NL2021197B1 - A device and method for continuously producing environment-friendly plasticizer - Google Patents

A device and method for continuously producing environment-friendly plasticizer Download PDF

Info

Publication number
NL2021197B1
NL2021197B1 NL2021197A NL2021197A NL2021197B1 NL 2021197 B1 NL2021197 B1 NL 2021197B1 NL 2021197 A NL2021197 A NL 2021197A NL 2021197 A NL2021197 A NL 2021197A NL 2021197 B1 NL2021197 B1 NL 2021197B1
Authority
NL
Netherlands
Prior art keywords
reactor
esterification
reaction
phase
series
Prior art date
Application number
NL2021197A
Other languages
Dutch (nl)
Inventor
Jiang Jianchun
Liu Peng
Xu Junming
Chen Shuigen
Xu Bin
Xu Yu
Xu Wei
Original Assignee
Inst Chemical Ind Forest Products Caf
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Inst Chemical Ind Forest Products Caf filed Critical Inst Chemical Ind Forest Products Caf
Application granted granted Critical
Publication of NL2021197B1 publication Critical patent/NL2021197B1/en

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/08—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0046—Sequential or parallel reactions, e.g. for the synthesis of polypeptides or polynucleotides; Apparatus and devices for combinatorial chemistry or for making molecular arrays
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1862—Stationary reactors having moving elements inside placed in series

Abstract

A device and method for continuously producing environment-friendly plasticizer. Solid acid and liquid alcohol material is added into a preheating and dehydrating reactor, stirred and heated until not water comes out, to realize material preheating and dehydration; The above mentioned reaction material which is preheated and dehydrated is conveyed from the preheating and dehydrating reactor to multi-stage esterification reactors connected in series through a pump or high potential difference, and catalyst is added into the first-stage esterification reactor, stirred and heated to realize reaction; With continuous input of the reaction material, when reaching the material outlet at the upper part of the esterification reactor, the reaction material in the reactor is conveyed to a next-stage esterification reactor for further reaction; the flow rate of the material into the esterification reactor is adjusted, and the liquid material generated at the end of the reaction is conveyed to a dealcoholization reactor for further dealcoholization. The device of the invention has advantages that the layout is reasonable, the working procedures are simple, the production efficiency is high, the operation is stable, the yield in unit time is effectively improved, and thus continuous and large-scale production of environment-friendly plasticizer is realized.

