CN103772107B - The method of preparing propylene by butene disproportionation - Google Patents

The method of preparing propylene by butene disproportionation Download PDF

Info

Publication number
CN103772107B
CN103772107B CN201210412602.9A CN201210412602A CN103772107B CN 103772107 B CN103772107 B CN 103772107B CN 201210412602 A CN201210412602 A CN 201210412602A CN 103772107 B CN103772107 B CN 103772107B
Authority
CN
China
Prior art keywords
hours
butylene
disproportionation
reaction
propylene
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201210412602.9A
Other languages
Chinese (zh)
Other versions
CN103772107A (en
Inventor
董静
王仰东
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Original Assignee
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by China Petroleum and Chemical Corp, Sinopec Shanghai Research Institute of Petrochemical Technology filed Critical China Petroleum and Chemical Corp
Priority to CN201210412602.9A priority Critical patent/CN103772107B/en
Publication of CN103772107A publication Critical patent/CN103772107A/en
Application granted granted Critical
Publication of CN103772107B publication Critical patent/CN103772107B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/50Improvements relating to the production of bulk chemicals
    • Y02P20/52Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Landscapes

  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

The present invention relates to a kind of method of preparing propylene by butene disproportionation, mainly solve the problem that there is poor catalyst stability in conventional art.The present invention is by adopting with butylene and ethene for raw material, and be 200 ~ 450 DEG C in temperature of reaction, reaction pressure counts 0 ~ 5MPa with absolute pressure, and weight space velocity is 1 ~ 50 hour -1the weight ratio 1: 0.5 ~ 5 of butylene and ethene is under condition, raw material passes through beds, generate target product propylene, wherein used catalyst is the disproportionation catalyst of load tungsten and the alkaline earth metal oxide auxiliary agent through acidolysis modification, the mass ratio of the two mixing is the technical scheme of 1: 1 ~ 15, solves this problem preferably, can be used for the industrial production that butylene disproportionation prepares propylene.

