CN104672059A - Production method of neopentyl glycol - Google Patents
Production method of neopentyl glycol Download PDFInfo
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- CN104672059A CN104672059A CN201510057499.4A CN201510057499A CN104672059A CN 104672059 A CN104672059 A CN 104672059A CN 201510057499 A CN201510057499 A CN 201510057499A CN 104672059 A CN104672059 A CN 104672059A
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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
- C07C29/36—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by reactions with formation of hydroxy groups, which may occur via intermediates being derivatives of hydroxy, e.g. O-metal
- C07C29/38—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by reactions with formation of hydroxy groups, which may occur via intermediates being derivatives of hydroxy, e.g. O-metal by reaction with aldehydes or ketones
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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
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to the technical field of chemical production, and particularly relates to a production method of neopentyl glycol. The production method of the neopentyl glycol comprises the following three steps: condensation, evaporation and distillation, and specifically comprises the following steps: with isobutyraldehyde and formaldehyde as raw materials, carrying out condensation reaction; adding alkali in the reaction process, warming for the second time, evaporating through an evaporator, and separating the neopentyl glycol from other substances; and finally obtaining a finished product neopentyl glycol by distillation. Compared with the methods disclosed by the prior art and background art, the method provided by the invention is low in energy consumption, and simple in technology; and the product is good in quality and low in investment cost.
Description
Technical field
The invention belongs to chemical production technical field, be specifically related to a kind of production method of neopentyl glycol.
Background technology
Along with the development of society and the raising of people's level of consumption, people are to the pay attention to day by day of environment, power saving.Since entering the nineties, energy-conservation, oligosaprobic powder and high solidity coating grow up abroad very soon, and have the trend replacing solvent based coating.In recent years, China's powder coating device also follows international trend closely, or joint introduction, or builds voluntarily, its tempo is swift and violent, but as the important source material neopentyl glycol of powder coating, due to the impact by raw material and technical elements, its development relatively lags behind, all need a large amount of import neopentyl glycol every year, substantially occurred the situation that supply falls short of demand, therefore this production development has a extensive future, and market potential is huge.
Neopentyl glycol is of many uses, is mainly used in the productions such as vibrin, urethane resin, synthetic lubricant, softening agent, and its derivative is widely used in the fields such as automobile, weaving, medicine, coating, agricultural chemicals, plastics and oil.U.S., day etc., country was all devoted to the Application and Development of frontier.But current is manufacture oil-free alkyd resin in China's main application, particularly unsaturated polyester powder coating, owing to having one in molecule, dimethyl structure, not having hydrogen atom on B position, this coating is made to have excellent hydrolytic resistance, ageing resistance, thermostability, weathering resistance and erosion resistance.The characteristicness of its paint film for not only splitting, not yellowing, less than other resin, also have good sticking power to metal.Therefore, be widely used in the industries such as the higher bike of appearance requirement, automobile, household electrical appliances, material of construction.
CN102304021 discloses " a kind of method preparing neopentyl glycol ", comprises the steps:
1) the solution organic solvent diluting containing hydroxy pivalin aldehyde is obtained hydrogenating materials; Contain in described hydrogenating materials
The hydroxy pivalin aldehyde of 18 ~ 42wt% and the organic solvent of 35 ~ 75wt%;
2) under the effect of hydrogenation catalyst, the hydrogenating materials that step 1) is obtained and hydrogen carry out hydrogenation reaction, and acquisition contains
The solution of product neopentyl glycol; Containing copper, zinc and aluminium three kinds of metallic elements in described hydrogenation catalyst, or containing copper, zinc, aluminium and manganese four kinds of metallic elements;
The described solution containing hydroxy pivalin aldehyde obtains by the following method: in the presence of triethyl amine, make isobutyric aldehyde and formalin
Solution carries out aldolization, and the hydroxy pivalin aldehyde reaction solution having reacted rear formation is the described solution containing hydroxy pivalin aldehyde;
Described hydrogenation reaction adopts continuous processing to carry out, and the temperature of described hydrogenation reaction is 120 ~ 150 DEG C, and pressure is 3 ~
4MPa, the mass space velocity of hydroxy pivalin aldehyde is 0.4 ~ 2.2g/gcat/hr;
Described containing in the catalyzer of copper, zinc and aluminium three kinds of metallic elements comprises cupric oxide, zinc oxide and aluminum oxide three kinds of components;
Wherein: the mol ratio of copper and aluminium is 1.0 ~ 1.5:1.2 ~ 1.8; The mol ratio of copper and zinc is 1.0 ~ 1.5:0.5 ~ 0.8;
The described catalyzer containing copper, zinc, aluminium and manganese four kinds of metallic elements comprises the component of following weight percentage: cupric oxide 20% ~ 50%, zinc oxide 20% ~ 40%, aluminum oxide 20% ~ 40%, manganese oxide 1% ~ 10%;
Described organic solvent is selected from one or more the mixing in methyl alcohol, ethanol, n-propyl alcohol, Virahol, propyl carbinol and isopropylcarbinol.