Description

Technical Field
The invention belongs to the technical field of environment-friendly plastic additive preparation, and especially relates to a method for continuously producing environmentfriendly plasticizer.
Background Technology
Cables are praised as “blood vessels” and “nerves” of national economy. The wire and cable manufacturing industry is one of the largest auxiliary industry in national economy, and the second largest industry in machinery, next to the automobile industry. Wire and cable products are broadly applied in energy, traffic, communication, automobiles, petrochemical engineering, etc. In recent years, the wire and cable industry of China maintains fast growth, and continues occupying an important position in national economy. With further development of industrialization, completion of infrastructure construction and improvement of urbanization level of China, the wire and cable industry will surely and quickly develop to maturity.
Environment-friendly plasticizer, DOTP, is a fine chemical product having broad application range and excellent performance. DOTP is mainly applied in PVC plastic products and is main additive in cable material production. Along with fast development of the cable industry, DOTP will be increasingly demanded and have broad market prospect.
Currently, industrial DOTP production is conducted by the batch method, which mainly has the following disadvantages: 1) match production consumes longer time, and generates greatly fluctuating and unstable product quality; 2) the process is outdated and requires high labor intensity; 3) batch esterification consumes more energy and materials, but gives low product yield; 4) the scale is small, and thus large-scale production cannot be realized, and the plasticizer output is restrained. Since a large amount of recovered PTA material is used as the raw material of reaction, the particle sizes are non-uniform, and thus compatibility between the esterification reaction of solid and liquid is low, and the reaction consumes long time. The invention proposes a
AO 18.06.1059 NL new method with stable process and high economic efficiency, which can realize continuous and large-scale production of environment-friendly plasticizer.
Description of Invention
Technical problem: the invention aims to provide a device and method for continuously producing environment-friendly plasticizer.
Technical scheme: a method for continuously producing environment-friendly plasticizer, comprising the following steps: (1) material preheating and dehydration: the solid acid and liquid alcohol material is added into a preheating and dehydrating reactor at a mass ratio of 1:2.4-1:3.2, stirred, and heated to a temperature over 160°C until no water comes out, to realize material preheating and dehydration; (2) continuous esterification reaction: the above mentioned reaction material which is preheated and dehydrated is conveyed from the preheating and dehydrating reactor to multi-stage esterification reactors connected in series through a pump or high potential difference, and catalyst, i.e., tetrabutyl titanate is added into the first-stage esterification reactor at an amount which is ().lwt.%-().5 wt.% of the total reaction material, stirred and heated to 180-240°C to realize reaction; with continuous input of the reaction material, when reaching the material outlet at the upper part of the esterification reactor, the reaction material in the reactor overflows naturally through a pipe or is conveyed to a next-stage esterification reactor for further reaction; the reaction temperature in the esterification reactors connected in series is controlled within 180-240°C, the flow rate of the material into the esterification reactor is adjusted such that the acid value of the liquid material flowing out of the final esterification reactor is lower than 0.50 mgKOH/g, and the liquid material generated at the end of the reaction is conveyed to a dealcoholization reactor for further dealcoholization.
The solid acid material in the step (1) is purified terephthalic acid (PTA), precipitated PTA, fallen PTA or recovered material from the alkali decrement process in the polyester fiber industry (commonly known as alkali dissolved PTA).
The multi-stage esterification reactors connected in series have two stages at least.
AO 18.06.1059 NL
The esterification reaction is performed in multi-stage fluidized bed reactors connected in series, which have two stages at least.
The addition amount of the catalyst, i.e., tetrabutyl titanate in the step (2) is 0.1wt.%-0.3 wt.% of the total reaction material.
A device for continuously producing environment-friendly plasticizer, in which a preheating and dehydrating reactor, multi-stage esterification reactors connected in series and a dealcoholization reactor are connected in sequence through pipes in the device; The preheating and dehydrating reactor is provided with a condenser and a wastewater receiving tank; the multi-stage esterification reactors connected in series are composed of esterification reactors connected in series or fluidized bed reactors connected in series which have two stages at least, the first-stage esterification reactor is connected with a catalyst tank through a metering pump, and the final-stage esterification reactor is connected with the dealcoholization reactor through a pipe.
Each stage of reactor in the multi-stage esterification reactors is installed at gradually lower height, and the reaction material overflows naturally to the adjacent next-stage esterification reactor.
Each stage of reactor in the multi-stage esterification reactors is installed at equal height, and the reaction material is conveyed to the next-stage esterification reactor through the pump.
