CN102974281A - Apparatus and method for continuous synthesis of long-chain fatty acid methyl esters - Google Patents
Apparatus and method for continuous synthesis of long-chain fatty acid methyl esters Download PDFInfo
- Publication number
- CN102974281A CN102974281A CN 201110263491 CN201110263491A CN102974281A CN 102974281 A CN102974281 A CN 102974281A CN 201110263491 CN201110263491 CN 201110263491 CN 201110263491 A CN201110263491 A CN 201110263491A CN 102974281 A CN102974281 A CN 102974281A
- Authority
- CN
- China
- Prior art keywords
- bringing
- section
- fatty acid
- reaction chamber
- reaction
- 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.)
- Pending
Links
Images
Landscapes
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
An apparatus and a method for continuous synthesis of long-chain fatty acid methyl esters. The apparatus comprises: a charging pump, a pipeline mixer, a rectifying column, an induced draft fan, and a reactor; and the core of the apparatus is the sectionalized heating, sectionalized reacting, double fixed bed reactor which comprises a housing, a liner, baffle plates, etc. The prominent characteristics of the apparatus are: (1) the static pressure of the reaction liquid is small, the generated water is easy to escape, which is conducive to the esterification reaction; (2) the outer wall of the liner is like a built-in high-efficient thin-film evaporator, so a high purity product can be obtained directly; (3) catalyst loading is convenient and in large quantity, so high reaction capability is improved; and (4) the reaction is subjected to uniform heating. By using the apparatus, under the operating conditions of a molar ratio of alcohol to acid being 3:1, space velocity being 0.5-0.8h<-1> and reaction temperature being 90-95 DEG C, the fatty acid conversion rate is more than 97%, and the product purity can reach 98%.
Description
(1) technical field under:
The present invention relates to a kind of device and method of esterification, especially a kind of device and method of continuously synthetic higher fatty acids methyl esters.
(2) background technology
Esterification is an important class organic synthesis, plays a part very important at modern industry.The carboxylate that esterification is synthetic is the raw material of the industry such as spices, daily use chemicals, fuel, coating, leather, medicine.The higher fatty acids methyl esters was as the reproducible energy in recent years, and to replace the aromatic carboxylic acid ester plasticiser be some important topics that people study.Traditional fatty acid methyl ester synthetic method is with aliphatic acid and methyl alcohol, and the concentrated sulfuric acid is made catalyst according to a certain percentage in the disposable input reactor, under certain temperature and pressure, through reaction in 6～8 hours.The deficiency that this method exists: 1. the concentrated sulfuric acid is serious to equipment corrosion, pays and reacts many, the post processing trouble; 2. the reaction time long, energy consumption is high; 3. methyl alcohol occupies the dischargeable capacity of very large reactor, and utilization rate of equipment and installations is low; For this reason, in the last few years, people had developed the many kinds of solids acid catalyst and had been used for esterification, these catalyst are insoluble to reactant liquor, after reaction finishes easily by filter, the separation means such as centrifugal or precipitation separate and reclaim catalyst, and recycling, therefore can economize on resources, reduce and pollute.The heterogeneous synthetic main form of reactor that adopts of higher fatty acids methyl esters has at present:
1, tank reactor.Utilize mechanical agitation to strengthen contacting of aliphatic acid and alcohol, and solid catalyst is suspended in the reactant liquor, utilize external centrifuge or filter to separate and reclaim catalyst.
2, tower reactor.Solid catalyst is wrapped in (or being placed on the column plate) within the filler, and reactant carries out esterification at catalyst surface.
3, fixed bed reactors.Solid catalyst is filled in forms porous fixed bed in the reaction tube, reactant contacts with catalyst when the space of fixed bed, discharge from the fixed bed outlet subsequently, and directly and catalyst separation.
In the esterification of catalysis of solid catalyst higher fatty acids, fixed bed reactors have certain advantage with respect to other two class, and with respect to tank reactor: 1. machinery-free stirs, the equipment good seal performance.2. can be continuously produced, bear higher temperature and pressure.3. the solid catalyst wearing and tearing are little.Relative tower reactor: 1. volume is little.2. catalyst regeneration is convenient.Yet conventional fixed bed reactors are applied in the suitability for industrialized production of fatty acid methyl ester still exists some problems, shows: 1. calandria type fixed bed reactor, adopt the pipe apparatus with catalyst inside, and unit heat exchange area inner catalyst amount is little, and respond is little.2. equipment making complex process.3. reaction conversion ratio is low.4. reaction temperature is inhomogeneous.
