CN102070391B - The method of comprehensive utilization mixed c 4 preparing isobutene - Google Patents
The method of comprehensive utilization mixed c 4 preparing isobutene Download PDFInfo
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- CN102070391B CN102070391B CN201110005342.9A CN201110005342A CN102070391B CN 102070391 B CN102070391 B CN 102070391B CN 201110005342 A CN201110005342 A CN 201110005342A CN 102070391 B CN102070391 B CN 102070391B
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Abstract
Fully utilize a method for mixed c 4 preparing isobutene, mainly solve the problem that the overall utilising efficiency of mixed c 4 is not high and added value is low of refinery or steam cracking device by-product in conventional art.The present invention achieves the goal by adopting the technical scheme comprised the following steps: the divinyl in (1) selective hydrogenation removing mixed c 4; (2) adopt catalytic distillation technology, the butene-1 in the mixed c 4 that the first step is obtained tautomerizes to butene-2, and mixed c 4 is divided into two strands of materials simultaneously: material one is iso-butylene and Trimethylmethane; Material two is normal butane and butene-2; (3) material one is separated by ether-based device and obtains high-purity iso-butylene, obtains high density Trimethylmethane simultaneously; (4) Trimethylmethane is by dehydrogenation, obtains highly purified iso-butylene; (5) material two is by isomerization technique, makes butene-2 tautomerize to iso-butylene, is separated the normal butane obtaining higher degree simultaneously.The present invention can be applicable to the industrial circle producing high-purity isobutylene.
Description
Technical field
The present invention relates to a kind of method fully utilizing mixed c 4 preparing isobutene.
Background technology
Iso-butylene is one of important basic organic, be mainly used in the production of methyl tertiary-butyl ether (MTBE), polyisobutene etc., iso-butylene is also the main raw material of synthetic rubber as isoprene-isobutylene rubber, and iso-butylene or multiple Organic Chemicals are as the raw material of the trimethyl carbinol, methacrylonitrile, oxidation inhibitor etc. simultaneously.Iso-butylene is mainly derived from the by-product mixed c 4 of steam cracking device and refinery catalytic cracking device (FCC).The method that isobutylene separation is most widely used from mixed c 4 is at present etherification technology, can synthesize MTBE on the one hand, on the other hand can by the cracking of MTBE for highly purified iso-butylene.
Mixed c 4 is one of Main By product of steam cracking device and catalytic cracking unit.According to the difference of raw material, reaction depth and catalyzer, the composition comparison in difference of mixed c 4 is obvious.Under normal circumstances, mixed c 4 composition (weight) of steam cracking device by-product is about: alkane: 3%, iso-butylene: 22%, butene-1: 14%, butene-2: 11%, divinyl: 50%.Mixed c 4 composition (weight) of catalytic cracking unit by-product is about: Trimethylmethane: 34%, normal butane: 10%, iso-butylene: 15%, butene-1: 13%, butene-2: 28%.From total amount, generally the mixed c 4 of catalytic cracking unit by-product is approximately the 9%-12% (weight) of device fresh feed, and the mixed c 4 of steam cracking device by-product is approximately the 40-50% of ethene ability.At present, the divinyl in mixed c 4, iso-butylene major part are separated, and their added value is utilized preferably, and are remainingly used as liquefied gas as fuel by major part, and added value is lower.
By the end of the year 2009, Chinese crude oil time processing ability will reach 4.77 hundred million tons, and over the past two years, and China is constructed and put into operation and the oil-refining capacity of building can reach more than 5,000 ten thousand tons, building or the steam cracking device scale of planning construction also considerable.Therefore, following will have a large amount of mixed c 4s to occur, the comprehensive utilization ratio and its chemical utilization value that how to improve mixed c 4 have great realistic meaning.
