CN1247502C - Method for continuously producing lower alcohol from low carbon olefines - Google Patents
Method for continuously producing lower alcohol from low carbon olefines Download PDFInfo
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- CN1247502C CN1247502C CN 200410001112 CN200410001112A CN1247502C CN 1247502 C CN1247502 C CN 1247502C CN 200410001112 CN200410001112 CN 200410001112 CN 200410001112 A CN200410001112 A CN 200410001112A CN 1247502 C CN1247502 C CN 1247502C
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- 238000000034 method Methods 0.000 title claims abstract description 34
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 24
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title 1
- 238000006243 chemical reaction Methods 0.000 claims abstract description 48
- 239000003054 catalyst Substances 0.000 claims abstract description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 238000006703 hydration reaction Methods 0.000 claims abstract description 26
- 230000036571 hydration Effects 0.000 claims abstract description 20
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000003729 cation exchange resin Substances 0.000 claims abstract description 18
- 125000004432 carbon atom Chemical group C* 0.000 claims abstract description 8
- 239000002994 raw material Substances 0.000 claims abstract description 7
- 239000008367 deionised water Substances 0.000 claims abstract description 6
- 229910021641 deionized water Inorganic materials 0.000 claims abstract description 6
- 230000003197 catalytic effect Effects 0.000 claims abstract description 5
- 150000001336 alkenes Chemical class 0.000 claims description 8
- 230000000694 effects Effects 0.000 claims description 7
- 238000010924 continuous production Methods 0.000 claims description 5
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 claims description 3
- 229920001577 copolymer Polymers 0.000 claims description 3
- MYRTYDVEIRVNKP-UHFFFAOYSA-N divinylbenzene Substances C=CC1=CC=CC=C1C=C MYRTYDVEIRVNKP-UHFFFAOYSA-N 0.000 claims description 3
- 238000007781 pre-processing Methods 0.000 abstract description 4
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 3
- 238000012545 processing Methods 0.000 abstract description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 15
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 14
- BTANRVKWQNVYAZ-UHFFFAOYSA-N butan-2-ol Chemical compound CCC(C)O BTANRVKWQNVYAZ-UHFFFAOYSA-N 0.000 description 12
- 239000012071 phase Substances 0.000 description 11
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 9
- 238000002203 pretreatment Methods 0.000 description 9
- 239000007788 liquid Substances 0.000 description 7
- 238000012360 testing method Methods 0.000 description 7
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 6
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 5
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- 230000007306 turnover Effects 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- 230000005587 bubbling Effects 0.000 description 3
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 3
- 229910052736 halogen Inorganic materials 0.000 description 3
- 150000002367 halogens Chemical class 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 150000002500 ions Chemical class 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 125000000542 sulfonic acid group Chemical group 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 description 2
- 239000001273 butane Substances 0.000 description 2
- 239000012295 chemical reaction liquid Substances 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 125000005843 halogen group Chemical group 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000012263 liquid product Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- HHBZZTKMMLDNDN-UHFFFAOYSA-N 2-butan-2-yloxybutane Chemical compound CCC(C)OC(C)CC HHBZZTKMMLDNDN-UHFFFAOYSA-N 0.000 description 1
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- ZAFNJMIOTHYJRJ-UHFFFAOYSA-N Diisopropyl ether Chemical compound CC(C)OC(C)C ZAFNJMIOTHYJRJ-UHFFFAOYSA-N 0.000 description 1
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000008346 aqueous phase Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 1
- 229910052794 bromium Inorganic materials 0.000 description 1
- PCWZHTGDXLRULT-UHFFFAOYSA-N buta-1,3-dienylbenzene styrene Chemical compound C(=C)C=CC1=CC=CC=C1.C=CC1=CC=CC=C1 PCWZHTGDXLRULT-UHFFFAOYSA-N 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- -1 sulfonate ion Chemical class 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The present invention relates to a method for continuously producing lower alcohol with 2 to 5 carbon atoms. The method comprises: reaction temperature is from 100 to 300 DEG C, and reaction pressure is from 4.0 to 20.0MPa. Under the action of cation exchange resin catalysts, low-carbon olefin with 2 to 5 carbon atoms is processed by catalytic hydration so as to prepare low-carbon alcohol. The present invention is characterized in that the catalyst used in reaction processes is preprocessed, the present invention has the preprocessing conditions that hydration raw materials of the low-carbon olefin and deionized water are directly used for processing the catalyst under the conditions of 150 to 180 DEG C of reaction temperature, 1.0 to 4.0MPa of pressure and 50 to 100 of water-olefin molar ratio, and preprocessing time is from 50 to 120 hours.
