CN104672046B - Method of increasing ethylene and propylene yields by freshening C-4 olefins in catalytic cracking or pyrolysis process after separation - Google Patents
Method of increasing ethylene and propylene yields by freshening C-4 olefins in catalytic cracking or pyrolysis process after separation Download PDFInfo
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- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The invention discloses a method of increasing ethylene and propylene yields by freshening C-4 olefins in catalytic cracking or pyrolysis process after separation. The technical method is as follows: 1) directly conveying etherified C-4 into a reactor, and firstly reacting with acetic acid under the action of a catalyst to generate sec-butyl acetate; 2) carrying out conventional distillation on materials at the outlet of the reactor to obtain alkane at the tower top and the sec-butyl acetate at the tower bottom; 3) using the material at the tower bottom as a raw material for increasing the propylene yield by cracking, and carrying out a cleavage reaction on the material in a catalytic cracking riser reactor. A mass separating agent (acetic acid) generating no influence on subsequent reaction and needing no separation is added in the invention to strengthen the separation process of alkane and olefin, and under the condition of not separating the mass separating agent, high-selectivity freshening is carried out on olefin components with high reaction activity to solve the problem of efficient separation of alkane and olefin in a traditional manufacturing process and achieve the target of increasing the propylene yield by freshening. The process can be used for utilizing the original device to improve the olefin utilization rate under the condition of small investment.
Description
Technical field
The present invention relates to a kind of by freshening increasing output of ethylene in catalytic cracking or cracking process after C 4 olefin separation
With the method for propylene, belong to liquefied gas deep processing and petroleum resources efficiently utilize field, be especially suitable for use and urge
The mixing carbon four changing cracking unit by-product 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 a kind of on the basis of existing technology urged by freshening after C 4 olefin separation
Change increasing output of ethylene and the method for propylene in cracking or cracking process, mainly for the most as liquefied gas as fuel
C 4 olefin lacks effective recovery and separates Application way, it is provided that a kind of by alkene and second in carbon four or other lighter hydrocarbons
Acid reaction generates sec-butyl acetate so that be easily isolated between alkane and alkene, is then introduced by sec-butyl acetate
Catalytic cracking riser reactor carries out cracking reaction, the method for producing more propylene.The method Propylene Selectivity height,
Energy consumption is low, can increase substantially the economy of carbon fourth class 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). alkene and acetic acidreaction: the mixing C 4 materials containing alkene enters filling catalysis with acetic acid 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, second
Acid: olefin molar feed ratio is to react under the conditions of 0.1～10:1, generates sec-butyl acetate.Reactor outlet
Material enters step 2)；
2). separation process: from step 1) mainly contain alkane, sec-butyl acetate, the reactor of acetic acid go out
Mouth material, enters Dealkylater, only need to carry out conventional distillation, and tower top obtains mixed alkanes, and materials at bottom of tower enters
To step 3)；
3). cracking reaction: from step 2) mainly containing sec-butyl acetate, unreacted acetic acid Dealkylater at the bottom of
Material enters in catalytic cracking riser reactor, reaction temperature 350～650 DEG C, and absolute pressure 0.08～0.4MPa,
Reactant contacts with catalyst and reacts, and generates the low-carbon alkene comprising propylene.
Described step 1) reactor that used of alkene and acetic acidreaction is fixed bed reactors or catalytic distillation
Tower, could be arranged to a reactor or multiple tandem reactor, and unreacting material also can reenter reaction
Device circular response.The catalyst that this course of reaction is used be ion-exchange resin catalyst or its modified product,
Strong acidic ion liquid, concentrated sulphuric acid, carried heteropoly acid, Y type molecular sieve or its modified product, ZSM molecule
Sieve or its modified product, SAPO molecular sieve or its modified product in one or more.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 outlet thing of reactor
Containing alkane, sec-butyl acetate in material, it is also possible to there is unreacted acetic acid etc..
