CN101260016A - Refining device for preparing high-pure isobutene by cracking methyl tertiary butyl ether and technique thereof - Google Patents
Refining device for preparing high-pure isobutene by cracking methyl tertiary butyl ether and technique thereof Download PDFInfo
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Abstract
The invention discloses a refining device and a technical method used to make high-purity isobutene through the cracking of methyl tert-butyl ether. The technical method contains a six-tower continuous rectification technical process, and comprises a cooling absorption double tower system, a methanol dehydrating tower system, a methanol refining tower system, an isobutene light fraction-removal tower system and an isobutene heavy fraction-removal tower system, wherein the water discharged from the methanol dehydrating tower system is cooled down and then is returned to a cooling absorption tower to undergo cooling absorption operation once again; therefore, the refining process realizes zero release of cooling absorption water; moreover, the internal top of a cooling absorption tower 2 is provided with a foam destroyer which catches the liquid droplets carried in gas, thereby ensuring the purity of isobutene product. All internal parts of each rectification tower device adopt efficient regular filler and multi-row hole distribution, which ensures that the purity of high-purity isobutene product is more than 99.7 percent.
Description
Technical field
The present invention relates to the distillation technology field, particularly relate to the refining plant and the processing method of preparing high-pure isobutene by cracking methyl tertiary butyl ether.Adopting six tower continuous rectification technical process is raw material with methyl tertiary butyl ether (MTBE) splitting gas, the rectifying tower internals adopt efficient structured packing and the refining high-purity iso-butylene product of many rounds distribution internals, make sepn process realize the zero release of recirculated water simultaneously, reach the purpose that energy consumption reduces, reduces investment outlay.
Background technology
Iso-butylene is important Organic Chemicals, is widely used in petrochemical complex production fields such as isoprene-isobutylene rubber, polyisobutene, tert-butyl mercaptan, tert-butylamine, tert-butyl acetate, methyl methacrylate, the trimethyl carbinol, methacrylic acid, methacrylonitrile, pivalyl aldehyde and isoprene.Along with the continuous development of fine chemistry industry, more and more higher to the specification of quality of iso-butylene.The method of producing iso-butylene in industrial production mainly contains: sulfuric acid extraction process, trimethyl carbinol cracking process and methyl tertiary butyl ether (MTBE) cracking process.The iso-butylene industry of China is started late, Beijing Yanshan Petrochemical Company's triumph seventies refinery has built up a cover 10000t/a sulfuric acid extraction process preparing isobutene device, because problems such as equipment corrosion is serious, poor product quality, production cost height are eliminated after the eighties.Trimethyl carbinol cracking process product yield is low, lack of material, solution equipment corrosion are still a very problem of difficulty.Methyl tertiary butyl ether (MTBE) cracking preparing isobutene is the state-of-the-art method of a kind of production iso-butylene that generally adopts in recent years, advantage such as it has low in the pollution of the environment, no equipment corrosion, catalyzer transformation efficiency height, selectivity is good, technical process is simple, reduced investment, energy consumption and material consumption are relatively low, all there are large-scale industrial production in the U.S., West Germany, France, Italy and Japan etc.
China is by the refining separation process scheme that producer adopted of methyl tertiary butyl ether (MTBE) cracking preparing isobutene, and it is not thorough to exist methyl alcohol to absorb, and is brought in the iso-butylene product and influences the problem of its purity.Hongye Fine Chemical Co., Lanzhou's application number be described in 200610041851.6 the patent in the iso-butylene technological process of production separating technology adopt two towers (cooling and absorbing tower, methanol dehydration tower) separating technology, the iso-butylene product purity of being separated reaches 99.41% at most, can't produce high-purity (purity is higher than 99.7%) iso-butylene product.
Summary of the invention
The object of the invention is to provide a kind of high-purity iso-butylene purified continuous rectificating technique flow process and device, this method is used for the treating process of the high-purity iso-butylene product of methyl tertiary butyl ether (MTBE) cracking system, realize the zero release of recirculated water, in industrial application, have advantages such as energy consumption and production cost are low.
The present invention is realized by the following technical programs:
The refining plant of preparing high-pure isobutene by cracking methyl tertiary butyl ether of the present invention, the six tower continuous rectification flow path devices that comprise cooling and absorbing double tower, methanol dehydration tower, refining methanol tower, iso-butylene lightness-removing column and iso-butylene weight-removing column, wherein scum dredger is set, captures droplets entrained in the exhaust gas body at cooling and absorbing tower 2 tower inner tops.