A condenser and an alcohol-water separator are connected at the top of each stage of esterification reactor, and iso-octyl alcohol generated through condensation flows from the alcohol-water separator to the corresponding esterification reactor through a pipe. The esterification reactors connected in series are connected to a condenser for centralized condensation and heat exchange, and iso-octyl alcohol generated through condensation is conveyed to each stage of esterification reactor.
Beneficial effects: the invention provides a device and method for continuously producing environment-friendly plasticizer. Before reaction, the solid and liquid
AO 18.06.1059 NL reaction materials are preheated and dehydrated through the dehydrating reactor, to realize overall uniform mobility of the materials and remarkably improve the material conveying speed and reaction speed. In the invention, the esterification reactors or fluidized bed reactors connected in series are used to realize continuous reaction through natural overflow and pump conveying; in addition, the device of the invention has advantages that the layout is reasonable, the working procedures are simple, the production efficiency is high, the operation is stable, the yield in unit time is effectively improved, and thus continuous and large-scale production of environment-friendly plasticizer is realized.
Brief Description of Drawings
Lig. 1 shows the diagram of a preferred device for continuously producing the environment-friendly plasticizer with four esterification reactors connected in series in the invention.
Lig. 2 shows the diagram of a preferred device for continuously producing the environment-friendly plasticizer with six esterification reactors connected in series in the invention.
In the figures, 1: preheating and dehydrating reactor; 2: first esterification reactor; 3: catalyst metering pump; 4: second esterification reactor; 5: third esterification reactor; 6: fourth esterification reactor; 7: fifth esterification reactor; 8: sixth esterification reactor; 9: dealcoholization reactor.
Lig. 1 shows the diagram of a preferred device for continuously producing the environment-friendly plasticizer with four esterification reactors connected in series in the invention. As shown in Lig. 1, the reaction material which is preheated and dehydrated is conveyed from the preheating and dehydrating reactor to the first esterification reactor in the esterification system through a pump, the four esterification reactors in the esterification system are installed at gradually lower height, and the reaction material overflows naturally to the next esterification reactor.
Lig. 2 shows the diagram of a preferred device for continuously producing the
AO 18.06.1059 NL environment-friendly plasticizer with six esterification reactors connected in series in the invention. As shown in Eig. 2, the reaction material which is preheated and dehydrated is conveyed from the preheating and dehydrating reactor to the first esterification reactor in the esterification system through high potential difference, the six esterification reactors in the esterification system are installed at equal height, and the reaction material is conveyed to the next esterification reactor at certain flow rate.
Specific Implementation
The following embodiments further describe the invention, but the invention is not limited thereto.
Embodiment 1
Precipitated PTA and 98% iso-octyl alcohol with a mass ratio of 1:2.8 are added into the preheating and dehydrating reactor, stirred mechanically and heated through heat transfer oil, with the temperature in the reactor not lower than 160°C during mechanical stirring, to realize material preheating and dehydration; the reaction material which is preheated and dehydrated is conveyed from the preheating and dehydrating reactor to the first esterification reactor in the esterification system through a pump (or high potential difference), the catalyst metering pump at the top of the reactor is turned on, and mechanical stirring and heating are started for reaction; with continuous input of the reaction material, when reaching the material outlet at the upper part of the first esterification reactor, the reaction material in the reactor overflows naturally through the pipe or is conveyed to the second esterification reactor through the pump for further reaction at certain flow rate; along with the reaction progress, similarly, when reaching the material outlet at the upper part of the second esterification reactor, the reaction material in the reactor overflows naturally through the pipe or is conveyed to the third esterification reactor through the pump for further reaction, and so on; the reaction material finally flows into the final fourth esterification reactor; the reaction temperature in the esterification reactors connected in series is controlled within 180-240°C, the flow rate of the material into the first esterification reactor is adjusted such that the acid value of the liquid material flowing out of the final fourth esterification reactor is lower than 0.50 mgKOH/g, and the material generated at the end of the reaction is conveyed to the dealcoholization reactor for further dealcoholization.
AO 18.06.1059 NL
Table 1 Change of acid value in the fourth esterification reactor over time
Time / h 2 4 6 8 10 12 14 16 18 20 22 24
Acid value / mgKOH/g 0.42 0.43 0.48 0.45 0.49 0.48 0.5 0.47 0.46 0.44 0.5 0.46
Embodiment 2
