CN113617385A - Preparation method of catalyst for olefin hydration reaction - Google Patents
Preparation method of catalyst for olefin hydration reaction Download PDFInfo
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- CN113617385A CN113617385A CN202110947091.XA CN202110947091A CN113617385A CN 113617385 A CN113617385 A CN 113617385A CN 202110947091 A CN202110947091 A CN 202110947091A CN 113617385 A CN113617385 A CN 113617385A
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/78—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J29/7815—Zeolite Beta
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- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
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- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/7049—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
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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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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
- C10G11/04—Oxides
- C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
- B01J2229/186—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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Abstract
The invention discloses a preparation method of a catalyst for olefin hydration reaction, which comprises the following steps: firstly, preparing a substrate catalyst by using pseudo-boehmite as a binder and a beta molecular sieve as an active component; and then modifying the substrate catalyst by adopting an isometric impregnation method to finally prepare the catalyst for olefin hydration reaction. The catalyst prepared by the method can be used for the hydration olefin reduction process of catalytic cracking light gasoline, not only can reduce the occurrence of side reactions and improve the selectivity, but also ensures that the catalyst has good stability, and in addition, the catalyst can be regenerated by a high-temperature roasting mode after being deactivated, the preparation process is simple and easy to operate, and the cost is low.
Description
Technical Field
The invention belongs to the field of olefin hydration reaction catalysts, and particularly relates to a preparation method of a catalyst for olefin hydration reaction.
Background
In recent years, environmental protection requirements are becoming stricter, the upgrading of gasoline quality is accelerated obviously, the content of olefin is restricted to no more than 18% in national VI gasoline standards, and the future gasoline standards are becoming stricter. Domestic gasoline mainly comes from a catalytic cracking process, and the olefin content is high, so that how to effectively reduce the olefin and retain the octane number becomes a research hotspot in the oil product processing industry.
The existing method for reducing olefin in gasoline mainly comprises the following steps: the method comprises the steps of FCC raw material pretreatment, the use of a novel olefin reduction catalyst and an auxiliary agent, and catalytic gasoline aftertreatment technology (gasoline hydration, catalytic reforming and aromatization, alkylation and isomerization). The methods have the problem of serious octane number loss while reducing the content of olefin in gasoline, so that the method for efficiently reducing olefin and achieving the purposes of preserving the octane number and even improving the octane number becomes the key for researching the olefin reduction technology.
The light gasoline contains a large amount of C5 and C6 olefins, and the hydration reaction is carried out on the light gasoline, so that the aim of efficiently reducing the olefins can be achieved, and simultaneously, alcohol products with high octane number are generated, and the alcohols directly enter the gasoline components, so that the antiknock property and the oxygen content of the gasoline are effectively improved. There are two general ways of olefin hydration, one is a direct hydration method, the other is an indirect hydration method, and the direct hydration method is mostly applied in industry at present. Olefin hydration is electrophilic addition, a protonic acid catalyzed process, which follows the mahalanobis rule, and hydration yields secondary or tertiary alcohols in addition to ethanol. Olefin hydration also tends to induce side reactions such as olefin oligomerization, intramolecular and intermolecular dehydration of the product alcohol.
The hydration of olefins to form alcohols is typically an acid-catalyzed reaction, requiring strongly acidic catalysts, generally classified as homogeneous and heterogeneous catalysts. Most of early olefin hydration catalysts are homogeneous catalysts, and then a series of heterogeneous catalysts, such as acidic macroporous cation exchange resins, immobilized heteropoly acids, molecular sieves and the like, are developed successively in view of the defects of corrosion of equipment, difficulty in product separation, environmental pollution and the like.
The macroporous strong-acid cation exchange resin is widely applied in industry, and has the advantages of excellent selectivity, good activity, long service life, good temperature resistance, no corrosion and the like. But the disadvantages are also evident: the exothermic reaction causes over-high temperature, possibly leads sulfonic acid groups to fall off, olefin oligomerization and other side reactions to occur, the activity is reduced, and the service life is reduced; the filling is difficult and the crushing is easy; the reaction volume is not utilized sufficiently.