Described step 2) separation process only need to use simple conventional distillation to operate, and can realize alkane and acetic acid
The separation of secondary butyl ester, acetic acid etc., dealkylate tower top isolates alkane, materials at bottom of tower mainly by sec-butyl acetate with
And unreacted acetic acid composition.
Main material boiling point (standard atmosphere pressure) in table 1, Dealkylater
| Component | Acetic acid | Sec-butyl acetate | Normal butane | Iso-butane |
| Boiling point DEG C | 117.9 | 112.3 | -0.5 | -11.72 |
In system, each typical material boiling point understands as shown in Table 1, and alkane and sec-butyl acetate boiling-point difference (connect relatively greatly
Nearly 100 DEG C), much larger than boiling-point difference (shown in table 2) between alkane, alkene in carbon four component, between component point
From easily, low compared with process energy consumptions such as extraction and distillation technologies, 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 acetic acid reacted the most completely in material after removing alkane, can be with second without separating with sec-butyl acetate
The secondary butyl ester of acid enters together and carries out cracking reaction in catalytic cracking riser reactor.
Described step 3) catalytic cracking reaction process carries out in catalytic cracking riser reactor, Dealkylater
In substrate material, the position of the entrance such as sec-butyl acetate, acetic acid riser reactor may be located at heavy charge oil-in
Top, lower section or identical height, wherein preferred lower section.Heavy crude hydro carbons and sec-butyl acetate, acetic acid etc.
React in the same space, reach to 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 being reacted with acetic acid by C 4 materials so that alkene group therein
Mitogenetic one-tenth sec-butyl acetate, utilizes the feature that the sec-butyl acetate generated differs greatly with boiling point of alkanes, by alkane
Hydrocarbon separates with sec-butyl acetate, so that it is guaranteed that do not contain the inertia such as alkane in the material of freshening propylene enhancing
Component.Owing to alkane during lighter hydrocarbons freshening is isolated system in time, available purity higher alkane material,
Therefore can reduce catalytic cracking unit load, reduce energy consumption；Improve lighter hydrocarbons and produce the production capacity of propylene.Therefore should
Method Propylene Selectivity is high, energy consumption is 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 is reacted with acetic acid, by carbon tetraene by carbon four or other lighter hydrocarbons logistics containing alkene
Hydrocarbon changes into sec-butyl acetate so that the difficult olefin/paraffin separated realizes the separation of high selectivity, low energy consumption,
And propylene enhancing target.
2) in the inventive method, sec-butyl acetate is big with boiling point of alkanes difference, only needs conventional distillation can realize alkane
The high Selective Separation of hydrocarbon/alkene, 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 freshening increasing output of ethylene and third in catalytic cracking or cracking process after C 4 olefin of the present invention separates
The methodological principle flow chart of alkene
Fig. 2 is comparative example 1 catalytic cracking or the process chart of cracking process processing carbon four component propylene enhancing.
