CN103145743B - A kind of preparation method of zinc ethyl - Google Patents
A kind of preparation method of zinc ethyl Download PDFInfo
- Publication number
- CN103145743B CN103145743B CN201310095037.2A CN201310095037A CN103145743B CN 103145743 B CN103145743 B CN 103145743B CN 201310095037 A CN201310095037 A CN 201310095037A CN 103145743 B CN103145743 B CN 103145743B
- Authority
- CN
- China
- Prior art keywords
- zinc
- reaction
- zinc ethyl
- preparation
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Abstract
The invention discloses a kind of preparation method of zinc ethyl; comprise the steps: under protection of inert gas; under Zr catalyst existent condition; in zinc chloride, add triethyl aluminum react; control temperature of reaction not higher than 60 DEG C; after reacting completely, obtain described zinc ethyl and evaporated mother liquor through underpressure distillation.This preparation method by adding Zr catalyst in reaction system, effectively can promote the reaction efficiency of zinc chloride and triethyl aluminum, reduce the temperature of reaction, reduce the generation of side reaction and the decomposition of product zinc ethyl, be conducive to the purity and the yield that improve product; Meanwhile, after adding Zr catalyst, the concentration requirement of the hydride contained by triethyl aluminum is not needed very strict, can directly use commercially available product, simplify operation steps.
Description
Technical field
The invention belongs to organometallic compound synthesis field, be specifically related to a kind of preparation method of zinc ethyl.
Background technology
Zinc ethyl is a kind of conventional organic zinc reagent, is normally used for catalyzer or the reaction reagent of polymerization or drug manufacture, is widely used in the relevant industries such as polymerizing catalyst, pharmaceutical synthesis and solar cell.
The synthetic method of current dialkyl group zinc mainly contains following three kinds: the reaction of (1) halides and metallic zinc; (2) various compound is with the permutoid reaction of zinc alkyl(s); (3) reaction of halo zinc and metal reagent is adopted.
In first method, usually adopt iodo thing and bromo-derivative with the zinc powder reaction activated, namely first obtained the halides of zinc ethyl with halohydrocarbon effect by zinc powder, then this halides is at high temperature dissociated, and generates zinc ethyl compound.Publication number is the preparation method that the Chinese patent of CN100408584C discloses a kind of zinc ethyl, hydrogen is first used to activate zinc powder, then cuprous iodide is added, dripping the mixing solutions of iodoethane and monobromethane, react at 100 ~ 150 DEG C, after reacting completely, carry out distillation at reduced pressure conditions and obtain zinc ethyl product.The method owing to relating to high temperature and hydrogen, and has used the raw material of this costliness of iodide, makes high expensive, and industrialization benefit is not high
In second method, adopt various compound with the permutoid reaction of zinc alkyl(s) as iodo-zinc permutoid reaction, boron-zinc permutoid reaction, mercury-zinc permutoid reaction time, be mainly used in synthesizing senior organic zinc compound, the preparation of zinc ethyl cannot be used for, and industrialization difficulty is large.
In the third method, metal reagent used can be Grignard reagent, fragrant organolithium reagent or alkyllithium reagent.When the reaction using Grignard reagent or fragrant organolithium reagent with halo zinc, reaction yield is low, and product is difficult to be separated with the ether material in organolithium reagent with Grignard reagent, is thus seldom used; And aluminum alkyls method is because reaction is simple, low raw-material cost and by extensive concern.Publication number is that the Chinese patent application of CN102015730A discloses a kind of method for the preparation of dialkyl group zinc and an aluminum dialkyl monohalide, the method is by using hydride concentration to be that the trialkylaluminium of 0.01 quality % to 0.10 quality % is as raw material, the generation of the precipitation agent in reaction process can be suppressed, and suppress throw out to enter in product attachment of equipment and composition thereof.The shortcoming of this preparation method is that the concentration of higher to the purity requirement of raw material, contained hydride can not be too high, needs to adopt special preparation method's preparation.
