CN209383684U - A kind of device of aromatic polyester polyol synthesis - Google Patents
A kind of device of aromatic polyester polyol synthesis Download PDFInfo
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- CN209383684U CN209383684U CN201821865198.XU CN201821865198U CN209383684U CN 209383684 U CN209383684 U CN 209383684U CN 201821865198 U CN201821865198 U CN 201821865198U CN 209383684 U CN209383684 U CN 209383684U
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- polyalcohol
- reaction kettle
- esterification
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- discharge port
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Abstract
The utility model discloses a kind of device of aromatic polyester polyol synthesis, including mixer, polyalcohol pans, reaction kettle of the esterification, batch condensation polymerization reactor, reconciliation reaction kettle and polyalcohol recovery tower etc.；Organic polycarboxylic acid is preheating to after certain temperature successively passes through reaction kettle of the esterification with the polyalcohol of certain temperature after mixer mixes, and batch condensation polymerization reactor, the reaction kettle that reconciles react to obtain the polyester polyol product of different size；Gas phase in reaction kettle of the esterification and batch condensation polymerization reactor enters polyalcohol recovery tower, and the polyalcohol of extraction enters the recycling of polyalcohol pans.Utility model device and method are compared with the more still reaction techniques of traditional batch, by rationally controlling esterification, polycondensation and reconciliation three phases technical data, so that properties of product specification adjustable extent wide (average molecular weight, carboxylic value and hydroxyl value etc.), polyalcohol recovery efficiency are high, loss is few, esterification and polycondensation process reaction efficiency are effectively promoted, external same performance index is reached while reducing products material consumption.
Description
Technical field
The utility model relates to a kind of devices of polyester polyol synthesis, and in particular to the synthesis of aromatic polyester polyol
Technology belongs to polyester polyol technical field.
Background technique
Polyester polyol is usually by polyalcohol and Dicarboxylic Acids (acid anhydrides) through esterification and polycondensation or by polyalcohol
With lactones be polymerized with a hydroxy-end capped kind polyester, average molecular weight is no more than in 1000-4000, carboxyl concentration
0.02mol•kg.Polyester polyol is mainly used to the raw material synthesized as polyurethane, wear-resisting, resistance to compared with polyether polyol
Oil and heat resistance are preferable, high mechanical strength.According to the difference for using dicarboxylic acids, it is polynary to can be generally divided into aliphatic polyester
Alcohol, aromatic polyester polyol and mixing polyester polyols.Aromatic polyester polyol is due to introducing benzene in molecular structure
Ring structure improves the phenyl ring content in polyurethane chain, so that being enbrittled by the rigid polyurethane foam that it is prepared
Low, good toughness, intensity are high, thermal coefficient is low, flame retardant property is good and the advantages such as price is low, in insulation, shockproof, sound insulation, packaging
Material Field is widely used.
Polyester polyol mostly uses batch stirred tank reactor to produce at present, and one-pot production capacity has reached ten thousand tons of rule
Mould, the companies such as Du Pont, Bayer, BASF have applied for related patents in the batch production process of polyester polyol and formula.State
It is interior also to have gone out continuous production technology route at present, but above-mentioned continuous process technology all rests on lab scale and pilot scale rank at present
Section, apart from commercial applications, there are also huge distances.The synthesis of polyester polyol is generally divided into two stages, and the first stage is normal
Esterification Stage is pressed, this stage since polyalcohol and dicarboxylic acids concentration are high, do not need catalyst energy fast reaction and generates largely
Water；Second stage is polycondensation phase, needs additionally to add catalyst to promote the further polycondensation of polyester polyols alcohol monomer for big point
The polymer of son, the stage usually use vacuumizing, promote water and small-molecule substance that can leave system in time, improve reaction
Efficiency reduces the generation of side reaction.However batch stirred tank reaction process technology does not consider the spy in differential responses stage at present
Point, two stages reaction usually occur in one or more reaction kettle simultaneously, and polyalcohol is caused to lose, and process energy consumption is high,
The problems such as polyester polyol product specification is poor.
