CN112520931A - Purification method and device for PTA (purified terephthalic acid) refining mother liquor - Google Patents
Purification method and device for PTA (purified terephthalic acid) refining mother liquor Download PDFInfo
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- CN112520931A CN112520931A CN202110097033.2A CN202110097033A CN112520931A CN 112520931 A CN112520931 A CN 112520931A CN 202110097033 A CN202110097033 A CN 202110097033A CN 112520931 A CN112520931 A CN 112520931A
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- 239000012452 mother liquor Substances 0.000 title claims abstract description 66
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000000746 purification Methods 0.000 title claims abstract description 21
- 238000007670 refining Methods 0.000 title claims abstract description 19
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 title description 57
- LPNBBFKOUUSUDB-UHFFFAOYSA-N p-toluic acid Chemical compound CC1=CC=C(C(O)=O)C=C1 LPNBBFKOUUSUDB-UHFFFAOYSA-N 0.000 claims abstract description 78
- 238000000605 extraction Methods 0.000 claims abstract description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000008213 purified water Substances 0.000 claims abstract description 10
- 238000004065 wastewater treatment Methods 0.000 claims abstract description 9
- 239000012071 phase Substances 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 6
- 239000000945 filler Substances 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 4
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 238000004064 recycling Methods 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 4
- ZWLPBLYKEWSWPD-UHFFFAOYSA-N o-toluic acid Chemical compound CC1=CC=CC=C1C(O)=O ZWLPBLYKEWSWPD-UHFFFAOYSA-N 0.000 abstract description 4
- 238000010924 continuous production Methods 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- 239000002351 wastewater Substances 0.000 description 14
- 230000008569 process Effects 0.000 description 11
- 238000007254 oxidation reaction Methods 0.000 description 10
- 230000003647 oxidation Effects 0.000 description 9
- 239000002904 solvent Substances 0.000 description 7
- GOUHYARYYWKXHS-UHFFFAOYSA-N 4-formylbenzoic acid Chemical compound OC(=O)C1=CC=C(C=O)C=C1 GOUHYARYYWKXHS-UHFFFAOYSA-N 0.000 description 6
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- 239000012535 impurity Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000001223 reverse osmosis Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000007792 gaseous phase Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000000108 ultra-filtration Methods 0.000 description 3
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical compound OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- XNGIFLGASWRNHJ-UHFFFAOYSA-N phthalic acid Chemical compound OC(=O)C1=CC=CC=C1C(O)=O XNGIFLGASWRNHJ-UHFFFAOYSA-N 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- WWYFPDXEIFBNKE-UHFFFAOYSA-N 4-(hydroxymethyl)benzoic acid Chemical compound OCC1=CC=C(C(O)=O)C=C1 WWYFPDXEIFBNKE-UHFFFAOYSA-N 0.000 description 1
- 239000005711 Benzoic acid Substances 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 235000010233 benzoic acid Nutrition 0.000 description 1
- 150000001735 carboxylic acids Chemical class 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/48—Separation; Purification; Stabilisation; Use of additives by liquid-liquid treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/26—Treatment of water, waste water, or sewage by extraction
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to the technical field of chemical wastewater treatment, and discloses a purification method of PTA refining mother liquor, which comprises the following steps: step a: extracting p-toluic acid in PTA refining mother liquor by PX; step b: stripping the refined mother liquor from which the p-toluic acid is removed; step c: rectifying the refined mother liquor with PX removed. The invention also discloses a device for purifying the PTA refined mother liquor, which comprises an extraction tower, a stripping tower and a rectifying tower, wherein the top of the rectifying tower is connected with a heat pump compressor through a pipeline, and a tower kettle of the rectifying tower is connected with a tower kettle reboiler through a pipeline. The invention realizes the recycling of the methyl benzoic acid, realizes the heat pump rectification by the rectifying tower, the heat pump compressor and the tower kettle reboiler, can obtain high-quality purified water, realizes the recycling of water resources, and has the characteristics of short flow, low energy consumption, less pollution and continuous production.
Description
Technical Field
The invention relates to the technical field of chemical wastewater treatment, in particular to a purification method and a purification device for PTA refining mother liquor.