Description

The method of preparing propylene by butene disproportionation
Technical field
The present invention relates to a kind of method of butylene and ethene disproportionation propylene.
Background technology
Olefin metathesis is by under the effect of transition metal compound catalyst, makes C=C double bond fracture in alkene and is again formed, to obtain the process of new olefin product.
Utilize the cross disproportionation effect of butylene and ethene, by adding appropriate ethene, by relative surplus, C that added value is lower 4olefin feedstock is converted into high added value propylene product.
Butene feedstock in disproportionation reaction is often from steam cracking or catalytic cracking unit, and containing a small amount of water, oxygenatedchemicals, sulfocompound etc., wherein oxygenatedchemicals mostly is alcohol or ether.These compounds are easy to be combined with the unoccupied orbital of disproportionation catalyst atoms metal occupy active sites, thus cause poisoning of catalyst, and therefore raw material has to pass through purification and just can enter bed and contact with disproportionation catalyst.
Preparing propylene through olefin disproportionation reaction adopts fixed-bed process more, and before raw material enters beds, liquid starting material and gas raw material need be pre-mixed evenly, is conducive to the reaction stability increasing catalyzer like this.
US5898091 and US6166279 reports C 4, C 5olefin treated, wherein in preparing propylene through olefin disproportionation process, the catalyzer adopted is Re 2o 7/ Al 2o 3, reactor is moving-bed.US6358482 proposes one C 4cut hydrocarbon produces the device of iso-butylene and propylene.C 4cut hydrocarbon isolates iso-butylene and 1-butylene and 2-butylene after selec-tive hydrogenation and rectifying, and the 1-butylene separated generates 2-butylene by double-bond isomerization, and rich 2-butylene material and ethene disproportionation reaction generate propylene, and disproportionation reaction catalyzer used is Re 2o 7/ Al 2o 3.What US6743958 introduced is the improving technique of US6358482, and the iso-butylene separated generates n-butene through skeletal isomerization and recycles.WO00014038 describes a kind of method of preparing propylene by butene disproportionation, and raw material butylene is 1-butylene, 2-butylene or its mixture, and catalyzer is WO 3/ SiO 2or Cs +, PO 4 3-deng the WO of modification 3/ SiO 2.When preparing propylene reaction for butylene disproportionation, all there is the problem of poor catalyst stability in the method in above document.
In disproportionation reaction, alkaline earth metal oxide auxiliary agent can produce with disproportionation catalyst and act synergistically, and promotes the carrying out of disproportionation reaction, can also play the impurity in absorption raw material simultaneously, the effect of purification raw material.The report improved about auxiliary agent is had no in above document.Have the report about alkaline earth metal oxide hydration modification in Chinese patent CN200610029981.8, but the stability of modified disproportionation reaction can only reach 360 hours.
Summary of the invention
Technical problem to be solved by this invention is the problem of the poor stability existed in prior art, provides a kind of new butylene disproportionation to prepare the method for propylene.When the method is used for butylene disproportionation reaction, there is the good advantage of stability.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method of preparing propylene by butene disproportionation, and with butylene and ethene for raw material, be 200 ~ 450 DEG C in temperature of reaction, reaction pressure is 0 ~ 5MPa(absolute pressure), weight space velocity is 1 ~ 50 hour -1, butylene and ethene weight ratio be under the condition of 1: 0.5 ~ 5, raw material and catalyst exposure react the product generating and comprise propylene, and used catalyst comprises disproportionation catalyst host and the alkaline earth metal oxide auxiliary agent of load tungsten; With host weight parts, host comprises the SiO of a) 85 ~ 95 parts 2or mesopore molecular sieve carrier, and load b thereon) Tungsten oxide 99.999 of 5 ~ 15 parts; The weight ratio of host and auxiliary agent is 1:1 ~ 15; Wherein alkaline earth metal oxide obtains required auxiliary agent through peracid treatment, drying and roasting, and the mol ratio of acid used and alkaline earth metal oxide is 0.1 ~ 5:1.
In technique scheme, the preferable range of temperature of reaction is 200 ~ 400 DEG C, and more preferably scope is 250 ~ 350 DEG C; Reaction pressure is in absolute pressure preferable range for 0.2 ~ 4MPa, and more preferably scope is 0.5 ~ 3MPa; Weight space velocity preferable range is 2 ~ 25 hours -1, more preferably scope is 4 ~ 10 hours -1.
In technique scheme, auxiliary agent treatment condition: acid solution mass concentration is 1 ~ 15%, acid treatment temperature is 20 ~ 100 DEG C, and the acid treatment time is 1 ~ 12 hour; Drying temperature is 60 ~ 120 DEG C, and time of drying is 6 ~ 18 hours; Maturing temperature is 500 ~ 650 DEG C, and roasting time is 3 ~ 10 hours.More preferably scheme is acid solution mass concentration is 3 ~ 10%, and acid treatment temperature is 50 ~ 90 DEG C, and the acid treatment time is 2 ~ 10 hours.The mol ratio preferable range of acid used and alkaline earth metal oxide is 0.5 ~ 3:1,
In technique scheme, the preparation method of disproportionation catalyst host is as follows: the mesoporous supports of aequum and sesbania powder are mixed, add the soluble tungsten salt of aequum after certain hour, after kneading, extrusion, drying, at 450 ~ 650 DEG C, roasting obtains for 2 ~ 8 hours.