The processing method of the refining plant of preparing high-pure isobutene by cracking methyl tertiary butyl ether of the present invention is: at the bottom of cooling and absorbing tower 1 tower opening for feed is set, methyl tertiary butyl ether raw cracked gas 0 enters system by cooling and absorbing tower 1, cooling and absorbing tower 1 overhead product material 9 directly enters cooling and absorbing tower 2 bottoms by sealing-duct, the tower reactor distillate by the pump extraction after, part material is a recycle stock, and another part material is for distillating material.Cooling and absorbing tower 1 tower stilling goes out recycle stock 10 to be sent into and returns Ben Tanei after interchanger is lowered the temperature and carry out cyclical operation, and 11 in cooling and absorbing tower 1 tower reactor distillate material is directly sent in the methanol dehydration tower 3 by sealing-duct.Cooling and absorbing tower 2 overhead product material 14 by behind the scum dredger capture drop, enter the operation that removes light constituent in the iso-butylene lightness-removing column 5 by sealing-duct in cooling and absorbing tower 2.Cooling and absorbing tower 2 tower reactor distillates are after the pump extraction, and a part of material is a recycle stock, and another part is the tower reactor distillate.Cooling and absorbing tower 2 recycle stocks 13 are sent into and are returned Ben Tanei after interchanger is lowered the temperature and carry out cyclical operation, and 12 of cooling and absorbing tower 2 tower still distilled materials are directly sent in the cooling and absorbing tower 1 by sealing-duct.Methanol dehydration tower 3 cats head distillate thick methyl alcohol 16 and enter refining methanol tower 4 by sealing-duct, and methanol dehydration Tata reactor distillate material 15 is by being pumped in the cooling and absorbing tower 2.Refining methanol tower 4 cat head light constituents 17 are sent system, and tower reactor distillate material is a methanol product 18; Iso-butylene lightness-removing column cat head distillates light constituent 20 and sends system from iso-butylene lightness-removing column 5 cats head, and iso-butylene lightness-removing column tower reactor distillate material 19 is by being pumped into the distillation operation that iso-butylene weight-removing column 6 removes heavy constituent; Iso-butylene weight-removing column 6 cats head are iso-butylene product 22, and iso-butylene weight-removing column tower stilling goes out heavy constituent 21 and sends system.
The processing method of the refining plant of described preparing high-pure isobutene by cracking methyl tertiary butyl ether, it is characterized in that described cooling and absorbing tower 1 operates under normal pressure or pressure-fired, number of theoretical plate is 15-20, returning the interior internal circulating load of tower and the recycle ratio of produced quantity is 1-5, and column internals adopts efficient structured packing and many rounds distribution internals.
Described cooling and absorbing tower 2 is operated under normal pressure or pressure-fired, and number of theoretical plate is 15-20, and returning the interior internal circulating load of tower and the recycle ratio of produced quantity is 1-5, and the tower inner top is provided with scum dredger, and column internals adopts efficient structured packing and many rounds distribution internals.
Temperature is 63-99.2 ℃ in described methanol dehydration tower 3 atmospheric operations, corresponding tower, and reflux ratio is 1-4, and number of theoretical plate is 30-40, and column internals adopts efficient structured packing and many rounds distribution internals.
Temperature is 39-66.2 ℃ in described refining methanol tower 4 normal pressures or the micro-pressure operation, corresponding tower, and reflux ratio is 50-70, and number of theoretical plate is 30-40, and column internals adopts efficient structured packing and many rounds distribution internals.
Temperature is 26-40.8 ℃ in the described iso-butylene lightness-removing column 5 pressure 300～500kPa, corresponding tower, and number of theoretical plate is 25-40, and column internals adopts efficient structured packing and many rounds distribution internals.
Temperature is 24-95.5 ℃ in the described iso-butylene weight-removing column 6 pressure 300～500kPa, corresponding tower, and number of theoretical plate is 25-40, and column internals adopts efficient structured packing and many rounds distribution internals.
