CN1304917A - Process for preparing tert-butanol from isobutylene by hydration - Google Patents
Process for preparing tert-butanol from isobutylene by hydration Download PDFInfo
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- CN1304917A CN1304917A CN 00129128 CN00129128A CN1304917A CN 1304917 A CN1304917 A CN 1304917A CN 00129128 CN00129128 CN 00129128 CN 00129128 A CN00129128 A CN 00129128A CN 1304917 A CN1304917 A CN 1304917A
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Abstract
A process for preparing tert-butanol from isobutylene by hydration reaction features use of cationic exchange resin as catalyst and the counterflow hydration reaction. Its advantages are simple process, high conversion and selectivity and low consumption of energy and raw material.
Description
The present invention relates to a kind of synthetic method of the trimethyl carbinol, particularly from C
4The method of preparing tert-butanol from isobutylene by hydration in the hydrocarbon.
Contain the hydrocarbon polymer of iso-butylene and water and in various catalyzer, react the method that generates the trimethyl carbinol and have multiplely, make catalyzer as modal useful sulfuric acid; Use the sulfonic acid solution compositing catalyst of 40～50wt% among the JP23524/72; Also available ferric sulfate or the muriatic solution compositing catalyst of antimony (JP7125/74) are made catalyzer (JP137906/75) or the like with acidic cation-exchange resin.Use inorganic acid solution to have many shortcomings as catalyzer, when utilizing lower concentration acid to reduce acid to the corrosion of device, catalyst activity has also reduced; When using high concentrated acid, not only produce etching problem, and increased side reaction, as olefinic polyreaction to device.When using hydrochloric acid or sulfate liquor to make catalyzer, remove metal ion wherein, can produce many problems, as removing heavy metal in the decontaminated water etc.
Utilize the Zeo-karb of band sulfonic acid group to be catalyzer, the process that iso-butylene and water react the continuous production trimethyl carbinol is in the public eye, and resin is the spherical particle that particle diameter is lower than 1.5mm.For example, Ind.Eng.Chem.vol.53.N, No.3, the isobutene conversion in this technological process that announce (1961) is very low, is approximately 30%.United States Patent (USP) 4180668 discloses the method that the trimethyl carbinol is produced in a kind of serialization, for and flow technology, employing be that (particle diameter is that 0.3～1.2mm) ion exchange resin is catalyzer to small-particle, and bed resistance is big, and flow direction of material is C
4Mix the back with water and flow enterprisingly to go out down, once pass through whole reactor, the reaction product concentration difference is little, and isobutene conversion only is 40～50%.In addition, the catalytic distillation production equipment is very strict to the filling substantive requirements of form of catalyzer, the most frequently used filling method is small-particle ion exchange resin ball shape particle to be wrapped in make sausage-like in the Stainless Steel Cloth at present, after coiling, in layer be placed in the catalytic distillation tower, obviously, this filling method takes a lot of work, time-consuming, be unfavorable for that also catalyzer changes.If this spherical catalyst particle is directly packed in the tower, tower inner catalyst Reynolds number is too little, bed resistance is big, can cause tower to stop up, and material can't proper flow, causes operation to carry out.
The object of the present invention is to provide a kind of iso-butylene hydration transformation efficiency and selectivity of increasing substantially, the material consumption that cuts down the consumption of energy be catalyzer with the Zeo-karb, carry out the method for iso-butylene and the water reaction continuous production trimethyl carbinol.
For realizing the object of the invention, the method for employing is:
With the strong acidic ion resin is catalyzer, and this resin particle size is that length, particle diameter have one at least greater than 2mm; Deionized water enters from reactor top, contains the C of iso-butylene
4Hydrocarbon stream enters from reactor lower part, and water and C are discharged in the trimethyl carbinol that reaction generates bottom from reactor after condensation
4Fraction add-on volume ratio is 6～8, and temperature of reaction is 90～98 ℃, and reaction pressure is 2.0～2.3MPa, and the reaction mass residence time is 0.5～2h.
The strong acidic ion resin catalyzer that relates among the present invention can be: styrene sulfonic acid type resin, Phenylsulfonic acid type resin etc., specific surface area is preferably 30～50m
2/ g, cation exchange capacity (CEC) is preferably 3.6～5.0mmolH
+/ g (dry catalyst) (analyzing) with chemical titration; The shape of catalyzer is not limited, as being column, wheel shape, corrugated plate shape or the like, the geometrical dimension of column is generally φ (2～8) * (3～8) mm, the corrugated plate shape depth of packing is general 0.8～2.5mm, and the beds voidage is preferably 30～60% (soaking the fluid-discharge therapy test).