Utility model content
Purpose of utility model: the purpose of this utility model is that being deposited for traditional batch stirred-tank reactor production technology
The technical issues of, a kind of device of aromatic polyester polyol synthesis, the spy of Dicarboxylic Acids and diol reaction are provided
Whole flow process is divided into three phases by point, is carried out for the reaction characteristics of different phase to entire reaction process and device structure
Optimization.
Technical solution: a kind of device of aromatic polyester polyol synthesis described in the utility model, including it is mixer, polynary
Alcohol pans, reaction kettle of the esterification, batch condensation polymerization reactor, Intermediate Heat Exchanger, reconcile reaction kettle, polyalcohol recovery tower, overhead condenser,
Return tank of top of the tower, control valve group and delivery pump；
The mixer is equipped with organic carboxyl acid feed inlet, mixer polyalcohol feed inlet and mixer discharge port, described more
First alcohol pans are equipped with fresh polyalcohol feed inlet, polyalcohol feed inlet and pans polyalcohol discharge port after recycling, it is described in
Between tank polyalcohol discharge port connect with mixer polyalcohol feed inlet, and connecting tube be equipped with the first control valve group；
Reaction kettle of the esterification gaseous phase outlet, reaction kettle of the esterification inert gas import, side are equipped at the top of the reaction kettle of the esterification
Equipped with reaction kettle of the esterification feed inlet, the reaction kettle of the esterification feed inlet is connect with mixer discharge port, after bottom portion is equipped with esterification
Material discharge port, which connect with the first conveying pump inlet, and discharge port is equipped with the second control valve group；Reaction kettle of the esterification
For atmospheric operation；
Batch condensation polymerization reactor gaseous phase outlet, batch condensation polymerization reactor vacuum system interface and benefit are equipped at the top of the batch condensation polymerization reactor
Polyalcohol feed inlet is filled, side is equipped with batch condensation polymerization reactor mixed material feed inlet, and the outlet of the feed inlet and the first delivery pump connects
It connects；Bottom portion is equipped with material discharge port after polycondensation, which connect with the second conveying pump inlet, and discharge port is equipped with the 4th
Control valve group, while the import of the second delivery pump is also connected with catalyst charge pipe；The Intermediate Heat Exchanger is set to the second conveying
On the efferent duct of pump；The supplement polyalcohol feed inlet is connect with pans polyalcohol discharge port, and connecting tube is equipped with third
Control valve group；Batch condensation polymerization reactor is vacuumizing；
It is true that additive inlet port, reconciliation reaction kettle inert gas import and reconciliation reaction kettle are equipped at the top of the reconciliation reaction kettle
Empty system interface, side are equipped with batch condensation polymerization reactor and are mixed into material mouth, and the feed inlet and the second conveying pump main outlet connect, and adjust
Polyester polyol outlet for product is equipped with reactor bottom；The reaction kettle that reconciles is normal pressure or vacuumizing；
The polyalcohol recovery tower tower bottom has recovery tower polyalcohol discharge port, and the discharge port and polyalcohol intermediate storage tank are fed
Mouthful connection, the polyalcohol recovery tower lower side are equipped with gas-phase feed mouth at two, at one with reaction kettle of the esterification gaseous phase outlet phase
Even, another place is connected with batch condensation polymerization reactor gaseous phase outlet, and recovery tower gaseous phase outlet, the gas are equipped at the top of the polyalcohol recovery tower
Mutually outlet is connected with overhead condenser import；The overhead condenser outlet is connect with return tank of top of the tower feed inlet, the tower top
The material refluxing opening of return tank is connect with the refluxing opening of polyalcohol recovery tower top-side, and the overhead reflux tank top is equipped with not
Solidifying gas outlet, bottom is equipped with material and produces mouth.
Further, it is equipped with agitating device inside the reaction kettle of the esterification and batch condensation polymerization reactor, outer surface, which is equipped with, leads
Hot oil heat tracing collet or steam tracing coil pipe.
Further, also being provided with agitating device in the reconciliation reaction kettle.