The cooling and absorbing double tower is adopted in the present invention's six tower continuous rectification technical process, and scum dredger is set in cooling and absorbing tower 2 cat head inside, light constituents such as methyl alcohol in the iso-butylene better can be absorbed, each rectifying tower adopts efficient structured packing and many rounds distribution internals to improve mass-transfer efficiency, realize that iso-butylene purity is higher than 99.7% and the zero release of recirculated water, reduce energy consumption greatly, the purpose that reduces production costs.
The present invention has following advantage: 1. adopt efficient structured packing and many rounds distribution internals can improve the rectifying tower mass-transfer efficiency, reduce full tower pressure drop; 2. the iso-butylene product purity height of separating belongs to high-purity iso-butylene product greater than 99.7%; 3. cooling and absorbing water does not have discharging, reduces energy consumption and production cost.
Description of drawings
Fig. 1 is the refining six tower continuous rectification schematic flow sheets of high-purity iso-butylene.
Among the figure, 0 splitting gas; 1 cooling and absorbing tower; 2 cooling and absorbing towers; 3 methanol dehydration towers; 4 refining methanol towers; 5 iso-butylene lightness-removing columns; 6 iso-butylene weight-removing columns; 7 fresh waters; The 2 tower stilling water outlets of 8 cooling and absorbing towers; 9 cooling and absorbing towers, 1 overhead product material; 10 cooling and absorbing towers, 1 tower stilling goes out recycle stock; 11 cooling and absorbing towers, 1 tower reactor distillate material; 12 cooling and absorbing towers, 2 tower still distilled materials; 13 cooling and absorbing towers, 2 recycle stocks; 14 cooling and absorbing towers, 2 overhead product material; 15 methanol dehydration Tata reactor distillate material; 16 thick methyl alcohol; 17 light constituents; 18 methanol product; 19 iso-butylene lightness-removing column tower reactor distillate material; 20 iso-butylene lightness-removing column cats head distillate light constituent; 21 iso-butylene weight-removing column tower stillings go out heavy constituent; 22 iso-butylene products.
Embodiment
Below in conjunction with embodiment and accompanying drawing the present invention is described in further detail, but the present invention is not limited to this.
The splitting gas 0 that contains iso-butylene 58.75% (wt), methyl alcohol 34.52% (wt), MTBE 4.92% (wt), dme 0.51% (wt), the trimethyl carbinol 0.15% (wt), water 0.25% (wt) and C80.9% (wt) after methyl tertiary butyl ether (MTBE) cracking enters described cooling and absorbing double tower system from the tower still of cooling and absorbing tower 1 and begins to cool down and absorb operation, and cooling and absorbing tower 2 tower stilling water outlets 8 (being fresh water 7 when just driving) enter described cooling and absorbing tower 1 from cat head.In cooling and absorbing tower 1 tower is normal pressure or micro-pressure operation, and 16 theoretical stages, column internals adopt efficient structured packing and many rounds distribution internals.Cooling and absorbing tower 1 overhead product material 9 through overcooling and after being absorbed methyl alcohol directly enters the bottom of cooling and absorbing tower 2 by sealing-duct from described cooling and absorbing tower 1 top.Described cooling and absorbing tower 1 tower reactor distillate by the pump extraction after, a part of material is a recycle stock, another part material is a tower reactor distillate material.Cooling and absorbing tower 1 tower stilling goes out recycle stock 10 and enters interchanger and cool return Ben Tanei after 40 ℃, carries out cyclical operation.11 in cooling and absorbing tower 1 tower reactor distillate material enters by sealing-duct in the methanol dehydration tower 3 of methanol dehydration rectifying tower system and carries out dehydration operation.The recycle ratio of round-robin inventory and extraction inventory is 2.0.Enter methanol dehydration Tata reactor distillate material 15 cooling and absorbing that the cooling and absorbing tower 1 overhead product material 9 at the bottom of cooling and absorbing tower 2 towers is entered from top of tower.In cooling and absorbing tower 2 towers is normal pressure or pressure-fired, and number of theoretical plate is 13, and cat head inside is provided with scum dredger, and column internals adopts efficient structured packing and many rounds distribution internals.From described cooling and absorbing tower 2 interior process scum dredgers, the cooling and absorbing tower 2 overhead product material 14 that come out are for containing the thick isobutene gas of 90.38% (wt), send into tundish after the compressed machine compression, the thick iso-butylene liquid in the tundish is sent into the iso-butylene lightness-removing column 5 of iso-butylene lightness-removing column system by pump.Described cooling and absorbing