Summary of the invention
The invention provides a kind of preparation method of zinc ethyl, this preparation method can directly use commercially available triethyl aluminum as raw material, effectively can prevent the generation of side reaction simultaneously, improves purity and the yield of product.
A preparation method for zinc ethyl, comprises the steps:
Under protection of inert gas, under Zr catalyst existent condition, in zinc chloride, add triethyl aluminum react, control temperature of reaction not higher than 60 DEG C, after reacting completely, obtain described zinc ethyl and evaporated mother liquor through underpressure distillation.
In the present invention, by adding Zr catalyst in reaction system, effectively can promote the reaction efficiency of zinc chloride and triethyl aluminum, reducing the temperature of reaction, reduce the generation of side reaction and the decomposition of product zinc ethyl, be conducive to the purity and the yield that improve product; Meanwhile, after adding Zr catalyst, the concentration requirement of the hydride contained by triethyl aluminum is not needed very strict, can directly use commercially available product, simplify operation steps.The reaction formula of this preparation method is as follows:
2(C
2H
5)
;Al+ZnCl
2→(C
2H
5)
2Zn+2(C
2H
5)
2AlCl
Described Zr catalyst can be zirconium chloride, zirconium white, tetrabutyl zirconate, organic zirconates such as two (methyl cyclopentadiene) zirconium dichloride or bis cyclopentadienyl zirconium dichloride etc. or inorganic zirconium salts; Be preferably two (methyl cyclopentadiene) zirconium dichloride or bis cyclopentadienyl zirconium dichloride, with organic micromolecule ligand in these zirconates, better can promote the carrying out reacted; As most preferably, described Zr catalyst is bis cyclopentadienyl zirconium dichloride, and now, reaction most effective, side reaction is minimum.
Described bis cyclopentadienyl zirconium dichloride consumption is very few, effectively can not promote reaction, the consumption of described bis cyclopentadienyl zirconium dichloride is excessive, cost increase can be caused, and can have an impact to the purity of product, as preferably, the consumption of described bis cyclopentadienyl zirconium dichloride is 0.01% ~ 1% of triethyl aluminum molar weight, as further preferred, the consumption of described bis cyclopentadienyl zirconium dichloride is 0.01% ~ 0.1% of triethyl aluminum molar weight.
Because triethyl aluminum is easy and water reacts, need through dewatering before described zinc chloride reaction.
In the present invention, the zinc chloride of one mole needs the triethyl aluminum of consumption two moles when reacting, the consumption of triethyl aluminum is crossed conference and is caused cost increase, and final product may be made not easily separated, too small meeting makes reaction incomplete, as preferably, described zinc chloride and the mol ratio of triethyl aluminum are 1:1.8 ~ 2.2.
As preferably, described temperature of reaction is 25 ~ 45 DEG C, and temperature of reaction is too high, and side reaction can be caused to increase, and temperature of reaction is too low, and speed of reaction can be made slack-off.
As preferably, the time of reaction is 2 ~ 10 hours.
As preferably, the pressure of described underpressure distillation is-0.08-0.09MPa;
The temperature of fraction collection is 30 ~ 50 DEG C; Now, higher yields can obtain described zinc ethyl, and in the zinc ethyl obtained, impurity is less, purity is higher.
In the present invention, except generating zinc ethyl, can also generate diethylaluminum chloride, diethylaluminum chloride is also a kind of important chemical reagent simultaneously, as preferably, carries out further distillation obtain diethylaluminum chloride to described evaporated mother liquor.
As further preferred, pressure during distillation diethylaluminum chloride is-0.08-0.09MPa;
The temperature of fraction collection is 60 ~ 150 DEG C; Now, the diethylaluminum chloride of higher degree can be obtained.
