CN104478657B - Method for preparing tertiary butanol by using hydration of isobutene in mixed C4 - Google Patents
Method for preparing tertiary butanol by using hydration of isobutene in mixed C4 Download PDFInfo
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- CN104478657B CN104478657B CN201410670727.0A CN201410670727A CN104478657B CN 104478657 B CN104478657 B CN 104478657B CN 201410670727 A CN201410670727 A CN 201410670727A CN 104478657 B CN104478657 B CN 104478657B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/03—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2
- C07C29/04—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2 by hydration of carbon-to-carbon double bonds
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Abstract
The invention relates to the field of chemical industry and in particular relates to a method for preparing tertiary butanol by using hydration of isobutene in mixed C4. By adopting a catalytic distillation tower, the technical process is simplified, so that the equipment and operation costs can be reduced; the mixed C4 and deionized water enter the tower by using a reverse flowing manner; the concentration difference of the gas phase and the liquid phase is improved; the product tertiary butanol is continuously discharged out of the tower; the reaction is accelerated to progress in the positive direction; the reaction balance limit is broken, so that the conversion rate of isobutylene is increased. In addition, the deionized water is directly charged into the top of the tower and is used for sucking tertiary butanol in the residual gas; the conversion rate of isobutylene is increased; the top of the tower is free of reflux; the energy consumption is reduced; the reflux of the isobutene is avoided, so that the generation of by-products comprising polymers and C8 ether are reduced; the selectivity of isobutylene is improved; the reaction temperature is easy to control; the heat accumulation in a catalyst layer is avoided; the generation of the polymers is reduced; the selectivity of isobutylene is improved. The conversion rate of the isobutylene is greater than 90%; the selectivity is greater than 99%; the method is suitable for industrial production.
Description
Technical field
The present invention relates to chemical field, the method for preparing tert-butanol by isobutene hydration in more particularly, to a kind of mixing carbon four.
Background technology
The boiling point difference very little of isobutene and n-butene in mixing carbon four, with conventional distillating method by isobutene from carbon four
In separate uneconomical, generally carbon four is all directly burnt as fuel, causes the waste of resource.
Tert-butyl alcohol tool has been widely used, such as：Produce high-purity isobutylene, gasoline additive, methyl methacrylate etc.
Important chemical products.
One of existing isobutene hydration process be isobutene is mixed with the water containing surfactant or the tert-butyl alcohol after, with
The mode of cocurrent is reacted by the fixed bed being filled with strong-acid cation-exchange resin catalyst.This method is passed through to increase
Isobutene and the intersolubility of water, to improve isobutene conversion.
Patent CN1511815A discloses a kind of tert-butyl alcohol production method being made solvent by polyethers, will mix carbon four and water with
Surfactant mixing after, entered by fixed bed reactors top, go out reactor material enter catalytic distillation tower, isobutene and
Water continues to generate the tert-butyl alcohol, completes carbon four simultaneously and separates with tertiary butanol aqueous solution.The tertiary butanol aqueous solution that tower reactor obtains is sent into
Tert-butyl alcohol treating column, obtains the tert-butyl alcohol in tower top.The selectivity of the method is more than 99%, and conversion ratio is more than 90%.But, it adds
Enter solvent, increased cost, and bring difficulty to the separation of later stage solvent, increased energy consumption and cost of equipment.
Patent CN101293813B discloses by the method for the preparing tert-butanol by isobutene hydration in carbon four component, its emulsification
Agent structure is RC6H5O (CH2CH2O) nH, and wherein R is iso-octyl, new decyl or Permethyl 99A base.Carbon four with containing emulsifying agent
Hydration reactor top is sent into, water is added at middle part after forming water-in-oil emulsion after deionized water mixing.Emulsifying agent is not required to separate,
Directly return entrance together with water after ion exchange bed.But the cocurrent mode that it adopts is so that conversion ratio is restricted.
A kind of preparation method of the tert-butyl alcohol is disclosed in patent CN103804139A.The method is multiple solid using joining end to end
Fixed bed reactor, adds tertiary butanol aqueous solution in the first stage reactor, after mixing carbon four isobutene that adds of every stage reactor
Effective mass air speed is equal.Add the tert-butyl alcohol in the method raw material, increased cost, and control the isobutene matter of every grade of addition
Measure equal process more complicated and loaded down with trivial details.