Alkaline earth metal oxide and acid solution are had an effect, and generate water-fast alkaline earth salt.High temperature sintering can make alkaline earth salt again dehydration obtain oxide compound.In said process, the Sauerstoffatom of dehydration may be from the Sauerstoffatom in solvent, also may be the Sauerstoffatom from former alkaline earth metal oxide plane of crystal.Therefore, dehydration will cause the surface imperfection of alkaline earth metal oxide, make to there is the positively charged ion of exposure and the negative oxygen ion center of different ligancy on the surface, on limit, angle, cationic omission can form more negative oxygen ion group, alkalescence is improved, and specific surface area also can increase simultaneously, thus is conducive to producing with disproportionation catalyst better acting synergistically, better adsorbing contaminant, thus be conducive to the stability extending reaction.
Adopt technical scheme of the present invention, be 200 ~ 450 DEG C in temperature of reaction, reaction pressure counts 0 ~ 5MPa with absolute pressure, and raw material weight air speed is 1 ~ 50 hour -1condition under, after catalyzer host is mixed with auxiliary agent, with butene feedstock contact reacts, its reaction stability can reach 650 hours, achieve good technique effect.
Below by embodiment, the invention will be further elaborated.
Embodiment
[embodiment 1]
Take 50 grams of commodity MgO, the mass concentration added containing 112.5 grams of oxalic acid is the acid solution of 5%, obtains mixing solutions, after 50 DEG C of heating in water bath stir 5 hours, moisture in suction filtration solution, product is dried 6 hours at 120 DEG C, 500 DEG C of roastings obtain auxiliary agent finished product in 10 hours, are designated as JT-1.
By the mesoporous SiO of load tungsten 8% 2host and JT-1 are with 1: 5(mass ratio) mix, be arranged in the fixed-bed reactor of Φ 25mm, with butylene and ethene for raw material, the two mass ratio is 1: 1, is 4 hours at weight space velocity -1, temperature of reaction is 250 DEG C, and reaction pressure is check and rate catalyst performance under the condition of 1MPa, the results are shown in list 1.
[embodiment 2]
Take 50 grams of commodity MgO, the mass concentration added containing 120.09 grams of citric acids is the solution of 1%, obtains mixing solutions, after 80 DEG C of heating in water bath stir 4 hours, leave standstill 3 hours again, moisture in suction filtration solution, product is 80 DEG C of oven dry, 550 DEG C of roastings obtain auxiliary agent finished product in 8 hours, are designated as JT-2.
By the mesoporous MCM-41 host of load tungsten 5% with JT-2 with 1: 2(mass ratio) mix, be arranged in the fixed-bed reactor of Φ 25mm, with butylene and ethene for raw material, the two mass ratio is 1: 0.5, is 10 hours at weight space velocity -1, temperature of reaction is 300 DEG C, and reaction pressure is check and rate catalyst performance under the condition of 0.5MPa, the results are shown in list 1.
[embodiment 3]
Take 50 grams of commodity CaO, the mass concentration added containing 5.54 grams of carbonic acid is the solution of 10%, obtains mixing solutions, after 90 DEG C of heating in water bath stir 1 hour, leave standstill 3 hours again, moisture in suction filtration solution, product is dried 10 hours at 100 DEG C, 600 DEG C of roastings obtain auxiliary agent finished product in 6 hours, are designated as JT-3.
By the mesoporous MCM-48 host of load tungsten 12% with JT-3 with 1: 10(mass ratio) mix, be arranged in the fixed-bed reactor of Φ 25mm, with butylene and ethene for raw material, the two mass ratio is 1: 2.5, is 25 hours at weight space velocity -1, temperature of reaction is 400 DEG C, and reaction pressure is check and rate catalyst performance under the condition of 3MPa, the results are shown in list 1.
[embodiment 4]
Take 50 grams of commodity BaO, the mass concentration added containing 148.5 grams of oxalic acid is the solution of 15%, obtains mixing solutions, and after stirring 10 hours in 30 DEG C of heating in water bath, moisture in suction filtration solution, product is dried 18 hours at 60 DEG C, and 650 DEG C of roastings are designated as JT-4 in 3 hours.
By the mesoporous SBA-15 host of load tungsten 15% with JT-4 with 1: 15(mass ratio) mix, be arranged in the fixed-bed reactor of Φ 25mm, with butylene and ethene for raw material, the two mass ratio is 1: 5, is 50 hours at weight space velocity -1, temperature of reaction is 450 DEG C, and reaction pressure is check and rate catalyst performance under 5MPa condition, the results are shown in list 1.
[comparative example 1]
By the mesoporous SiO of load tungsten 8% 2host and commodity MgO are with 1: 5(mass ratio) mix, be arranged in the fixed-bed reactor of Φ 25mm, with butylene and ethene for raw material, the two mass ratio is 1: 1, is 4 hours at weight space velocity -1, temperature of reaction is 250 DEG C, and reaction pressure is check and rate catalyst performance under the condition of 1MPa, the results are shown in list 1.
[comparative example 2]
By the mesoporous MCM-48 host of load tungsten 12% with commodity CaO with 1: 10(mass ratio) mix, be arranged in the fixed-bed reactor of Φ 25mm, with butylene and ethene for raw material, the two mass ratio is 1: 2.5, is 25 hours at weight space velocity -1, temperature of reaction is 400 DEG C, and reaction pressure is check and rate catalyst performance under the condition of 3MPa, the results are shown in list 1.
Table 1 catalyst catalytic performance evaluation result
Note: reaction pressure is absolute pressure.
As can be seen from Table 1, under identical reaction conditions, through acid-treated alkaline earth metal oxide auxiliary agent, catalyst stability is significantly improved, 650 hours can be reached, illustrate that preparing propylene for butylene disproportionation reacts, the alkaline earth metal oxide through acidolysis modification is suitable catalyst adjuvant.