Compared with the existing technology, beneficial effect of the present invention is embodied in:
(1) add Zr catalyst in reaction process, effectively can promote the generation of reacting, improve yield and the purity of product;
(2) reaction product is through fractionation by distillation, simple to operate, is easy to carry out suitability for industrialized production;
(3) evaporated mother liquor obtained can obtain useful industrial chemicals diethylaluminum chloride through being further separated.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of reaction and separation processes device used in the present invention.
Embodiment
As shown in Figure 1, main reactor is the reactor of 500L, be equipped with triethyl aluminum, white oil, normal hexane header tank, rectifying tower, zinc ethyl receives test tank, and diethylaluminum chloride receives test tank, mixture receives test tank, the residual container of still etc., heating and cooling system, dry vacuum and distillation vacuum, and be connected to argon system.Below in conjunction with specific embodiment, the present invention is further described.
Embodiment 1
1, argon replaces reactor, pipeline, header tank, receiving tank 2-3 time.Open manhole, under argon shield, drop into bis cyclopentadienyl zirconium dichloride 0.74kg and zinc chloride 170kg, be heated to 90 DEG C, stop argon gas, drying under reduced pressure 2-4 hour, be cooled to less than 25 DEG C for subsequent use;
2, under argon shield, raw material 292.5kg triethyl aluminum is depressed into triethyl aluminum header tank, by header tank triethyl aluminum under argon shield, put into the reactor of low rate mixing, reactor system automatic heat evolution is slowly warming up to 30-35 DEG C, finishes, be warming up to 40-45 DEG C, react 2 hours;
3, be cooled to less than 30 DEG C, open zinc ethyl distillation valve, underpressure distillation (pressure is-0.08-0.09MPa) zinc ethyl product, slow temperature reaction still, collect the zinc ethyl product of gas phase temperature 30-50 DEG C to zinc ethyl receiving tank; When temperature-measuring port temperature starts to decline, improve temperature of reaction kettle 5 DEG C, underpressure distillation 30 minutes, close zinc ethyl distillation valve, open mixture distillation valve, collect the mixture of a small amount of 50-60 DEG C, cut is analyzed, zinc ethyl quality purity is not less than 99.9%, and aluminium mass concentration is not more than 10ppm, and zirconium mass concentration is not more than 10ppm;
4, diethylaluminum chloride distillation valve is opened, opening vacuum to pressure is-0.08-0.09MPa, slow temperature reaction still, collect the diethylaluminum chloride of gas phase temperature 60-150 DEG C to diethylaluminum chloride receiving tank, confirm the distillation end point of good side product chlorinated diethyl aluminum, reactor stops heating, below slow cooling to 50 DEG C, stop vacuum, logical argon gas, continues cooling, cut is analyzed, the quality purity of diethylaluminum chloride is not less than 99.9 quality %, and zinc mass concentration is not more than 10ppm, and zirconium mass concentration is not more than 10ppm;
5,80kg white oil is pressed into white oil header tank, press-in 80kg normal hexane is to normal hexane header tank, stand-by, temperature of reaction kettle is down to less than 25 DEG C, under argon shield, slowly add white oil to reactor, open and stir, washing reaction still still is residual, stops stirring, under argon shield, white oil washings is loaded in specified containers;
6, add normal hexane to reactor, open and stir, washing reaction still, under argon shield, n-hexane liquid is loaded in specified containers.
The output being not more than the zinc ethyl of 10ppm by distilling the aluminum concentration obtained is 132kg, and the output being not more than the diethylaluminum chloride of 10ppm by distilling the zinc concentration obtained is 210kg.
