CN108358756A - A kind of method of purification of 3- methyl-3-butene-1-alcohols - Google Patents
A kind of method of purification of 3- methyl-3-butene-1-alcohols Download PDFInfo
- Publication number
- CN108358756A CN108358756A CN201810131833.XA CN201810131833A CN108358756A CN 108358756 A CN108358756 A CN 108358756A CN 201810131833 A CN201810131833 A CN 201810131833A CN 108358756 A CN108358756 A CN 108358756A
- Authority
- CN
- China
- Prior art keywords
- methyl
- tower
- alcohol
- butene
- solvent
- 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.)
- Granted
Links
Classifications
-
- 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
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
- C07C29/84—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation by extractive distillation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of method of purification of 3 methyl, 3 butylene, 1 alcohol, this method is detached by adding solvent using extraction and distillation technology；The solvent added is high boiling fat alkane or the fat alkane containing fatty alcohol；Solvent upper region from rectifying column is added, and the raw material containing 3 methyl, 3 butylene, 1 alcohol and isoamyl alcohol is added from the central region of rectifying column；Bottom liquid is gasified partially liq by a heater, and obtained gas is returned from the gas phase import of bottom of tower in tower；The gas of tower top is sent after a condenser is all condensed into liquid to return tank of top of the tower, then is sent into partially liq in tower from the refluxing opening of tower top by reflux pump.Rectifying column operates at reduced pressure conditions, and tower top obtains 3 methyl, 3 butylene, 1 alcohol sterling, and bottom of tower is the mixture of isoamyl alcohol and solvent.The advantages of this method is that the solvent used is relatively stablized at high temperature, and obtains 3 methyl, 3 butylene, 1 alcohol product from tower top and be conducive to avoid the autohemagglutination of product to lose.
Description
Invention field
The invention belongs to the separation fields of fine chemistry industry water reducer midbody, are related to a kind of by adding solvent to extract essence
Evaporate the method that enol is separated and purified from enol and saturation alcohol mixture for means.
Background technology
3- methyl-3-butene-1-alcohols are a kind of water reducer midbodies, can further be synthesized by hysomer again different
Pentenol（3-M2BOL）.In hysomer, part 3- first is also had in addition to mainly obtaining prenol
Base -3- butene-1-ols are converted into isoamyl alcohol.In order to obtain higher prenol yield, needed in production by 3- methyl -3- fourths
Alkene -1- alcohol is detached with isoamyl alcohol.Since the boiling point of 3- methyl-3-butene-1-alcohols and isoamyl alcohol is sufficiently close to, conventional point
It is all extremely difficult to ideal separating effect from means, exploitation is needed to efficiently separate method.
Detaching the conventional method of alkane and alkene mixture can use extraction fractional distillation, generally use ethylene glycol, dimethyl sub-
The intensive polar solvents such as sulfone, DMAC N,N' dimethyl acetamide are extractant.Such solvent and unsaturated bond interaction force are stronger, are dividing
From when be easier to be combined into rectifying column bottom with alkene and obtain high-purity alkane from tower top, in butadiene, isoprene
Deng separation field have been widely used.Since alkene enters rectifying column bottom with solvent, the temperature of bottom of tower is again often higher,
The problems such as yield declines, equipment blocks is be easy to cause for the unsaturated hydrocarbons of easy autohemagglutination, when using nitrogenous or sulfur-bearing molten
There is also the unfavorable factors such as solvent pyrolytic when agent.
For containing easily from the separation problem of polyolefin, a suitable possible alternative is that selection interacts with saturated bond
Stronger solvent makes easily to enter tower top, but the generally more difficult selection of this kind of solvent from polyolefin as volatile components.The present invention is
From the angle for improving dicyandiamide solution, a kind of method of purification of 3- methyl-3-butene-1-alcohols is proposed.By selecting low polarity
For example high boiling fat alkane of solvent or the fat alkane containing fatty alcohol, so that solvent is more easy to the isoamyl with not carbon-carbon double bonds
Alcohol phase combines into bottom of tower, and the 3- methyl-3-butene-1-alcohols containing carbon-carbon double bond are quickly isolated from tower top.Secondly,
Operation temperature is further decreased in conjunction with decompression operation, is conducive to inhibit the autohemagglutination of 3- methyl-3-butene-1-alcohols and improve product receipts
Rate.