The supported heteropoly acid is a novel catalyst, and the heteropoly acid is an oxygen-containing polyacid which is formed by coordination bridging of heteroatoms (such as P, Si, Fe, Co and the like) and polyatomic atoms (such as Mo, Nb, Ta, V and the like) through oxygen atoms and according to a certain structure. The supported heteropoly acid not only increases the specific surface area but also improves the catalytic activity, but also has the problem of acid center loss, and the preparation process is complex and the cost is higher.
The molecular sieve catalyst is considered as the most potential hydration catalyst, and has the advantages of good stability, high selectivity, high catalyst strength, high active center density, large specific surface area, easy activation and regeneration, environmental protection and the like. The molecular sieves currently used for hydration research mainly comprise HY series, ZSM series, beta type molecular sieves and the like. Different molecular sieves have different structures and silicon-aluminum ratios, so that the molecular sieves have different acid properties and acid strengths, and different shape-selectivity on reactants, intermediate products and final products, so that the hydration performance of the molecular sieves is characterized.
The aim and development direction of the future research on the olefin hydration catalyst are to improve the activity and selectivity of the catalyst and ensure that the catalyst has good stability and regenerability as far as possible. The hydration catalyst has the advantages and disadvantages, and intensive research is needed to improve the molecular sieve catalyst and further improve the activity of the molecular sieve catalyst applied to the olefin hydration reaction of light gasoline.
Disclosure of Invention
The present invention has been made to overcome the disadvantages of the prior art, and an object of the present invention is to provide a method for preparing a catalyst for olefin hydration reaction.
The invention is realized by the following technical scheme:
a method of preparing a catalyst for olefin hydration reactions, comprising the steps of:
preparing a base catalyst
Fully mixing the active component, the binder and the extrusion aid, adding a peptizing agent, kneading, extruding, drying and roasting to obtain a substrate catalyst;
(ii) modifying the base catalyst
The catalyst is modified by an isometric impregnation method, and the catalyst for olefin hydration reaction is finally prepared by drying and roasting after impregnation.
In the technical scheme, the active component is a molecular sieve, and the content of the molecular sieve is 30-90 wt% of the mass of the substrate catalyst
In the technical scheme, the molecular sieve is a hydrogen type or sodium type beta molecular sieve, the silica-alumina ratio is 20-80, and the specific surface area is 200m2/g~500m2/g。
In the technical scheme, the binder is pseudo-boehmite, the content of the pseudo-boehmite is 10-70 wt% of the mass of the substrate catalyst, the boehmite is medium-pore or macroporous boehmite powder, and the pore volume of the boehmite is more than or equal to 0.35cm3Per g, specific surface area of 200m2/g~400m2/g 。
In the technical scheme, the extrusion aid is sesbania powder, and the content of the sesbania powder is 1-8 wt% of the mass of the substrate catalyst.
In the technical scheme, the peptizing agent is a dilute nitric acid solution, the concentration of the dilute nitric acid solution is 0.1-1.0 mol/L, and the adding amount of the peptizing agent is 1-3% of the mass of the pseudo-boehmite.
In the above technical scheme, the drying conditions after kneading and extruding the base catalyst in the step (i) are as follows: drying the mixture in an oven at the temperature of 50-110 ℃ for 4-10 h; the roasting conditions are as follows: roasting in a muffle furnace at 400-650 ℃ for 2-6 h; and cooling and smashing the roasted mixture into 20-40-mesh particles after roasting.
In the technical scheme, the impregnation liquid adopted by the equal-volume impregnation method is any one or a mixture of more of an ammonium niobium oxalate solution, a lanthanum nitrate solution, a cerium nitrate solution or a phosphoric acid solution; the dipping time is 8h, the drying condition after dipping is 8h at 90 ℃, and the roasting condition is 4h after the temperature is programmed to 550 ℃ in a muffle furnace.
In the technical scheme, the catalyst for the olefin hydration reaction is used for the hydration olefin reduction process of the catalytic cracking light gasoline.
In the above technical scheme, the catalyst for olefin hydration reaction is used for 1-hexene hydration reaction.