Embodiment 2
1, argon replaces reactor, pipeline, header tank, receiving tank 2-3 time.Open manhole, under argon shield, drop into zirconium chloride 0.59kg and zinc chloride 170kg, be heated to 90 DEG C, stop argon gas, drying under reduced pressure 2-4 hour, be cooled to less than 25 DEG C for subsequent use;
2, under argon shield, raw material 292.5kg triethyl aluminum is depressed into triethyl aluminum header tank, by header tank triethyl aluminum under argon shield, put into the reactor of low rate mixing, reactor system automatic heat evolution is slowly warming up to 30-35 DEG C, finishes, be warming up to 40-45 DEG C, react 2 hours;
3, be cooled to less than 30 DEG C, open zinc ethyl distillation valve, underpressure distillation (pressure is-0.08-0.09MPa) zinc ethyl product, slow temperature reaction still, collect the zinc ethyl product of gas phase temperature 30-50 DEG C to zinc ethyl receiving tank; When temperature-measuring port temperature starts to decline, improve temperature of reaction kettle 5 DEG C, underpressure distillation 30 minutes, close zinc ethyl distillation valve, open mixture distillation valve, collect the mixture of a small amount of 50-60 DEG C, cut is analyzed, zinc ethyl quality purity is not less than 99.9%, and aluminium mass concentration is not more than 10ppm, and zirconium mass concentration is not more than 10ppm;
4, diethylaluminum chloride distillation valve is opened, opening vacuum to pressure is-0.08-0.09MPa, slow temperature reaction still, collect the diethylaluminum chloride of gas phase temperature 60-150 DEG C to diethylaluminum chloride receiving tank, confirm the distillation end point of good side product chlorinated diethyl aluminum, reactor stops heating, below slow cooling to 50 DEG C, stop vacuum, logical argon gas, continues cooling, cut is analyzed, the quality purity of diethylaluminum chloride is not less than 99.9 quality %, and zinc mass concentration is 320ppm, and zirconium mass concentration is not more than 10ppm;
5,80kg white oil is pressed into white oil header tank, press-in 80kg normal hexane is to normal hexane header tank, stand-by, temperature of reaction kettle is down to less than 25 DEG C, under argon shield, slowly add white oil to reactor, open and stir, washing reaction still still is residual, stops stirring, under argon shield, white oil washings is loaded in specified containers;
6, add normal hexane to reactor, open and stir, washing reaction still, under argon shield, n-hexane liquid is loaded in specified containers.
The output being not more than the zinc ethyl of 10ppm by distilling the aluminum concentration obtained is 105kg, and the zinc concentration obtained by distillation is the output of the diethylaluminum chloride of 320ppm is 172kg.
Embodiment 3
1, argon replaces reactor, pipeline, header tank, receiving tank 2-3 time.Open manhole, under argon shield, drop into bis cyclopentadienyl zirconium dichloride 6.0kg and zinc chloride 170kg, be heated to 90 DEG C, stop argon gas, drying under reduced pressure 2-4 hour, be cooled to less than 25 DEG C for subsequent use;
2, under argon shield, raw material 292.5kg triethyl aluminum is depressed into triethyl aluminum header tank, by header tank triethyl aluminum under argon shield, put into the reactor of low rate mixing, reactor system automatic heat evolution is slowly warming up to 30-35 DEG C, finishes, be warming up to 40-45 DEG C, react 2 hours;
3, be cooled to less than 30 DEG C, open zinc ethyl distillation valve, underpressure distillation (pressure is-0.08-0.09MPa) zinc ethyl product, slow temperature reaction still, collect the zinc ethyl product of gas phase temperature 30-50 DEG C to zinc ethyl receiving tank; When temperature-measuring port temperature starts to decline, improve temperature of reaction kettle 5 DEG C, underpressure distillation 30 minutes, close zinc ethyl distillation valve, open mixture distillation valve, collect the mixture of a small amount of 50-60 DEG C, cut is analyzed, zinc ethyl quality purity is not less than 99.9%, and aluminium mass concentration is not more than 10ppm, and zirconium mass concentration is 610ppm;
4, diethylaluminum chloride distillation valve is opened, opening vacuum to pressure is-0.08-0.09MPa, slow temperature reaction still, collect the diethylaluminum chloride of gas phase temperature 60-150 DEG C to diethylaluminum chloride receiving tank, confirm the distillation end point of good side product chlorinated diethyl aluminum, reactor stops heating, below slow cooling to 50 DEG C, stop vacuum, logical argon gas, continues cooling, cut is analyzed, the quality purity of diethylaluminum chloride is not less than 99.9 quality %, and zinc mass concentration is not more than 10ppm, and zirconium mass concentration is 780ppm;
5,80kg white oil is pressed into white oil header tank, press-in 80kg normal hexane is to normal hexane header tank, stand-by, temperature of reaction kettle is down to less than 25 DEG C, under argon shield, slowly add white oil to reactor, open and stir, washing reaction still still is residual, stops stirring, under argon shield, white oil washings is loaded in specified containers;
6, add normal hexane to reactor, open and stir, washing reaction still, under argon shield, n-hexane liquid is loaded in specified containers.