One of existing isobutene hydration process is to combine reactor and rectifying column or extraction tower, goes into an equipment,
There is hydration reaction and rectifying or extractive reaction wherein simultaneously.In this method, water and C_4 hydrocarbon pass through catalysis in a counter-current configuration
Oxidant layer, water is taken away in time by reacting the tert-butyl alcohol generating, and so that isobutene is hydrated and carries out to positive direction, breaks through the limit of chemical balance
System, to improve isobutene conversion and selectivity.
A kind of utilization reactive distillation mode is disclosed by the C_4 hydrocarbon hydration preparation uncle containing isobutene in patent US4012456
The method of butanol.Stage casing filling is cast into the resin of structured packing shape, and tower top adds water, and the bottom of catalyst section adds carbon four
Hydrocarbon, the isobutene that C_4 hydrocarbon contains generates the tert-butyl alcohol in catalyst section hydration reaction.The tert-butyl alcohol is flowed to tower bottom with water, in tower
Kettle produces.Unreacted C_4 hydrocarbon rises, in the molten tert-butyl alcohol of rectifying section removing, in overhead extraction.Produce in reaction rectification method
The thing tert-butyl alcohol is taken away by the water in time, reacts and carries out to positive direction, so that the conversion ratio of isobutene is greatly enhanced, reaches 90
～99%.But, in the method, catalyst first passes through casting in advance and processes, and increased cost, and water enters from tower top, catalyst section
Temperature is wayward, and overhead reflux, easily generates accessory substance, and technological process is more complicated.
A kind of method by the C_4 hydrocarbon reaction, extraction preparing tert-butanol containing isobutene is disclosed in patent CN101423454B.
In the method, reactor is combined with extraction tower in same equipment, reactant enters catalysis in a counter-current fashion through external heat-exchanging
Extraction tower, the tert-butyl alcohol carried secretly in C_4 hydrocarbon is extracted by the above water of catalyst layer, flows to bottom of towe together through catalyst layer,
Continuously produce from tower reactor.In this method, water hydrocarbon ratio is bigger, and concentration difference is bigger, and the bigger reaction power of motive force is bigger.So,
In the method, than greatly, water consumption is big for water hydrocarbon, and the amount of liquid of tower reactor extraction is big.And catalyst has filler effect concurrently in the method,
Large usage quantity.
Content of the invention
It is an object of the invention to provide a kind of method mixing preparing tert-butanol by isobutene hydration in carbon four, catalyst use
Measure less, load easily, water consumption is little, temperature is easier to control, the conversion ratio of isobutene is high with selective.
In order to achieve the above object, the technical scheme is that and be achieved in that：
In a kind of mixing carbon four, the method for preparing tert-butanol by isobutene hydration, comprises the steps：
Liquid is mixed carbon four be passed into catalytic distillation tower bottom of towe and be heated to uniform temperature gasification；
In mixing carbon four uphill process after gasification, the generation tert-butyl alcohol is reacted by the water of catalyst and catalyst upper strata；
The tert-butyl alcohol being blended in mixing carbon four after the water of catalytic distillation tower top of tower will react absorbs.
Preferably, catalyst is large hole cation exchanger resin.
Preferably, a diameter of the 0.45～1.25 of large hole cation exchanger resin, water content is 40～50%, functional group
>=3.10 [H+], maximum operating temperature is 180 DEG C.
Preferably, propylene, iso-butane, normal butane, anti-butylene, n-butene, isobutene, maleic are contained in mixing carbon four；
Isobutene content scope is 10～40%.
Preferably, the temperature of catalytic distillation tower bottom of towe is 80-180 DEG C.
Preferably, the temperature of catalyst lower floor is 75-95 DEG C；Catalyst upper strata is 1-10 with the temperature difference of catalyst lower floor
℃；In mixing carbon four, isobutene is 0.1～2.0Mpa by the pressure that catalyst is reacted with water.
Preferably, mixing carbon four and the mass ratio of total Water are 1: 0.1-2.0.
Preferably, the water used by the method is deionized water；Deionized water is heated to 60-100 DEG C.