The invention has the beneficial effects that:
the invention provides a preparation method of a 1-hexene hydration reaction catalyst, the prepared catalyst can be used for the hydration olefin reduction process of catalytic cracking light gasoline, the side reaction can be reduced, the selectivity is improved, the catalyst has good stability, in addition, the catalyst can be regenerated in a high-temperature roasting mode after being deactivated, the preparation process is simple and easy to operate, and the cost is low.
Detailed Description
In order to make the technical solution of the present invention better understood by those skilled in the art, the technical solution of the present invention is further described below by the specific embodiments.
A method of preparing a catalyst for olefin hydration reactions, comprising the steps of:
preparing a base catalyst
Firstly, weighing beta molecular sieve, pseudo-boehmite and sesbania powder according to a proportion, wherein the content of the beta molecular sieve is 30-90 wt%, preferably 30-80 wt%, and most preferably 40-80 wt% of the mass of a carrier; the content of the pseudoboehmite is 10-70 wt% of the mass of the carrier, preferably 20-70 wt%, and most preferably 20-60 wt%; the sesbania powder content is 1.0 wt% to 8.0 wt%, preferably 1.0 wt% to 6.0 wt%, and most preferably 2 wt% to 5 wt% of the carrier mass. Then preparing a dilute nitric acid solution with the concentration of 0.1-1.0 mol/L, preferably 0.2-0.8 mol/L, and most preferably 0.3-0.5 mol/L. Adding a dilute nitric acid solution into the mixed powder, fully kneading, extruding into strips, drying in an oven at 50-110 ℃ for 4-10 h, roasting in a muffle furnace at 400-650 ℃ for 2-6 h, cooling, and smashing into 20-40-mesh particles for later use. The addition amount of the dilute nitric acid solution is 1-3% of the mass of the pseudo-boehmite.
(ii) modifying the base catalyst
Firstly, deionized water is adopted to dissolve a certain amount of NH4·[NbO(C2O4)2(H2O)2]·3H2O、La(NO3)3、Ce(NO3)3And one or more of phosphoric acid, soaking the mixture on a substrate catalyst (20-40 meshes) in an equal volume for 8 hours, drying the mixture for 8 hours at 90 ℃, and then roasting the mixture for 4 hours in a muffle furnace at a programmed temperature of 550 ℃ to obtain the corresponding catalyst.
The equal-volume impregnation method comprises the following specific steps: weighing 5 g-10 g of substrate catalyst and recording as m1Soaking in deionized water for 1 hr, draining, wiping off surface free water with absorbent paper, and weighing2Then the water absorption is = (m)2-m1)/m1100%, the mass of water that can be absorbed per mass of base catalyst, since the density of water is about 1g/mL, the volume of solution that can be absorbed per mass of base catalyst can be obtained.
The evaluation of the hydration activity of the catalyst prepared by the method is carried out in a self-made miniature fixed bed reactor, the inner diameter of a reaction tube is 10mm, the length of the reaction tube is 600mm, the reaction tube adopts three-section temperature control, 5mL of catalyst is filled in a constant temperature section, and the rest part of the reaction tube is filled with inert small ceramic balls. The hydrated raw oil is simulated oil prepared from normal hexane and n-hexene according to the mass ratio of 7: 3, after the preparation is finished, the mixture is vibrated for 30 minutes in an ultrasonic oscillator, and the mixture of the mixture and deionized water is in contact reaction with a catalyst under the following reaction conditions:
the molar ratio of water to n-hexylene is 5-8, preferably 5.5-8, and most preferably 6-7.5; the reaction temperature is 150-190 ℃, preferably 160-185 ℃, and most preferably 165-180 ℃; the reaction pressure is 1.0-4.0 MPa, preferably 2.0-4.0 MPa, and most preferably 2.0-3.0 MPa; the volume space velocity is 1h-1~4 .0h-1Preferably 1.5h-1~4.0h-1Most preferably 2h-1~3h-1。
Example 1
The content of the beta molecular sieve is 60 percent of the mass of the substrate catalyst, the content of the pseudo-boehmite is 37 percent of the mass of the substrate catalyst,
the sesbania powder content is 3% of the mass of the substrate catalyst, the three are fully mixed, then a dilute nitric acid solution with the concentration of 0.4mol/L is added, the mixture is extruded into strips after being uniformly stirred, and the strips are cooled and crushed into particles of 20-40 meshes after being dried in an oven at 110 ℃ for 10 hours and roasted in a muffle furnace at 550 ℃ for 4 hours, so that the substrate catalyst is finally prepared.