CN 101863738 B discloses " a kind of preparation method of neopentyl glycol ", the method comprises the following steps: (1) is by formalin, isobutyric aldehyde and catalyst mix, under protection of inert gas, make isobutyric aldehyde and formaldehyde condensation reaction, obtain the solution being dissolved with hydrogenation of hydroxypentylaldehyd; (2) by solution decompression obtained in (1) distillation, the concentrated solution of hydrogenation of hydroxypentylaldehyd is obtained; (3) in concentrated solution, add anhydrous methanol and copper-based catalysts, hydrogenation is carried out to hydrogenation of hydroxypentylaldehyd, obtain the mixture comprising neopentyl glycol; (4) obtained in purification (3) mixture, obtains neopentyl glycol solution; (5) by after neopentyl glycol solution decompression obtained in (4) distillation, neopentyl glycol crude product is obtained; (6) heat the neopentyl glycol that neopentyl glycol crude product obtains gaseous state, can target product be obtained by after the neopentyl glycol condensation of gaseous state.The method waste water generation is little, good product quality, and yield is high, and power consumption is few.
CN103351277A discloses a kind of preparation method of neopentyl glycol, comprises the following steps:
1) by formaldehyde and isobutyric aldehyde, the condensated liquid being rich in the special valeral of hydroxyl is prepared in condensation under the effect of basic catalyst;
2) by step 1) condensated liquid prepared contacts with the first hydrogenation catalyst in first paragraph hydrogenator, and and hydrogen
Gas carries out first paragraph hydrogenation reaction, obtains the first hydrogenation reaction solution; The first described hydrogenation catalyst contains 20-50wt%
CuO, Al2O3 and/or ZrO2 of the MnO of 10-30wt %, 15-40wt %, CdO and/or ZnO of 1-15wt %,
The In2O3 of 0.1-1wt%, and CeO2 and/or Nd2O3 of 0.1-3wt%, based on total restatement of catalyzer;
3) step 2) in the first hydrogenation reaction solution contact with the second hydrogenation catalyst in second segment hydrogenator, and with
Hydrogen carries out second segment hydrogenation reaction, obtains the second hydrogenation reaction solution of neopentyl glycol containing; The second described hydrogenation catalyst contains
There is the CuO of 10-35wt%, ZrO2 and/or TiO2 of the ZnO of the MnO of 10-25wt%, 10-25wt%, 20-45wt%,
The Y2O3 of 1-15wt%, and the In2O3 of 0.1-1wt%, based on total restatement of catalyzer.
Its shortcoming of above-mentioned method is, infusion of financial resources is large, and technique is comparatively loaded down with trivial details.Therefore, need to improve for above-mentioned method, design the low and production method of the better simply neopentyl glycol of technique of a kind of cost.
Summary of the invention
In order to solve above-mentioned technical problem, the invention provides the low and production method of the better simply neopentyl glycol of technique of a kind of cost.
The present invention is realized by following technical scheme:
A production method for neopentyl glycol, above-mentioned method comprises following step:
(1) condensation
With isobutyric aldehyde and formaldehyde for raw material, the volume ratio that feeds intake of described isobutyric aldehyde and formaldehyde is 1:15-19;
Prepare raw material, described raw material is placed in reaction kettle for reaction, obtains reaction soln, the temperature controlled in reactor is no more than 40 DEG C, limit coronite at the uniform velocity add alkali, make the pH of reaction soln be 13.0-13.5 after adding alkali; After adding alkali, reaction soln in reactor is stirred, open the batch turning valve of reactor, material is inputted intensification still, be warming up to 50-58 DEG C, keep 1.5-2.5 hour at this temperature, carry out second time again to heat up, keep 1.0-2.0 hour after rising to 65-75 DEG C, the pH value being neutralized to solution with formic acid is 6.8-7.2, then it is for subsequent use that reacted condensation solution is transferred to storage tank;
(2) evaporate
The condensation solution prepared in step (1) is squeezed in vaporizer, when liquid level reaches the tubulation 30-35cm of vaporizer,
Start to heat up, keep vacuum tightness at-0.08Mpa, when reaching 95 DEG C, open spray water;
In evaporative process, neopentyl glycol in condensation solution and water rise to evaporator tower in a gaseous form, after the condensation of tower top spray water, because water is different with the boiling point of neopentyl glycol, neopentyl glycol solution falls into evaporating kettle, and the impurity such as high boiling material and sodium formiate is in continuous evaporative process, with the form crystallization of supersaturated solution, be stored in base of evaporator, centrifugation, and obtain sodium formiate;
Neopentyl glycol solution in evaporating kettle is warming up to 120 DEG C after flowing into concentration kettle, keeps vacuum tightness to be-0.008 Mpa, uses in order to still kettle;
(3) distill
The concentrated solution heated up is transferred to still kettle, heats up, when pot temperature reaches 150-160 DEG C, maintenance vacuum tightness is-0.078Mpa, product is inputted finished product still, opens temperature lowering water simultaneously, and the temperature controlling material is between 135-140 DEG C, vacuum tightness is 0.086Mpa;
When finished product still material reaches 2/3, be switched to another finished product still, material neopentyl glycol be placed on steel band and carry out scraping blade packaging.
Preferably, above-mentioned alkali is NaOH.
In above-mentioned step (2), the rotating speed of centrifugation is 200-800rmp.
Fusing point 124-130 DEG C of above-mentioned neopentyl glycol, boiling point 210 DEG C, density 1.06, flash-point 129 DEG C.
The color and luster < 15 of above-mentioned neopentyl glycol, free acid < 0.05, moisture≤0.5, hydroxy radical content >=31.8.
The volume ratio that feeds intake of above-mentioned isobutyric aldehyde and formaldehyde is 1:17.
In above-mentioned step (1), with isobutyric aldehyde and formaldehyde for raw material, the volume ratio that feeds intake of described isobutyric aldehyde and formaldehyde is 1:17;
Prepare raw material, described raw material is placed in reaction kettle for reaction, obtains reaction soln, the temperature controlled in reactor is no more than 40 DEG C, limit coronite at the uniform velocity add alkali, make the pH of reaction soln be 13.0 after adding alkali; After adding alkali, reaction soln in reactor is stirred, open the batch turning valve of reactor, material is inputted intensification still, be warming up to 55 DEG C, keep 2 hours at this temperature, carry out second time again to heat up, keep 1.5 hours after rising to 70 DEG C, the pH value being neutralized to solution with formic acid is 7.0, then it is for subsequent use that reacted condensation solution is transferred to storage tank.
In above-mentioned step (3), the concentrated solution heated up is transferred to still kettle, heat up, when pot temperature reaches 155 DEG C, maintenance vacuum tightness is-0.078Mpa, product is inputted finished product still, opens temperature lowering water simultaneously, and the temperature controlling material is between 135-140 DEG C, vacuum tightness is 0.086Mpa.
Relative to the method disclosed in prior art and background technology, method energy consumption of the present invention is low, and technique is simple, and good product quality, cost of investment is low.
Embodiment
Below in conjunction with specific embodiment, the present invention is further described, so that those skilled in the art more understands the present invention, but does not therefore limit the present invention.
Embodiment 1
The production method of neopentyl glycol comprises following step:
(1) condensation
With isobutyric aldehyde and formaldehyde for raw material, the volume ratio that feeds intake of described isobutyric aldehyde and formaldehyde is 1:17;
Prepare raw material, described raw material is placed in reaction kettle for reaction, obtains reaction soln, the temperature controlled in reactor is no more than 40 DEG C, limit coronite at the uniform velocity add NaOH, make the pH of reaction soln be about 13.0 after adding NaOH; After adding NaOH, reaction soln in reactor is stirred, open the batch turning valve of reactor, material is inputted intensification still, be warming up to 55 DEG C, keep 2 hours at this temperature, carry out second time again to heat up, keep 1.5 hours after rising to 70 DEG C, the pH value being neutralized to solution with formic acid is 7.0, then it is for subsequent use that reacted condensation solution is transferred to storage tank;
(2) evaporate
The condensation solution prepared in step (1) is squeezed in vaporizer, when liquid level reaches tubulation about the 30cm of vaporizer,
Start to heat up, keep vacuum tightness at-0.08Mpa, when reaching 95 DEG C, open spray water;
In evaporative process, neopentyl glycol in condensation solution and water rise to evaporator tower in a gaseous form, after the condensation of tower top spray water, because water is different with the boiling point of neopentyl glycol, neopentyl glycol solution falls into evaporating kettle, the impurity such as high boiling material and sodium formiate is in continuous evaporative process, with the form crystallization of supersaturated solution, be stored in base of evaporator, centrifugation, the rotating speed of centrifugation is 200-800rmp, obtains sodium formiate;
Neopentyl glycol solution in evaporating kettle is warming up to 120 DEG C after flowing into concentration kettle, keeps vacuum tightness to be-0.008 Mpa, uses in order to still kettle;
(3) distill
The concentrated solution heated up is transferred to still kettle, heats up, when pot temperature reaches 155 DEG C, maintenance vacuum tightness is-0.078Mpa, product is inputted finished product still, opens temperature lowering water simultaneously, and the temperature controlling material is between 135-140 DEG C, vacuum tightness is 0.086Mpa;
When finished product still material reaches 2/3, be switched to another finished product still, material neopentyl glycol be placed on steel band and carry out scraping blade packaging.
Fusing point 124-130 DEG C of finished product neopentyl glycol, boiling point 210 DEG C, density 1.06, flash-point 129 DEG C.
The color and luster < 15 of neopentyl glycol, free acid < 0.05, moisture≤0.5, hydroxy radical content >=31.8.
Yield of the present invention is for produce 1T neopentyl glycol by the every 0.745T isobutyric aldehyde of isobutyric aldehyde consumption, and quality product is that colourity reaches less than 10, hydroxy radical content more than 32.
Embodiment 2
The production method of neopentyl glycol comprises following step:
(1) condensation
With isobutyric aldehyde and formaldehyde for raw material, the volume ratio that feeds intake of described isobutyric aldehyde and formaldehyde is 1:15;
Prepare raw material, described raw material is placed in reaction kettle for reaction, obtains reaction soln, the temperature controlled in reactor is no more than 40 DEG C, limit coronite at the uniform velocity add NaOH, make the pH of reaction soln be about 13.0 after adding NaOH; After adding NaOH, reaction soln in reactor is stirred, open the batch turning valve of reactor, material is inputted intensification still, be warming up to 50 DEG C, keep 1.5 hours at this temperature, carry out second time again to heat up, keep 1.5 hours after rising to 70 DEG C, the pH value being neutralized to solution with formic acid is 6.8, then it is for subsequent use that reacted condensation solution is transferred to storage tank;
(2) evaporate
The condensation solution prepared in step (1) is squeezed in vaporizer, when liquid level reaches the tubulation 32cm of vaporizer,
Start to heat up, keep vacuum tightness at-0.08Mpa, when reaching 95 DEG C, open spray water;
In evaporative process, neopentyl glycol in condensation solution and water rise to evaporator tower in a gaseous form, after the condensation of tower top spray water, because water is different with the boiling point of neopentyl glycol, neopentyl glycol solution falls into evaporating kettle, the impurity such as high boiling material and sodium formiate is in continuous evaporative process, with the form crystallization of supersaturated solution, be stored in base of evaporator, centrifugation, the rotating speed of centrifugation is 200-800rmp, obtains sodium formiate;
Neopentyl glycol solution in evaporating kettle is warming up to 120 DEG C after flowing into concentration kettle, keeps vacuum tightness to be-0.008 Mpa, uses in order to still kettle;
(3) distill
The concentrated solution heated up is transferred to still kettle, heats up, when pot temperature reaches 150 DEG C, maintenance vacuum tightness is-0.078Mpa, product is inputted finished product still, opens temperature lowering water simultaneously, and the temperature controlling material is between 135-140 DEG C, vacuum tightness is 0.086Mpa;
When finished product still material reaches 2/3, be switched to another finished product still, material neopentyl glycol be placed on steel band and carry out scraping blade packaging.