Fig. 1 is iso-butylene of the present invention and water reaction continuous production trimethyl carbinol process flow diagram.1-hydration reactor among the figure; The 2-distillation tower; The 3-product storage tank.
Below in conjunction with accompanying drawing, technical process of the present invention is further described:
Deionized water is squeezed into reactor top through pump, contains the C of isobutene4Fraction is squeezed into reactor through pump The bottom. Both materials carry out reverse contact, and according to the density contrast of two kinds of materials, water is 1Kg/m3,C
4Be 0.54Kg/m3, under reaction temperature (90～98 ℃), water flows down from reactor top, light component C4Make progress away, material is discharged from reactor bottom after condensation through the tert-butyl alcohol that generates after the abundant exchange, and to produce concentration be 99.5% the tert-butyl alcohol through steaming dehydration of alcohols again, and water is used for circular response, tower top unreacted C4Discharge enters useless C4In the tank.
The mechanism of action of the present invention is:
1. at reactor bottom, C4The concentration of isobutene is very big in the fraction, in order to keep poised state, Isobutene can react with water very soon, produces the tert-butyl alcohol;
2. on reactor top, the concentration of iso-butylene is lower, but comparatively speaking, the concentration of water is but very big, and this moment, a large amount of water can generate the trimethyl carbinol with isobutene reaction again very soon.
Because reactant concn differs greatly in the reaction system, so the reaction impellent increases, speed of reaction improves, thereby improved reaction effect.This shows, no matter in the reactor upper and lower part, all there is bigger reaction impellent, molecular balance is moved to the resultant direction, impel building-up reactions to carry out as far as possible fully, so just improved reaction-ure conversion-age, also overcome backward reaction simultaneously, improve the hydration reaction effect, improved product production.
Since the catalyzer among the present invention adopts be the macrobead resin as catalyzer, the bed voidage of resin is big, bed resistance is little, helps the material countercurrent flow, the concentration of reactants difference is big in addition, the exchange of liquid liquid is more abundant, has improved transformation efficiency.Adopt adverse current hydrating process of the present invention, C
4Conversion for isobutene reaches 75～90% in the fraction, even higher, and and flow that conversion for isobutene only is 40～50% in the technology, the two is compared, the former isobutene conversion has improved 20～30 percentage points, and product cost is reduced significantly.
The invention will be further described below by embodiment.
In two sections fixed-bed reactor of 30L, adding geometrical dimension is φ 5 * 5mm column Phenylsulfonic acid type resin catalyst-catalyzer, and its specific surface area is 40m
2/ g, cation exchange capacity (CEC) is 4.5mmolH
+/ g (dry catalyst is analyzed with chemical titration), catalyzer loads with bulk form, and reaction pressure is 2.3Mpa, and residence time of material is 1 hour.Water, C
4Fraction is fed respectively by the reactor upper/lower terminal.Owing to there is big voidage (40%) between the catalyzer, and reaction raw materials proportion differs greatly, so the two can realize countercurrent flow in reactor.At water: C
4Be 6 (V/V), temperature of reaction is under 95～98 ℃ the condition, and reaction back conversion for isobutene can reach 92%, and iso-butylene content is below 0.5% in the tail gas.
In the reactor in embodiment 1, with bulk form loading vehicle colyliform φ 13.5 * 13.5mm * 3.5mm styrene sulfonic acid type resin catalyst, wherein specific surface area is 45m
2/ g, cation exchange capacity (CEC) is 4.5mmolH
+/ g (dry catalyst is analyzed with chemical titration), the voidage between the catalyzer is 48%, reaction pressure is 2.3MPa.Be under 94～96 ℃ the condition in temperature of reaction, water: C
4Be under the condition of 8 (V/V), water, C
4Fraction is fed respectively by the reactor upper/lower terminal, carries out counter current contact smoothly, and residence time of material is 1.5h.Reaction back conversion for isobutene can reach 95%, and iso-butylene content is below 0.5% in the tail gas.
In the fixed-bed reactor of 6L, filling corrugated plate shape styrene sulfonic acid type catalyzer, thickness is 1.4mm, specific surface area is 50m
2/ g, cation exchange capacity (CEC) is 3.9mmolH
+/ g (dry catalyst is analyzed with chemical titration), the voidage between the catalyzer is 50%, reaction pressure 2.0MPa, the residence time is 2h, temperature of reaction is 96～98 ℃, water: C
4Be 6 (V/V).Water and C
4Counter current contact, isobutene conversion are 90%.