Dissolving a certain amount of NH in deionized water4·[NbO(C2O4)2(H2O)2]·3H2Soaking O on the substrate catalyst in the same volume for 8h, Nb2O3The content is 0 wt% (namely unmodified), and the mixture is dried in an oven for 8 hours at the temperature of 90 ℃, roasted for 4 hours in a muffle furnace at the temperature of 550 ℃ and cooled for standby.
Hydration reaction evaluation reaction conditions: the water/n-hexylene molar ratio is 7.5, the reaction temperature is 175 ℃, the reaction pressure is 3MPa, and the volume space velocity is 2.3h-1。
Example 2
The preparation method of the base catalyst is the same as that of example 1, except that the modified base catalyst Nb2O3The content was 1 wt%, the procedure was as described in example 1, and the conditions for evaluating the hydration activity were also as described in example 1.
Example 3
The preparation method of the base catalyst is the same as that of example 1, except that the modified base catalyst Nb2O3The content was 2 wt%, the procedure was as described in example 1, and the conditions for evaluating the hydration activity were also as described in example 1.
Example 4
The preparation method of the base catalyst is the same as that of example 1, except that the modified base catalyst Nb2O3The content was 3% by weight, the procedure was as described in example 1, and the conditions for evaluating the hydration activity were also as described in example 1.
Example 5
The preparation method of the base catalyst is the same as that of example 1, except that the modified base catalyst Nb2O3At a level of 4.5 wt%, according to the procedure described in example 1,the conditions for evaluation of hydration activity were also as described in example 1.
Example 6
The preparation method of the base catalyst is the same as that of example 1, except that the modified base catalyst Nb2O3The content was 6% by weight, the procedure was as described in example 1, and the conditions for evaluating the hydration activity were also as described in example 1.
Example 7
The base catalyst was prepared in the same manner as in example 1, except that a certain amount of La (NO) was dissolved in deionized water3)3Equal volume of impregnated on base catalyst, La2O3The content is 0.5 wt%, drying in an oven at 90 ℃ for 8h, roasting in a muffle furnace at 550 ℃ for 4h, and cooling for later use. The conditions for evaluation of hydration activity were as described in example 1.
Example 8
The base catalyst was prepared in the same manner as in example 1, except that the base catalyst La was modified as described in example 72O3The content was 1% by weight, and the conditions for evaluating the hydration activity were as described in example 1.
Example 9
The base catalyst was prepared in the same manner as in example 1, except that a certain amount of Ce (NO) was dissolved in deionized water3)3Equal volume impregnated on the base catalyst, Ce2O3The content is 0.5 wt%, drying in an oven at 90 ℃ for 8h, roasting in a muffle furnace at 550 ℃ for 4h, and cooling for later use. The conditions for evaluation of hydration activity were as described in example 1.
Example 10
The preparation method of the base catalyst is the same as that of example 1, and other steps are as described in example 9, except that the modified base catalyst Ce is used2O3The content was 1 wt%, and the hydration activity evaluation conditions were as described in example 1.
Example 11
By loading Nb2O3The modified catalyst having a content of 2 wt% was used as a base catalyst, the base catalyst was prepared in the same manner as in example 3, and dissolved in deionized waterA certain amount of phosphoric acid, which is dipped on the base catalyst in equal volume, P2O5The content is 1 wt%, and the mixture is dried in an oven at 90 ℃ for 8h, roasted in a muffle furnace at 550 ℃ for 4h and then cooled for standby. The hydration activity evaluation conditions were as described in example 1.
Example 12
The base catalyst was prepared in the same manner as in example 11, except that the modified base catalyst P was used2O5The content was 2 wt%. The hydration activity evaluation conditions were as described in example 1.