The output being not more than the zinc ethyl of 10ppm by distilling the aluminum concentration obtained is 129kg, and the output being not more than the diethylaluminum chloride of 10ppm by distilling the zinc concentration obtained is 215kg.
Embodiment 4
1, argon replaces reactor, pipeline, header tank, receiving tank 2-3 time.Open manhole, under argon shield, drop into bis cyclopentadienyl zirconium dichloride 0.37kg and zinc chloride 170kg, be heated to 90 DEG C, stop argon gas, drying under reduced pressure 2-4 hour, be cooled to less than 25 DEG C for subsequent use;
2, under argon shield, raw material 292.5kg triethyl aluminum is depressed into triethyl aluminum header tank, by header tank triethyl aluminum under argon shield, put into the reactor of low rate mixing, reactor system automatic heat evolution is slowly warming up to 30-35 DEG C, finishes, be warming up to 40-45 DEG C, react 2 hours;
3, be cooled to less than 30 DEG C, open zinc ethyl distillation valve, underpressure distillation (pressure is-0.08-0.09MPa) zinc ethyl product, slow temperature reaction still, collect the zinc ethyl product of gas phase temperature 30-50 DEG C to zinc ethyl receiving tank; When temperature-measuring port temperature starts to decline, improve temperature of reaction kettle 5 DEG C, underpressure distillation 30 minutes, close zinc ethyl distillation valve, open mixture distillation valve, collect the mixture of a small amount of 50-60 DEG C, cut is analyzed, zinc ethyl quality purity is not less than 99.9%, and aluminium mass concentration is not more than 10ppm;
4, open diethylaluminum chloride distillation valve, opening vacuum to pressure is-0.08-0.09MPa, slow temperature reaction still, collect the diethylaluminum chloride of gas phase temperature 60-150 DEG C to diethylaluminum chloride receiving tank, confirm the distillation end point of good side product chlorinated diethyl aluminum, reactor stops heating, below slow cooling to 50 DEG C, stop vacuum, logical argon gas, continues cooling, analyzes cut, the quality purity of diethylaluminum chloride is not less than 99.9 quality %, and zinc mass concentration is not more than 10ppm;
5,80kg white oil is pressed into white oil header tank, press-in 80kg normal hexane is to normal hexane header tank, stand-by, temperature of reaction kettle is down to less than 25 DEG C, under argon shield, slowly add white oil to reactor, open and stir, washing reaction still still is residual, stops stirring, under argon shield, white oil washings is loaded in specified containers;
6, add normal hexane to reactor, open and stir, washing reaction still, under argon shield, n-hexane liquid is loaded in specified containers.
The aluminum concentration obtained by distillation is the output of the zinc ethyl of 130ppm is 95kg, and the zinc concentration obtained by distillation is the output of the diethylaluminum chloride of 530ppm is 159kg.