Embodiment 3
The production method of neopentyl glycol comprises following step:
(1) condensation
With isobutyric aldehyde and formaldehyde for raw material, the volume ratio that feeds intake of described isobutyric aldehyde and formaldehyde is 1:19;
Prepare raw material, described raw material is placed in reaction kettle for reaction, obtains reaction soln, the temperature controlled in reactor is no more than 40 DEG C, limit coronite at the uniform velocity add NaOH, make the pH of reaction soln be about 13.0 after adding NaOH; After adding NaOH, reaction soln in reactor is stirred, open the batch turning valve of reactor, material is inputted intensification still, be warming up to 50 DEG C, keep 1.5 hours at this temperature, carry out second time again to heat up, keep 2.0 hours after rising to 70 DEG C, the pH value being neutralized to solution with formic acid is 7.2, then it is for subsequent use that reacted condensation solution is transferred to storage tank;
(2) evaporate
The condensation solution prepared in step (1) is squeezed in vaporizer, when liquid level reaches the tubulation 32cm of vaporizer,
Start to heat up, keep vacuum tightness at-0.08Mpa, when reaching 95 DEG C, open spray water;
In evaporative process, neopentyl glycol in condensation solution and water rise to evaporator tower in a gaseous form, after the condensation of tower top spray water, because water is different with the boiling point of neopentyl glycol, neopentyl glycol solution falls into evaporating kettle, the impurity such as high boiling material and sodium formiate is in continuous evaporative process, with the form crystallization of supersaturated solution, be stored in base of evaporator, centrifugation, the rotating speed of centrifugation is 200-800rmp, obtains sodium formiate;
Neopentyl glycol solution in evaporating kettle is warming up to 120 DEG C after flowing into concentration kettle, keeps vacuum tightness to be-0.008 Mpa, uses in order to still kettle;
(3) distill
The concentrated solution heated up is transferred to still kettle, heats up, when pot temperature reaches 155 DEG C, maintenance vacuum tightness is-0.078Mpa, product is inputted finished product still, opens temperature lowering water simultaneously, and the temperature controlling material is between 135-140 DEG C, vacuum tightness is 0.086Mpa;
When finished product still material reaches 2/3, be switched to another finished product still, material neopentyl glycol be placed on steel band and carry out scraping blade packaging.
Claims (8)
1. a production method for neopentyl glycol, is characterized in that, described method comprises following step:
(1) condensation
With isobutyric aldehyde and formaldehyde for raw material, the volume ratio that feeds intake of described isobutyric aldehyde and formaldehyde is 1:15-19;
Prepare raw material, described raw material is placed in reaction kettle for reaction, obtains reaction soln, the temperature controlled in reactor is no more than 40 DEG C, limit coronite at the uniform velocity add alkali, make the pH of reaction soln be 13.0-13.5 after adding alkali; After adding alkali, reaction soln in reactor is stirred, open the batch turning valve of reactor, material is inputted intensification still, be warming up to 50-58 DEG C, keep 1.5-2.5 hour at this temperature, carry out second time again to heat up, keep 1.0-2.0 hour after rising to 65-75 DEG C, the pH value being neutralized to solution with formic acid is 6.8-7.2, then it is for subsequent use that reacted condensation solution is transferred to storage tank;
(2) evaporate
The condensation solution prepared in step (1) is squeezed in vaporizer, when liquid level reaches the tubulation 30-35cm of vaporizer,
Start to heat up, keep vacuum tightness at-0.08Mpa, when reaching 95 DEG C, open spray water;
In evaporative process, neopentyl glycol in condensation solution and water rise to evaporator tower in a gaseous form, after the condensation of tower top spray water, because water is different with the boiling point of neopentyl glycol, neopentyl glycol solution falls into evaporating kettle, and the impurity such as high boiling material and sodium formiate is in continuous evaporative process, with the form crystallization of supersaturated solution, be stored in base of evaporator, centrifugation, and obtain sodium formiate;
Neopentyl glycol solution in evaporating kettle is warming up to 120 DEG C after flowing into concentration kettle, keeps vacuum tightness to be-0.008 Mpa, uses in order to still kettle;
(3) distill
The concentrated solution heated up is transferred to still kettle, heats up, when pot temperature reaches 150-160 DEG C, maintenance vacuum tightness is-0.078Mpa, product is inputted finished product still, opens temperature lowering water simultaneously, and the temperature controlling material is between 135-140 DEG C, vacuum tightness is 0.086Mpa;
When finished product still material reaches 2/3, be switched to another finished product still, material neopentyl glycol be placed on steel band and carry out scraping blade packaging.