Example 13
The base catalyst was prepared in the same manner as in example 11, except that the modified base catalyst P was used2O5The content was 3 wt%. The hydration activity evaluation conditions were as described in example 1.
The results of evaluation of hydration activity of each catalyst in examples are shown in table 1 below.
Table 1 evaluation results of hydration activity of catalyst in examples
The results in table 1 show that the catalyst for olefin hydration reaction can be prepared by using a modification mode of composite treatment of soaking ammonium niobium oxalate and phosphoric acid under proper operation conditions, and the catalyst not only can reduce the occurrence of side reactions and improve the selectivity, but also can ensure that the catalyst has good stability.
It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
The applicant declares that the above description is only a specific embodiment of the present invention, but the scope of the present invention is not limited thereto, and it should be understood by those skilled in the art that any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are within the scope and disclosure of the present invention.
Claims (10)
1. A method for preparing a catalyst for olefin hydration reactions, characterized by: the method comprises the following steps:
preparing a base catalyst
Fully mixing the active component, the binder and the extrusion aid, adding a peptizing agent, kneading, extruding, drying and roasting to obtain a substrate catalyst;
(ii) modifying the base catalyst
The catalyst is modified by an isometric impregnation method, and the catalyst for olefin hydration reaction is finally prepared by drying and roasting after impregnation.
2. The method for preparing a catalyst for olefin hydration reaction according to claim 1, characterized in that: the active component is a molecular sieve, and the content of the molecular sieve is 30-90 wt% of the mass of the substrate catalyst.
3. The method for preparing a catalyst for olefin hydration reaction according to claim 2, characterized in that: the molecular sieve is a hydrogen type or sodium type beta molecular sieve, the silicon-aluminum ratio is 20-80, and the specific surface area is 200m2/g~500m2/g。
4. The method for preparing a catalyst for olefin hydration reaction according to claim 1, characterized in that: the binder is pseudo-boehmite, the content of the pseudo-boehmite is 10 wt% -70 wt% of the mass of the substrate catalyst, the boehmite is medium-pore or macroporous boehmite powder, and the pore volume of the boehmite is more than or equal to 0.35cm3Per g, specific surface area of 200m2/g~400m2/g 。
5. The method for preparing a catalyst for olefin hydration reaction according to claim 1, characterized in that: the extrusion aid is sesbania powder, and the content of the sesbania powder is 1-8 wt% of the mass of the base catalyst.
6. The method for preparing a catalyst for olefin hydration reaction according to claim 1, characterized in that: the peptizing agent is a dilute nitric acid solution, the concentration of the dilute nitric acid solution is 0.1-1.0 mol/L, and the adding amount of the peptizing agent is 1-3% of the mass of the pseudo-boehmite.
7. The method for preparing a catalyst for olefin hydration reaction according to claim 1, characterized in that: the drying conditions after kneading and extruding in the preparation of the base catalyst in the step (i) are as follows: drying the mixture in an oven at the temperature of 50-110 ℃ for 4-10 h; the roasting conditions are as follows: roasting in a muffle furnace at 400-650 ℃ for 2-6 h; and cooling and smashing the roasted mixture into 20-40-mesh particles after roasting.
8. The method for preparing a catalyst for olefin hydration reaction according to claim 1, characterized in that: the impregnation liquid adopted by the equal-volume impregnation method is one or a mixture of more of an ammonium niobium oxalate solution, a lanthanum nitrate solution, a cerium nitrate solution or a phosphoric acid solution; the dipping time is 8h, the drying condition after dipping is 8h at 90 ℃, and the roasting condition is 4h after the temperature is programmed to 550 ℃ in a muffle furnace.
9. The method for preparing a catalyst for olefin hydration reaction according to claim 1, characterized in that: the catalyst for olefin hydration reaction is used for the hydration olefin reduction process of catalytic cracking light gasoline.
10. The method for preparing a catalyst for olefin hydration reaction according to claim 1, characterized in that: the catalyst for olefin hydration reaction is used for 1-hexene hydration reaction.
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| 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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