Document DE102008007081 describes a kind of method extracted butene-1 and produce n-butene oligopolymer from mixed c 4.First from mixed c 4, extracting extracts divinyl, residue mixed c 4 and methyl alcohol isolate iso-butylene by ether-based device, then mixed c 4 is divided into two parts: low boiling mixture is mainly n-butene and Trimethylmethane and high boiling mixture and is mainly normal butane and butene-2, again selective hydrogenation is carried out to low boiling mixture, removing residue diene wherein, lower boiling mixed c 4 after hydrogenation obtains butene-1 and Trimethylmethane by rectifying separation, finally copolyreaction is carried out to high boiling mixture, the n-butene in high boiling mixture is made to form n-butene oligopolymer.This method make use of divinyl, iso-butylene and n-butene in mixed c 4, but remaining iso-butylene, butene-2 and butane are not fully utilized, and overall utilising efficiency is not very high.
Document ZL200710039072 describes a kind of method fully utilizing mixed c 4 production propylene, first mixed c 4 passes through deep catalytic cracking technology, obtain part propylene and ethene, pass through isomerization technique again, butene-1 in residue mixed c 4 is tautomerized to butene-2, then by olefin metathesis technology, butene-2 and ethene generation disproportionation reaction is made to produce propylene.This method can obtain the propylene of high added value, but also has a lot of component such as iso-butylene, Trimethylmethane etc. not to be fully utilized simultaneously, and the added value of mixed c 4 does not maximize.
Summary of the invention
The present invention relates to a kind of method fully utilizing mixed c 4 preparing isobutene, be mainly used in preparing iso-butylene by mixed c 4.
The object of the invention is to produce iso-butylene by mixed c 4, technical problem to be solved is the problem that the overall utilising efficiency of mixed c 4 is not high, mixed c 4 added value is low of steam cracking device or catalytic cracking unit by-product in conventional art, provides a kind of method of being produced iso-butylene by mixed c 4 newly.Present method takes full advantage of each component in mixed c 4, makes it to be converted into iso-butylene, improves the ultimate production of iso-butylene; Obtain the normal butane of high density simultaneously.Present method has that mixed c 4 comprehensive utilization ratio is high, iso-butylene yield is high and mixed c 4 added value obtains putting forward advantages of higher more greatly.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method fully utilizing mixed c 4 preparing isobutene, comprises the following steps:
(1) divinyl in selective hydrogenation removing mixed c 4;
(2) adopt catalytic distillation technology, the butene-1 in the mixed c 4 that the first step is obtained tautomerizes to butene-2, and mixed c 4 is divided into two strands of materials simultaneously: material one is iso-butylene and Trimethylmethane; Material two is normal butane and butene-2;
(3) material one is separated by ether-based device and obtains MTBE and then cracking obtains high-purity isobutylene, is separated simultaneously and obtains high density Trimethylmethane;
(4) Trimethylmethane is by dehydrogenation, obtains highly purified iso-butylene;
(5) material two is by isomerization technique, makes butene-2 tautomerize to iso-butylene;
(6) by conventional rectification, the normal butane obtaining high-purity isobutylene and high density is separated.
In technique scheme, mixed c 4 is preferably the mixed c 4 of steam cracking device or catalytic cracking unit by-product.Divinyl is preferably hydrogenated to butene-1 and/or butene-2 by selectivity, and selective hydrogenation catalyst is preferably alumina load metallic nickel, zinc and/or palladium.
Catalytic distillation is preferably to adopt and shares raw material, and shared raw material is preferably hydrogen; Conversion zone preferably loads hydroisomerisation catalysts, and catalyzer is preferably alumina load metallic nickel, zinc and/or palladium.
Ether-based device is preferably and adopts catalytic distillation reactor, and catalyzer is preferably macropore strong acid cation exchange resin, ZSM-5 molecular sieve, heteropolyacid etc.
Dehydrogenation of isobutane preferably adopts fluidized-bed reactor, and catalyzer is preferably alumina load metal platinum, tin and/or zinc.
Butene-2 isomery turns to iso-butylene and is preferably employing fixed-bed reactor or fluidized-bed reactor, and catalyzer is preferably SAPO, ZSM or the zeolite molecular sieve of modification.
Normal butane is preferably as steam cracking device raw material.
The present invention is by selective hydrogenation technology, hydroisomerization technology and skeletal isomerization technology and De-hydrogen Technology, make the divinyl in mixed c 4, butene-1 and butene-2, Trimethylmethane major part is converted into iso-butylene, remaining concentration of n-butane is very high, is the steam cracking device raw material of high-quality.Therefore, present invention utilizes each component in mixed c 4, obtain the iso-butylene that added value is higher, greatly improve the added value of mixed c 4.Consider the iso-butylene yield of unit, the overall yield of iso-butylene can reach more than 80% (the mixed c 4 raw material for except normal butane).