Invention content
The technical problem to be solved in the present invention is to provide a kind of methods of purification of 3- methyl-3-butene-1-alcohols.
The purpose of the present invention is achieved through the following technical solutions：This approach includes the following steps：
The purification of 3- methyl-3-butene-1-alcohols carries out in an extractive distillation column, and rectifying column operates at reduced pressure conditions；Height boiling
Upper region is added from rectifying column at a certain temperature for the fat alkane of point or the fat alkane containing fatty alcohol, contains 3-
The raw material of methyl-3-butene-1-alcohol and isoamyl alcohol is added from the central region of rectifying column at a certain temperature；Bottom liquid is logical
It crosses a heater partially liq gasifies, obtained gas is returned from the gas phase import of bottom of tower in tower；The gas of tower top is cold through one
Condenser is sent after being all condensed into liquid to return tank of top of the tower, then by reflux pump by certain reflux ratio by partially liq from tower top
Refluxing opening be sent into tower in.Extra liquid is that 3- methyl-3-butene-1-alcohol sterlings are discharged out of tank and send to production in return tank
Product tank, remaining liquid is that the mixture of isoamyl alcohol and solvent carries out later separation again after the discharge of bottom of tower after the heating of bottom of tower.
Further, the rectifying column operating pressure is -0.095 ~ -0.07MPa.
Further, the higher boiling fat alkane is n-dodecane, and fatty alcohol is n-octyl alcohol or n-nonyl alcohol, feeding temperature
It is 75 ~ 100 DEG C.
Further, the mass fraction of fatty alcohol is 0 ~ 0.2 in the solvent, and solvent quality flow is material quality flow
4 ~ 8 times.
Further, the material temperature containing 3- methyl-3-butene-1-alcohols and isoamyl alcohol is room temperature.
Further, the number of theoretical plate of the rectifying column is 45 ~ 75 pieces.
Further, the reflux ratio of the rectifying column tower top operation is 4 ~ 10:1.
Further, the feedboard of the solvent is the 8th ~ 14 piece of theoretical plate.
Further, the feedboard of the raw material is the 25th ~ 45 piece of theoretical plate.
The beneficial effects of the present invention are：
（1）The present invention uses high boiling fat alkane or fat alkane containing fatty alcohol for solvent, is conducive to and isoamyl alcohol
It is combined by being operated into rectifying column bottom step by step, and quickly obtains 3- methyl-3-butene-1-alcohol sterlings from tower top.
（2）The present invention uses in fat alkane solvent and fatty alcohol is added, and is conducive to enhance dissolving each other for separation system and solvent
Property, improve the separative efficiency operated step by step.
（3）The present invention advantageously reduces the operation temperature of separation system using decompression operation, reduces 3- methyl -3- butylene -
The autohemagglutination of 1- alcohol loses.
（4）The dicyandiamide solution thermal stability that the present invention uses is higher, is conducive to the decomposition penalty that long-term production reduces solvent.
Description of the drawings
Fig. 1 is the process flow diagram of the present invention；
In figure, 1- solvents, 2- solvent heaters, 3- solvent inlets, 4- raw materials, 5- material inlets, 6- overhead condensers, 7- reflux
Tank, 8- reflux pumps, the import of 9- phegmas, 10- overhead products, 11- products pots, the bottoms of tower 12- heater, the import of 13- gas phases, 14-
Kettle liquid pump, 15- bottom products.
Specific implementation mode
A kind of method of purification of 3- methyl-3-butene-1-alcohols proposed by the present invention, includes the following steps：
Purifying in an extractive distillation column shown in Fig. 1 for 3- methyl-3-butene-1-alcohols carries out, and rectifying column is at reduced pressure conditions
Operation；High boiling fat alkane or fat alkane solvent 1 containing fatty alcohol are heated to certain temperature by solvent heater 2
The solvent inlet 3 in upper region is added from rectifying column afterwards, and the raw material 4 containing 3- methyl-3-butene-1-alcohols and isoamyl alcohol is certain
At a temperature of from the material inlet 5 of rectifying column central region be added；Bottom liquid is gasified partially liq by bottom of tower heater 12,
Obtained gas is returned from the gas phase import 13 of bottom of tower in tower；The gas of tower top is after overhead condenser 6 is all condensed into liquid
It send to return tank of top of the tower 7, then is sent into partially liq from the phegma import 9 of tower top by certain reflux ratio by reflux pump 8
In tower.Extra liquid is overhead product 10 in return tank 7（High-purity 3- methyl-3-butene-1-alcohols）It is discharged and send out of tank
To products pot 11, remaining liquid is bottom product 15 after the heating of bottom of tower（The mixture of isoamyl alcohol and solvent）14 rows are pumped through kettle liquid
Later separation is carried out after going out again.