tower 2 tower reactor distillate material by the pump extraction after, a part of material is a recycle stock, another part material is a tower reactor distillate material.Cooling and absorbing tower 2 recycle stocks 13 enter interchanger and cool return Ben Tanei after 30 ℃, carry out cyclical operation.12 of cooling and absorbing tower 2 tower still distilled materials carry out the cooling and absorbing operation by enter cooling and absorbing tower 1 top by sealing-duct.Returning the inventory of tower internal recycle and the recycle ratio of extraction inventory is 2.0.Cooling and absorbing tower 1 tower reactor distillate material 11 enters described methanol dehydration rectifying tower system, by being pumped in the methanol dehydration tower 3.Described methanol dehydration tower 3 is an atmospheric operation, and temperature is 63-99.2 ℃ in the tower, and reflux ratio is 2.0, and column internals is efficient structured packing and many rounds distribution internals.Methanol dehydration tower 3 cats head distillate thick methyl alcohol 16 (97.22% (wt)) through being pumped into the refining methanol Tower System, and methanol dehydration Tata reactor distillate material 15 is through being pumped into described cooling and absorbing tower 2 cats head.Methanol dehydration tower atmospheric operation, number of theoretical plate are 35, and column internals adopts efficient structured packing and many rounds distribution internals.Enter described refining methanol Tower System from the thick methyl alcohol 16 of described methanol dehydration tower 3, by being pumped in the refining methanol tower 4.Refining methanol tower 4 is normal pressure or micro-pressure operation, and temperature is 39-66.2 ℃ in the tower, and number of theoretical plate is 35, and internals adopt efficient structured packing and many rounds distribution internals.Cat head distillates the light constituent 17 that contains iso-butylene and MTBE, and the tower stilling goes out the methanol product 18 that concentration is higher than 99% (wt), by being pumped into the methanol product jar.Enter the tail gas buffer of iso-butylene lightness-removing column system from the next thick iso-butylene that contains iso-butylene 90.38% (wt) of described cooling and absorbing tower 2 cats head, be compressed into liquid state from the compressed machine of tail gas buffer and send into the iso-butylene tundish, by being pumped in the iso-butylene lightness-removing column 5.Working pressure 300kPa in the described iso-butylene lightness-removing column 5, temperature is 26-40.8 ℃ in the tower, and number of theoretical plate is 30, and column internals adopts efficient structured packing and many rounds distribution internals.Iso-butylene lightness-removing column cat head distillates the light constituent that light constituent 20 contains DME etc., and the tower stilling goes out the iso-butylene lightness-removing column tower reactor distillate material 19 of 90.86% (wt), through being pumped into iso-butylene weight-removing column system.Enter described iso-butylene weight-removing column system from the iso-butylene lightness-removing column tower reactor distillate material 19 of described iso-butylene lightness-removing column 5, send in the iso-butylene weight-removing column 6 by sealing-duct by pump.Temperature is 24-95.5 ℃ in the working pressure 300kPa in the iso-butylene weight-removing column 6, corresponding tower, and number of theoretical plate is 30, and column internals adopts efficient structured packing and many rounds distribution internals.Iso-butylene weight-removing column 6 cats head distillate concentration and are higher than 99.7% iso-butylene product 22, and by being pumped into iso-butylene product jar, iso-butylene weight-removing column tower stilling goes out the heavy constituent that heavy constituent 21 contain MTBE etc., by pumping out system.
Whole process has realized the zero release of water.
The refining plant and the processing method of the preparing high-pure isobutene by cracking methyl tertiary butyl ether that the present invention proposes, be described by embodiment, person skilled obviously can be changed or suitably change and combination content as herein described in not breaking away from content of the present invention, spirit and scope, realizes the present invention.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they are regarded as being included in spirit of the present invention, scope and the content.
Claims (8)
1. the refining plant of preparing high-pure isobutene by cracking methyl tertiary butyl ether, comprise cooling and absorbing double tower, methanol dehydration tower, refining methanol tower, iso-butylene lightness-removing column and iso-butylene weight-removing column, it is characterized in that adopting six tower continuous rectification flow path devices of two cooling and absorbing towers, the top is provided with scum dredger in cooling and absorbing tower (2) tower, captures droplets entrained in the exhaust gas body.
2. by the processing method of the refining plant of the described preparing high-pure isobutene by cracking methyl tertiary butyl ether of claim 1, it is characterized in that: at the bottom of cooling and absorbing tower (1) tower opening for feed is set, the methyl tertiary butyl ether raw cracked gas enters described system by cooling and absorbing tower (1), cooling and absorbing tower (1) overhead product material (9) directly enters cooling and absorbing tower (2) bottom by sealing-duct, the tower reactor distillate by the pump extraction after, part material is a recycle stock, and another part is a tower reactor distillate material; Cooling and absorbing tower (1) tower stilling goes out recycle stock (10) to be sent into and returns Ben Tanei after interchanger is lowered the temperature and carry out cyclical operation, and cooling and absorbing tower 1 tower reactor distillate material (11) is then directly sent in the methanol dehydration tower (3) by sealing-duct; Cooling and absorbing tower (2) overhead product material (14) enters the operation that removes light constituent in the iso-butylene lightness-removing column (5) after capturing drop by scum dredger; Cooling and absorbing tower (2) tower reactor distillate is after the pump extraction, and a part of material is a recycle stock, and another part is a tower reactor distillate material; Cooling and absorbing tower (2) recycle stock (13) is sent into and is returned Ben Tanei after interchanger is lowered the temperature and carry out cyclical operation, and cooling and absorbing tower (2) tower still distilled material (12) is then directly sent in the cooling and absorbing tower (1) by sealing-duct; Methanol dehydration tower (3) overhead product material is that thick methyl alcohol (16) enters refining methanol tower (4) by sealing-duct, and methanol dehydration Tata reactor distillate material (15) is by being pumped in the cooling and absorbing tower (2); Refining methanol tower (4) cat head is that light constituent (17) is sent system, and the tower reactor distillate is methanol product (18); Iso-butylene lightness-removing column cat head distillates light constituent (20) and sends system from iso-butylene lightness-removing column (5) cat head, and iso-butylene lightness-removing column tower reactor distillate material (19) is by being pumped into the distillation operation that iso-butylene weight-removing column (6) removes heavy constituent; Iso-butylene weight-removing column (6) cat head is high-purity iso-butylene product (22), and iso-butylene weight-removing column tower stilling goes out heavy constituent (21) and is sent system.
3. the processing method of the refining plant of preparing high-pure isobutene by cracking methyl tertiary butyl ether as claimed in claim 2, it is characterized in that described cooling and absorbing tower (1) operates under normal pressure or pressure-fired, number of theoretical plate is 15-20, returning the interior internal circulating load of tower and the recycle ratio of produced quantity is 1-5, and column internals adopts efficient structured packing and many rounds distribution internals.
4. the processing method of the refining plant of preparing high-pure isobutene by cracking methyl tertiary butyl ether as claimed in claim 2, it is characterized in that described cooling and absorbing tower (2) operates under normal pressure or pressure-fired, number of theoretical plate is 15-20, returning the interior internal circulating load of tower and the recycle ratio of produced quantity is 1-5, cat head is provided with scum dredger, and column internals adopts efficient structured packing and many rounds distribution internals.
5. the processing method of the refining plant of preparing high-pure isobutene by cracking methyl tertiary butyl ether as claimed in claim 2, it is characterized in that described methanol dehydration tower (3) atmospheric operation, temperature is 63-99.2 ℃ in the corresponding tower, reflux ratio is 1-4, number of theoretical plate is 30-40, and column internals adopts efficient structured packing and many rounds distribution internals.
6. the processing method of the refining plant of preparing high-pure isobutene by cracking methyl tertiary butyl ether as claimed in claim 2, it is characterized in that described refining methanol tower (4) normal pressure or micro-pressure operation, temperature is 39-66.2 ℃ in the corresponding tower, reflux ratio is 50-70, number of theoretical plate is 30-40, and column internals adopts efficient structured packing and many rounds distribution internals.
7. the processing method of the refining plant of preparing high-pure isobutene by cracking methyl tertiary butyl ether as claimed in claim 2, it is characterized in that described iso-butylene lightness-removing column (5) pressure 300～500kPa, temperature is 26-40.8 ℃ in the corresponding tower, number of theoretical plate is 25-40, and column internals adopts efficient structured packing and many rounds distribution internals.