Claims (1)

1. the method for a preparing propylene by butene disproportionation, take 50 grams of commodity MgO, the mass concentration added containing 112.5 grams of oxalic acid is the acid solution of 5%, obtain mixing solutions, after 50 DEG C of heating in water bath stir 5 hours, moisture in suction filtration solution, product is dried 6 hours at 120 DEG C, 500 DEG C of roastings obtain auxiliary agent finished product in 10 hours, are designated as JT-1;
By the mesoporous SiO of load tungsten 8% 2host mixes with 1: 5 (mass ratio) with JT-1, is arranged in the fixed-bed reactor of Φ 25mm, and with butylene and ethene for raw material, the two mass ratio is 1: 1, is 4 hours at weight space velocity -1, temperature of reaction is 250 DEG C, and reaction pressure is check and rate catalyst performance under the condition of 1MPa, and the transformation efficiency of result display butylene is 70.1%, and the selectivity of propylene is 99.0%, and stability is 650 hours.
CN201210412602.9A 2012-10-25 2012-10-25 The method of preparing propylene by butene disproportionation Active CN103772107B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201210412602.9A CN103772107B (en) 2012-10-25 2012-10-25 The method of preparing propylene by butene disproportionation

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201210412602.9A CN103772107B (en) 2012-10-25 2012-10-25 The method of preparing propylene by butene disproportionation

Publications (2)

Publication Number Publication Date
CN103772107A CN103772107A (en) 2014-05-07
CN103772107B true CN103772107B (en) 2015-09-09

Family

ID=50564940

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201210412602.9A Active CN103772107B (en) 2012-10-25 2012-10-25 The method of preparing propylene by butene disproportionation

Country Status (1)

Country Link
CN (1) CN103772107B (en)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107973686A (en) * 2016-10-21 2018-05-01 中国石油化工股份有限公司 The method of olefin(e) disproportionation

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101121629A (en) * 2006-08-11 2008-02-13 中国石油化工股份有限公司 Method for preparing propylene by butylene-containing C4 fractioning hydrocarbon dismutation
CN101121121A (en) * 2006-08-11 2008-02-13 中国石油化工股份有限公司 Olefines double bond isomerizing catalyst and its preparation method
CN101992119A (en) * 2009-08-31 2011-03-30 中国石油化工股份有限公司上海石油化工研究院 Catalyst for preparing propylene from butane and ethylene and preparation method thereof
CN102188965A (en) * 2010-03-03 2011-09-21 中国石油化工股份有限公司 Method for preparing catalyst for olefin double bond isomerization

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080146856A1 (en) * 2006-12-19 2008-06-19 Leyshon David W Propylene production

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101121629A (en) * 2006-08-11 2008-02-13 中国石油化工股份有限公司 Method for preparing propylene by butylene-containing C4 fractioning hydrocarbon dismutation
CN101121121A (en) * 2006-08-11 2008-02-13 中国石油化工股份有限公司 Olefines double bond isomerizing catalyst and its preparation method
CN101992119A (en) * 2009-08-31 2011-03-30 中国石油化工股份有限公司上海石油化工研究院 Catalyst for preparing propylene from butane and ethylene and preparation method thereof
CN102188965A (en) * 2010-03-03 2011-09-21 中国石油化工股份有限公司 Method for preparing catalyst for olefin double bond isomerization

Also Published As

Publication number Publication date
CN103772107A (en) 2014-05-07

Similar Documents

Publication Publication Date Title
CN105233824B (en) A kind of high-selective ethylene oxidation epoxy ethane silver catalyst and its application method
CN103772107B (en) The method of preparing propylene by butene disproportionation
CN101190876B (en) Method for preparing ethylene glycol ether
CN101172228A (en) Catalyzer for propylene glycol aether preparation with epoxypropane
CN107973684A (en) The method of propylene disproportionation ethene
Wang et al. Synthesis of zirconia porous phosphate heterostructures (Zr-PPH) for Prins condensation
CN103420766B (en) Method for preparing 2-butene through 1-butene double bond isomerization
CN101768040B (en) Method for preparing propylene from butylene and ethylene
CN103030495B (en) Method for manufacturing propylene by butene and ethylene disproportionation
CN104557399B (en) The method that amylene is disproportionated propylene processed with ethene
CN101121629B (en) Method for preparing propylene by butylene-containing C4 fractioning hydrocarbon dismutation
CN105622551B (en) A kind of method that 2,5 dihydroxymethyl tetrahydrofurans are directly prepared by carbohydrate
CN104045619B (en) Prepare the method for ethylene (propylene) carbonate
CN103071519B (en) Catalyst used in production of isobutene through cracking of methyl tert-butyl ether and preparation method thereof
CN106732700B (en) A kind of oligomeric acrylamide prepares the catalyst and preparation method and purposes of nonene and laurylene
CN103420775B (en) Method for preparing hexene-1 through C6 component isomerization
CN100484628C (en) Mesopore structured heteropoly acid/silicon dioxide catalyst
CN103071520B (en) Preparation method for catalyst used in production of isobutene through cracking of methyl tert-butyl ether
CN104549232B (en) Rhenium-based disproportionation catalyst
CN104177314B (en) A kind of method preparing epoxy butane
CN101596463A (en) Granular titanium-silicon molecular sieve catalyst and preparation method
CN103030507B (en) Method for producing propylene by virtue of disproportionating of amylene and ethylene
CN102875313B (en) Olefin isomerization method
CN105712822A (en) Method for preparation of ethylene by ethanol dehydration
CN107970916A (en) Olefin disproportionation catalyst and application thereof

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant