains unreacted butane (logistics 14), obtains sec-butyl alcohol (thing at the bottom of tower Stream 15).This logistics (logistics 15) introduces the riser catalysis containing H-ZSM-5 molecular sieve catalyst split Change reaction unit (module 1), reaction temperature 540 DEG C, split with heavy oil feedstock (logistics 16) simultaneously Change reaction.Compared with the operating mode that reaction is not participated in logistics 15, cracking reactor outlet can additionally obtain 51.6% Propylene+36.1% ethylene (accounts for charging butene-1 weight/mass percentage composition, total carbon effective rate of utilization is 87.7%). The product that fcc riser reactor (module 1) exports includes gasoline, diesel oil and dry gas (logistics 6) With liquefied gas (logistics 7), wherein logistics 6 directly goes out device as product, and liquefied gas logistics (logistics 7) is entered Enter to gas separation unit (module 2), isolate propylene product (logistics 8), additionally obtain mixing carbon four logistics (thing Stream 9).This logistics, after MTBE device (module 3) converts, obtains this example and starts described fourth The mixture (logistics 11) of alkane and butene-1.
Comparative example 1
As in figure 2 it is shown, the mixture (logistics 11) containing butane and butene-1 is directly entered diverter (mould Block 5), obtain the mixture (logistics 14) of one butane going out device and butene-1, and the fourth of one freshening The mixture (logistics 15) of alkane and butene-1.This logistics (logistics 15) is introduced and divides containing H-ZSM-5 The fcc riser reactor (module 1) of sub-sieve catalyst, reaction temperature 540 DEG C, former with heavy oil There is cracking reaction in material (logistics 16) simultaneously.Compared with the operating mode that reaction is not participated in logistics 15, cracking reaction Device outlet can additionally obtain 31.6% propylene+16.1% ethylene (account for butene-1 weight/mass percentage composition in logistics 11, Total carbon effective rate of utilization is 47.7%).The product bag that fcc riser reactor (module 1) exports Including gasoline, diesel oil and dry gas (logistics 6) and liquefied gas (logistics 7), wherein logistics 6 directly goes out as product Device, liquefied gas logistics (logistics 7) enters into gas separation unit (module 2), isolates propylene product (logistics 8), additionally obtain mixing carbon four logistics (logistics 9).This logistics converts through MTBE device (module 3) After, obtain this example and start the mixture (logistics 11) of described butane and butene-1.This process and reality The difference executing example 1 is, the butylene in logistics 11 does not carry out hydration reaction, directly carries out cracking reaction.By Butane-component in the middle of logistics 11 does not reacts in catalytic cracking/cracking process, for preventing butane-component Accumulate in systems, need the material containing butane is discharged system (logistics 14).Logistics 14 has A part of butylene discharges system with butane, causes the yield losses of target product propylene.Freshening complete with butylene is (real Execute example 1) scheme compare, the effective rate of utilization of carbon is relatively low during this, according to butylene contained in logistics 11 Amount calculate, the efficiency of recycling is only 47.7%.
From the Comparative result of above example and comparative example it can be seen that the light hydrocarbon feedstocks that will be enriched in alkene is first hydrated Separate again and then crack, can significantly ethylene and the yield of propylene in pyrolysis product, improve utilization of resources rate, Reduce the volume of reactor, therefore this technology path and the method for direct freshening of routine compare possess the brightest Aobvious advantage.

Claims (8)

1. the method that by catalytic cracking or cracking process, C 4 olefin is changed into propylene, it is characterised in that its processing step As described below:
1) containing the carbon four of alkene under hydration reaction catalyst action with water, reaction temperature 30～200 DEG C, absolute pressure 0.1～ 6MPa, mass space velocity is 0.1～10h-1Under the conditions of carry out hydration reaction, Qi Zhongshui: olefin molar feed ratio be 0.1～ 10:1, generates corresponding alcohol, and the material obtained by reactor outlet enters into step 2；
2) reactor outlet material from step 1 carries out conventional distillation in Dealkylater, it is not necessary to add extractant or other Quality of assistance separating medium, tower top isolates alkane, the alcohol comprising generation obtained at the bottom of tower and the dealkylate thing of unreacted water Material；Materials at bottom of tower enters step 3；
3) enter catalytic cracking from the dealkylate material mainly comprising alcohol and unreacted water at the bottom of Dealkylater in step 2 to promote In pipe reactor, reaction temperature 350～650 DEG C, in the environment of absolute pressure 0.08～0.4MPa, connect with catalyst Touch and react, generating the low-carbon alkene comprising propylene.
2. according to the method described in claim 1, it is characterised in that: step 1) described in hydration reaction catalyst be ion hand over Change resin catalyst or its modified product, ionic liquid, sulphuric acid, carried heteropoly acid, Y type molecular sieve or its modified product, One or more in ZSM molecular sieve or its modified product, SAPO molecular sieve or its modified product；All types of catalyst can To be used alone, it is also possible to by bonding, blend or be combined as composite catalyst system by the way of grating.
3. according to the method described in claim 1, it is characterised in that: step 1) described in hydration reaction use reactor be Tubular reactor, fixed bed reactors or reactive distillation column, can arrange the reactor of one or more series connection, unreacted Water also can reenter reactor and be further continued for reacting.
4. according to the method described in claim 1, it is characterised in that: step 2) described in separation process be conventional distillation, will not The alkane that hydration reaction can occur is separated with the alcohol generated by reaction and unreacted water, is removed at the bottom of tower The material of alkane.
5. according to the method described in claim 1, it is characterised in that: except reaction generation in the material obtained at the bottom of Dealkylater Beyond alcohol, it is also possible to containing the water not reacted, this strand of material can be directly entered catalytic cracking riser reactor and enter Row reaction, it is not necessary to it is completely separated with product.
6. according to the method described in claim 1, it is characterised in that: step 3) described in alcohol cracking reaction used in urge At least one in following of agent: Y type molecular sieve or its modified product, ZSM molecular sieve or its modified product, SAPO Molecular sieve or its modified product；All types of catalyst can be used alone, it is also possible to combines by the way of bonding or blending For mixed catalyst.
7. according to the method described in claim 1, it is characterised in that: step 3) in catalytic cracking reaction process be in catalytic cracking Carrying out in riser reactor, reaction raw materials includes the boiling spread heavy raw oil more than 350 DEG C, containing alcohol and unreacted Water dealkylate materials at bottom of tower enter riser reactor position may be located at the top of heavy charge oil-in, lower section Or identical height；Heavy raw oil reacts in the same space with alcohol, reaches to improve the target of propene yield.
8. according to the method described in claim 7, it is characterised in that: step 3) in catalytic cracking reaction process be in catalytic cracking Carrying out in riser reactor, reaction raw materials includes the boiling spread heavy raw oil more than 350 DEG C, containing alcohol and unreacted The dealkylate materials at bottom of tower of water enter the position of riser reactor and be positioned at the lower section of heavy charge oil-in；Heavy charge Oil reacts in the same space with alcohol etc., reaches to improve the target of propene yield.
CN201510125761.4A 2015-03-20 2015-03-20 A kind of method that by catalytic cracking or cracking process, C 4 olefin is changed into propylene Expired - Fee Related CN104725176B (en)

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Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6049017A (en) * 1998-04-13 2000-04-11 Uop Llc Enhanced light olefin production

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6049017A (en) * 1998-04-13 2000-04-11 Uop Llc Enhanced light olefin production

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
正丁烯水合制仲丁醇工艺分析;李彬等;《化工中间体》;20111231(第3期);第58-62页 *
碳四烃的综合利用;李明辉;《石油化工》;20031231;第32卷(第9期);第808-814页 *

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