CN217661977U

CN217661977U - Bisphenol A is with purification system

Info

Publication number: CN217661977U
Application number: CN202221866642.6U
Authority: CN
Inventors: 韩向阳; 田大春; 江岭; 黄成�; 陈丽
Original assignee: Sichuan Fengyong Technology Co ltd
Current assignee: Sichuan Fengyong Technology Co ltd
Priority date: 2022-07-20
Filing date: 2022-07-20
Publication date: 2022-10-28
Anticipated expiration: 2032-07-20

Abstract

The utility model discloses a purification system for bisphenol A belongs to bisphenol A production technical field, including resin adsorption unit, crystal unit and filter unit, the feed end of resin adsorption unit links to each other with thick bisphenol A inlet pipe and phenol inlet pipe, and the discharge end of resin adsorption unit links to each other with the feed end of crystal unit, and the discharge end of crystal unit links to each other with the feed end of filter unit. Crude bisphenol A enters the resin adsorption unit through a crude bisphenol A feeding pipe, impurities which are not beneficial to crystallization are selectively adsorbed by specific resin in the resin adsorption unit, mainly chroman, dimer, trisenol, trischroman and the like, so that the crystallization mixture mainly contains phenol, P-bisphenol A, other impurities are greatly reduced, and then the high-purity bisphenol A meeting the requirements can be obtained through the crystallization unit and the filtration unit. The utility model has the advantages of reduce investment and operation cost, obtain high-purity bisphenol A.

Description

Bisphenol A is with purification system

Technical Field

The utility model belongs to the technical field of bisphenol A production, concretely relates to bisphenol A is purification system for technology, because the innovation of purification system has optimized bisphenol A production procedure, reduced the required energy consumption of the processing equipment of purification processing and purification processing.

Background

"bisphenol A" or "p, p' -bisphenol A" is well known as an abbreviation for 2, 2-bis (4-hydroxyphenyl) -propane prepared by the condensation reaction of phenol and acetone. Bisphenol-a is a product of high technical and commercial importance when used in the manufacture of many commercial products such as polycarbonates and epoxy resins. Worldwide production of bisphenol a in excess of 600 million tons in 2020, and still continues to increase. High-purity bisphenol A is required in the production of high-quality epoxy resins, especially polycarbonates.

Bisphenol A can be produced by condensation reaction of acetone and an excess amount of phenol in the presence of a catalyst according to various known methods. The products of these known processes are bisphenol A and certain impurities including isomers, analogues and homologues, such as 2- (2-hydroxyphenyl) -2- (4-hydroxyphenyl) propane (hereinafter referred to as o, p' -bisphenol A), 2, 4-trimethyl-4- (4-hydroxyphenyl) chroman, trisphenol, polyphenolic and undesirable coloured substances. To meet the high technical and commercial requirements for producing high purity bisphenol-A, much research has been conducted on its purification. According to a known method, a mixture of bisphenol A and water can be prepared and the bisphenol A recrystallized by heating and subsequent cooling.

Chinese patent with publication number CN100424060C and publication date 20081008 discloses a method for purifying bisphenol-A, which comprises the following steps: a) Cooling a liquid mixture comprising bisphenol a and water in a bisphenol a crystallizer to form bisphenol a crystals in a liquid phase; b) Separating the bisphenol A crystals from the liquid phase; c) Separating at least a portion of the liquid phase into a bisphenol-rich organic phase and a water-rich phase; d) Feeding phenol and at least a portion of the bisphenol-rich organic phase to an adduct crystallizer to form a crystalline adduct of phenol and bisphenol-A in a mother liquor; e) Separating the crystalline adduct from the mother liquor; g) Contacting at least a portion of the mother liquor obtained in step e) with a catalyst to isomerize isomers of bisphenol a to bisphenol a; and h) recycling at least a portion of the mother liquor treated in step g) by feeding it to step d). The bisphenol A obtained by the method has low purity and large energy consumption.

SUMMERY OF THE UTILITY MODEL

In order to overcome the defects that the prior art generally carries out crystallization in a solution containing a large amount of impurities, the crystals are separated from the solution, and the crystals adsorb a large amount of impurities, so that the product purity is poor, and multiple crystallization is needed, the utility model aims to provide a purification system for bisphenol A, crude bisphenol A containing a large amount of impurities enters a resin adsorption unit of the application through a crude bisphenol A feeding pipe, and impurities which are not beneficial to crystallization, mainly chroman, dipolymer, trisenol, trischroman and the like, are selectively adsorbed by specific resin in the resin adsorption unit, so that a crystallization mixture solution mainly contains phenol, P-bisphenol A, other impurities are greatly reduced, and then the high-purity bisphenol A meeting the requirements can be obtained through a crystallization unit and a filtering unit; when the performance of the specific resin in the resin adsorption unit for adsorbing impurities is reduced, heated phenol enters the resin adsorption unit through the phenol feeding pipe to be desorbed, so that the resin adsorption unit obtains good impurity adsorption performance again, and the washed phenol containing a large amount of impurities is subjected to isomerization treatment and is recovered. The utility model has the advantages of reduce investment and operation cost, obtain high-purity bisphenol A.

The utility model aims at realizing through the following technical scheme:

the utility model provides a purification system for bisphenol A, includes resin adsorption unit, crystallization unit and filter unit, the feed end of resin adsorption unit links to each other with thick bisphenol A inlet pipe and phenol inlet pipe, the discharge end of resin adsorption unit links to each other with the feed end of crystallization unit, the discharge end of crystallization unit links to each other with the feed end of filter unit.

Preferably, the resin adsorption unit adopts an adsorption resin fixed bed or an adsorption resin fluidized bed, the crystallization unit adopts a crystallizer, and the filtration unit adopts a centrifuge or a plate-and-frame filter press or a filter.

Preferably, the discharge end of the filtering unit is connected with the feed end of the falling film dephenolizing unit, the discharge end of the falling film dephenolizing unit is connected with the feed end of the stripping unit, and the discharge end of the stripping unit is connected with the feed end of the granulating unit.

Preferably, the falling film dephenolization unit adopts a tube type film falling device, the stripping unit adopts a stripping tower, and the granulation unit adopts a granulation tower.

Preferably, the gas outlet end of the tube array type membrane falling device is connected with a tail gas condensing device.

Preferably, the regenerated material discharge end of the resin adsorption unit is connected with the feed end of the isomerization unit, the discharge end of the isomerization unit is connected with the feed end of the recovery crystallization unit, the discharge end of the recovery crystallization unit is connected with the feed end of the recovery filtration unit, the liquid outlet end of the recovery filtration unit is connected with the feed end of the crystallization unit, and the discharge end of the recovery filtration unit is connected with the feed end of the cracking unit.

Preferably, the isomerization unit adopts a cation exchange resin tower, the recovery crystallization unit adopts a crystallizer, the recovery filtration unit adopts a centrifuge or a plate and frame filter press or a filter, and the cracking unit adopts a cracking tower.

The beneficial effects of this technical scheme are as follows:

1. the utility model provides a pair of bisphenol A is with purification system, the thick bisphenol A who contains a large amount of impurity gets into the resin adsorption unit of this patent application through thick bisphenol A inlet pipe, and the impurity that is unfavorable for the crystallization is fallen in the selective absorption of specific resin in the resin adsorption unit, mainly is chroman, dimer, triphenol, trischroman etc. lets mainly contain phenol, P-bisphenol A in the crystallization mixture, and other impurity reduce by a wide margin, can obtain the high-purity bisphenol A who satisfies the requirement through crystallization unit and filter unit afterwards; when the performance of the specific resin in the resin adsorption unit for adsorbing impurities is reduced, heated phenol enters the resin adsorption unit through the phenol feeding pipe to be desorbed, so that the resin adsorption unit obtains good impurity adsorption performance again, and the washed phenol containing a large amount of impurities is subjected to isomerization treatment and is recovered. The utility model has the advantages of reduce investment and operation cost, obtain high-purity bisphenol A.

2. The utility model provides a pair of bisphenol A is with purification system, bisphenol A after resin adsorption, crystallization and filtration can obtain the bisphenol A that purity can reach 99.95% again after dephenolization and steam stripping, can obtain bisphenol A granule product through the granulation unit.

3. The utility model provides a pair of bisphenol A is with purification system, phenol through after the heating gets into the resin adsorption unit through the phenol inlet pipe and desorbs, the adsorbed impurity of resin can be dissolved in the heating phenol of desorption, then send cation exchange resin tower to carry out the isomerization and react, with 2,4-BPA, trisenol etc. transform into 4,4-BPA etc. because impurity content is high and is reached 20%, not only isomerization reaction efficiency is high, and, retrieve the crystal height, the filter liquor volume reduces by a wide margin, only be the existing technology third, thereby do not need the phenol distillation column, can directly get into the schizolysis unit, because the feeding contains trace luck group propionic acid, the schizolysis adopts sulphuric acid to be the catalyst, this catalytic process is lower than alkaline process temperature, regeneration impurity reduces.

Drawings

The foregoing and following detailed description of the invention will be apparent when read in conjunction with the following drawings, in which:

fig. 1 is a schematic structural diagram of the present invention;

fig. 2 is a schematic structural diagram of another embodiment of the present invention;

in the figure: 1. a resin adsorption unit; 2. a crystallization unit; 3. a filtration unit; 4. a crude bisphenol A feed tube; 5. a phenol feed pipe; 6. falling film dephenolizing mono; 7. a stripping unit; 8. a granulation unit; 9. an isomerization unit; 10. a crystallization unit is recovered; 11. a recovery filtration unit; 12. a cleavage unit.

Detailed Description

The technical solution for achieving the objectives of the present invention will be further described by using several specific examples, and it should be noted that the technical solution claimed in the present invention includes, but is not limited to, the following examples.

Example 1

As a basic embodiment of the utility model, the embodiment discloses a purification system for bisphenol A, as shown in FIG. 1, a purification system for bisphenol A, including resin adsorption unit 1, crystallization unit 2 and filter unit 3, the feed end of resin adsorption unit 1 links to each other with thick bisphenol A inlet pipe 4 and phenol inlet pipe 5, the discharge end of resin adsorption unit 1 links to each other with the feed end of crystallization unit 2, the discharge end of crystallization unit 2 links to each other with the feed end of filter unit 3. Crude bisphenol A containing a large amount of impurities enters the resin adsorption unit 1 of the application through a crude bisphenol A feeding pipe 4, specific resin (the specific resin comprises one or more of sulfonated styrene-divinylbenzene copolymer, sulfonated cross-linked styrene polymer, phenol formaldehyde-sulfonic acid resin and benzaldehyde-sulfonic acid resin) in the resin adsorption unit 1 selectively adsorbs impurities which are not beneficial to crystallization, mainly chroman, dimer, triphenol, trichlorman and the like, so that a crystallization mixture mainly contains phenol, P-bisphenol A, other impurities are greatly reduced, and then high-purity bisphenol A meeting the requirements can be obtained through a crystallization unit 2 and a filtering unit 3; when the impurity adsorption performance of the specific resin in the resin adsorption unit 1 is reduced, heated phenol (the temperature of the phenol is 100-150 ℃, and the amount of desorption solvent is not less than that of the phenol: resin = 600-800 g/l) enters the resin adsorption unit 1 through the phenol feeding pipe 5 for desorption, so that the resin adsorption unit 1 obtains good impurity adsorption performance again, and the washed phenol containing a large amount of impurities is subjected to de-isomerization treatment and is recovered. The utility model has the advantages of reduce investment and operation cost, obtain high-purity bisphenol A.

The resin adsorption unit 1 adopts an adsorption resin fixed bed or an adsorption resin fluidized bed, the crystallization unit 2 adopts a crystallizer, and the filtration unit 3 adopts a centrifuge or a plate and frame filter press or a filter.

Example 2

As shown in fig. 2, the present embodiment is different from embodiment 1 in that: the discharge end of the filtering unit 3 is connected with the feed end of the falling film dephenolizing unit 6, the discharge end of the falling film dephenolizing unit 6 is connected with the feed end of the stripping unit 7, and the discharge end of the stripping unit 7 is connected with the feed end of the granulating unit 8. Bisphenol A after resin adsorption, crystallization and filtration is dephenolized and stripped to obtain bisphenol A with the purity of 99.95 percent, and bisphenol A granular products can be obtained through a granulation unit 8.

The falling-film dephenolizing unit adopts a tube type film falling device for 6 units, the steam stripping unit 7 adopts a steam stripping tower, and the granulation unit 8 adopts a granulation tower.

And the gas outlet end of the tube array type membrane falling device is connected with a tail gas condensing device. The waste gas generated by the tube array type falling film device is treated by a tail gas condensing device and then discharged, so that the air pollution is reduced.

Wherein, the reclaimed material discharge end of the resin adsorption unit 1 is connected with the feed end of the isomerization unit 9, the discharge end of the isomerization unit 9 is connected with the feed end of the recovery crystallization unit 10, the discharge end of the recovery crystallization unit 10 is connected with the feed end of the recovery filtration unit 11, the liquid outlet end of the recovery filtration unit 11 is connected with the feed end of the crystallization unit 2, and the discharge end of the recovery filtration unit 11 is connected with the feed end of the cracking unit 12. The heated phenol enters the resin adsorption unit 1 through the phenol feeding pipe 5 for desorption, impurities adsorbed by the resin can be dissolved in the desorbed heated phenol, then the heated phenol is sent to a cation exchange resin tower for isomerization reaction, 2,4-BPA, triphenol and the like are converted into 4,4-BPA and the like, the content of the impurities reaches 20 percent, the isomerization reaction efficiency is high, the recovered crystal content is high, the amount of filter liquor is greatly reduced, which is only one third of the existing process, so that a phenol distillation tower is not needed, the phenol distillation tower can directly enter the cracking unit 12, and the cracking adopts sulfuric acid as a catalyst due to the fact that the feeding contains trace amount of thiopropionic acid, the catalytic process has lower temperature than an alkaline process, and the regeneration impurities are reduced.

The isomerization unit 9 adopts a cation exchange resin tower, the recovery crystallization unit 10 adopts a crystallizer, the recovery filtering unit 11 adopts a centrifuge or a plate-and-frame filter press or a filter, and the cracking unit 12 adopts a cracking tower.

Example 3

In this example, the same system as in example 2 is used, and the composition of crude bisphenol a includes P, P-BPA 21.87%, phenol 68.72%, water 1.2%, and other impurities about 8.21%, and mainly includes O, P-BPA 3.10%, O-BPA 0.05%, trisphenol 1.5285%, trisphenol 2.3269%, indane 0.787%, spiroindane 1.41%, trisphenol 1.13%, trischroman 0.3%, and trace amounts of IPP, chroman, and the like; crude bisphenol A enters a resin adsorbent of 100m ³ After the flow rate is 30 tons/hour, the composition of the reaction mixture is changed into P, P-BPA 24%, phenol 74%, water 0.2%, and other impurities about 1.80%, and the reaction mixture mainly comprises O, P-BPA 1.10%, O-BPA 0.01%, other impurities: trisphenol 1, trisphenol 2, indane, spiroindane, trisphenol, chroman, IPP, chroman, etc. in total about 0.8%; the reaction mixture is cooled to 54 ℃ to generate 12940kg of crystals in the crystallizer, wherein the crystals comprise 42.34 percent of phenol, 57.55 percent of 4,4-BPA and 0.11 percent of other impurities. The product can reach 99.93 percent after dephenolization and steam stripping.

After the fixed bed of the adsorption resin is saturated, phenol is desorbed by heating to 120-130 ℃, and the heated phenol components comprise 80% of phenol, 4% of P, P-BPA and about 16% of other impurities, and mainly comprise O, P-BPA, O-BPA, triphenol 1, triphenol 2, indane, spiroindane, trisphenol, trichloran, IPP, chroman and the like. And then carrying out isomerization treatment by a cation exchange resin tower, wherein O, P-BPA, O-BPA, trisphenol 1 and trisphenol 2 participate in the reaction, the treatment efficiency is 60-65%, and indan, spiroindan, trisphenol, trischroman, IPP, chroman and the like are cracked to realize maximum recovery.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A purification system for bisphenol A, characterized in that: including resin adsorption unit (1), crystallization unit (2) and filter unit (3), the feed end of resin adsorption unit (1) links to each other with thick bisphenol A inlet pipe (4) and phenol inlet pipe (5), the discharge end of resin adsorption unit (1) links to each other with the feed end of crystallization unit (2), the discharge end of crystallization unit (2) links to each other with the feed end of filter unit (3).

2. The purification system for bisphenol a as recited in claim 1, wherein: the resin adsorption unit (1) adopts an adsorption resin fixed bed or an adsorption resin fluidized bed, the crystallization unit (2) adopts a crystallizer, and the filtration unit (3) adopts a centrifuge or a plate-and-frame filter press or a filter.

3. A purification system for bisphenol a as described in claim 1 or 2, wherein: the discharge end of the filtering unit (3) is connected with the feed end of the falling film dephenolizing unit (6), the discharge end of the falling film dephenolizing unit (6) is connected with the feed end of the stripping unit (7), and the discharge end of the stripping unit (7) is connected with the feed end of the granulating unit (8).

4. A purification system for bisphenol a as defined in claim 3, wherein: the falling film dephenolizing unit (6) adopts a tube type film falling device, the steam stripping unit (7) adopts a steam stripping tower, and the granulating unit (8) adopts a granulating tower.

5. The purification system for bisphenol a as recited in claim 4, wherein: and the gas outlet end of the tube array type membrane falling device is connected with a tail gas condensing device.

6. A purification system for bisphenol a as defined in claim 3, wherein: the regeneration material discharge end of resin adsorption unit (1) links to each other with the feed end of isomerization unit (9), the discharge end of isomerization unit (9) links to each other with the feed end of retrieving crystallization unit (10), the discharge end of retrieving crystallization unit (10) links to each other with the feed end of retrieving filter unit (11), the play liquid end of retrieving filter unit (11) links to each other with the feed end of crystallization unit (2), the discharge end of retrieving filter unit (11) links to each other with the feed end of schizolysis unit (12).

7. The purification system for bisphenol a as recited in claim 6, wherein: the isomerization unit (9) adopts a cation exchange resin tower, the recovery crystallization unit (10) adopts a crystallizer, the recovery filtering unit (11) adopts a centrifuge or a plate and frame filter press or a filter, and the cracking unit (12) adopts a cracking tower.