Comparative example 1
1, argon replaces reactor, pipeline, header tank, receiving tank 2-3 time.Open manhole, under argon shield, drop into zinc chloride 170kg, be heated to 90 DEG C, stop argon gas, drying under reduced pressure 2-4 hour, be cooled to less than 25 DEG C for subsequent use;
2, under argon shield, raw material 292.5kg triethyl aluminum is depressed into triethyl aluminum header tank, by header tank triethyl aluminum under argon shield, put into the reactor of low rate mixing, reactor system automatic heat evolution is slowly warming up to 30-35 DEG C, finishes, be warming up to 40-45 DEG C, react 2 hours;
3, be cooled to less than 30 DEG C, open zinc ethyl distillation valve, underpressure distillation (pressure is-0.08-0.09MPa) zinc ethyl product, slow temperature reaction still, collect the zinc ethyl product of gas phase temperature 30-50 DEG C to zinc ethyl receiving tank; When temperature-measuring port temperature starts to decline, improve temperature of reaction kettle 5 DEG C, underpressure distillation 30 minutes, close zinc ethyl distillation valve, open mixture distillation valve, collect the mixture of a small amount of 50-60 DEG C, cut is analyzed, zinc ethyl quality purity is not less than 99.9%, and aluminium mass concentration is 130ppm;
4, open diethylaluminum chloride distillation valve, opening vacuum to pressure is-0.08-0.09MPa, slow temperature reaction still, collect the diethylaluminum chloride of gas phase temperature 60-150 DEG C to diethylaluminum chloride receiving tank, confirm the distillation end point of good side product chlorinated diethyl aluminum, reactor stops heating, below slow cooling to 50 DEG C, stop vacuum, logical argon gas, continues cooling, analyzes cut, the quality purity of diethylaluminum chloride is not less than 99.9 quality %, and zinc mass concentration is 530ppm;
5,80kg white oil is pressed into white oil header tank, press-in 80kg normal hexane is to normal hexane header tank, stand-by, temperature of reaction kettle is down to less than 25 DEG C, under argon shield, slowly add white oil to reactor, open and stir, washing reaction still still is residual, stops stirring, under argon shield, white oil washings is loaded in specified containers;
6, add normal hexane to reactor, open and stir, washing reaction still, under argon shield, n-hexane liquid is loaded in specified containers.
The aluminum concentration obtained by distillation is the output of the zinc ethyl of 130ppm is 78kg, and the zinc concentration obtained by distillation is the output of the diethylaluminum chloride of 530ppm is 137kg.
Claims (7)
1. a preparation method for zinc ethyl, is characterized in that, comprises the steps:
Under protection of inert gas, under Zr catalyst existent condition, in zinc chloride, add triethyl aluminum react, control temperature of reaction not higher than 60 DEG C, after reacting completely, obtain described zinc ethyl and evaporated mother liquor through underpressure distillation;
Described Zr catalyst is bis cyclopentadienyl zirconium dichloride, and the consumption of described bis cyclopentadienyl zirconium dichloride is 0.01% ~ 1% of triethyl aluminum molar weight.
2. the preparation method of zinc ethyl according to claim 1, is characterized in that, the consumption of described bis cyclopentadienyl zirconium dichloride is 0.01% ~ 0.1% of triethyl aluminum molar weight.
3. the preparation method of zinc ethyl according to claim 1, is characterized in that, described zinc chloride and the mol ratio of triethyl aluminum are 1:1.8 ~ 2.2.
4. the preparation method of zinc ethyl according to claim 1, is characterized in that, described temperature of reaction is 25 ~ 45 DEG C.
5. the preparation method of zinc ethyl according to claim 1, is characterized in that, the pressure of described underpressure distillation is-0.08-0.09MPa;
The temperature of fraction collection is 30 ~ 50 DEG C.
6. the preparation method of zinc ethyl according to claim 1, is characterized in that, carries out further distillation obtain diethylaluminum chloride to described evaporated mother liquor.