2. the production method of a kind of neopentyl glycol as claimed in claim 1, is characterized in that, described alkali is NaOH.
3. the production method of a kind of neopentyl glycol as claimed in claim 1, is characterized in that, in described step (2), the rotating speed of centrifugation is 200-800rmp.
4. the production method of a kind of neopentyl glycol as claimed in claim 1, is characterized in that, fusing point 124-130 DEG C of described neopentyl glycol, boiling point 210 DEG C, density 1.06, flash-point 129 DEG C.
5. the production method of a kind of neopentyl glycol as claimed in claim 1, is characterized in that, the color and luster < 15 of described neopentyl glycol, free acid < 0.05, moisture≤0.5, hydroxy radical content >=31.8.
6. the production method of a kind of neopentyl glycol as claimed in claim 1, is characterized in that, the volume ratio that feeds intake of described isobutyric aldehyde and formaldehyde is 1:17.
7. the production method of a kind of neopentyl glycol as claimed in claim 1, is characterized in that, in described step (1), with isobutyric aldehyde and formaldehyde for raw material, the volume ratio that feeds intake of described isobutyric aldehyde and formaldehyde is 1:17;
Prepare raw material, described raw material is placed in reaction kettle for reaction, obtains reaction soln, the temperature controlled in reactor is no more than 40 DEG C, limit coronite at the uniform velocity add alkali, make the pH of reaction soln be 13.0 after adding alkali; After adding alkali, reaction soln in reactor is stirred, open the batch turning valve of reactor, material is inputted intensification still, be warming up to 55 DEG C, keep 2 hours at this temperature, carry out second time again to heat up, keep 1.5 hours after rising to 70 DEG C, the pH value being neutralized to solution with formic acid is 7.0, then it is for subsequent use that reacted condensation solution is transferred to storage tank.
8. the production method of a kind of neopentyl glycol as claimed in claim 1, it is characterized in that, in described step (3), the concentrated solution heated up is transferred to still kettle, heats up, when pot temperature reaches 155 DEG C, maintenance vacuum tightness is-0.078Mpa, product is inputted finished product still, opens temperature lowering water simultaneously, and the temperature controlling material is between 135-140 DEG C, vacuum tightness is 0.086Mpa.
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Cited By (6)
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| CN105503573A (en) * | 2015-12-23 | 2016-04-20 | 安徽金禾实业股份有限公司 | Method and device for separation treatment of sodium formate in NPG (neopentyl glycol) production technology |
| CN105541556A (en) * | 2016-02-23 | 2016-05-04 | 山东省化工研究院 | Neopentyl glycol and sodium formate separating method |
| CN106802061A (en) * | 2015-11-25 | 2017-06-06 | 衡阳屹顺化工有限公司 | A kind of drying process of neopentyl glycol production |
| CN109651088A (en) * | 2019-02-22 | 2019-04-19 | 山东建筑大学 | The method for extracting neopentyl glycol in neopentyl glycol purifying waste liquid |
| CN109704949A (en) * | 2018-12-10 | 2019-05-03 | 安徽金禾实业股份有限公司 | The separation method of sodium formate in a kind of production of neopentyl glycol |
| CN110790663A (en) * | 2019-09-30 | 2020-02-14 | 安徽金禾实业股份有限公司 | Device and method for purifying neopentyl glycol byproduct sodium formate |
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| CN105541556A (en) * | 2016-02-23 | 2016-05-04 | 山东省化工研究院 | Neopentyl glycol and sodium formate separating method |
| CN109704949A (en) * | 2018-12-10 | 2019-05-03 | 安徽金禾实业股份有限公司 | The separation method of sodium formate in a kind of production of neopentyl glycol |
| CN109651088A (en) * | 2019-02-22 | 2019-04-19 | 山东建筑大学 | The method for extracting neopentyl glycol in neopentyl glycol purifying waste liquid |
| CN110790663A (en) * | 2019-09-30 | 2020-02-14 | 安徽金禾实业股份有限公司 | Device and method for purifying neopentyl glycol byproduct sodium formate |
| CN110790663B (en) * | 2019-09-30 | 2021-11-23 | 安徽金禾实业股份有限公司 | Device and method for purifying neopentyl glycol byproduct sodium formate |
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