Claims (4)
1. the method for a preparing tert-butanol from isobutylene by hydration is characterized in that with the strong acidic ion resin being catalyzer, and resin particle size is that length, particle diameter have one at least greater than 2mm; Deionized water enters from reactor top, contains the C of iso-butylene
4Enter from reactor lower part, water and C are discharged in the trimethyl carbinol that reaction generates bottom from reactor after condensation
4Fraction add-on volume ratio is 6～8, and temperature of reaction is 90～98 ℃, and reaction pressure is 2.0～2.3Mpa, and the reaction mass residence time is 0.5～2 hour.
2. method according to claim 1, the specific surface area that it is characterized in that strong acidic ion resin is 30～50m
2/ g, cation exchange capacity (CEC) is 3.6～5.0mmol H
+/ g.
3. method according to claim 1 is characterized in that strong acidic ion resin is a sulfonic resin.
4. method according to claim 1 is characterized in that the beds voidage is 30～60%.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 00129128 CN1108283C (en) | 2000-09-28 | 2000-09-28 | Process for preparing tert-butanol from isobutylene by hydration |
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| CN 00129128 CN1108283C (en) | 2000-09-28 | 2000-09-28 | Process for preparing tert-butanol from isobutylene by hydration |
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| CN1304917A true CN1304917A (en) | 2001-07-25 |
| CN1108283C CN1108283C (en) | 2003-05-14 |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100519498C (en) * | 2006-11-08 | 2009-07-29 | 褚雅志 | Phrcess of coproducing methyl tert-butyl ether and tert-butyl alcohol |
| CN101444752B (en) * | 2008-12-17 | 2010-08-25 | 凯瑞化工有限责任公司 | Catalytic resin produced by using polystyrene/SBS/waste white ball composite material and preparation method thereof |
| CN101124188B (en) * | 2004-12-17 | 2010-12-29 | 三菱丽阳株式会社 | Method for producing tertiary butyl alcohol |
| CN102229522A (en) * | 2011-04-28 | 2011-11-02 | 宁波尖锋紫星生物科技有限公司 | Method for preparing 1-chloro-2-methyl-2-propanol |
| CN101440018B (en) * | 2007-11-22 | 2012-05-30 | 中国石油化工股份有限公司 | Hydration reaction method for light olefins |
| WO2022089530A1 (en) | 2020-10-28 | 2022-05-05 | 中国石油化工股份有限公司 | Liquid-liquid mixer, liquid-liquid reaction apparatus comprising liquid-liquid mixer, and liquid-liquid reaction method using liquid-liquid mixer |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101423454B (en) * | 2007-11-01 | 2012-01-11 | 中国石油天然气股份有限公司 | Method for preparing tert-butanol by extraction of carbon 4 hydrocarbon containing isobutene |
| IN2014KN00748A (en) * | 2011-11-07 | 2015-10-02 | Mitsubishi Rayon Co |
-
2000
- 2000-09-28 CN CN 00129128 patent/CN1108283C/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101124188B (en) * | 2004-12-17 | 2010-12-29 | 三菱丽阳株式会社 | Method for producing tertiary butyl alcohol |
| CN100519498C (en) * | 2006-11-08 | 2009-07-29 | 褚雅志 | Phrcess of coproducing methyl tert-butyl ether and tert-butyl alcohol |
| CN101440018B (en) * | 2007-11-22 | 2012-05-30 | 中国石油化工股份有限公司 | Hydration reaction method for light olefins |
| CN101444752B (en) * | 2008-12-17 | 2010-08-25 | 凯瑞化工有限责任公司 | Catalytic resin produced by using polystyrene/SBS/waste white ball composite material and preparation method thereof |
| CN102229522A (en) * | 2011-04-28 | 2011-11-02 | 宁波尖锋紫星生物科技有限公司 | Method for preparing 1-chloro-2-methyl-2-propanol |
| CN102229522B (en) * | 2011-04-28 | 2013-12-04 | 宁波尖锋紫星生物科技有限公司 | Method for preparing 1-chloro-2-methyl-2-propanol |
| WO2022089530A1 (en) | 2020-10-28 | 2022-05-05 | 中国石油化工股份有限公司 | Liquid-liquid mixer, liquid-liquid reaction apparatus comprising liquid-liquid mixer, and liquid-liquid reaction method using liquid-liquid mixer |
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| CN1108283C (en) | 2003-05-14 |
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Granted publication date: 20030514 |