A kind of device preparing the tert-butyl alcohol using said method, including catalytic distillation tower；Catalytic distillation tower include from down to
On the bottom of towe, filler lower floor, catalyst layer, filler upper strata and the tower top that set gradually；Bottom of towe is provided with charging aperture and discharge outlet；Tower
Bottom is provided with reboiler；Reboiler is connected with charging aperture and filler lower floor；The upper end of catalyst layer is provided with the first water inlet；Tower
Top is provided with the second water inlet and exhaust outlet.
Preferably, filler lower floor and filler upper strata are filled with the θ ring filler of a diameter of 3mm；The number of theoretical plate on filler upper strata
For 10-50；The number of theoretical plate of catalyst lower floor is 5-70.
Compared with prior art, this have the advantage that：Under reaction pressure, using mixing carbon four feed pump
To catalytic distillation tower bottom of towe press-in liquid mixing carbon four.Liquid mixing carbon four is heated to uniform temperature gasification through tower bottom reboiler,
Self-catalysis distillation tower bottom rises.In catalyst layer, isobutene in the mixing carbon four of rising gradually with top-down go from
The reaction of sub- water generates the tert-butyl alcohol, and the reacted mixing carbon four gas fraction tert-butyl alcohol of carrying under one's arms continues to rise, the tert-butyl alcohol therein
Absorbed by the deionized water under tower top on filler upper strata.Finally remaining mixing carbon four gas is excluded by tower top, residual gas
Comprise only a small amount of isobutene in body and do not contain the tert-butyl alcohol.
The present invention adopts catalytic distillation tower and the method, simplifies technological process, reduces equipment and operating cost.Mixing
Carbon four and deionized water enter tower using reverse flow mode, improve gas-liquid two-phase concentration difference, and the product tert-butyl alcohol continuously goes out tower,
Promote reaction to carry out to positive direction, break through reaction balance and limit, thus improving isobutene conversion.In addition, tower top of the present invention is straight
Connect deionized water in order to absorb the tert-butyl alcohol in residual gas, improve isobutene conversion.
Tower top of the present invention no flows back, and reduces energy consumption.And because of no isobutene backflow, thus decreasing by-product polymer
With the generation of carbon eight ether, improve selective isobutene.
Water inlet in the middle part of catalytic distillation tower of the present invention, it is easy to controlling reaction temperature, prevents heat from assembling in catalyst layer, reduces
The generation of polymer, improves selective isobutene.
Catalyst packing of the present invention is simple to operate, and catalyst amount is few, is not required to tie up, and is not required to cast, low cost.
Be not required to add surfactant in present invention mixing carbon four raw material, reduce cost, the later stage separate simple, energy consumption and
Operating cost is low.
Isobutene conversion of the present invention more than 90%, selectively more than 99%, suitable industrialized production.
Brief description
Fig. 1 is the structural representation of catalytic distillation tower provided in an embodiment of the present invention.
Specific embodiment
Below with reference to accompanying drawing, clear, complete description is carried out it is clear that being retouched to the technical scheme of various embodiments of the present invention
The embodiment stated is only a part of embodiment of the present invention, rather than whole embodiments.Based on the embodiment in the present invention,
The obtained all other embodiment on the premise of not making creative work of those of ordinary skill in the art, broadly falls into this
Invent protected scope.
Embodiment 1
Mixing carbon four is with air speed 0.20h-1, and enters catalytic distillation tower with total Water with 1: 0.6 mass ratio.Mixing carbon four
Raw material composition is shown in Table 1.In catalytic distillation tower, the number of theoretical plate of filler lower floor is 20；Catalyst section divides 4 sections, and filling 25g urges respectively
Agent；The number of theoretical plate on filler upper strata is 35, operating pressure 0.8Mpa, 125 DEG C of column bottom temperature, 78 DEG C of catalyst lower floor temperature,
74 DEG C of catalyst upper strata temperature, 75 DEG C of deionized water feeding temperature.Isobutene conversion reaches 95.2%, selectively reaches
99.7%, the not aqueous and tert-butyl alcohol in residual gas.
Table 1
| Raw material components | Wt% |
| Propylene | 1.356 |
| Iso-butane | 1.197 |
| Normal butane | 1.955 |
| Trans-2-butene | 22.741 |
| N-butene | 36.430 |
| Isobutene | 24.414 |
| Cis-2-butene | 11.907 |
Embodiment 2
Mixing carbon four is with air speed 0.60h-1, and enters catalytic distillation tower with total Water with 1: 1.1 mass ratio.Mixing carbon four
Raw material forms with table 1.In catalytic distillation tower, the number of theoretical plate of filler lower floor is 20；Catalyst section divides 5 sections, and filling 50g urges respectively
Agent；The number of theoretical plate on filler upper strata is 15, operating pressure 1.3Mpa, 140 DEG C of column bottom temperature, 81 DEG C of catalyst lower floor temperature,
76 DEG C of catalyst upper strata temperature, 77 DEG C of deionized water feeding temperature.Isobutene conversion reaches 96.5%, selectively reaches
99.6%, the not aqueous and tert-butyl alcohol in residual gas.
Embodiment 3
Mixing carbon four is with air speed 0.15h-1, and enters catalytic distillation tower with total Water with 1: 0.6 mass ratio.Mixing carbon four
Raw material composition is shown in Table 2.In catalytic distillation tower, the number of theoretical plate of filler lower floor is 65；Catalyst section divides 3 sections, and filling 50g urges respectively
Agent；The number of theoretical plate on filler upper strata is 45, operating pressure 1.3Mpa, 140 DEG C of column bottom temperature, 81 DEG C of catalyst lower floor temperature,
82 DEG C of catalyst upper strata temperature, 83 DEG C of deionized water feeding temperature.Isobutene conversion reaches 94.5%, selectively reaches
99.9%, the not aqueous and tert-butyl alcohol in residual gas.
Table 2
| Raw material components | Wt% |
| Propylene | 0.918 |
| Iso-butane | 1.546 |
| Normal butane | 3.257 |
| Trans-2-butene | 18.756 |
| N-butene | 20.746 |
| Isobutene | 33.567 |
| Cis-2-butene | 21.210 |
Embodiment 4
Mixing carbon four is with air speed 0.55h-1, and enters catalytic distillation tower with total Water with 1: 1.1 mass ratio.Mixing carbon four
Raw material composition is shown in Table 2.In catalytic distillation tower, the number of theoretical plate of filler lower floor is 50；Catalyst section divides 6 sections, and filling 35g urges respectively
Agent；The number of theoretical plate on filler upper strata is 45, operating pressure 0.8Mpa, 120 DEG C of column bottom temperature, 77 DEG C of catalyst lower floor temperature,
74 DEG C of catalyst upper strata temperature, 75 DEG C of deionized water feeding temperature.Isobutene conversion reaches 91.5%, selectively reaches
99.7%, the not aqueous and tert-butyl alcohol in residual gas.
Embodiment 5
The embodiment of the present invention provides a kind of device preparing the tert-butyl alcohol using said method, as shown in figure 1, include catalysis steaming
Evaporate tower；Bottom of towe 104 that catalytic distillation tower includes setting gradually from bottom to up, filler lower floor 105, catalyst layer 106, filler upper strata
107 and tower top；Bottom of towe 104 is provided with charging aperture 102 and discharge outlet 103；Bottom of towe 104 is provided with reboiler；Reboiler and charging
Mouth 102 and filler lower floor 105 connect；The upper end of catalyst layer 106 is provided with the first water inlet 114；Tower top is provided with second and enters
The mouth of a river 109 and exhaust outlet 108.
Under reaction pressure, using mixing carbon four feed pump 101 to catalytic distillation tower bottom of towe 104 press-in liquid mixing carbon
Four.The liquid mixing reboiler through bottom of towe 104 for the carbon four is heated to uniform temperature gasification, and the bottom of self-catalysis destilling tower rises.?
Catalyst layer 106, the isobutene in the mixing carbon four of rising gradually reacts the generation tert-butyl alcohol, instead with top-down deionized water
Should after mixing carbon four gas carry under one's arms the fraction tert-butyl alcohol continue rise, the tert-butyl alcohol therein is on filler upper strata 107 by from tower top
And under deionized water water absorb.Finally remaining mixing carbon four gas is discharged by the exhaust outlet 108 of tower top, in residual gas only
Containing a small amount of isobutene and without the tert-butyl alcohol.
Under reaction pressure, it is passed through to the superiors of catalyst layer 106 with water feed pump 112 in the middle part of tower and is heated to a constant temperature
The deionized water of degree, wherein deionized water heats through water feed exchanger 113 in the middle part of tower.Deionized water after being heated is along catalyst
Layer 106 decline, the gradually work with the catalyst in sulfonic acid cation exchange resin for the isobutene in the mixing carbon four of bottom of towe
With the lower generation tert-butyl alcohol.The product tert-butyl alcohol of generation is taken away and is flowed to bottom of towe together, by discharge outlet 103 row of bottom of towe by excessive water
Go out.