8. the processing method of the refining plant of preparing high-pure isobutene by cracking methyl tertiary butyl ether as claimed in claim 2, it is characterized in that described iso-butylene weight-removing column (6) pressure 300～500kPa, temperature is 24-95.5 ℃ in the corresponding tower, number of theoretical plate is 25-40, and column internals adopts efficient structured packing and many rounds distribution internals.
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| CNA2008100528680A CN101260016A (en) | 2008-04-23 | 2008-04-23 | Refining device for preparing high-pure isobutene by cracking methyl tertiary butyl ether and technique thereof |
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| CNA2008100528680A CN101260016A (en) | 2008-04-23 | 2008-04-23 | Refining device for preparing high-pure isobutene by cracking methyl tertiary butyl ether and technique thereof |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103130606A (en) * | 2013-03-11 | 2013-06-05 | 岳阳兴长石化股份有限公司 | Unacceptable product reprocessing technique in isobutylene production |
| CN103772113A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Method for preparing polymer-grade isobutene by cracking methyl tertbutyl ether |
| CN103804116A (en) * | 2012-11-08 | 2014-05-21 | 中国石油化工股份有限公司 | Method for preparing polymer-grade isobutylene through cracking of methyl tert-butyl ether |
| CN103992202A (en) * | 2013-03-11 | 2014-08-20 | 上海蓝科石化工程技术有限公司 | System and method for cracking of methyl tertiary butyl ether to prepare high purity isobutylene |
| CN104591947A (en) * | 2013-11-03 | 2015-05-06 | 中国石油化工股份有限公司 | Method for producing isobutylene from methyl tert-butyl ether by pyrolysis |
| CN109134175A (en) * | 2018-10-24 | 2019-01-04 | 凯瑞环保科技股份有限公司 | A kind of technique and device of MTBE cracking high-purity isobutylene |
| CN110204409A (en) * | 2018-08-31 | 2019-09-06 | 住友化学株式会社 | The manufacturing device of isobutene and the manufacturing method of isobutene |
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- 2008-04-23 CN CNA2008100528680A patent/CN101260016A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103772113A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Method for preparing polymer-grade isobutene by cracking methyl tertbutyl ether |
| CN103772113B (en) * | 2012-10-24 | 2016-02-03 | 中国石油化工股份有限公司 | A kind of method of methyl tertiary butyl ether cracking isobutene polymer grade |
| CN103804116A (en) * | 2012-11-08 | 2014-05-21 | 中国石油化工股份有限公司 | Method for preparing polymer-grade isobutylene through cracking of methyl tert-butyl ether |
| CN103804116B (en) * | 2012-11-08 | 2016-03-30 | 中国石油化工股份有限公司 | A kind of method of methyl tertiary butyl ether cracking isobutene polymer grade |
| CN103130606A (en) * | 2013-03-11 | 2013-06-05 | 岳阳兴长石化股份有限公司 | Unacceptable product reprocessing technique in isobutylene production |
| CN103992202A (en) * | 2013-03-11 | 2014-08-20 | 上海蓝科石化工程技术有限公司 | System and method for cracking of methyl tertiary butyl ether to prepare high purity isobutylene |
| CN104591947A (en) * | 2013-11-03 | 2015-05-06 | 中国石油化工股份有限公司 | Method for producing isobutylene from methyl tert-butyl ether by pyrolysis |
| CN104591947B (en) * | 2013-11-03 | 2017-01-04 | 中国石油化工股份有限公司 | The method that the cracking of a kind of methyl tertiary butyl ether(MTBE) produces isobutene. |
| CN110204409A (en) * | 2018-08-31 | 2019-09-06 | 住友化学株式会社 | The manufacturing device of isobutene and the manufacturing method of isobutene |
| CN110204409B (en) * | 2018-08-31 | 2020-05-05 | 住友化学株式会社 | Apparatus for producing isobutylene and method for producing isobutylene |
| CN109134175A (en) * | 2018-10-24 | 2019-01-04 | 凯瑞环保科技股份有限公司 | A kind of technique and device of MTBE cracking high-purity isobutylene |
| CN109134175B (en) * | 2018-10-24 | 2023-09-01 | 凯瑞环保科技股份有限公司 | Process and device for preparing high-purity isobutene through MTBE pyrolysis |
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