(3) summary of the invention:
In order to overcome the deficiency of traditional handicraft and device, the invention provides a kind of device and method of continuously synthetic higher fatty acids methyl esters.It is simple to operate, sufficient reacting, energy consumption are low, finished product purity is high, the Catalyst packing coefficient is large.
The technical scheme that the present invention solves its technical problem employing is:
1. the device of a continuously synthetic higher fatty acids methyl esters comprises: feed pump, pipe-line mixer, rectifying column, air-introduced machine, reactor.Wherein reactor has the formations such as shell, inner bag and deflection plate.Shell blocks with method with inner bag and links to each other, and forms interlayer, and discharging opening is arranged at the interlayer bottom, and deflection plate is arranged at interlayer top.Cover top portion has gaseous phase outlet to link to each other with methanol rectifying tower; Charging aperture is arranged at the inner bag bottom, distributor, and successively up: one-level bringing-up section, first order reaction chamber, secondary bringing-up section, second order reaction chamber are blocked continuous with method; I and II reative cell top, the end, all have built-in method to block, and the orifice plate that the centre accompanies silk screen is fixed on method and blocks.
2. such as the device of a kind of continuously synthetic higher fatty acids methyl esters as described in the above-mentioned the 1st, wherein, deflection plate is up big and down small truncated cone-shaped.The deflection plate upper end is equal with the inner bag top, and the lower end of deflection plate is 0.5～1cm apart from the outer wall of inner bag, and deflection plate is fixed on the inwall of shell with lattice.
3. such as the device of a kind of continuously synthetic higher fatty acids methyl esters as described in the above-mentioned the 1st, wherein, the ratio of I and II bringing-up section heat exchange area is 1: 0.5～1.
4. such as the device of a kind of continuously synthetic higher fatty acids methyl esters as described in the above-mentioned the 1st, wherein, I and II reaction chamber volume ratio is 1～1.5: 1.
5. such as the device of a kind of continuously synthetic higher fatty acids methyl esters as described in the above-mentioned the 1st, wherein, should satisfy 20～80m between the gross area of I and II heat exchanging segment and the I and II reative cell total measurement (volume)
2/ m
3Relation.
6. such as the device of a kind of continuously synthetic higher fatty acids methyl esters as described in the above-mentioned the 1st, wherein, the interlayer of shell and inner bag formation, the bottom position of interlayer is in one-level bringing-up section outer wall center.
7. another aspect of the present invention provides a kind of method of synthesizing continuously the higher fatty acids methyl esters, uses device of the present invention, reaction mass evenly enters the one-level bringing-up section through pipe-line mixer, distributor, rises to reaction temperature, enters the first order reaction chamber, under the effect of catalyst, esterification occurs.This reaction is the endothermic reaction, after the heating of secondary bringing-up section, enters the second order reaction chamber esterification occurs again.Vapor phase enters rectifying column from gaseous phase outlet, recycles after the rectifying; Liquid phase flows down with film-form along inner bladder outer wall under the deflection plate effect, under certain temperature, negative pressure, boils off volatile component, the fatty acid methyl ester that is high-load that flows out from the interlayer bottom.
8. such as the method for a kind of continuously synthetic higher fatty acids methyl esters as described in the above-mentioned the 7th, wherein, reaction temperature is 95～100 ℃.
9. such as the method for a kind of continuously synthetic higher fatty acids methyl esters as described in above-mentioned 7, wherein, the air-introduced machine outlet pressure is-3000～-4000Pa.
10. such as the method for a kind of continuously synthetic higher fatty acids methyl esters as described in above-mentioned 7, wherein, molar ratio of alcohol to acid is 3: 1.
11. such as the method for a kind of continuously synthetic higher fatty acids methyl esters as described in above-mentioned 7, wherein, feed rate is controlled at 0.5～0.8V/h (V is the total measurement (volume) of I and II reative cell).
Beneficial effect of the present invention: 1. reactant is heated evenly, and has avoided the phenomenon of catalyst overheating inactivation, and 2. loaded catalyst is large, convenient, production capacity is large.3. reduced the catalyst surface fluid pressure, the water of generation is easily selected, and is conducive to catalyst to the absorption of reactant, has both improved reaction speed, has increased again the conversion ratio of aliphatic acid.4. deflection plate makes the liquid that flows out from top, second order reaction chamber flow down with film-form along inner bladder outer wall, inner bladder outer wall is like built-in thin film evaporator, under the effect of negative pressure, the low boiling component very easily is distilled out of in the mixture, need not separation equipment and can obtain the high-load fatty acid methyl ester.5. molar ratio of alcohol to acid is little.6. product yield and purity are high.
(4) description of drawings:
Fig. 1 is the device schematic diagram of a kind of continuous synthesizing fatty acid methyl ester of the present invention.
Fig. 2 is deflection plate profilograph among Fig. 1.
Among Fig. 1: 1. methanol pump; 2. aliphatic acid pump; 3. pipe-line mixer; 4. charging aperture; 5. distributor; 6. method is blocked; 7. one-level bringing-up section; 8. discharging opening; 9. built-in method is blocked; 10. interlayer; 11. first order reaction chamber; 12. secondary bringing-up section; 13. orifice plate; 14. second order reaction chamber; 15. deflection plate; 16. silk screen; 17. gaseous phase outlet; 18. thermometer; 19. shell; 20. manhole; 21. inner bag; 22. unload the catalyst mouth; 23 dress catalyst mouths; 24 lattice; 25 rectifying columns; 26. condenser; 27. tower reactor; 28. receiving tank; 29. surge tank; 30. air-introduced machine.
(5) specific embodiment:
The present invention will be further described below in conjunction with the drawings and specific embodiments, and embodiment is unrestricted.
As shown in Figure 1, squeeze into pipe-line mixer 3 with methyl alcohol measuring pump 1 and oleic acid feed pump 2 with certain proportion, flow respectively, be evenly distributed into one-level bringing-up section 7 through charging aperture 4 with through distributor 5, after the one-level bringing-up section heats up, enter first order reaction chamber 11, large hole cation exchanger resin is equipped with in first order reaction chamber 11, under the effect of catalyst, esterification occurs.After the mixture that flows out from first order reaction chamber 11 enters secondary bringing-up section 12 heat temperature raisings, enter second order reaction chamber 14, macropore strong acid ion exchange resin is equipped with in second order reaction chamber 14, does not have the aliphatic acid of reaction and excessive methyl alcohol generation esterification to generate fatty acid methyl ester under the effect of catalyst.From 14 tops, second order reaction chamber component out, mainly contain fatty acid methyl ester, first alcohol and water.Water and methyl alcohol major part enter rectifying column 25 with vapor form from gaseous phase outlet 17, get smart alcohol after the rectifying, recycle; Fatty acid methyl ester and a small amount of water are dirty with filminess along inner bladder outer wall 21, outside the tank wall 21 and the lower further dehydration by evaporation of air-introduced machine 30 effects, and interlayer 10 bottoms are the fatty acid methyl ester of high-load, flow out through discharging opening 8 to be finished product.Content through the gas chromatographic detection fatty acid methyl ester can reach more than 98%; The conversion ratio that calculates oleic acid through the acid value of chemical examination product reaches 99%.
Embodiment 1: install as shown in Figure 1, the diameter of this device inner bag 21 is 1700mm, and the heat exchange area of one-level bringing-up section 7 is 120m
2, the heat exchange area of secondary bringing-up section 12 is 80m
2, the volume of first order reaction chamber 11 is 2.8m
3, the volume of second order reaction chamber 14 is 2.6m
3Prepare methyl oleate take the oleic acid of acid value as 197 as raw material.Step is as follows:
(1) use respectively methyl alcohol measuring pump 1 and oleic acid feed pump 2 take the flow of 3: 1 mol ratios, reactant as 4m
3/ h squeezes into pipe-line mixer 3, being evenly distributed through charging aperture 4 and distributor 5 is warmed up to 95～100 ℃ into one-level bringing-up section 7, and reactant enters first order reaction chamber 11, and large hole cation exchanger resin is equipped with in first order reaction chamber 11, under the effect of catalyst, oleic acid and methyl alcohol generation esterification.
(2) mixture that flows out from first order reaction chamber 11 enters secondary bringing-up section 12 and heats to 95 ℃, enter second order reaction chamber 14, macropore strong acid ion exchange resin is equipped with in second order reaction chamber 14, does not have the aliphatic acid of reaction and excessive methyl alcohol generation esterification to generate fatty acid methyl ester under the effect of catalyst.
(3) from 14 tops, second order reaction chamber component out, mainly contain fatty acid methyl ester, first alcohol and water, the reaction temperature at 14 tops, second order reaction chamber is controlled at 95 ℃, at air-introduced machine 30 outlet pressures be-3000Pa under, water and methyl alcohol major part enter rectifying column 25 with vapor form from gaseous phase outlet 17; Fatty acid methyl ester and a small amount of water are dirty with filminess along inner bladder outer wall 21, further dehydration by evaporation in dirty process, and interlayer 10 bottom liquids are the extremely low fatty acid methyl ester of water content.
(4) enter the component of rectifying column 25, can get methyl alcohol more than 99% through rectifying, recycle.
(5) content through the gas chromatographic detection fatty acid methyl ester can reach more than 98%; The conversion ratio that calculates oleic acid through the acid value of chemical examination product reaches 97%.
Embodiment 2: install as shown in Figure 1, the diameter of this device inner bag 21 is 1700mm, and the heat exchange area of one-level bringing-up section 7 is 120m
2, the heat exchange area of secondary bringing-up section 12 is 70m
2, the volume of first order reaction chamber 11 is 2.8m
3, the volume of second order reaction chamber 14 is 2.6m
3Be that raw material prepares Methyl palmitoleinate with palm oil fatty acid.Consisting of of palm oil fatty acid: laurate 0.3%; Meat is stepped on acid 3%; Palmitic acid 43%; Stearic acid 3%; Arachidic acid 0.5%; Oleic acid 39%; Linoleic acid 10%; Palmitoleic acid 0.2%.Step is as follows:
(1) with the palm oil fatty acid heat fused.
(2) use respectively methyl alcohol measuring pump 1 and palm oil fatty acid feed pump 2 with 3: 1 mol ratios.The flow of reactant is 3.8m
3/ h squeezes into pipe-line mixer 3, and being evenly distributed through charging aperture 4 and distributor 5 is warmed up to 90～95 ℃ into one-level bringing-up section 7.Reactant enters first order reaction chamber 11, and large hole cation exchanger resin is equipped with in first order reaction chamber 11, under the effect of catalyst, and aliphatic acid and methyl alcohol generation esterification.
(3) mixture that flows out from first order reaction chamber 11 enters secondary bringing-up section 12 and heats to 95 ℃, enter second order reaction chamber 14, macropore strong acid ion exchange resin is equipped with in second order reaction chamber 14, does not have the aliphatic acid of reaction and excessive methyl alcohol generation esterification to generate fatty acid methyl ester under the effect of catalyst.
(4) from 14 tops, second order reaction chamber component out, mainly contain fatty acid methyl ester, first alcohol and water, the reaction temperature at 14 tops, second order reaction chamber is controlled at 95 ℃, outlet pressure at air-introduced machine 30 is-3000Pa under, hydration methyl alcohol major part enters rectifying column 25 with vapor form from gaseous phase outlet; Fatty acid methyl ester and a small amount of water are dirty with filminess along inner bladder outer wall 21, further dehydration by evaporation in dirty process, and interlayer 10 bottom liquids are the extremely low fatty acid methyl ester of water content.
(5) enter the component of rectifying column 25, can get methyl alcohol more than 99% through rectifying, recycle.
(6) content through the gas chromatographic detection fatty acid methyl ester can reach more than 98%; The conversion ratio that calculates palm oil fatty acid through the acid value of chemical examination product reaches 97%.
Embodiment 3: install as shown in Figure 1, the diameter of this device inner bag is 1700mm, and the heat exchange area of one-level bringing-up section is 120m
2, the heat exchange area of secondary bringing-up section is 90m
2, the volume of first order reaction chamber is 2.8m
3, the volume of second order reaction chamber is 2.6m
3Prepare methyl laurate take laurate as raw material.Step is as follows:
(1) with the laurate heat fused.
(2) use respectively methyl alcohol measuring pump 1 and laurate feed pump 2 take the flow of 3: 1 mol ratios, reactant as 4.2m
3/ h squeezes into pipe-line mixer 3, and being evenly distributed through charging aperture 4 and distributor 5 is warmed up to 90～95 ℃ into one-level bringing-up section 7.Reactant enters first order reaction chamber 11, and large hole cation exchanger resin is equipped with in first order reaction chamber 11, under the effect of catalyst, and aliphatic acid and methyl alcohol generation esterification.
(3) mixture that flows out from first order reaction chamber 11 enters secondary bringing-up section 12 and heats to 95 ℃, enter second order reaction chamber 14, macropore strong acid ion exchange resin is equipped with in second order reaction chamber 14, does not have the aliphatic acid of reaction and excessive methyl alcohol generation esterification to generate fatty acid methyl ester under the effect of catalyst.
(4) from 14 tops, second order reaction chamber component out, mainly contain fatty acid methyl ester, first alcohol and water, the reaction temperature at 14 tops, second order reaction chamber is controlled at 95 ℃, outlet pressure at air-introduced machine 30 is-3000P under, hydration methyl alcohol major part enters rectifying column 25 with vapor form from gaseous phase outlet; Fatty acid methyl ester and a small amount of water are dirty with filminess along inner bladder outer wall 21, further dehydration by evaporation in dirty process, and interlayer 10 bottom liquids are the extremely low fatty acid methyl ester of water content.
(5) enter the component of rectifying column 25, can get methyl alcohol more than 99% through rectifying, recycle.
(6) content through the gas chromatographic detection fatty acid methyl ester can reach more than 98%; The conversion ratio that calculates laurate acid through the acid value of chemical examination product reaches 97%.
Claims (10)
1. continuous device and method of synthetic higher fatty acids methyl esters, device comprises: feed pump, pipe-line mixer, rectifying column, air-introduced machine, reactor.Wherein reactor is a heat stepwise, segmentation reaction, double-deck fixed bed type reactor, is made of shell, inner bag, deflection plate.Shell blocks with method with inner bag and links to each other, and forms interlayer, and discharging opening is arranged at the interlayer bottom, and deflection plate is arranged at interlayer top; Cover top portion has gaseous phase outlet to link to each other with rectifying column; Inner bag bottom feed mouth, distributor, successively up: the one-level bringing-up section, the first order reaction chamber, the secondary bringing-up section, the second order reaction chamber is blocked continuous with method; I and II reative cell two ends all have interior method to block, and the orifice plate that accompanies silk screen is fixed on interior method and blocks.
2. according to the reaction unit of right 1, it is characterized in that: the big up and small down truncated cone-shaped of described deflection plate, the deflection plate upper end is equal with the inner bag top, and the lower end of deflection plate is 0.5～1cm apart from the outer wall of inner bag, and deflection plate is fixed on the inwall of shell with lattice.
3. according to the reaction unit of right 1, it is characterized in that: the heat exchange area of I and II bringing-up section is 1: 0.5-1.
4. according to the reaction unit of right 1, it is characterized in that: the total measurement (volume) of reative cell should satisfy 20～80 (m with the area of total bringing-up section heat exchange
2/ m
3).
5. according to the reaction unit of right 1, it is characterized in that: the interlayer that shell and inner bag form, the bottom position of interlayer is in one-level bringing-up section outer wall center.
6. the method for a continuous synthesizing fatty acid methyl ester, its right to use 1～5 each described esterification device, wherein reactant enters the heating of one-level bringing-up section with charging rate through pipe-line mixer according to a certain percentage, flow into the first order reaction chamber, esterification occurs under the effect of catalyst, because this reaction is the endothermic reaction, first order reaction liquid is after the heating of secondary bringing-up section, enter again the second order reaction chamber and carry out esterification, vapor phase enters rectifying column rectifying from gaseous phase outlet, and liquid phase is dirty with film-form along inner bladder outer wall, under suction function, boil off volatile component, can obtain high-purity fatty acid methyl ester from interlayer bottom discharging opening.
7. according to right 6 described esterification process, wherein, the mol ratio of methyl alcohol and aliphatic acid is 3: 1.
8. according to right 6 described esterification process, wherein, the charging rate of reactant is controlled at 0.5～0.8V/h, (V is the total measurement (volume) of reative cell).
9. according to right 6 described esterification process, wherein, the temperature of I and II bringing-up section outlet is controlled at 90～95 ℃.