Further, the rectifying column operating pressure is -0.095 ~ -0.07MPa.
Further, the higher boiling fat alkane is n-dodecane, and fatty alcohol is n-octyl alcohol or n-nonyl alcohol, feeding temperature
It is 75 ~ 100 DEG C.
Further, the mass fraction of fatty alcohol is 0 ~ 0.2 in the solvent, and solvent quality flow is material quality flow
4 ~ 8 times.
Further, the material temperature containing 3- methyl-3-butene-1-alcohols and isoamyl alcohol is room temperature.
Further, the number of theoretical plate of the rectifying column is 45 ~ 75 pieces.
Further, the reflux ratio of the rectifying column tower top operation is 4 ~ 10:1.
Further, the feedboard of the solvent is the 8th ~ 14 piece of theoretical plate.
Further, the feedboard of the raw material is the 25th ~ 45 piece of theoretical plate.
Below by specific embodiment, the invention will be further described, and raw material is by 30 DEG C of down-offs in embodiment
The material of 500kg/h（Methyl-3-butene-1-alcohol containing 3- 75% contains isoamyl alcohol 25%, and wt% is similarly hereinafter）On the basis of, but should not be by this
Invention is interpreted as being only applicable to case as described below.
Embodiment 1
As shown in Fig. 1, extractive distillation column tower top pressure is -0.075MPa, and total number of theoretical plate is 68, and solvent inlet is the 12nd piece
Theoretical version, material inlet are the 28th piece of theoretical plate.Solvent is pure dodecane, solvent flux 2500kg/h（For material quality
5 times of flow）, solvent feed temperature is 90 DEG C.Operating reflux ratio is 8.
The overhead product flow obtained after stable operation is 378kg/h（Methyl-3-butene-1-alcohol containing 3- 98.94%, containing different
Amylalcohol 0.98% contains solvent 0.08%）；Obtained bottom product flow is 2622kg/h（Methyl-3-butene-1-alcohol containing 3-
0.04%, contain isoamyl alcohol 4.63%, contains solvent 95.34%）.
It is 99.73% to be computed yield of the 3- methyl-3-butene-1-alcohols in overhead product, and isoamyl alcohol is in bottom product
Yield be 97.04%.
Embodiment 2
As shown in Fig. 1, extractive distillation column tower top pressure is -0.09MPa, and total number of theoretical plate is 50, and solvent inlet is the 8th piece of reason
By version, material inlet is the 25th piece of theoretical plate.Contain n-octyl alcohol 10% in solvent（Remaining is n-dodecane）, solvent flux is
2500kg/h（It is 5 times of material quality flow）, solvent feed temperature is 80 DEG C.Operating reflux ratio is 5.
The overhead product flow obtained after stable operation is 376.5kg/h（Methyl-3-butene-1-alcohol containing 3- 99.29%, contains
Isoamyl alcohol 0.57% contains solvent 0.14%）；Obtained bottom product flow is 2623.5kg/h（Methyl-3-butene-1-alcohol containing 3-
0.04%, contain isoamyl alcohol 4.68%, contains solvent 95.27%）.
It is 99.69% to be computed yield of the 3- methyl-3-butene-1-alcohols in overhead product, and isoamyl alcohol is in bottom product
Yield be 98.28%.
Embodiment 3
As shown in Fig. 1, extractive distillation column tower top pressure is -0.085MPa, and total number of theoretical plate is 75, and solvent inlet is the 14th piece
Theoretical version, material inlet are the 45th piece of theoretical plate.Contain n-octyl alcohol 15% in solvent（Remaining is n-dodecane）, solvent flux is
2000kg/h（It is 4 times of material quality flow）, solvent feed temperature is 85 DEG C.Operating reflux ratio is 6.