Description
Technical field
The present invention relates to a kind of continuous production and contain the method for the lower alcohol of 2 to 5 carbon atoms, improve catalyzer mechanical stability and reactive behavior stability by a kind of simple catalyst preconditioning process, say it is pre-treatment accurately cation exchange resin catalyst.
Background technology
The low-carbon alkene direct hydration technology that with the Zeo-karb is catalyzer be with raw material olefin with after reaction process water mixes, be preheated to 100～200 ℃ and enter the direct hydration catalyticreactor and react, reaction pressure is 4.0～20.0MPa.Several sections beds are set in the reactor, and reactant is by each section of catalyzer bed in the catalyticreactor, and the reaction product of generation is separated after being derived reactor.Aqueous phase also contains the various ions and the impurity that produce in the reaction process except that containing trace alcohol, cause disadvantageous effect in order to prevent various ions and impurity to the corrosion of equipment or to reaction, needs through purifying treatment before process water loops back reactor.
Under the cation exchange resin catalyst effect, low-carbon alkene can generate corresponding low-carbon alcohol by acid catalyzed effect.Because low-carbon alkene and water dissolve each other hardly, therefore reaction is to carry out under three-phase (solid catalyst phase, liquid phase water gas phase, low-carbon alkene phase) condition.
The catalyzer that reaction is used is the heatproof strong-acid ion exchange resin of modification, and the characteristics of this catalyzer are that space-time yield height, the corrosion of reactive behavior height, catalyzer is little, pollution is light.
The reaction process that various hydration reaction processes adopt in the industrial production because the reaction process the when low-carbon alkene that contains 2 to 5 carbon atoms carries out hydration and mechanism do not coexist is different.For example the butylene direct hydration adopts, and what be that bubbling style three-phase fixed-bed reactor third rare direct hydration then adopts is the three phase trickle flow bed.But the problem that exists in its reaction process and the industrial production is similar substantially.
In catalyzing cation exchange resin propylene direct hydration process, propylene and water enter catalyticreactor through after the preheating, hydration reaction takes place form Virahol.Be reflected at gas phase or liquid phase and carry out, reaction pressure 25～250bar, 120～200 ℃ of temperature of reaction.The catalyzer of canonical process is a cation exchange resin catalyst, and the per pass conversion of propylene direct hydration reaction propylene is at 60～70mol%.
The propylene hydration reaction product is sent into water wash column, and unreacted propylene loops back reactor after separating with Virahol.Anhydrous isopropyl alcohol then separates aqueous Virahol with water through 3～6 distillation towers with a small amount of other weight component if desired.General benzene, diisopropyl ether or the C of adopting
6Alkane is made the entrainment reagent of water in sepn process.
In cation exchange resin catalyst catalysis n-butene direct hydration process, butylene and water enter catalyticreactor through after the preheating, hydration reaction takes place generate sec-butyl alcohol, reaction pressure 25～250bar, 150～200 ℃ of temperature of reaction.The catalyzer of canonical process is a Zeo-karb, and the per pass conversion of the n-butene of gas, liquid reaction is at 6～7mol%.
Resultant of reaction is flowed through from reactor head and is divided behind the heat exchanger water-yielding stratum to enter the liquid liquid separator to take off C
4Tower, water loop back reactive system after treatment.Take off C
4Cat head distilled butylene-butane cut major part is circulated back to reactive system, and the small part discharging is to avoid the accumulation of inertia butane.The crude secbutyl alcohol that the tower still obtains contains a small amount of C
4Impurity such as hydrocarbon, di-secondary butyl ether, not moisture substantially.The purification system of the crude secbutyl alcohol distillation system with the indirect hydration method of sulfuric acid basically is identical, and the purity of the back sec-butyl alcohol of purifying can reach 99.9%.
In the aforesaid method with other method together in US Patent specification 4,579, obtain in 984 and 4,456,776 describing.These methods are applied in the production of the sec-butyl alcohol (SBA) and the trimethyl carbinol (TBA) especially at Virahol (IPA).
Owing to the catalytic active center that with vinylbenzene-Vinylstyrene is the cation exchange resin catalyst of matrix is a sulfonic acid group, height along with temperature of reaction, the turnover rate of sulfonic acid group increases gradually, and the general use temperature of common cation exchange resin catalyst is no more than 120 ℃.For thermostability and the use temperature that improves cation exchange resin catalyst, with halogen group as: fluorine or chlorine or bromine are introduced on the phenyl ring of Zeo-karb and improve the thermally-stabilised of cation exchange resin catalyst, the use temperature of practicalization can reach more than 170 ℃, relatively is fit to low-carbon alkene such as C
2～C
5The direct hydration of alkene.But this catalyzer in use still has the loss of sulfonic acid group, particularly because the introduction of halogen group, sulfonate ion has stronger corrodibility to equipment under the effect of halogen, and has seriously influenced the mechanical stability of catalyzer and the stability of reactive behavior.
In Chinese patent 86012001, proposed to carry out under a kind of new condition that is used for low-carbon alkene direct hydration resin, be attached to the halogen and the azochlorosulfonate acid ion of catalyst surface by release, reduce catalyzer in use corrodibility and also handle after the catalyzer stable mechanical performance, in the work-ing life that can reduce equipment corrosion and improve catalyzer, the treatment time of general catalyzer is 360 hours.But this method exists the treatment time to grow, need with aqueous solution of alcohol, can not use the shortcoming of hardware need with equipment such as non-metallic containers.
Summary of the invention
The objective of the invention is to propose a kind of new catalyst preconditioning process, make the strong acid cation exchange resin catalyst of vinylbenzene/divinyl benzene copolymer system pass through simply, handle fast, improve the mechanical stability of catalyzer and the stability of reactive behavior.And preprocessing process is to finish in reactor, and the processing raw material of use is exactly the used raw material of low-carbon alkene direct hydration.
Method of the present invention is the method that a kind of continuous production contains the lower alcohol of 2 to 5 carbon atoms, be 100～200 ℃ of temperature of reaction, reaction pressure 4.0～20.0MPa, under the effect of cation exchange resin catalyst, the low-carbon alkene catalytic hydration that will contain 2 to 5 carbon atoms becomes low-carbon alcohol, it is characterized in that catalyzer is carried out pre-treatment, directly use hydration raw material low-carbon alkene and water 150～180 ℃ of temperature of reaction, pressure 2.0～4.0MPa, water alkene mol ratio is under 50～100 the condition catalyzer to be handled, and is 100～120 hours at pretreatment time.The catalytic activity that the loss speed of sulfonic acid and halogen obviously reduces and maintenance is more stable when pretreated like this catalyzer is used for the low-carbon alkene direct hydration process.
In above-mentioned method, treating processes can for example be carried out in the fixed-bed reactor at reactor, and catalyst system therefor can be used the Zeo-karb of vinylbenzene/divinylbenzene copolymer system.
Therefore, the present invention is simple, the easy row that becomes with a kind of preprocessing process more economical, that more efficient methods makes low-carbon alkene carry out hydration reaction process catalyzer.Before the reaction of low-carbon alkene direct hydration, adopt reaction raw materials that catalyzer is carried out pre-treatment according to the present invention, can reduce of the corrosion of reacted effluent, and keep the machinery and the active stability of reaction process equipment.
Description of drawings
Fig. 1 is a propylene direct hydration preparing isopropanol schematic flow sheet.
Fig. 2 is the catalyst pretreatment schematic flow sheet.
Embodiment
Below by embodiment the present invention is described.
Embodiment 1
The pre-treatment of catalyzer is at a Φ
InThe pipe reactor of 28 * 300mm list carries out, and adopts three-phase bubbling bed pretreatment catalyst, and the catalyst pretreatment schematic flow sheet is seen Fig. 2.Filling 100 milliliters of cation exchange resin catalysts (chemical plant in the Ji, Cangzhou, the trade mark are the D008 commercial catalyst) in the reactor in the pretreater.The charging density of propylene is: 95.5m%, reaction water is deionized water (specific conductivity is ∠ 5 μ s/cm).Treatment condition are: pressure 1.5MPa, and 155 ℃ of treatment temps, propylene liquid charging air speed is 0.03h
-1, reaction water alkene mol ratio is 80, pretreatment time is 72 hours.
Embodiment 2
At internal diameter is in the Glass tubing of Φ 10, pack into and be respectively charged into 8 altogether of catalyzer 3ml catalyst samples unprocessed and that handled through embodiment 1, the 6ml water of packing in each catalyzer sample bottle, tube sealing is placed in the autoclave of water, strengthens the heatproof test under 200 ℃.After between static test and appraisal are measured respectively, measure its exchanging equivalent and calculate the sulfonic acid turnover rate.
Table 2
| Treatment time, hour | 16 | 32 | 48 | 64 |
| The sulfonic acid turnover rate, % | ||||
| Catalyzer is untreated | 20 | 28 | 36 | 41 |
| The pre-treatment rear catalyst | 8 | 12 | 14 | 15 |
Embodiment 3
Implement test and carry out in the reactor identical with Comparative Examples 1, the cation exchange resin catalyst that loads in the reactor is the catalyzer after handling through embodiment 1.Reaction conditions and analytical procedure are with Comparative Examples 1.
Table 3
| Runtime, hour | Initially | 250 | 500 | 750 | 1000 |
| Propylene conversion, % | 66.53 | 63.23 | 62.18 | 61.89 | 60.99 |
Embodiment 4
The pre-treatment of catalyzer is at a Φ
InThe pipe reactor of 28 * 300mm list carries out, and adopts three-phase bubbling bed pretreatment catalyst, and the catalyst pretreatment schematic flow sheet is seen Fig. 2.Filling 100 milliliters of cation exchange resin catalysts (chemical plant in the Ji, Cangzhou, the trade mark are the D008 commercial catalyst) in the reactor in the pretreater.Charging mixed butene concentration is: 78.2m%, reaction water is deionized water (specific conductivity is ∠ 5 μ s/cm).Treatment condition are: pressure 1.5MPa, and 165 ℃ of treatment temps, butylene liquid feeding air speed is 0.03h
-1, treating processes water alkene mol ratio is 40, pretreatment time is 96 hours.
Embodiment 5
At internal diameter is in the Glass tubing of Φ 10, pack into and be respectively charged into 8 altogether of catalyzer 3ml catalyst samples unprocessed and that handled through embodiment 1, the 6ml water of packing in each catalyzer sample bottle, tube sealing is placed in the autoclave of water, strengthens the heatproof test under 200 ℃.After between static test and appraisal are measured respectively, measure its exchanging equivalent and calculate the sulfonic acid turnover rate.
Table 4
| Treatment time, hour | 16 | 32 | 48 | 64 |
| The sulfonic acid turnover rate, % | ||||
| Catalyzer is untreated | 30 | 36 | 41 | 50 |
| The pre-treatment rear catalyst | 12 | 15 | 17 | 18 |
Comparative Examples 1
This simultaneous test is at a Φ
InThe pipe reactor of 28 * 300mm list carries out, and adopts the trickle bed feeding manner, filling 100 milliliters of cation exchange resin catalysts (chemical plant in the Ji, Cangzhou, the trade mark are the D008 commercial catalyst) in the reactor.The reaction process synoptic diagram is shown in figure one.The charging density of propylene is: 95.5m%, reaction water is deionized water (specific conductivity is ∠ 5 μ s/cm).Reaction conditions: pressure 8.0MPa, 135 ℃ of temperature of reaction, propylene liquid charging air speed is 0.3h
-1, reaction water alkene mol ratio is 15, continuous operation 1000 hours.Reacted product discharges unreacted propylene gas by decompression separation, collects reaction liquid phase product analysis gas, liquid product composition and obtains the propylene molar yield.
Table 1
| Runtime, hour | Initially | 250 | 500 | 750 | 1000 |
| Propylene conversion, % | 70.55 | 68.03 | 60.18 | 56.39 | 48.67 |
Embodiment 6
Implement test and carry out in the reactor identical with Comparative Examples 1, the cation exchange resin catalyst that loads in the reactor is respectively the catalyzer after handling through embodiment 5.Charging mixed butene concentration is: 78.2m%, reaction water is deionized water (specific conductivity is ∠ 5 μ s/cm).Reaction conditions is: pressure 7.8MPa, and 155 ℃ of temperature of reaction, butylene liquid feeding air speed is 0.8h
-1, reaction water alkene mol ratio is 3.0, continuous operation 1000 hours.Reacted product discharges unreacted butylene gas by decompression separation, collects reaction liquid phase product analysis gas, liquid product composition and obtains the butylene molar yield.
Table 5
| Runtime, hour | Initially | 250 | 500 | 750 |
| Butene conversion, mol% | ||||
| The catalyzer that is untreated, | 7.63 | 6.32 | 5.78 | 5.16 |
| The pre-treatment rear catalyst | 6.42 | 6.37 | 6.28 | 6.19 |
By the result of the foregoing description and Comparative Examples as can be known, in reaction,, activity of such catalysts is stablized as long as catalyzer is carried out pre-treatment by condition of the present invention by low-carbon alkene continuous production lower alcohol.
Claims (4)
1, a kind of continuous production contains the method for the lower alcohol of 2 to 5 carbon atoms, be 100～200 ℃ of temperature of reaction, reaction pressure 4.0～20.0MPa, under the effect of cation exchange resin catalyst, the low-carbon alkene catalytic hydration that will contain 2 to 5 carbon atoms becomes low-carbon alcohol, the catalyzer that it is characterized in that reacting use is through pretreated, pretreatment condition is directly to use hydration raw material low-carbon alkene and deionized water 150～180 ℃ of temperature of reaction, pressure 1.0～4.0MPa, water alkene mol ratio is under 50～100 the condition catalyzer to be handled, and pretreatment time is 50～120 hours.
2,, it is characterized in that treating processes carries out in reactor according to the method for claim 1.
3,, it is characterized in that described reactor is fixed-bed reactor according to the method for claim 2.
4,, it is characterized in that catalyzer is the Zeo-karb of vinylbenzene/divinylbenzene copolymer system according to the method for claim 1.
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| CN 200410001112 CN1247502C (en) | 2004-01-19 | 2004-01-19 | Method for continuously producing lower alcohol from low carbon olefines |
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| CN 200410001112 CN1247502C (en) | 2004-01-19 | 2004-01-19 | Method for continuously producing lower alcohol from low carbon olefines |
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| 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 |
| CN116063152A (en) * | 2023-03-01 | 2023-05-05 | 山东京博石油化工有限公司 | Method for preparing alcohol from light gasoline |
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Assignee: ZHEJIANG XINHUA CHEMICAL Co.,Ltd. Assignor: Dalian Institute of Chemical Physics, Chinese Academy of Sciences Contract record no.: 2011330001362 Denomination of invention: Method for continuously producing lower alcohol from low carbon olefines Granted publication date: 20060329 License type: Common License Open date: 20050803 Record date: 20111111 |
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Granted publication date: 20060329 |
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