7. the preparation method of zinc ethyl according to claim 6, is characterized in that, pressure during distillation diethylaluminum chloride is-0.08-0.09MPa;
The temperature of fraction collection is 60 ~ 150 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310095037.2A CN103145743B (en) | 2013-03-22 | 2013-03-22 | A kind of preparation method of zinc ethyl |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310095037.2A CN103145743B (en) | 2013-03-22 | 2013-03-22 | A kind of preparation method of zinc ethyl |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103145743A CN103145743A (en) | 2013-06-12 |
| CN103145743B true CN103145743B (en) | 2015-08-05 |
Family
ID=48544114
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310095037.2A Active CN103145743B (en) | 2013-03-22 | 2013-03-22 | A kind of preparation method of zinc ethyl |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103145743B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104774214B (en) * | 2015-04-28 | 2016-08-24 | 河南承明光电新材料股份有限公司 | A kind of preparation method of zinc methide |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102015730A (en) * | 2008-04-30 | 2011-04-13 | 日本烷基铝株式会社 | Method for manufacturing dialkyl zinc and dialkyl aluminum monohalide |
-
2013
- 2013-03-22 CN CN201310095037.2A patent/CN103145743B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102015730A (en) * | 2008-04-30 | 2011-04-13 | 日本烷基铝株式会社 | Method for manufacturing dialkyl zinc and dialkyl aluminum monohalide |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103145743A (en) | 2013-06-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2021063930A1 (en) | Process for polymerization of polypropylene using ziegler-natta procatalyst with novel 1,3-diether internal electron donors | |
| Ashby et al. | New, convenient, and stereospecific method for the dehydration of alcohols. Thermal decomposition of magnesium, zinc, and aluminum alkoxides | |
| CA1244044A (en) | Preparation of alkaline earth metal organometallic compounds | |
| CN103012074B (en) | Prepare the method for aromatic methyl ether compound | |
| CN103145743B (en) | A kind of preparation method of zinc ethyl | |
| CN100516010C (en) | Method for preparing 2,6-dimethyl-2-heptanol | |
| CN102020669A (en) | Method for industrially preparing trimethyl gallium | |
| CN108558943B (en) | Method for dissociating methyl phosphine dichloride and aluminum trichloride complex | |
| CN112430280B (en) | Zirconium-based olefin polymerization catalyst and preparation method and application thereof | |
| US4634786A (en) | Hydrocarbon and chlorinated hydrocarbon-soluble magnesium dialkoxides | |
| CN109180490A (en) | The lithium electricity homogeneous production technology of high-purity diethyl carbonate | |
| CN104230662B (en) | A kind of preparation method of high-purity 5N aluminum isopropylate | |
| Benkeser et al. | The first documented reversible addition of allylmagnesium bromide to a ketone | |
| CN104995163B (en) | The low viscosity concentrate solution of alkaline-earth alkoxides in aprotic solvent and preparation method thereof | |
| CN102850299B (en) | Preparation method for (methyl)glycidyl acrylate | |
| CN105111039A (en) | Preparation method of chloroisopentene | |
| CN103483151A (en) | Ebanol preparation method | |
| CN108530492A (en) | A kind of bridged binuclear metallocene compound and the preparation method and application thereof | |
| JP6038375B1 (en) | Catalyst production method | |
| CN102020670B (en) | Method for industrially preparing triethyl gallium | |
| CN1962670A (en) | Tetrabutyl tin preparation method | |
| CN110041354A (en) | A kind of synthetic method of four penta phenyl fluoride borons acid potassium salt | |
| CN215996573U (en) | A preparation system that is used for methyl sesqui aluminium to react with phosphorus trichloride | |
| CN101555254B (en) | Preparation method of methyl-magnesium chloride | |
| CN102276421A (en) | Method for preparing 2-substituted-2-adamantane alcohol compound |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 312369, No. three, No. 2, Shangyu Industrial Park, Beizhen, Shaoxing, Zhejiang, Shangyu Patentee after: Shangyu Shaoxing Warren Chemical Co., Ltd. Address before: 312369, No. three, No. 2, Shangyu Industrial Park, Beizhen, Shaoxing, Zhejiang, Shangyu Patentee before: Shangyu Hualun Chemical Co., Ltd. |