Fallen PTA and 98% iso-octyl alcohol with a mass ratio of 1:2.6 are added into the preheating and dehydrating reactor, stirred mechanically and heated through heat transfer oil, with the temperature in the reactor not lower than 160°C during mechanical stirring, to realize material preheating and dehydration; the reaction material which is preheated and dehydrated is conveyed from the preheating and dehydrating reactor to the first esterification reactor in the esterification system through a pump (or high potential difference), the catalyst metering pump at the top of the reactor is turned on, and mechanical stirring and heating are started for reaction; with continuous input of the reaction material, when reaching the material outlet at the upper part of the first esterification reactor, the reaction material in the reactor overflows naturally through the pipe or is conveyed to the second esterification reactor through the pump for further reaction at certain flow rate; along with the reaction progress, similarly, when reaching the material outlet at the upper part of the second esterification reactor, the reaction material in the reactor overflows naturally through the pipe or is conveyed to the third esterification reactor through the pump for further reaction, and so on; the reaction material finally flows into the final fifth esterification reactor; the reaction temperature in the esterification reactors connected in series is controlled within 180-240°C, the flow rate of the material into the first esterification reactor is adjusted such that the acid value of the liquid material flowing out of the final fifth esterification reactor is lower than 0.50 mgKOH/g, and the material generated at the end of the reaction is conveyed to the dealcoholization reactor for further dealcoholization.
AO 18.06.1059 NL
Table 2 Change of acid value in the fifth esterification reactor over time
Time 1 h 2 4 6 8 10 12 14 16 18 20 22 24
Acid value / mgKOH/ g 0.4 7 0.4 7 0.4 8 0.5 0 0.4 9 0.4 8 0.4 2 0.4 1 0.4 3 0.4 4 0.4 2 0.4 6
Embodiment 3
Alkali dissolved PTA and 98% iso-octyl alcohol with a mass ratio of 1:3.2 are added into the preheating and dehydrating reactor, stirred mechanically and heated through heat transfer oil, with the temperature in the reactor not lower than 160°C during mechanical stirring, to realize material preheating and dehydration; the reaction material which is preheated and dehydrated is conveyed from the preheating and dehydrating reactor to the first esterification reactor in the esterification system through a pump (or high potential difference), the catalyst metering pump at the top of the reactor is turned on, and mechanical stirring and heating are started for reaction; with continuous input of the reaction material, when reaching the material outlet at the upper part of the first esterification reactor, the reaction material in the reactor overflows naturally through the pipe or is conveyed to the second esterification reactor through the pump for further reaction at certain flow rate; along with the reaction progress, similarly, when reaching the material outlet at the upper part of the second esterification reactor, the reaction material in the reactor overflows naturally through the pipe or is conveyed to the third esterification reactor through the pump for further reaction, and so on; the reaction material finally flows into the final sixth esterification reactor; the reaction temperature in the esterification reactors connected in series is controlled within 180-240°C, the flow rate of the material into the first esterification reactor is adjusted such that the acid value of the liquid material flowing out of the final sixth esterification reactor is lower than 0.50 mgKOH/g, and the material generated at the end of the reaction is conveyed to the dealcoholization reactor for further dealcoholization.
AO 18.06.1059 NL
Table 3 Change of acid value in the sixth esterification reactor over time
Time / h 2 4 6 8 10 12 14 16 18 20 22 24
Acid value / mgKOH/ g 0.4 5 0.4 4 0.4 7 0.4 7 0.4 7 0.4 4 0. 5 0.4 9 0.4 6 0.5 0 0.5 0 0.4 8
Embodiment 4
PTA and 98% iso-octyl alcohol with a mass ratio of 1:2.4 are added into the preheating and dehydrating reactor, stirred mechanically and heated through heat transfer oil, with the temperature in the reactor not lower than 160°C during mechanical stirring, to realize material preheating and dehydration; the reaction material which is preheated and dehydrated is conveyed from the preheating and dehydrating reactor to the first esterification reactor in the esterification system through a pump (or high potential difference), the catalyst metering pump at the top of the reactor is turned on, and mechanical stirring and heating are started for reaction; with continuous input of the reaction material, when reaching the material outlet at the upper part of the first esterification reactor, the reaction material in the reactor overflows naturally through the pipe or is conveyed to the second esterification reactor through the pump for further reaction at certain flow rate; along with the reaction progress, similarly, when reaching the material outlet at the upper part of the second esterification reactor, the reaction material in the reactor overflows naturally through the pipe or is conveyed to the final third esterification reactor through the pump for further reaction; the reaction temperature in the esterification reactors connected in series is controlled within 180240°C, the flow rate of the material into the first esterification reactor is adjusted such that the acid value of the liquid material flowing out of the final third esterification reactor is lower than 0.50 mgKOH/g, and the material generated at the end of the reaction is conveyed to the dealcoholization reactor for further dealcoholization.
AO 18.06.1059 NL
Time / h 2 4 6 8 10 12 14 16 18 20 22 24
Acid value / mgKOH/ g 0.4 8 0.4 5 0.4 7 0.4 5 0.4 9 0.4 7 0.5 0 0.4 7 0.4 8 0.4 9 0.4 2 0.5 0
AO 18.06.1059 NL