The overhead product flow obtained after stable operation is 377kg/h（Methyl-3-butene-1-alcohol containing 3- 99.37%, containing different
Amylalcohol 0.59% contains solvent 0.04%）；Obtained bottom product flow is 2123kg/h（Methyl-3-butene-1-alcohol containing 3-
0.02%, contain isoamyl alcohol 5.78%, contains solvent 94.20%）.
It is 99.90% to be computed yield of the 3- methyl-3-butene-1-alcohols in overhead product, and isoamyl alcohol is in bottom product
Yield be 98.22%.
Embodiment 4
As shown in Fig. 1, extractive distillation column tower top pressure is -0.07MPa, and total number of theoretical plate is 60, and solvent inlet is the 10th piece
Theoretical version, material inlet are the 30th piece of theoretical plate.Contain n-octyl alcohol 20% in solvent（Remaining is n-dodecane）, solvent flux is
4000kg/h（It is 8 times of material quality flow）, solvent feed temperature is 95 DEG C.Operating reflux ratio is 10.
The overhead product flow obtained after stable operation is 377kg/h（Methyl-3-butene-1-alcohol containing 3- 98.98%, containing different
Amylalcohol 0.77% contains solvent 0.25%）；Obtained bottom product flow is 4123kg/h（Methyl-3-butene-1-alcohol containing 3-
0.04%, contain isoamyl alcohol 2.96%, contains solvent 96.99%）.
It is 99.51% to be computed yield of the 3- methyl-3-butene-1-alcohols in overhead product, and isoamyl alcohol is in bottom product
Yield be 97.67%.
Embodiment 5
As shown in Fig. 1, extractive distillation column tower top pressure is -0.08MPa, and total number of theoretical plate is 68, and solvent inlet is the 12nd piece
Theoretical version, material inlet are the 30th piece of theoretical plate.Solvent is pure dodecane, solvent flux 2500kg/h（For material quality
5 times of flow）, solvent feed temperature is 90 DEG C.Operating reflux ratio is 7.
The overhead product flow obtained after stable operation is 377kg/h（Methyl-3-butene-1-alcohol containing 3- 99.31%, containing different
Amylalcohol 0.63% contains solvent 0.07%）；Obtained bottom product flow is 2623kg/h（Methyl-3-butene-1-alcohol containing 3-
0.02%, contain isoamyl alcohol 4.68%, contains solvent 95.30%）.
It is 99.83% to be computed yield of the 3- methyl-3-butene-1-alcohols in overhead product, and isoamyl alcohol is in bottom product
Yield be 98.11%.
Embodiment 6
As shown in Fig. 1, extractive distillation column tower top pressure is -0.094MPa, and total number of theoretical plate is 45, and solvent inlet is the 9th piece
Theoretical version, material inlet are the 25th piece of theoretical plate.Contain n-octyl alcohol 5% in solvent（Remaining is n-dodecane）, solvent flux is
3000kg/h（It is 6 times of material quality flow）, solvent feed temperature is 75 DEG C.Operating reflux ratio is 4.
The overhead product flow obtained after stable operation is 377kg/h（Methyl-3-butene-1-alcohol containing 3- 99.07%, containing different
Amylalcohol 0.86% contains solvent 0.07%）；Obtained bottom product flow is 3123kg/h（Methyl-3-butene-1-alcohol containing 3-
0.05%, contain isoamyl alcohol 3.90%, contains solvent 96.05%）.
It is 99.60% to be computed yield of the 3- methyl-3-butene-1-alcohols in overhead product, and isoamyl alcohol is in bottom product
Yield be 97.41%.
Claims (9)
1. a kind of method of purification of 3- methyl-3-butene-1-alcohols, which is characterized in that this approach includes the following steps：3- methyl-
The purification of 3- butene-1-ols carries out in an extractive distillation column, and rectifying column operates at reduced pressure conditions；High boiling fat alkane
Or upper region is added the fat alkane containing fatty alcohol from rectifying column at a certain temperature, contains 3- methyl -3- butylene -
The raw material of 1- alcohol and isoamyl alcohol is added from the central region of rectifying column at a certain temperature；Bottom liquid will by a heater
Partially liq gasifies, and obtained gas is returned from the gas phase import of bottom of tower in tower；The gas of tower top is all condensed through a condenser
Partially liq is sent into from the refluxing opening of tower top by certain reflux ratio at being sent to return tank of top of the tower after liquid, then by reflux pump
In tower；
Extra liquid is that 3- methyl-3-butene-1-alcohol sterlings are discharged out of tank and send to products pot in return tank, bottom of tower heating
Remaining liquid is that the mixture of isoamyl alcohol and solvent carries out later separation again after the discharge of bottom of tower afterwards.