In figure: 1, catalytic cracking (or cracking) device, 2, gas separation unit, 3, MTBE device, 4, second
Acid esters catalytic synthesis device, 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, acetic acid, 13,
Reactor outlet material, 14, be not involved in the low-carbon alkanes of etherification reaction, 15, the acetas 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 acetic acid (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-1Synthesize
Reaction, wherein acetic acid is 0.5～3:1 with the raw materials components mole ratio of butylene, generates sec-butyl acetate.Reactor outlet
Material (logistics 13) enters Dealkylater (module 5), and at tower top, the alkane in mixed material is distillated (thing
Stream 14), the catalytic cracking that residue materials at bottom of tower (logistics 15) enters containing ZSM-5 molecular sieve catalyst carries
In riser reactors (module 1), reaction temperature 400～600 DEG C, gauge pressure 0～0.1MPa, catalyst and reaction
Under the conditions of material time of contact 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.Acetic acid (logistics 12) and the mixture (thing containing butane and butene-1
Stream 11) press acetic acid/alkene mol ratio 1:1, mass space velocity is 3h-1, enter acetas catalytic synthesis device (figure
Module 4 in 1), carry out contacting reacting with catalyst, temperature 120 DEG C, acetas catalytic synthesis device
Outlet obtains the mixture (logistics 13) of reacted sec-butyl acetate and butane.Acetas is catalyzed and synthesized instead
Answering device to export the product liquid obtained, carry out rectification separation (module 5), tower top obtains unreacted butane (thing
Stream 14), obtain sec-butyl acetate (logistics 15) at the bottom of tower.This logistics (logistics 15) is introduced containing H-ZSM-5
The fcc riser reactor (module 1) of molecular sieve catalyst, reaction temperature 540 DEG C, with heavy oil
There is cracking reaction in raw material (logistics 16) simultaneously.Compared with the operating mode that reaction is not participated in logistics 15, cracking is anti-
Answer device outlet can additionally obtain 83.6% propylene+39.1% ethylene and (account for charging butene-1 weight/mass percentage composition, portion
Dividing carbon is 91% from acetic acid, total carbon effective rate of utilization).Fcc riser reactor (module 1)
The product of outlet includes gasoline, diesel oil and dry gas (logistics 6) and liquefied gas (logistics 7), wherein logistics 6
Directly go out device as product, liquefied gas logistics (logistics 7) enters into gas separation unit (module 2), isolates
Propylene product (logistics 8), additionally obtains mixing carbon four logistics (logistics 9).This logistics is through MTBE device
After (module 3) converts, obtain this example and start the mixture (logistics 11) of described butane 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 is not translated to butyl acetate, directly carries out cracking reaction.
Owing to the butane-component in the middle of logistics 11 does not reacts in catalytic cracking/cracking process, for preventing butane group
Divide and accumulate in systems, need the material containing butane is discharged system (logistics 14).Meeting in logistics 14
Some butylene discharges system with butane, causes the yield losses of target product propylene.Freshening complete with butylene
The scheme of (embodiment 1) is compared, and during this, the effective rate of utilization of carbon is relatively low, according to contained in logistics 11
The amount of butylene calculates, and the efficiency of recycling is only 47.7%.
From the Comparative result of above example and comparative example it can be seen that the alkene that will be enriched in the light hydrocarbon feedstocks of alkene
Hydrocarbon carries out cracking conversion reaction after first changing into acetas and separating again, can notable ethylene in pyrolysis product
With the yield of propylene, improving utilization of resources rate, reduce the volume of reactor, therefore this technology path is with often
The method of the direct freshening of rule compares and possesses more significantly advantage.
Claims (8)
1. one kind by C 4 olefin separate after freshening increasing output of ethylene and method of propylene in catalytic cracking or cracking process, it is characterised in that its processing step
As follows:
1). the carbon four containing alkene under catalyst action with acetic acid, reaction temperature 30～200 DEG C, absolute pressure 0.1～6MPa, mass space velocity is
0.1～10h-1Under the conditions of react, wherein acetic acid: olefin molar feed ratio is 0.1～10:1, generate sec-butyl acetate, reactor outlet gained
To material enter into step 2；
2). the 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, obtains the material that the molecular weight that generated by olefine reaction is bigger at the bottom of tower；Materials at bottom of tower enters step 3；
3). dealkylate materials at bottom of tower in step 2 enters in catalytic cracking riser reactor, in reaction temperature 350～650 DEG C, absolute pressure
In the environment of 0.08～0.4MPa, contact with catalyst 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 C 4 olefin and acetic acid between the catalyst of reaction that occurs
For ion-exchange resin catalyst or its modified product, ionic liquid, concentrated sulphuric acid, carried heteropoly acid, Y type molecular sieve or its modified product, ZSM
One or more in molecular sieve or its modified product, SAPO molecular sieve or its modified product；All types of catalyst can be used alone, it is possible to
It is combined as composite catalyst system in the way of by bonding, blending or grating.