Claims (10)

ConclusiesConclusions 1. Een werkwijze voor het continu produceren van een milieuvriendelijke weekmaker, met het kenmerk dat de werkwijze de volgende stappen omvat: (1)A method for continuously producing an environmentally friendly plasticizer, characterized in that the method comprises the following steps: (1) 5 voorverwarmen en dehydrateren van materiaal: het vaste zuur en vloeibare alcoholmateriaal wordt toegevoegd aan een voorverwarmings- en dehydratatiereactor met een massaverhouding van 1: 2.4 - 1: 3.2, geroerd en verhit tot een temperatuur van hoger dan 160 °C totdat er geen water uitkomt, om materiaal voorverwarming en dehydratatie te realiseren; (2) continue veresteringsreactie: het bovengenoemde5 preheating and dehydrating material: the solid acid and liquid alcohol material is added to a preheating and dehydrating reactor with a mass ratio of 1: 2.4 - 1: 3.2, stirred and heated to a temperature higher than 160 ° C until no water comes out , to realize material preheating and dehydration; (2) continuous esterification reaction: the above 10 reactiemateriaal dat wordt voorverwarmd en gedehydrateerd wordt getransporteerd van de voorverwarmings- en de dehydratatiereactor naai' meer-fasen veresteringsreactoren die in serie zijn geschakeld via een pomp of een hoog potentiaalverschil, en wordt er een katalysator, dwz tetrabutyltitanaat toegevoegd aan de eerste-fase veresteringsreactor in een hoeveelheid die 0,1 gew.% - 0,5 gew.% van het totale reactiemateriaal bedraagt,Reaction material that is preheated and dehydrated is transported from the preheating and dehydration reactor to multi-phase esterification reactors connected in series via a pump or a high potential difference, and a catalyst, ie tetrabutyl titanate, is added to the first-phase esterification reactor in an amount that is 0.1% by weight - 0.5% by weight of the total reaction material, 15 geroerd en verwarmd tot 180 - 240 °C om reactie te realiseren; bij continue invoer van het reactiemateriaal, bij het bereiken van de materiaaluitgang in het bovenste deel van de veresteringsreactor, stroomt het reactiemateriaal in de reactor op natuurlijke wijze over door een pijp of wordt het naai' een veresteringsreactor in de volgende fase geleid voor verdere reactie; de reactietemperatuur in de veresteringsreactoren die in serie zijnStirred and heated to 180 - 240 ° C to realize reaction; upon continuous introduction of the reaction material, upon reaching the material exit in the upper part of the esterification reactor, the reaction material in the reactor naturally overflows through a pipe or the sewing of an esterification reactor is passed into the next phase for further reaction; the reaction temperature in the esterification reactors that are in series 20 geschakeld, wordt gehouden op 180 - 240 °C, de stroomsnelheid van het materiaal in de veresteringsreactor wordt zodanig aangepast dat de zuur concentratie van het vloeibare materiaal dat uit de laatste veresteringsreactor stroomt, lager is dan 0,50 mg KOH/g, en het vloeibare materiaal gegenereerd aan het einde van de reactie wordt getransporteerd naar een ont-alcoholisering reactor voor verdere ont-alcoholisering.20 is maintained at 180 - 240 ° C, the flow rate of the material in the esterification reactor is adjusted such that the acid concentration of the liquid material flowing out of the last esterification reactor is lower than 0.50 mg KOH / g, and the liquid material generated at the end of the reaction is transported to a de-alcoholization reactor for further de-alcoholization. 2. Werkwijze voor het continu produceren van een milieuvriendelijke weekmaker volgens conclusie 1, met het kenmerk, dat het vaste zuur materiaal in stap (1) gezuiverd tereftaalzuur (PTA), neergeslagen PTA, bezonken PTA of teruggewonnen materiaal van het alkali-verlagingsproces in de polyester vezelindustrie is.Method for continuously producing an environmentally friendly plasticizer according to claim 1, characterized in that the solid acid material in step (1) is purified terephthalic acid (PTA), precipitated PTA, settled PTA or recovered material from the alkali lowering process in the polyester fiber industry. 3. Werkwijze voor het continu produceren van een milieuvriendelijke weekmaker volgens conclusie 1, met het kenmerk, dat de meer-fasen veresteringsreactoren die in serie zijn geschakeld ten minste twee fasen hebben.Method for continuously producing an environmentally friendly plasticizer according to claim 1, characterized in that the multi-phase esterification reactors connected in series have at least two phases. AO 18.06.1059 NLAO 18.06.1059 NL 4. Werkwijze voor het continu produceren van een milieuvriendelijke weekmaker volgens conclusie 1, met het kenmerk, dat de veresteringsreactie wordt uitgevoerd in meer-fasen wervelbedreactoren met die in serie zijn geschakeld, die ten minste tweeMethod for continuously producing an environmentally-friendly plasticizer according to claim 1, characterized in that the esterification reaction is carried out in multi-phase fluidized bed reactors with those connected in series, comprising at least two 5 fasen hebben.Have 5 phases. 5. Werkwijze voor het continu produceren van een milieuvriendelijke weekmaker volgens conclusie 1, met het kenmerk, dat de toegevoegde hoeveelheid van de katalysator, dat wil zeggen tetrabutyltitanaat in stap (2), 0,1 gew.% - 0,3 gew.% van hetProcess for the continuous production of an environmentally friendly plasticizer according to claim 1, characterized in that the added amount of the catalyst, i.e. tetrabutyl titanate in step (2), 0.1 wt% - 0.3 wt% from the 10 totale reactiemateriaal bedraagt.Total reaction material. 6. Inrichting voor het continu produceren van een milieuvriendelijke weekmaker, met het kenmerk, dat een voorverwarmings en dehydratatiereactor, meer-fasen veresteringsreactoren die in serie zijn geschakeld en een ont-alcoholiseringreactorDevice for continuously producing an environmentally friendly plasticizer, characterized in that a preheating and dehydrating reactor, multi-phase esterification reactors connected in series and a de-alcoholization reactor 15 achtereenvolgens zijn verbonden via pijpen in de inrichting, waarbij de voorverwarmings- en dehydratatiereactor is voorzien van een condensor en een afvalwater ontvangsttank, waarbij de meer-fasen veresteringsreactoren die in serie zijn geschakeld, bestaan uit veresteringsreactoren die in serie zijn geschakeld of wervelbedreactoren die in serie zijn geschakeld en die minstens twee fasen hebben,15 are successively connected via pipes in the device, the preheating and dehydration reactor being provided with a condenser and a waste water receiving tank, the multi-phase esterification reactors connected in series consisting of esterification reactors connected in series or fluidized bed reactors connected in series connected in series and which have at least two phases, 20 waarbij de eerste fase veresteringsreactor is verbonden met een katalysatortank via een doseerpomp en de laatste fase veresteringsreactor met de ont-alcoholiseringreactor is verbonden via een pijp.Wherein the first phase esterification reactor is connected to a catalyst tank via a dosing pump and the last phase esterification reactor is connected to the de-alcoholization reactor via a pipe. 7. Inrichting voor het continu produceren van een milieuvriendelijke weekmaker7. Device for the continuous production of an environmentally friendly plasticizer 25 volgens conclusie 6, met het kenmerk, dat elke reactorfase in de meer-fasen veresteringsreactoren geleidelijk lager wordt geïnstalleerd en het reactiemateriaal op natuurlijke wijze overstroomt naar de aangrenzende veresteringsreactor in de volgende fase.According to claim 6, characterized in that each reactor phase in the multi-phase esterification reactors is gradually installed lower and the reaction material naturally overflows to the adjacent esterification reactor in the next phase. 3030 8. Een inrichting voor het continu produceren van een milieuvriendelijke weekmaker volgens conclusie 6, met het kenmerk, dat elke reactorfase in de meer-fasen veresteringsreactoren op een geleidelijk lagere hoogte wordt geïnstalleerd en het reactiemateriaal op natuurlijke wijze overstroomt naai' de aangrenzende volgende faseA device for continuously producing an environmentally friendly plasticizer according to claim 6, characterized in that each reactor phase is installed in the multi-phase esterification reactors at a gradually lower height and the reaction material naturally overflows to the adjacent next phase AO 18.06.1059 NL veresteringsreactor.AO 18.06.1059 NL esterification reactor. 9. Inrichting voor het continu produceren van een milieuvriendelijke weekmaker volgens conclusie 6, met het kenmerk, dat aan de bovenkant van elkeDevice for continuously producing an environmentally friendly plasticizer according to claim 6, characterized in that at the top of each 5 veresteringsreactor een condensor en een alcohol-water scheider verbonden zijn, en isooctylalcohol gegenereerd door condensatiestromen uit de alcohol-waterafscheider door een pijp naar de overeenkomstige veresteringsreactor stroomt.5 esterification reactor, a condenser and an alcohol-water separator are connected, and isooctyl alcohol generated by condensation flows from the alcohol-water separator flows through a pipe to the corresponding esterification reactor. 10. Inrichting voor het continu produceren van een milieuvriendelijke weekmaker10. Device for the continuous production of an environmentally friendly plasticizer 10 volgens conclusie 6, met het kenmerk, dat de in serie geschakelde veresteringsreactoren verbonden zijn met een condensor voor gecentraliseerde condensatie en warmte uitwisseling, en door condensatie gegenereerde iso-octylalcohol naar elke fase van de veresteringsreactor wordt getransporteerd.10 according to claim 6, characterized in that the esterification reactors connected in series are connected to a condenser for centralized condensation and heat exchange, and condensation-generated iso-octyl alcohol is transported to each phase of the esterification reactor. AO 18.06.1059 NLAO 18.06.1059 NL 1/11/1
NL2021197A 2017-11-03 2018-06-28 A device and method for continuously producing environment-friendly plasticizer NL2021197B1 (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201711070334.6A CN107935846B (en) 2017-11-03 2017-11-03 Device and method for continuously producing environment-friendly plasticizer

Publications (1)

Publication Number Publication Date
NL2021197B1 true NL2021197B1 (en) 2019-01-15

Family

ID=61933185

Family Applications (1)

Application Number Title Priority Date Filing Date
NL2021197A NL2021197B1 (en) 2017-11-03 2018-06-28 A device and method for continuously producing environment-friendly plasticizer

Country Status (2)

Country Link
CN (1) CN107935846B (en)
NL (1) NL2021197B1 (en)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP4023629A4 (en) * 2020-11-17 2022-12-21 LG Chem, Ltd. Method for preparing diester compound
EP4029852A4 (en) * 2020-11-17 2022-12-21 LG Chem, Ltd. Method for preparing diester-based material
EP4032875A4 (en) * 2020-11-17 2022-12-21 LG Chem, Ltd. Method for preparing diester compound
US11605505B2 (en) 2018-08-16 2023-03-14 Samsung Electro-Mechanics Co., Ltd. Multilayer ceramic electronic component

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109107503A (en) * 2018-09-19 2019-01-01 长园华盛(泰兴)锂电材料有限公司 Tandem reaction equipment of vinylene carbonate and preparation method thereof
CN110302737A (en) * 2019-07-29 2019-10-08 潍坊益华化工有限公司 A kind of continuous esterification device and process
CN113457571A (en) * 2020-03-30 2021-10-01 中石油吉林化工工程有限公司 Polymerization inhibitor mechanism for MMA (methyl methacrylate) production device and polymerization inhibitor adding method
CN111732510A (en) * 2020-07-03 2020-10-02 山东朗晖石油化学股份有限公司 Continuous production equipment and process for DOTP plasticizer
CN111909037B (en) * 2020-09-01 2023-04-18 潍坊弘润新材料有限公司 Continuous production method of tetraisooctyl pyromellitate
KR20220067352A (en) * 2020-11-17 2022-05-24 주식회사 엘지화학 Method for preparing diester-based material
CN112569621B (en) * 2020-11-23 2021-12-03 湖北兴瑞硅材料有限公司 Continuous dehydration device and dehydration process for dimethyl cyclosiloxane
CN112920094A (en) * 2021-01-29 2021-06-08 江苏奥洁生物科技有限公司 Method for adjusting production load and improving yield of N-methyl sodium taurate
CN114933534A (en) * 2022-04-28 2022-08-23 山东蓝帆化工有限公司 Continuous esterification production process of diisooctyl terephthalate heterogeneous system
CN115010633B (en) * 2022-07-11 2024-04-12 宁夏汉润生物科技有限公司 Synthesis method and device of ring-closing compound

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102503831A (en) * 2011-11-07 2012-06-20 潍坊市元利化工有限公司 Continuous esterification production method for plasticizer
CN104496819B (en) * 2014-12-17 2016-07-06 中国林业科学研究院林产化学工业研究所 A kind of method that environment-friendly plasticizer is prepared in waste resource recycling

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11605505B2 (en) 2018-08-16 2023-03-14 Samsung Electro-Mechanics Co., Ltd. Multilayer ceramic electronic component
EP4023629A4 (en) * 2020-11-17 2022-12-21 LG Chem, Ltd. Method for preparing diester compound
EP4029852A4 (en) * 2020-11-17 2022-12-21 LG Chem, Ltd. Method for preparing diester-based material
EP4032875A4 (en) * 2020-11-17 2022-12-21 LG Chem, Ltd. Method for preparing diester compound

Also Published As

Publication number Publication date
CN107935846B (en) 2020-01-10
CN107935846A (en) 2018-04-20

Similar Documents

Publication Publication Date Title
NL2021197B1 (en) A device and method for continuously producing environment-friendly plasticizer
CN103242164B (en) Continuous preparation process for environment-friendly plasticizer and device used in process
CN106800976A (en) A kind of method that glycerine round-robin method continous way prepares biodiesel
CN104151138B (en) The technique that a kind of octyl alconyl residual liquid produces alcohols high-carbon organic solvent
CN103451027A (en) Esterification method for preparing biodiesel using waste oils and fats
CN102079799B (en) Preparation method of binary polymer wax oil pour point reducer
CN206372821U (en) A kind of device for producing DOTP
CN204369837U (en) Waste lubricating oil distillation and clay-filtered merging device
CN101982523A (en) Washing oil continuous processing method
CN107840808A (en) Continuous reaction rectification production cyanoacetate compound, malonate compound device and its production technology
CN108558694A (en) A kind of process and device of continuous production N- ethoxies oxalyl-l-Alanine ethyl ester
CN101289628A (en) Process for producing biodiesel from mixed fatty acid
CN101468980A (en) Process for producing lactide by using waste lactic acid oligomer
CN202465566U (en) Crude methyl tetrahydrophthalic anhydride continuous production device
CN105732368B (en) A kind of method using luwa evaporator synthesizing polyatomic alcohol fatty acid ester
CN207537372U (en) Continuous reaction rectification production cyanoacetate compound, malonate compound device
CN107236597B (en) Biodiesel transesterification real-time dynamic separation continuous reaction system and application thereof
CN1156717A (en) Process for producing n-butyl acetate
CN105732369A (en) Method for synthesizing polyol fatty acid ester by adopting falling-film evaporator
CN103467726A (en) Preparation method for degradable polyester from 10-undecenoic acid and vanillic acid
CN108976121B (en) Device and method for producing 2-methyl chloropropionate by continuous kettle type reaction
CN204644245U (en) A kind of reactive system for unsaturated polyester resin
CN114829334B (en) Process for producing diester compound
CN204816514U (en) Production load adjustable reation kettle
CN220238539U (en) Butyl acrylate production system