2. the method for purification of 3- methyl-3-butene-1-alcohols according to claim 1, which is characterized in that the rectifying column
Operating pressure is -0.095 ~ -0.07MPa.
3. the method for purification of 3- methyl-3-butene-1-alcohols according to claim 1, which is characterized in that the higher boiling fat
Fat alkane is n-dodecane, and fatty alcohol is n-octyl alcohol or n-nonyl alcohol, and feeding temperature is 75 ~ 100 DEG C.
4. the method for purification of 3- methyl-3-butene-1-alcohols according to claim 1, which is characterized in that fat in the solvent
The mass fraction of fat alcohol is 0 ~ 0.2, and solvent quality flow is 4 ~ 8 times of material quality flow.
5. the method for purification of 3- methyl-3-butene-1-alcohols according to claim 1, which is characterized in that described to be detached
Material temperature is room temperature.
6. the method for purification of 3- methyl-3-butene-1-alcohols according to claim 1, which is characterized in that the rectifying column
Number of theoretical plate is 45 ~ 75 pieces.
7. the method for purification of 3- methyl-3-butene-1-alcohols according to claim 1, which is characterized in that the rectifying tower
The reflux ratio of top operation is 4 ~ 10:1.
8. the method for purification of 3- methyl-3-butene-1-alcohols according to claim 1, which is characterized in that the solvent into
Flitch is the 8th ~ 14 piece of theoretical plate.
9. the method for purification of 3- methyl-3-butene-1-alcohols according to claim 1, which is characterized in that the raw material into
Flitch is the 25th ~ 45 piece of theoretical plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810131833.XA CN108358756B (en) | 2018-02-09 | 2018-02-09 | Purification method of 3-methyl-3-butene-1-ol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810131833.XA CN108358756B (en) | 2018-02-09 | 2018-02-09 | Purification method of 3-methyl-3-butene-1-ol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108358756A true CN108358756A (en) | 2018-08-03 |
| CN108358756B CN108358756B (en) | 2021-09-28 |
Family
ID=63005378
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810131833.XA Active CN108358756B (en) | 2018-02-09 | 2018-02-09 | Purification method of 3-methyl-3-butene-1-ol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108358756B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111377798A (en) * | 2018-12-31 | 2020-07-07 | 江苏苏博特新材料股份有限公司 | Purification equipment and process of 3-methyl-3-buten-1-ol |
| CN111377799A (en) * | 2018-12-31 | 2020-07-07 | 江苏苏博特新材料股份有限公司 | 3-methyl-3-butene-1-ol dehydration method and device thereof |
| CN114315515A (en) * | 2022-01-19 | 2022-04-12 | 万华化学集团股份有限公司 | Recycling method of 3-methyl-3-butenol process by-product |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5069756A (en) * | 1990-11-26 | 1991-12-03 | Lloyd Berg | Separation of cyclohexane from cyclohexene by azeotropic or extractive distillation |
| US5851362A (en) * | 1997-05-27 | 1998-12-22 | Berg; Lloyd | Separation of 4-methyl-2-pentanol from 3-methyl-1-butanol by extractive distillation |
| CN105949036A (en) * | 2016-05-24 | 2016-09-21 | 济南大学 | Separation method of propyl alcohol-allyl alcohol mixture |
-
2018
- 2018-02-09 CN CN201810131833.XA patent/CN108358756B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5069756A (en) * | 1990-11-26 | 1991-12-03 | Lloyd Berg | Separation of cyclohexane from cyclohexene by azeotropic or extractive distillation |
| US5851362A (en) * | 1997-05-27 | 1998-12-22 | Berg; Lloyd | Separation of 4-methyl-2-pentanol from 3-methyl-1-butanol by extractive distillation |
| CN105949036A (en) * | 2016-05-24 | 2016-09-21 | 济南大学 | Separation method of propyl alcohol-allyl alcohol mixture |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111377798A (en) * | 2018-12-31 | 2020-07-07 | 江苏苏博特新材料股份有限公司 | Purification equipment and process of 3-methyl-3-buten-1-ol |