Background
The PTA production process mainly comprises an oxidation reaction process and a hydrofining process, wherein in the oxidation process, two methyl groups on a benzene ring are sequentially converted into alcohol, aldehyde and acid through p-xylene liquid-phase air oxidation to obtain solid Crude Terephthalic Acid (CTA), and then p-carboxybenzaldehyde (4-CBA) which is a main impurity in the solid is reduced into p-toluic acid which is easily soluble in water through the hydrofining process to be removed. According to the characteristic that the solubility of the p-toluic acid in water is much higher than that of the phthalic acid in water, the crude terephthalic acid is subjected to impurity removal by hydrogenation, and then is subjected to crystallization, centrifugal separation, drying, dehydration and other processes to produce a refined PTA finished product. Therefore, in the hydrorefining process, a large amount of water is practically required as the water for dissolving terephthalic acid, and a large amount of wastewater is generated after crystallization and centrifugal filtration, and is generally referred to as a refining mother liquor in the industry. P-toluic acid is both a major impurity in these refined mother liquors and an intermediate product of the PX oxidation process. If the p-toluic acid in the refined mother liquor can be recovered, the PTA wastewater can be purified and returned to the hydrofining process to be used as solvent water for recycling, and the p-toluic acid can be recovered to improve the yield of PTA, so that the two purposes are achieved.
In recent years, PX is mainly used as an extractant in the treatment of a purification mother liquor to extract the purification mother liquor. Raw material PX is used as a solvent to extract p-toluic acid in the wastewater, and then the PX and the p-toluic acid are returned to an oxidation reactor together, so that the p-toluic acid can be converted into a product PTA through deep oxidation. On one hand, the method saves the PX regeneration step, reduces the extraction cost, on the other hand, can purify PTA wastewater, returns the PTA wastewater to the hydrofining process to be used as solvent water for recycling, and can also recover the p-toluic acid, thereby achieving three purposes. PX is similar to the structure of p-toluic acid, p-toluic acid is easy to extract from a water phase to a solvent phase, the PX is insoluble in water, trace PX remained in the extracted water can be completely removed through gas stripping, and the PX is recovered after gas cooling, so that the PX is the optimal extractant.
The invention discloses a method for treating PTA refined wastewater by adopting a combination of extraction-ultrafiltration-reverse osmosis, wherein p-xylene is adopted to extract refined wastewater of purified terephthalic acid, an extract phase is returned to a preparation process of purified terephthalic acid, a raffinate phase is subjected to ultrafiltration and reverse osmosis treatment, the permeated water reaches the recycling standard, and concentrated water is returned to an extraction step of p-xylene or to a preparation process of purified terephthalic acid. The invention needs to be used by matching extraction with an ultrafiltration reverse osmosis system, but the ultrafiltration reverse osmosis system has short service life, needs to be replaced frequently and has high process cost.
The invention patent of the publication No. CN102910761B discloses a technology for reducing the COD in PTA wastewater by an extraction method, which firstly uses a solvent to extract a large amount of organic carboxylic acids such as benzoic acid, p-toluic acid, p-carboxybenzyl alcohol, p-carboxybenzaldehyde, terephthalic acid and the like in the wastewater, and then uses a stripping method to remove residual PX, thereby greatly reducing the COD concentration in the wastewater. The invention adopts extraction and stripping methods to reduce COD in the refined mother liquor, but the energy consumption of common stripping is higher.
Disclosure of Invention
The invention aims to provide a purification device of PTA refining mother liquor, which solves the problems in the prior art.
In order to achieve the above object, in one aspect, the present invention provides the following technical solutions: a purification method of PTA refining mother liquor comprises the following steps:
step a: extracting p-toluic acid in PTA refined mother liquor by PX in an extraction tower, collecting PX containing p-toluic acid at the top of the extraction tower, and collecting refined mother liquor from which p-toluic acid is removed from the tower kettle of the extraction tower;
step b: sending the refined mother liquor without the p-toluic acid to a stripping tower for stripping, extracting mixed steam of PX and water from the top of the stripping tower, and extracting the refined mother liquor without the PX from a tower kettle of the stripping tower;
step c: and (3) sending the refined mother liquor without PX to a rectifying tower for rectification, extracting purified water from the top of the rectifying tower, and sending the concentrated solution extracted from the tower kettle of the rectifying tower to a wastewater treatment device.
On the other hand, the invention also provides the following technical scheme: a purification device of PTA refining mother liquor comprises
The extraction tower is used for extracting the p-toluic acid in the PTA refining mother liquor through PX;
the stripping tower is used for stripping the PTA refined mother liquor from which the p-methylbenzoic acid is removed and removing PX in the PTA refined mother liquor;
the rectifying tower is used for rectifying the PTA refined mother liquor from which PX is removed and concentrating the PTA refined mother liquor;
the PTA refined mother liquor with PX removed enters the middle part of the rectifying tower, the top of the rectifying tower is connected with a heat pump compressor through a pipeline, a tower kettle of the rectifying tower is connected with a tower kettle reboiler through a pipeline, the heat pump compressor is used for heating a gas phase from the rectifying tower, and the tower kettle reboiler is used for heating a liquid phase from the rectifying tower by using the heated gas phase as a heat source.