The technique that aromatic polyester polyol synthesis is carried out using the device of above-mentioned aromatic polyester polyol synthesis, including
Following steps:
1.1, organic polycarboxylic acid and polyalcohol difference slave carboxylic acid feed mouth, the mixer for being preheating to certain temperature are polynary
Alcohol feed inlet enters mixer, is sent into reaction kettle of the esterification after mixing in mixer, carries out under inert gas protection
The esterification of one step, reaction generates a large amount of water, polyester polyols alcohol monomer, remaining polyalcohol and other by-products, wherein entirely
Portion's water and excessive polyalcohol and by-product enter polyalcohol recovery tower through gaseous phase outlet with gas phase, carry out polyalcohol
Recycling, wherein organic polycarboxylic acid is preheating to 100-200 DEG C, and dihydric alcohol is preheating to 70-150 DEG C；Reaction time is 0.5-6h, excellent
It is selected as 2-3.5h, reaction kettle of the esterification bottom discharge port control valve is opened, and polyester polyols alcohol monomer is from reactor bottom material outlet
Extraction, is pumped into batch condensation polymerization reactor through delivery pump together with catalyst；
1.2, polyester polyols alcohol monomer and catalyst that step 1.1 produces are pumped into batch condensation polymerization reactor through delivery pump, are contracted
Poly- reaction kettle uses vacuumizing, and under inert gas protection, polyester polyols alcohol monomer is under the action of catalyst in polycondensation reaction
Polycondensation dehydration is carried out in kettle, to supplement certain weight polyalcohol in reaction process, it is organic more in the polyalcohol of supplement and charging
The molar ratio of first carboxylic acid is 0.1-1, preferably 0.1-0.5；Polycondensation reaction is promoted to carry out thoroughly, polycondensation reaction time 0.5-
8h, preferably 2-4h, reaction time are determined by the carboxylic value and hydroxyl value of periodic measurement material, when hydroxyl value concentration is less than
500mgKOH/g, when carboxylic value is less than 5mgKOH/g, polycondensation reaction can terminate, and material goes out after the polycondensation of batch condensation polymerization reactor bottom
Material mouth produces polyester polyol polymer；The water and a small amount of polyalcohol that polycondensation reaction generates enter polyalcohol through gaseous phase outlet and recycle
In tower, the recycling of polyalcohol is carried out；
1.3, the polyester polyol polymer that step 1.2 produces is pumped into Intermediate Heat Exchanger, through Intermediate Heat Exchanger that polyester is more
First alcohol polymer is cooled to 30-100 DEG C, preferably 40-80 DEG C, rear to be sent into reconciliation reaction kettle, under inert gas protection, by adding
Add different additive components to adjust the average molecular weight of polyester polyol polymer, the degree of polymerization, carboxylic value and hydroxyl value index, adjusts
Vacuum or atmospheric operation can be used with reaction kettle, the reaction kettle that reconciles is needed using inert gas seal, by going out in kettle
Material is detected and analyzed, and produces qualified products wait reconcile when material in reactor reaches desired value, which includes average
Molecular weight, carboxylic value and hydroxyl value index, average molecular weight 2000-5000, hydroxyl value are not more than 100mgKOH/g, and carboxylic value is little
In 1mgKOH/g；
1.4, step 1.1 and the gas phase of 1.2 extraction enter polyalcohol by two gas-phase feed mouth of polyalcohol recovery tower and recycle
In tower, after rectifying separates, polyalcohol feed inlet enters polyalcohol intermediate storage tank after tower bottom extraction polyalcohol is recovered, water and
A small amount of polyalcohol and other by-products enter return tank of top of the tower, return tank Partial Liquid Phase from tower top after overhead condenser condenses
Enter polyalcohol recovery tower, Partial Liquid Phase extraction through polyalcohol recovery tower refluxing opening, fixed gas is produced from overhead reflux tank top；
Preferably, the Dicarboxylic Acids are by phthalic acid, M-phthalic acid, terephthalic acid (TPA), 1,2,4- benzene
Tricarboxylic acid, 1, one or more kinds of in 3,5- benzenetricarboxylic acids and 2,6-naphthalenedicarboxylic acid to constitute, the polyalcohol is by ethylene glycol, two sweet
One of alcohol, polyethylene glycol, 1,2-PD, 1,3-PD, dipropylene glycol, 1,4-butanediol and neopentyl glycol or
The a variety of compositions of person.
Preferably, the catalyst is selected from following compounds: isopropyl titanate, tetrabutyl titanate, titanium ethylene glycolate, novel
Resistant to hydrolysis titanium catalyst, antimony oxide, antimony acetate, antimony glycol, germanium dioxide, dibutyl tin laurate, in phosphotungstic acid
It is one or more.
Preferably, the preferred isopropyl titanate of the catalyst or tetrabutyl titanate.
Further, the catalyst concn is 10-100ppm.
The preferred 20-50ppm of catalyst concn.
Further, the operating temperature of the mixer is 80-200 DEG C；Reaction kettle of the esterification operating pressure is -0.1Mpa-
0.1Mpa(absolute pressure), reaction temperature is 150-280 DEG C, and alcohol/acid molar ratio into reaction kettle of the esterification is 1.05-1.35；Polycondensation
Reaction kettle operating pressure is 0-0.1Mpa(absolute pressure), reaction temperature is 150-280 DEG C, supplement polyalcohol and more in batch condensation polymerization reactor
First carboxylic acid molar ratio is 0.05-0.30；The reaction kettle reaction temperature that reconciles is 30-150 DEG C, and operating pressure is -0.1Mpa-0.1Mpa
(absolute pressure)；
The additive includes antioxidant, acid value and hydroxyl value regulator；The antioxidant is acidic antioxidant or phosphorous
Acid esters kind antioxidant；Acidic antioxidant mainly has boric acid, hypophosphorous acid etc., and phosphite ester antioxidant mainly has phosphorous triphenyl phosphate
Ester, three nonyl phosphite esters etc..
The acid value and hydroxyl value regulator are the acid rich in hydroxyl value or carboxylic value, the alcohol rich in hydroxyl value or carboxylic value
Substance.Subsequent the reason of acids and alcohols material is added is the requirement according to different clients to the hydroxyl value and carboxylic value of product, is led to
Cross what addition acids or alcohols material in reconciliation reaction kettle were finally reached.
The theoretical cam curve of the polyalcohol recovery tower is 10-30 block, and operating pressure 0.01-0.4Mpa, reflux ratio is
1.2-5。
The utility model has the advantages that (1)
(1) production procedure is divided into esterification, polycondensation and reconciliation three phases, it is special for different phase material physical property and reaction
Property, different phase technological parameter and device parameter are optimized, norm controlling range of enhancing product performance, promotes esterification and contracting
Poly- reaction efficiency.
(2) esterification and polycondensation phase gas phase are taken out of to the polyalcohol and water and other by-products of reactor by setting rectifying column
Object is efficiently separated, and the system circulation of dihydric alcohol is realized, and is lost in the process less.
(3) a process route is realized by setting reconciliation reaction kettle, the polyester polyol of the production multiple performance trade mark produces
Product.
(4) the utility model method is simple, effect is good, high conversion rate, is conducive to reduce product in polyester polyol field
The content of the middle unfavorable impurity of nocuousness, index of enhancing product performance reduce the consumption of ton products material, meet industry development correlation political affairs
Plan.
Detailed description of the invention
Fig. 1 is the device and flow diagram of the synthesis of aromatic polyester polyol described in embodiment 1.
Wherein, V1- polyalcohol intermediate storage tank, M1- mixer, R1- reaction kettle of the esterification, R2- batch condensation polymerization reactor, R3- reconcile
Reaction kettle, T1- polyalcohol recovery tower, V2- return tank of top of the tower, E1- overhead condenser, E2- Intermediate Heat Exchanger, ZV1 ~ 4- first to
Five control valve groups, the first and second delivery pump of P1, P2-, 1- organic polycarboxylic acid, the charging of 2- polyalcohol, 3- enter the polynary of mixer
Alcohol, 4- polyester polyols alcohol monomer, 6- polyester polyol polymer, 8- catalyst, 9- polyester polyol product, 14- on-condensible gas,
17- vacuum system interface, 18- inert gas, 19- additive, 21- waste water.
Specific embodiment
Technical solutions of the utility model are described in detail below by attached drawing, but the protection scope of the utility model
It is not limited to the embodiment.
Embodiment 1: as shown in Figure 1, a kind of device of aromatic polyester polyol synthesis, including in mixer, polyalcohol
Between tank, reaction kettle of the esterification, batch condensation polymerization reactor, Intermediate Heat Exchanger, reconcile reaction kettle, polyalcohol recovery tower, overhead condenser, tower top
Return tank, control valve group and delivery pump；
The mixer is equipped with organic carboxyl acid feed inlet, mixer polyalcohol feed inlet and mixer discharge port, described more
First alcohol pans are equipped with fresh polyalcohol feed inlet, polyalcohol feed inlet and pans polyalcohol discharge port after recycling, it is described in
Between tank polyalcohol discharge port connect with mixer polyalcohol feed inlet, and connecting tube be equipped with the first control valve group；
Reaction kettle of the esterification gaseous phase outlet, reaction kettle of the esterification inert gas import, side are equipped at the top of the reaction kettle of the esterification
Equipped with reaction kettle of the esterification feed inlet, the reaction kettle of the esterification feed inlet is connect with mixer discharge port, after bottom portion is equipped with esterification
Material discharge port, which connect with the first conveying pump inlet, and discharge port is equipped with the second control valve group；Reaction kettle of the esterification
For atmospheric operation, agitating device and conduction oil heat tracing collet or steam tracing coil pipe are had；
Batch condensation polymerization reactor gaseous phase outlet, batch condensation polymerization reactor vacuum system interface and benefit are equipped at the top of the batch condensation polymerization reactor
Polyalcohol feed inlet is filled, side is equipped with batch condensation polymerization reactor mixed material feed inlet, and the outlet of the feed inlet and the first delivery pump connects
It connects；Bottom portion is equipped with material discharge port after polycondensation, which connect with the second conveying pump inlet, and discharge port is equipped with the 4th
Control valve group, while the import of the second delivery pump is also connected with catalyst charge pipe；The Intermediate Heat Exchanger is set to the second conveying
On the efferent duct of pump；The supplement polyalcohol feed inlet is connect with pans polyalcohol discharge port, and connecting tube is equipped with third
Control valve group；Batch condensation polymerization reactor is vacuumizing, with agitating device and conduction oil heat tracing collet or steam tracing coil pipe；Contracting
Vacuum system interface is equipped with the 5th control valve group at the top of poly- reaction kettle；
It is true that additive inlet port, reconciliation reaction kettle inert gas import and reconciliation reaction kettle are equipped at the top of the reconciliation reaction kettle
Empty system interface, side are equipped with batch condensation polymerization reactor and are mixed into material mouth, and the feed inlet and the second conveying pump main outlet connect, and adjust
Polyester polyol outlet for product is equipped with reactor bottom；The reaction kettle that reconciles is normal pressure or vacuumizing, with stirring dress
It sets；
The polyalcohol recovery tower tower bottom has recovery tower polyalcohol discharge port, and the discharge port and polyalcohol intermediate storage tank are fed
Mouthful connection, the polyalcohol recovery tower lower side are equipped with gas-phase feed mouth at two, at one with reaction kettle of the esterification gaseous phase outlet phase
Even, another place is connected with batch condensation polymerization reactor gaseous phase outlet, and recovery tower gaseous phase outlet, the gas are equipped at the top of the polyalcohol recovery tower
Mutually outlet is connected with overhead condenser import；The overhead condenser outlet is connect with return tank of top of the tower feed inlet, the tower top
The material refluxing opening of return tank is connect with the refluxing opening of polyalcohol recovery tower top-side, and the overhead reflux tank top is equipped with not
Solidifying gas outlet, bottom is equipped with material and produces mouth.
In the present embodiment, the processing step of aromatic polyester polyol synthesis is carried out using above-mentioned apparatus are as follows:
1.1, it is mixed that 140 DEG C of 16.6kg phthalic acid and the diethylene glycol (DEG) entrance for the 11.67kg for being preheating to 100 DEG C are preheating to
Clutch, mixer temperature are 140 DEG C, are sent into reaction kettle of the esterification, reaction kettle of the esterification operating pressure after mixing in mixer
For 0.1Mpa(absolute pressure), temperature is 180 DEG C, carries out the esterification of the first step under nitrogen protection, raw after reaction 2.5h reaction
At a large amount of water and polyester polyols alcohol monomer, remaining diethylene glycol (DEG) and other by-products, wherein water and excessive polyalcohol and pair
Product enters polyalcohol recovery tower through gaseous phase outlet with gas phase, carries out the recycling of polyalcohol.Reaction kettle of the esterification bottom discharge
Mouth control valve is opened, and polyester polyols alcohol monomer is produced from reactor bottom material outlet, is passed through together with catalyst tetrabutyl titanate
Delivery pump is pumped into batch condensation polymerization reactor；
1.2, that polyester polyols alcohol monomer and catalyst tetrabutyl titanate that step 1.1 produces are pumped into polycondensation through delivery pump is anti-
It answers in kettle, tetrabutyl titanate concentration is 50ppm, and batch condensation polymerization reactor uses vacuumizing, vacuum degree 5Kpa, and temperature is 225 DEG C.
Under nitrogen protection, polyester polyols alcohol monomer carries out polycondensation dehydration, reaction in batch condensation polymerization reactor under the action of catalyst
The diethylene glycol (DEG) of middle supplement 1.6Kg, reacts 2.5h, and the water and a small amount of polyalcohol that polycondensation reaction generates enter polyalcohol through gaseous phase outlet
In recovery tower, the recycling of polyalcohol is carried out；Material discharge port produces polyester polyol polymer after the polycondensation of batch condensation polymerization reactor bottom；
1.3, the polyester polyol polymer that step 1.2 produces is pumped into Intermediate Heat Exchanger, through Intermediate Heat Exchanger that polyester is more
First alcohol polymer is sent into reconciliation reaction kettle, reconciliation reaction kettle operating pressure 20Kpa after being cooled to 70 DEG C, temperature is 70 DEG C.In nitrogen
Under gas shielded, the modifying agent isophthalic anhydride of antioxidant triphenyl phosphite and 0.05wt% that 0.1wt% is added is poly- to adjust
The indexs such as average molecular weight, hydroxyl value and the carboxylic value of ester polyol polymer, final products average molecular weight are 2000, and water content is
0.03wt%, acid value 0.5mgKOH/g, hydroxyl value 80mgKOH/g.
1.4, step 1.1 and the gas phase of 1.2 extraction enter polyalcohol by two gas-phase feed mouth of polyalcohol recovery tower and recycle
In tower, the theoretical cam curve of polyalcohol recovery tower is 15 pieces, operating pressure 0.1Mpa, reflux ratio 1.5, tower top temperature 100
℃.After rectifying separates, tower bottom produces polyalcohol and enters polyalcohol intermediate storage tank through polyalcohol feed inlet, water and a small amount of polynary
Alcohol and other by-products enter return tank of top of the tower from tower top after overhead condenser condenses, and return tank Partial Liquid Phase is through polyalcohol
Recovery tower refluxing opening enters polyalcohol recovery tower, Partial Liquid Phase extraction, and fixed gas is produced from overhead reflux tank top.
As described above, although the utility model has been indicated and described referring to specific preferred embodiment, it must not
It is construed to the limitation to the utility model itself.In the spirit and scope for not departing from the utility model that appended claims define
Under the premise of, it can various changes can be made in the form and details to it.
Claims (3)
1. a kind of device of aromatic polyester polyol synthesis, it is characterised in that: including mixer, polyalcohol pans, esterification
Reaction kettle, batch condensation polymerization reactor, Intermediate Heat Exchanger, reconciliation reaction kettle, polyalcohol recovery tower, overhead condenser, return tank of top of the tower, control
Valve group processed and delivery pump；
The mixer is equipped with organic carboxyl acid feed inlet, mixer polyalcohol feed inlet and mixer discharge port, the polyalcohol
Pans are equipped with polyalcohol feed inlet and pans polyalcohol discharge port after fresh polyalcohol feed inlet, recycling, the pans
Polyalcohol discharge port is connect with mixer polyalcohol feed inlet, and connecting tube is equipped with the first control valve group；
Reaction kettle of the esterification gaseous phase outlet, reaction kettle of the esterification inert gas import are equipped at the top of the reaction kettle of the esterification, side is equipped with
Reaction kettle of the esterification feed inlet, the reaction kettle of the esterification feed inlet are connect with mixer discharge port, and bottom portion is equipped with material after esterification
Discharge port, which connect with the first conveying pump inlet, and discharge port is equipped with the second control valve group；
It is more that batch condensation polymerization reactor gaseous phase outlet, batch condensation polymerization reactor vacuum system interface and supplement are equipped at the top of the batch condensation polymerization reactor
First alcohol feed inlet, side are equipped with batch condensation polymerization reactor mixed material feed inlet, which connect with the outlet of the first delivery pump；Kettle
Bottom is equipped with material discharge port after polycondensation, which connect with the second conveying pump inlet, and discharge port is equipped with the 4th control
Valve group, while the import of the second delivery pump is also connected with catalyst charge pipe；The Intermediate Heat Exchanger is set to the second delivery pump
On efferent duct；The supplement polyalcohol feed inlet is connect with pans polyalcohol discharge port, and connecting tube is controlled equipped with third
Valve group；
Additive inlet port, reconciliation reaction kettle inert gas import and reconciliation reaction kettle vacuum system are equipped at the top of the reconciliation reaction kettle
System interface, side are equipped with batch condensation polymerization reactor and are mixed into material mouth, and the feed inlet and the second conveying pump main outlet connect, and reconciliation is anti-
Bottom portion is answered to be equipped with polyester polyol outlet for product；
The polyalcohol recovery tower tower bottom has recovery tower polyalcohol discharge port, and the discharge port and polyalcohol intermediate storage tank feed inlet connect
It connects, the polyalcohol recovery tower lower side is equipped with gas-phase feed mouth at two, is connected at one with reaction kettle of the esterification gaseous phase outlet, separately
It is connected at one with batch condensation polymerization reactor gaseous phase outlet, recovery tower gaseous phase outlet is equipped at the top of the polyalcohol recovery tower, which goes out
Mouth is connected with overhead condenser import；The overhead condenser outlet is connect with return tank of top of the tower feed inlet, the overhead reflux
The material refluxing opening of tank is connect with the refluxing opening of polyalcohol recovery tower top-side, and the overhead reflux tank top is equipped with fixed gas
Outlet, bottom are equipped with material and produce mouth.
2. a kind of device of aromatic polyester polyol synthesis according to claim 1, it is characterised in that: the esterification
Agitating device is equipped with inside kettle and batch condensation polymerization reactor, outer surface is equipped with conduction oil heat tracing collet or steam tracing coil pipe.
3. a kind of device of aromatic polyester polyol synthesis according to claim 1, it is characterised in that: the reconciliation reaction
Agitating device also is provided in kettle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201821865198.XU CN209383684U (en) | 2018-11-13 | 2018-11-13 | A kind of device of aromatic polyester polyol synthesis |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821865198.XU CN209383684U (en) | 2018-11-13 | 2018-11-13 | A kind of device of aromatic polyester polyol synthesis |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109096474A (en) * | 2018-11-13 | 2018-12-28 | 中建安装工程有限公司 | A kind of device and technique of aromatic polyester polyol synthesis |
| CN109762152A (en) * | 2018-11-28 | 2019-05-17 | 吕悦 | A kind of high-flexibility polyester resin and preparation method thereof and preparation facilities |
-
2018
- 2018-11-13 CN CN201821865198.XU patent/CN209383684U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109096474A (en) * | 2018-11-13 | 2018-12-28 | 中建安装工程有限公司 | A kind of device and technique of aromatic polyester polyol synthesis |
| CN109096474B (en) * | 2018-11-13 | 2023-08-25 | 中建安装集团有限公司 | Device and process for synthesizing aromatic polyester polyol |
| CN109762152A (en) * | 2018-11-28 | 2019-05-17 | 吕悦 | A kind of high-flexibility polyester resin and preparation method thereof and preparation facilities |
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