3. according to the method described in claim 1, it is characterised in that: step 1) described in C 4 olefin and acetic acid between react used anti-
Answering device is fixed bed reactors or reactive distillation column, can arrange the reactor of one or more series connection, and unreacted acetic acid also can reenter reaction
Device is 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, it is impossible to enough react
Alkane is separated with the sec-butyl acetate generated by reaction, obtains being stripped of the material of alkane at the bottom of tower.
5. according to the method described in claim 1, it is characterised in that: in the material obtained at the bottom of Dealkylater in addition to the sec-butyl acetate that reaction generates,
Can also be containing the acetic acid not reacted, this strand of material can be directly entered catalytic cracking riser reactor and react, it is not necessary to by it with anti-
Product is answered to be completely separated.
6. according to the method described in claim 1, it is characterised in that: step 3) described in dealkylate materials at bottom of tower the catalyst used by cracking reaction choosing
At least one in following: Y type molecular sieve or its modified product, ZSM molecular sieve or its modified product, SAPO molecular sieve or its modified product
Product；All types of catalyst can be used alone, it is also possible to is combined as mixed catalyst by the way of bonding or blending.
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 riser reactor
Carrying out, reaction raw materials includes the boiling spread heavy raw oil more than 350 DEG C, and in dealkylate materials at bottom of tower, sec-butyl acetate, acetic acid etc. enter and carries
The position of riser reactors may be located at the top of heavy charge oil-in, lower section or identical height；Heavy raw oil and sec-butyl acetate, acetic acid
React Deng in the same space, reach 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 riser reactor
Carrying out, reaction raw materials includes the boiling spread heavy raw oil more than 350 DEG C, and in dealkylate materials at bottom of tower, sec-butyl acetate, acetic acid etc. enter and carries
The position of riser reactors is positioned at the lower section of heavy charge oil-in；Heavy raw oil and sec-butyl acetate, acetic acid etc. occur instead in the same space
Should, reach to improve the target of propene yield.
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| CN201510124159.9A CN104672046B (en) | 2015-03-20 | 2015-03-20 | Method of increasing ethylene and propylene yields by freshening C-4 olefins in catalytic cracking or pyrolysis process after separation |
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| CN201510124159.9A CN104672046B (en) | 2015-03-20 | 2015-03-20 | Method of increasing ethylene and propylene yields by freshening C-4 olefins in catalytic cracking or pyrolysis process after separation |
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| CN105152833B (en) * | 2015-07-22 | 2017-08-08 | 珠海飞扬新材料股份有限公司 | A kind of method for preparing n-butene |
| CN109096035A (en) * | 2018-07-17 | 2018-12-28 | 天津大学 | Utilize the method and apparatus of kinetics differential separation alkane and alkene |
| CN112225654A (en) * | 2020-11-02 | 2021-01-15 | 中国海洋石油集团有限公司 | Device and method for comprehensively utilizing mixed C4 |
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| US6218589B1 (en) * | 1997-05-13 | 2001-04-17 | Uop Llc | Method for improving the operation of a propane-propylene splitter |
| CN101432254A (en) * | 2006-02-07 | 2009-05-13 | 塞拉尼斯国际公司 | Integrated process for the production of acetic acid and vinyl acetate |
| CN102264686A (en) * | 2008-11-14 | 2011-11-30 | 国际人造丝公司 | Integrated process for the production of vinyl acetate from acetic acid via ethylene |
-
2015
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3391215A (en) * | 1966-04-20 | 1968-07-02 | Halcon International Inc | Preparation of isoprene |
| US6218589B1 (en) * | 1997-05-13 | 2001-04-17 | Uop Llc | Method for improving the operation of a propane-propylene splitter |
| CN101432254A (en) * | 2006-02-07 | 2009-05-13 | 塞拉尼斯国际公司 | Integrated process for the production of acetic acid and vinyl acetate |
| CN102264686A (en) * | 2008-11-14 | 2011-11-30 | 国际人造丝公司 | Integrated process for the production of vinyl acetate from acetic acid via ethylene |
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