10. according to right 6 described esterification process, wherein, I and II catalyst that reative cell is filled out is the macropore strong acid cation exchanger resin.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110263491 CN102974281A (en) | 2011-09-07 | 2011-09-07 | Apparatus and method for continuous synthesis of long-chain fatty acid methyl esters |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110263491 CN102974281A (en) | 2011-09-07 | 2011-09-07 | Apparatus and method for continuous synthesis of long-chain fatty acid methyl esters |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102974281A true CN102974281A (en) | 2013-03-20 |
Family
ID=47848798
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110263491 Pending CN102974281A (en) | 2011-09-07 | 2011-09-07 | Apparatus and method for continuous synthesis of long-chain fatty acid methyl esters |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102974281A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109529619A (en) * | 2018-12-21 | 2019-03-29 | 袁家彬 | A kind of denitration reaction container |
| CN112546969A (en) * | 2020-12-07 | 2021-03-26 | 安徽贝克联合制药有限公司 | Catalytic hydrogenation continuous production device and preparation method of ritonavir intermediate |
| CN113617311A (en) * | 2021-09-10 | 2021-11-09 | 中国科学院电工研究所 | Electric heating catalytic reactor |
-
2011
- 2011-09-07 CN CN 201110263491 patent/CN102974281A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109529619A (en) * | 2018-12-21 | 2019-03-29 | 袁家彬 | A kind of denitration reaction container |
| CN109529619B (en) * | 2018-12-21 | 2021-04-30 | 广州威品技术研发有限公司 | Denitration reaction container |
| CN112546969A (en) * | 2020-12-07 | 2021-03-26 | 安徽贝克联合制药有限公司 | Catalytic hydrogenation continuous production device and preparation method of ritonavir intermediate |
| CN113617311A (en) * | 2021-09-10 | 2021-11-09 | 中国科学院电工研究所 | Electric heating catalytic reactor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN202214306U (en) | Process device for preparing ethanol by utilizing acetic acid | |
| CN103044257B (en) | Terylene waste material produces alcoholysis method and the apparatus system of dioctyl terephthalate | |
| CN202376983U (en) | Multifunctional reactor for preparing hexene-1 catalyst | |
| CN103007862A (en) | Gas-liquid stirring reactor for synthesizing acrylic acid and ester through acetylene carbonylation method | |
| CN109400443A (en) | A kind of device and method of preparing ethylene glycol by using dimethyl oxalate plus hydrogen | |
| CN105623861A (en) | Glycerol esterification reactor | |
| CN203408693U (en) | Hydrogenation reactor taking acetic acid as raw material | |
| CN102974281A (en) | Apparatus and method for continuous synthesis of long-chain fatty acid methyl esters | |
| CN109748790B (en) | Method for producing dimethyl adipate | |
| CN109748791B (en) | Energy-saving method for producing dimethyl adipate | |
| CN203816622U (en) | Macromolecule polymerizing reaction device | |
| CN202283465U (en) | C10-24 fatty acid methyl esterification device | |
| CN103102369B (en) | A kind of production method of diethyl ethylphosphate | |
| CN203007176U (en) | Alcoholysis device system for preparing dioctyl terephthalate from Dacron wastes | |
| CN201768553U (en) | Gas-phase synthesis dimethyl ether fluidized bed reactor | |
| CN213131978U (en) | Recovery system for recovering isobutanol in alcohol low-boiling-point substance by isobutyl ester plasticizer | |
| CN204170436U (en) | Evaporator condensation water reutilization system device in Isooctyl acrylate monomer esterification | |
| CN201543417U (en) | Device for continuously preparing 2,2,4-trimethyl-1,2-dihydrogenated quinoline | |
| CN202376971U (en) | Tubular continuous esterification reaction device for synthesizing binary carboxylic ester | |
| CN202752008U (en) | Gas phase hydrogenation reactor | |
| CN212833557U (en) | Continuous esterification device | |
| CN209490502U (en) | A kind of methyl ethyl carbonate rouge low-temperature fractionating tower | |
| CN209338420U (en) | Bromoalkane process units with material-saving mechanism | |
| CN201841008U (en) | Dimethyl ether preparing device | |
| CN209076655U (en) | Bromoalkane production raw materials recovery formula reaction unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20130320 |