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of present invention process;
Fig. 2 is the schematic flow sheet of document DE102008007081;
The explanation of Fig. 1 numbering:
A, selective hydrogenation of butadiene unit; B, catalytic distillation isomerization unit; C, etherificate unit; D, dehydrogenation of isobutane unit; E, butene-2 isomery turn to isobutene units; F, rectification cell.
1, mixed c 4; 2, Trimethylmethane+iso-butylene; 3, normal butane+butene-2; 4, Trimethylmethane; 5, MTBE (iso-butylene); 6, iso-butylene; 7, iso-butylene; 8, normal butane.
The explanation of Fig. 2 numbering:
G, etherificate unit; H, the first rectification cell; I, selective hydrogenation unit; J, the second rectification cell.
9, mixed c 4 after extracting divinyl; 10, mixed c 4 after etherificate; 11, to circulate light carbon four (Trimethylmethane+n-butene); 12, light carbon four (Trimethylmethane+n-butene); 13, circulation n-butene; 14, n-butene; 15, heavy carbon four (normal butane+butene-2); 16, heavy carbon four (normal butane+butene-2).
In Fig. 1, the mixed c 41 from steam cracking device or refinery catalytic cracking device enters selectively hydrogenating butadiene unit A, and by selective hydrogenation, divinyl is converted into butene-1 and/or butene-2.Mixed c 4 after hydrogenation enters catalytic distillation isomerization unit B, is isomerized to butene-2 at this element butene-1, and mixed c 4 is separated into two strands of materials simultaneously, and material 2 is light boiling point mixed c 4, mainly comprises iso-butylene and Trimethylmethane; Material 3 is attached most importance to boiling point mixed c 4, mainly comprises normal butane and butene-2.Material 2 is by etherificate unit, and iso-butylene wherein and methyl alcohol react to be produced gasoline dope MTBE product 5, MTBE and be further converted to highly purified iso-butylene by cracking.Remaining in material 2 is Trimethylmethane 4, and Trimethylmethane 4 is converted into iso-butylene product 6 by dehydrogenation unit D.Material 3 enters isomerization unit E, and butene-2 is wherein isomerized to iso-butylene, and this isomerization product is separated by rectification cell F and obtains iso-butylene 7 and normal butane 8.Normal butane can as the steam cracking device raw material of high-quality.
Below by embodiment, the invention will be further elaborated.
Embodiment
[comparative example 1]
Shown in Fig. 2, mixed c 4 composition (% by weight) after extracting divinyl is: Trimethylmethane: 5, normal butane: 11; Iso-butylene: 45, butene-1: 21, butene-2: 18.Experiment proves to adopt this invention, and the yield of iso-butylene is about 48% (the mixed c 4 raw material for except normal butane), and the rate of recovery of butene-1 is about 66%, and all the other are still the mixed c 4 do not utilized.
[embodiment 1]
Shown in Fig. 1, the mixed c 4 from steam cracking device forms (% by weight) and is: Trimethylmethane: 1, normal butane: 2, divinyl: 50, iso-butylene: 22, butene-1: 14, butene-2: 11.Selectively hydrogenating butadiene catalyzer is alumina load metallic nickel and zinc.It is hydrogen that catalytic distillation shares raw material, and the hydroisomerisation catalysts of conversion zone filling is alumina load metallic nickel and zinc.Ether-based device adopts catalytic distillation reactor, and catalyzer is macropore strong acid cation exchange resin.Dehydrogenation of isobutane adopts fluidized-bed reactor, and catalyzer is alumina load metal platinum and zinc.Butene-2 isomery turns to iso-butylene and adopts single hop fixed-bed reactor, and catalyzer is the metal-modified zeolite molecular sieve of magnesium.Experiment proves that the yield adopting the inventive method iso-butylene is 88% (the mixed c 4 raw material for except normal butane), and normal butane is 3%, and other are unconverted mixed c 4.