| CN111377799A (en) * | 2018-12-31 | 2020-07-07 | 江苏苏博特新材料股份有限公司 | 3-methyl-3-butene-1-ol dehydration method and device thereof |
| CN111377799B (en) * | 2018-12-31 | 2022-12-02 | 江苏苏博特新材料股份有限公司 | 3-methyl-3-butene-1-ol dehydration method and device thereof |
| CN111377798B (en) * | 2018-12-31 | 2022-12-02 | 江苏苏博特新材料股份有限公司 | Purification equipment and process of 3-methyl-3-butene-1-ol |
| CN114315515A (en) * | 2022-01-19 | 2022-04-12 | 万华化学集团股份有限公司 | Recycling method of 3-methyl-3-butenol process by-product |
| CN114315515B (en) * | 2022-01-19 | 2022-11-08 | 万华化学集团股份有限公司 | Recycling method of 3-methyl-3-butenol process by-product |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108358756B (en) | 2021-09-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| RU2396242C2 (en) | Method of methanol recuperation | |
| CN108358756A (en) | A kind of method of purification of 3- methyl-3-butene-1-alcohols | |
| CN105814029B (en) | With the relevant improvement of oxide purification | |
| CN106518640B (en) | A kind of method that cyclohexanone product efficiently separates purification | |
| CN103432761B (en) | Be separated the rectificating method of dichloro-benzenes isomer | |
| CN1454181A (en) | Method for producing concentrated nitric acid and installation for carrying out a method of this type | |
| CN103288601B (en) | Cyclohexanol distillation method | |
| CN107137949B (en) | Extraction and rectification partition plate tower device and method for dehydrating low-concentration isopropanol solution | |
| CN103484154A (en) | Condensed water stripped crude oil stabilization method and special device thereof | |
| CN107011172A (en) | A kind of utilization partition tower refines the method and device of vinyl acetate | |
| CN104447267B (en) | A kind of Separation of Benzene ethyl ketone, method of alpha-phenyl ethyl alcohol from 1-Phenylethanone. and alpha-phenyl ethyl alcohol mixture | |
| CN108383687A (en) | A kind of purification rectifying column and method of purification for 3- methyl-3-butene-1-alcohols | |
| CN106512462A (en) | Turpentine continuous rectification device | |
| CN106242948A (en) | A kind of it is thermally integrated variable-pressure rectification separation n-butyl alcohol and the method for octane azeotropic mixture | |
| JPH0475913B2 (en) | ||
| CN1024537C (en) | Method for extracting chloralkane from by-product chlorine oil | |
| CN206334372U (en) | A kind of turpentine oil continuous rectification apparatus | |
| CN113248469B (en) | Trioxymethylene recovery system and process | |
| CN107488094A (en) | A kind of ibuprofen sodium salt centrifuge mother liquor petrochina ether recovery process and device | |
| US9598394B2 (en) | Method of producing trioxane | |
| CN104829452B (en) | Energy-saving production system of ethyl acetate and corresponding energy-saving production technology | |
| CN109771980B (en) | Heterogeneous azeotropic rectification method for separating mixture of 2-pentanone, 4-heptanone, water and carbon dioxide | |
| CN105582811B (en) | A kind of purification of raw materials method for Separation of Boron Isotopes | |
| CN208482029U (en) | Butene-1 separator | |
| CN111643918A (en) | Rectification purification device and purification method for multi-component material |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20210701 Address after: 261313 No.1, Chengtai Road, Binhai (Xiaying) Economic Development Zone, Changyi City, Weifang City, Shandong Province Applicant after: Shandong Chengtai New Materials Co.,Ltd. Address before: 261300 Changyi Binhai (Xiaying) Economic Development Zone, Weifang City, Shandong Province Applicant before: SHANDONG CHENGTAI CHEMICAL Co.,Ltd. |
|
| TA01 | Transfer of patent application right | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |