CN1247503C - Method for continuously producing lower alcohol - Google Patents
Method for continuously producing lower alcohol Download PDFInfo
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- CN1247503C CN1247503C CN 200410001113 CN200410001113A CN1247503C CN 1247503 C CN1247503 C CN 1247503C CN 200410001113 CN200410001113 CN 200410001113 CN 200410001113 A CN200410001113 A CN 200410001113A CN 1247503 C CN1247503 C CN 1247503C
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- 238000000034 method Methods 0.000 title claims abstract description 39
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 57
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 36
- 239000003054 catalyst Substances 0.000 claims abstract description 21
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 16
- 125000004432 carbon atom Chemical group C* 0.000 claims abstract description 10
- 239000011973 solid acid Substances 0.000 claims abstract description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000008367 deionised water Substances 0.000 claims abstract description 8
- 229910021641 deionized water Inorganic materials 0.000 claims abstract description 8
- 239000001301 oxygen Substances 0.000 claims abstract description 8
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 8
- 238000006703 hydration reaction Methods 0.000 claims description 27
- 230000036571 hydration Effects 0.000 claims description 18
- 239000000203 mixture Substances 0.000 claims description 9
- 230000000694 effects Effects 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 7
- 230000003197 catalytic effect Effects 0.000 claims description 6
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 4
- 238000010924 continuous production Methods 0.000 claims description 4
- 239000002808 molecular sieve Substances 0.000 claims description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 2
- 150000001768 cations Chemical group 0.000 claims description 2
- 239000003795 chemical substances by application Substances 0.000 claims description 2
- 238000004090 dissolution Methods 0.000 claims description 2
- 239000011347 resin Substances 0.000 claims description 2
- 229920005989 resin Polymers 0.000 claims description 2
- 239000002994 raw material Substances 0.000 abstract description 5
- 230000000887 hydrating effect Effects 0.000 abstract 1
- BTANRVKWQNVYAZ-UHFFFAOYSA-N butan-2-ol Chemical compound CCC(C)O BTANRVKWQNVYAZ-UHFFFAOYSA-N 0.000 description 16
- 239000000047 product Substances 0.000 description 16
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 11
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 10
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 10
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 9
- 239000012535 impurity Substances 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- 150000001336 alkenes Chemical class 0.000 description 6
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 6
- 238000012360 testing method Methods 0.000 description 6
- 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 description 5
- 230000006837 decompression Effects 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 239000007791 liquid phase Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000376 reactant Substances 0.000 description 4
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 3
- 239000001273 butane Substances 0.000 description 3
- 239000003729 cation exchange resin Substances 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000012263 liquid product Substances 0.000 description 3
- 238000007086 side reaction Methods 0.000 description 3
- 239000010457 zeolite Substances 0.000 description 3
- RYPKRALMXUUNKS-UHFFFAOYSA-N 2-Hexene Natural products CCCC=CC RYPKRALMXUUNKS-UHFFFAOYSA-N 0.000 description 2
- 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
- 238000007171 acid catalysis Methods 0.000 description 2
- 230000005587 bubbling Effects 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 239000003456 ion exchange resin Substances 0.000 description 2
- 229920003303 ion-exchange polymer Polymers 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- XTUSEBKMEQERQV-UHFFFAOYSA-N propan-2-ol;hydrate Chemical compound O.CC(C)O XTUSEBKMEQERQV-UHFFFAOYSA-N 0.000 description 2
- JTXAHXNXKFGXIT-UHFFFAOYSA-N propane;prop-1-ene Chemical compound CCC.CC=C JTXAHXNXKFGXIT-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000003643 water by type Substances 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
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- ZAFNJMIOTHYJRJ-UHFFFAOYSA-N Diisopropyl ether Chemical compound CC(C)OC(C)C ZAFNJMIOTHYJRJ-UHFFFAOYSA-N 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 239000008346 aqueous phase Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003818 cinder Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 229940074869 marquis Drugs 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- VBUNOIXRZNJNAD-UHFFFAOYSA-N ponazuril Chemical compound CC1=CC(N2C(N(C)C(=O)NC2=O)=O)=CC=C1OC1=CC=C(S(=O)(=O)C(F)(F)F)C=C1 VBUNOIXRZNJNAD-UHFFFAOYSA-N 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Abstract
The present invention relates to a method for continuously producing lower alcohol containing 2 to 5 carbon atoms. In the method, lower-carbon alkene containing 2 to 5 carbon atoms is catalyzed and hydrated to form lower alcohol at a reaction temperature of 100 to 200 DEG C and reaction pressure of 4.0 to 20.0MPa under the action of a solid acid catalyst. The present invention is characterized in that water used as a raw material of a hydrating reaction is oxygen-free deionized water whose oxygen dissolving concentration is smaller than 50 mug/l.
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.This method is at 100～200 ℃ of temperature of reaction, reaction pressure 4.0～20.0MPa, and under the effect of solid acid catalyst, the direct catalytic hydration of low-carbon alkene that will contain 2 to 5 carbon atoms obtains containing the lower alcohol of 2 to 5 carbon atoms.
Background technology
The low-carbon alkene direct hydration technology that with the solid acid 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 product of generation contains and separates after pure material is 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 solid acid catalyst effect, low-carbon alkene can generate corresponding low-carbon alcohol by the catalytic effect of proton.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 also can be zeolite catalyst such as beta-zeolite, ZSM-5, Y-zeolite etc. as the heatproof strong-acid ion exchange resin of modification, and the characteristics of above catalyzer are the reactive behavior height, heat resistance is good, corrosion 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 propylene 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 solid acid catalysis 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 2.0～20.0MPa, 100～200 ℃ of temperature of reaction.The catalyzer of canonical process is Zeo-karb or molecular sieve, and the per pass conversion of gas-liquid phase propylene 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 or 87% Virahol then separate aqueous Virahol with water through 3～6 distillation towers with a small amount of other weight component if desired.Benzene, diisopropyl ether or C6 alkane are used as the entrainment reagent of water in sepn process.
In solid acid 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 2.0～25.0MPa, 100～200 ℃ 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 phase 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 4, water loop back reactive system after treatment.Take off C
4Column overhead 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 German Patent 2233967 and 2429770 specification sheetss, obtain together describing with other method in the aforesaid method.These methods are applied in the production of the sec-butyl alcohol (SBA) and the trimethyl carbinol (TBA) especially at Virahol (IPA).
Method described in German patent DE 2429770 specification sheetss, the n-butylene hydration that carries out has adopted the water cycle technology, is increasing gradually through 200-400 hour the operation post-reactor bottom and the pressure reduction at top.Along with the continuity of operating time, tangible compression shock can take place.These vibrations can make reaction process shut down, for eliminating this influence and must washing by water.
In the drip process described in the Deutsches Reichs-Patent DE2233967 specification sheets, there is the liquid material distribution problem, this shows how needs research makes the distribution of reactant better, particularly the time marquis of the industrial reactor entry into service that has refilled live catalyst, observed some focuses and generated, the generation of these focuses makes the distillatory Virahol that a kind of special smell be arranged.This can be assumed in the process of entry into service, be accompanied by local bad water distribution, run off in a large number and caused the cinder of burning fully of catalyzer and formed agglomerate at the activity of such catalysts group, and adopt ion exchange resin treatment round-robin water of productive use can not solve about reducing this problem of pressure reduction.
In Chinese patent CN86102121, mention and used cats product to reduce reactor bed resistance problem in the low-carbon alkene direct hydration process, make reactant be distributed in the surface of catalyzer better, reduced the pressure reduction problem that exists in the reaction process, this method has been widely used in propylene direct hydration, the butylene direct hydration reaction process.Yet the life-time service tensio-active agent can bring pollution problem to environment.
Impurity in reaction process recirculated water, particularly organic impurity be the major cause that produces pressure reduction in the reactor of olefin hydration production low-carbon alcohol, and these impurity gather with the continuous circulation of reaction water.The continuous increase of impurity not only can make reactor pressure reduction up and down increase gradually, also can compete the activity of such catalysts center and side reaction takes place with reactant.
Summary of the invention
The objective of the invention is to adopt a kind of more economical, more effective and nonpolluting method, the reactor bed pressure reduction that makes low-carbon alkene directly carry out the hydration reaction process is stabilized in a lower level, has guaranteed that olefin hydration stable production process ground carries out.Simultaneously since enforcement of the present invention can reduce side reaction generation, reduce the problem that bed layer pressure that focus that the beds of reaction process exists and reaction process exist increases.Owing to the focus that exists in generation that has suppressed side reaction effectively and the beds.Therefore also prolonged the work-ing life of catalyzer.
To achieve these goals, the present invention proposes to adopt in reaction process the method for the deionized water of removing trace dissolved oxygen to solve the above-mentioned method of putting forward.The method of removing micro amount of oxygen in the deionized water can realize by deaeration in condenser or the method by catalytic deoxidation.
Specifically, a kind of continuous production of the present invention contains the method for the lower alcohol of 2 to 5 carbon atoms, be at 100～200 ℃ of temperature of reaction, reaction pressure 4.0～20.0MPa, under the effect of solid acid catalyst, the low-carbon alkene catalytic hydration that will contain 2 to 5 carbon atoms becomes low-carbon alcohol, and the raw water that it is characterized in that being used for hydration reaction is the anaerobic deionized water of the concentration of ordinary dissolution＜50 μ g/l of oxygen.
In above-mentioned method, can use cation resin catalyzing agent, molecular sieve catalyst or phosphoric acid infusorial earth catalyst, reactor can be used fixed-bed reactor, at least a component is passed fixed bed catalyst for one section from reactor in reaction process, reaction back mixture shifts out from the reactor the other end, the alcohol that obtains generating by separation.
Embodiment
Simultaneous test 1
This simultaneous test is to carry out on 160 * 3000mm single tube trickle bed adiabatic reactor in a Φ, and the reactor external thermal insulation adopts adiabatic control.40 liters of cation exchange resin catalyst (commercial catalysts of filling in the reactor, the chemical plant produces in the Ji, Cangzhou, the trade mark is D008) catalyzer divides equally three sections fillings, be respectively equipped with cold water pipe to solve the problem of taking out reaction heat in two, three sections beds are annotated, the pressure reduction of whole reactor is measured by differential manometer.The charging density of propylene is greater than 95.0m%, and reaction water is that specific conductivity is the deionized water of ∠ 5 μ s/cm.Reacted product obtains reacting thick product after by decompression separation, analyzes the yield that product is formed and obtained to the gas, liquid product.Reaction conditions: pressure 8.0MPa, 135 ℃ of temperature of reaction.
Raw material input and output material such as following table:
3 hours material balances
| Component | Charging (g) | Discharging (g) |
| Propylene propane butylene butane water isopropyl alcohol diisopropyl ether 2, the loss of 3-dimethyl dibutene 3-methyl cinene adds up to | 11287 528 82000 93815 | 2533 528 79202 10287 805 41 72 347 93815 |
Pressure reduction is as follows in operating process:
| Operating time, hour | Pressure reduction, Mpa | The Virahol yield, Grams Per Hour |
| 24 | 0.08 | 3429 |
| 48 | 0.10 | 3311 |
| 72 | 0.13 | 3056 |
| 96 | 0.16 | 2910 |
Simultaneous test 2
A Φ is used in this test
In28 * 3000mm bubbling sheet pipe reactor.Filling 1 liter of cation exchange resin catalyst (commercial catalyst, H in the reactor
+The chemical plant produces in the Ji, type Cangzhou, and the trade mark is D008), the pressure reduction of whole reactor is measured by differential manometer, and the reaction process synoptic diagram is shown in figure two.Mix the n-butene raw material and enter reactor along the feed olefin pipeline, this mixture contains 85% n-butene, and water enters reactor along the feed water pipeline, and reacted product obtains thick product after by decompression separation, analyzes to obtain product and form.Reaction conditions is 160 ℃ of reaction pressure 6.0MPa, temperature of reaction.300.3g/hr the n-butene mixture and the deionized water of 300.3g/hr enter reactor from reactor bottom, reaction product obtains reacting thick product after by decompression separation, analyzes the yield that product is formed and obtained to the gas, liquid product.
Pressure reduction is as follows in operating process:
| Operating time, hour | Pressure reduction, MPa | The sec-butyl alcohol yield, Grams Per Hour |
| 24 | 0.12 | 231 |
| 48 | 0.15 | 220 |
| 72 | 0.17 | 216 |
| 96 | 0.19 | 203 |
Embodiment 1
Present embodiment adopts reaction unit and the catalyzer identical with simultaneous test 1.The concentration of charging propylene is greater than 95%, and reaction process water is that oxygen level is that ∠ 50 μ g/l, specific conductivity are ∠ 5 μ s/cm anaerobic deionized waters.Reacted product is analyzed the yield that product is formed and obtained to the gas, liquid product by arriving the thick product of reaction after the decompression separation.Reaction conditions is reaction pressure 8.0MPa, 135 ℃ of temperature of reaction.
Raw material input and output material such as following table:
3 hours material balances
| Component | Charging (g) | Discharging (g) |
| Propylene propane water isopropyl alcohol diisopropyl ether 2, the loss of 3-dimethyl dibutene 3-methyl cinene adds up to | 11287 528 82000 93815 | 2489 528 79241 10465 798 30 46 218 93815 |
Pressure reduction is as follows in operating process:
| Operating time (hour) | Pressure reduction, MPa | The Virahol yield, Grams Per Hour |
| 24 | 0.08 | 3488 |
| 48 | 0.10 | 3426 |
| 72 | 0.13 | 3433 |
| 96 | 0.16 | 3479 |
Embodiment 2
Present embodiment uses reaction unit and the catalyzer identical with simultaneous test 2.Filling 1 liter of cation exchange resin catalyst (commercial catalyst, H in the reactor
+Type), the pressure reduction of whole reactor is measured by differential manometer.The mixture of n-butene enters reactor along the feed olefin pipeline, and this mixture contains 85% n-butene, and reaction water enters reactor along the feed water pipeline.Reacted product obtains reacting thick product by after the decompression separation, analyzes to obtain the product composition.Reaction conditions: reaction pressure 6.0MPa, 160 ℃ of temperature of reaction, the charging of n-butene mixture is 300.3g/hr, the charging of reaction process water is 300.3g/hr, reaction process water be dissolved oxygen amount be ∠ 50 μ g/l,, specific conductivity is ∠ 5 μ s/cm anaerobic deionized waters.
Pressure reduction is as follows in operating process:
| Operating time, hour | Pressure reduction, MPa | The sec-butyl alcohol yield, Grams Per Hour |
| 24 | 0.10 | 231 |
| 48 | 0.11 | 233 |
| 72 | 0.12 | 230 |
| 96 | 0.11 | 229 |
Result by the foregoing description and contrast experiment can see, when the deionized water that adopts dissolved oxygen amount ∠ 50 μ g/l reacts when making the low-carbon alkene catalytic hydration become lower alcohol, reactor bed pressure reduction is stabilized in a lower level, has guaranteed that olefin hydration stable production process ground carries out.
Claims (4)
1, a kind of continuous production contains the method for the lower alcohol of 2 to 5 carbon atoms, be at 100～200 ℃ of temperature of reaction, reaction pressure 4.0～20.0MPa, under the effect of solid acid catalyst, the low-carbon alkene catalytic hydration that will contain 2 to 5 carbon atoms becomes low-carbon alcohol, and the raw water that it is characterized in that being used for hydration reaction is the anaerobic deionized water of the concentration of ordinary dissolution＜50 μ g/l of oxygen.
2,, it is characterized in that solid acid catalyst is cation resin catalyzing agent, molecular sieve catalyst or phosphoric acid infusorial earth catalyst according to the described method of claim 1.
3,, it is characterized in that reactor is fixed-bed reactor according to the described method of claim 1.
4, according to claim 1,2 or 3 described methods, it is characterized in that at least a component passes fixed bed catalyst for one section from reactor, reaction back mixture shifts out from the reactor the other end, the alcohol that obtains generating by separation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410001113 CN1247503C (en) | 2004-01-19 | 2004-01-19 | Method for continuously producing lower alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410001113 CN1247503C (en) | 2004-01-19 | 2004-01-19 | Method for continuously producing lower alcohol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1648116A CN1648116A (en) | 2005-08-03 |
| CN1247503C true CN1247503C (en) | 2006-03-29 |
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|---|---|---|---|
| CN 200410001113 Expired - Lifetime CN1247503C (en) | 2004-01-19 | 2004-01-19 | Method for continuously producing lower alcohol |
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| Country | Link |
|---|---|
| CN (1) | CN1247503C (en) |
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2004
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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 Granted publication date: 20060329 License type: Common License Open date: 20050803 Record date: 20111111 |
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