[embodiment 2]
Shown in Fig. 1, the mixed c 4 from steam cracking device forms (% by weight) and is: Trimethylmethane: 1, normal butane: 2, divinyl: 50, iso-butylene: 22, butene-1: 14, butene-2: 11.Selectively hydrogenating butadiene catalyzer is alumina load palladium metal and zinc.It is hydrogen that catalytic distillation shares raw material, and the hydroisomerisation catalysts of conversion zone filling is alumina load palladium metal and zinc.Ether-based device adopts catalytic distillation reactor, and catalyzer is ZSM-5 molecular sieve.Dehydrogenation of isobutane adopts fluidized-bed reactor, and catalyzer is alumina load metal platinum and zinc.Butene-2 isomery turns to iso-butylene and adopts fluidized-bed reactor, and catalyzer is the SAPO-11 molecular sieve of alkali metals modified.Experiment proves that the yield adopting iso-butylene of the present invention is 81%, and normal butane is 5%, and other are unconverted mixed c 4.
[embodiment 3]
Shown in Fig. 1, the mixed c 4 from refinery catalytic cracking device forms (% by weight) and is: Trimethylmethane: 34, normal butane: 10, divinyl: 0, iso-butylene: 15, butene-1: 13, butene-2: 28.Without selectively hydrogenating butadiene unit.It is hydrogen that catalytic distillation shares raw material, and the hydroisomerisation catalysts of conversion zone filling is alumina load palladium metal and zinc.Ether-based device adopts catalytic distillation reactor, and catalyzer is ZSM-5 molecular sieve.Dehydrogenation of isobutane adopts fluidized-bed reactor, and catalyzer is alumina load metal platinum and zinc.Butene-2 isomery turns to iso-butylene and adopts single hop fixed-bed reactor, and catalyzer is the zeolite molecular sieve of magnesium alkali metals modified.Experiment proves that the yield adopting iso-butylene of the present invention is 83%, and normal butane is 3%, and other are unconverted mixed c 4.
Claims (7)
1. fully utilize a method for mixed c 4 preparing isobutene, comprise the following steps:
(1) divinyl in selective hydrogenation removing mixed c 4;
(2) adopt catalytic distillation technology, the butene-1 in the mixed c 4 that the first step is obtained tautomerizes to butene-2, and mixed c 4 is divided into two strands of materials simultaneously: material one is iso-butylene and Trimethylmethane; Material two is normal butane and butene-2;
(3) material one is separated by ether-based device and obtains MTBE and then cracking obtains iso-butylene, is separated simultaneously and obtains Trimethylmethane;
(4) Trimethylmethane is by dehydrogenation, obtains iso-butylene; Dehydrogenation of isobutane adopts fluidized-bed reactor, and catalyzer is alumina load metal platinum, tin and/or zinc;
(5) material two is by isomerization technique, makes butene-2 tautomerize to iso-butylene;
(6) by conventional rectification, be separated and obtain iso-butylene and normal butane.
2. prepare the technique of iso-butylene according to claim 1, it is characterized in that mixed c 4 is the mixed c 4 of steam cracking device or catalytic cracking unit by-product.
3. prepare the technique of iso-butylene according to claim 1, it is characterized in that divinyl is hydrogenated to butene-1 and/or butene-2 by selectivity, selective hydrogenation catalyst is alumina load metallic nickel, zinc and/or palladium.
4. prepare the technique of iso-butylene according to claim 1, it is characterized in that catalytic distillation adopts shared raw material to be hydrogen; Conversion zone filling hydroisomerisation catalysts, catalyzer is alumina load metallic nickel, zinc and/or palladium.
5. prepare the technique of iso-butylene according to claim 1, it is characterized in that ether-based device adopts catalytic distillation reactor, catalyzer is macropore strong acid cation exchange resin, ZSM-5 molecular sieve, heteropolyacid.
6. prepare the technique of iso-butylene according to claim 1, it is characterized in that butene-2 isomery turns to iso-butylene and adopts fixed-bed reactor or fluidized-bed reactor, catalyzer is SAPO or the ZSM molecular sieve of modification.
7. prepare the technique of iso-butylene according to claim 1, it is characterized in that normal butane can as the steam cracking device raw material of high-quality.
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