Under reaction pressure, the deionized water being heated to uniform temperature is via overhead water feed pump 111 self-catalysis destilling tower
Top enter, wherein deionized water heats through top of tower water feed exchanger 110.The mistake flowing downward on filler upper strata 107
Cheng Zhong, absorbs the tert-butyl alcohol carried under one's arms in ascending air.The deionized water absorbing the tert-butyl alcohol continues to flow downward, in catalyst layer
106 generate the tert-butyl alcohol with the isobutene reaction in mixing carbon four from bottom to top.Excessive deionized water is flowed together with the tert-butyl alcohol
To bottom of towe, discharged by the discharge outlet 103 of bottom of towe.
Preferably, filler lower floor and filler upper strata are filled with the θ ring filler of a diameter of 3mm；The number of theoretical plate on filler upper strata
For 10-50；The number of theoretical plate of catalyst lower floor is 5-70.
The above, be only presently preferred embodiments of the present invention, not the present invention is made with any pro forma restriction, appoints
What those skilled in the art, in the range of without departing from technical solution of the present invention, when in the technology of available the disclosure above
Hold and make a little Equivalent embodiments changing or be modified to equivalent variations, as long as being the content without departing from technical solution of the present invention,
Any simple modification, equivalent variations and modification above example made according to the technical spirit of the present invention, all still falls within this
In the range of inventive technique scheme.
Claims (4)
1. a kind of method mixing preparing tert-butanol by isobutene hydration in carbon four is it is characterised in that comprise the steps：
Liquid is mixed carbon four be passed into catalytic distillation tower bottom of towe and be heated to uniform temperature gasification；
In mixing carbon four uphill process after gasification, the generation tert-butyl alcohol is reacted by the water of catalyst and catalyst upper strata；By urging
The water changing overhead portion will be blended in the tert-butyl alcohol absorption in mixing carbon four after reacting；Described catalyst is macroporous cation
Exchanger resin；A diameter of the 0.45～1.25 of described large hole cation exchanger resin, water content is 40～50%, functional group >=
3.10[H+], maximum operating temperature is 180 DEG C；Water used by the method is deionized water；Described deionized water is heated to 60-
100℃；Propylene, iso-butane, normal butane, anti-butylene, n-butene, isobutene, maleic is contained in described mixing carbon four；Described different
Butene content scope is 10～40%.
2. the method for claim 1 is it is characterised in that the temperature of described catalytic distillation tower bottom of towe is 80-180 DEG C.
3. the method for claim 1 is it is characterised in that the temperature of described catalyst lower floor is 75-95 DEG C；Described catalysis
Agent upper strata is 1-10 DEG C with the temperature difference of described catalyst lower floor；In described mixing carbon four, isobutene is reacted with water by catalyst
Pressure be 0.1～2.0Mpa.
4. the method for claim 1 is it is characterised in that described mixing carbon four is 1: 0.1- with the mass ratio of total Water
2.0.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1176957A (en) * | 1996-06-27 | 1998-03-25 | 中国石化齐鲁石油化工公司 | Method for preparing tert-butyl alcohol from isobutene in mixed C4 or extracted C4 |
| CN1511814A (en) * | 2002-12-31 | 2004-07-14 | 中国石化集团齐鲁石油化工公司 | Process for preparing tertiary butanol |
| CN1511815A (en) * | 2002-12-31 | 2004-07-14 | 中国石化集团齐鲁石油化工公司 | Process for preparing tertiary butanol |
-
2014
- 2014-11-20 CN CN201410670727.0A patent/CN104478657B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1176957A (en) * | 1996-06-27 | 1998-03-25 | 中国石化齐鲁石油化工公司 | Method for preparing tert-butyl alcohol from isobutene in mixed C4 or extracted C4 |
| CN1511814A (en) * | 2002-12-31 | 2004-07-14 | 中国石化集团齐鲁石油化工公司 | Process for preparing tertiary butanol |
| CN1511815A (en) * | 2002-12-31 | 2004-07-14 | 中国石化集团齐鲁石油化工公司 | Process for preparing tertiary butanol |
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