Optionally, a backup cooler is included for cooling the gas phase withdrawn from the kettle reboiler.
Optionally, the mass transfer element in the extraction tower is an anti-clogging filler or an anti-clogging tray, the operating pressure of the extraction tower is 0.2 MPaG-2.0 MPaG, and the operating temperature of the extraction tower is 50-170 ℃; PX and PTA refined mother liquor are in countercurrent contact in the extraction tower.
Optionally, the mass transfer element of the stripping tower is a filler or a tray, the operating pressure of the stripping tower is 0.02 MPaG-0.2 MPaG, and the operating temperature of the stripping tower is 105-120 ℃.
Optionally, the operating pressure of the rectifying tower is-0.04 MPaG to-0.06 MPaG, and the operating temperature of the rectifying tower is 50-90 ℃.
Optionally, the compression ratio of the heat pump compressor is 1.5-2.5.
Compared with the prior art, the invention provides a purification method and a purification device for PTA refining mother liquor, which have the following beneficial effects: the invention realizes the recycling of the methyl benzoic acid, realizes the heat pump rectification through the rectifying tower, the heat pump compressor and the tower kettle reboiler, can obtain high-quality purified water, realizes the recycling of water resources, greatly reduces the waste water discharge, has the characteristics of short flow, low energy consumption, less pollution, continuous production realization and great economic benefit, environmental benefit, social benefit and implementation value.
Drawings
Fig. 1 is a schematic structural view of the whole of the present invention.
In the figure: 1. an extraction tower; 2. a stripping column; 3. a rectifying tower; 4. a heat pump compressor; 5. a tower kettle reboiler; 6. a backup cooler.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example (b): referring to fig. 1, the present invention provides a purification method of PTA refining mother liquor, comprising the following steps:
step a: extracting p-toluic acid in PTA refined mother liquor by PX in an extraction tower 1, extracting PX containing p-toluic acid from the top of the extraction tower 1, and extracting refined mother liquor without p-toluic acid from the tower kettle of the extraction tower 1;
step b: sending the refined mother liquor without the p-toluic acid to a stripping tower 2 for stripping, extracting mixed steam of PX and water from the top of the stripping tower 2, and extracting the refined mother liquor without the PX from a tower kettle of the stripping tower 2;
step c: the refined mother liquor without PX is sent to a rectifying tower 3 for rectification, purified water is extracted from the top of the rectifying tower 3, and concentrated solution extracted from the tower kettle of the rectifying tower 3 is sent to a wastewater treatment device.
The invention also provides a device adopting the purification method of the PTA refined mother liquor, which comprises an extraction tower 1 for extracting the p-methylbenzoic acid in the PTA refined mother liquor through PX, a stripping tower 2 for stripping the PTA refined mother liquor without the p-methylbenzoic acid, a rectification tower 3 for rectifying the PTA refined mother liquor without the PX, a heat pump compressor 4 connected with the top of the rectification tower 3 through a pipeline, a tower kettle reboiler connected with the tower kettle of the rectification tower 3 through a pipeline, and a spare cooler 6 for cooling the gas phase extracted from the tower kettle reboiler 5. Wherein, the heat pump compressor 4 is used for heating the gaseous phase that comes from the rectifying column 3, and the cauldron reboiler 5 is used for adopting the gaseous phase that has heated as the heat source heating to come from the liquid phase of rectifying column 3, and the gaseous phase of following cauldron reboiler 5 after the condensation of reserve cooler 6, partly as the backward flow, flows back into rectifying column 3, and partly as the purified water, draws the retrieval and utilization.
Raw material PX in the PTA production process is used as an extracting agent in the extraction tower 1, the raw material PX and PTA refined mother liquor are in countercurrent contact in the extraction tower 1, the p-toluic acid is removed under the action of a mass transfer element in the extraction tower 1, and PX containing the p-toluic acid is extracted from the top of the extraction tower 1 and enters an oxidation unit. Wherein, the mass transfer element in the extraction tower 1 adopts anti-blocking filler, the operating pressure of the extraction tower 1 is 0.2 MPaG-2.0 MPaG, and the operating temperature of the extraction tower 1 is 50-170 ℃.
The stripping tower 2 removes PX in PTA refined mother liquor through stripping operation, a reboiler is arranged at a tower kettle of the stripping tower 2, stripping heat is provided through low-pressure steam, mixed steam of the PX and part of water is extracted from the top of the stripping tower 2, and the refined mother liquor with the PX removed is extracted from the tower kettle of the stripping tower 2. Wherein, the mass transfer element of the stripping tower 2 adopts a conventional tower tray, the operating pressure of the stripping tower 2 is 0.02 MPaG-0.2 MPaG, and the operating temperature of the stripping tower 2 is 105-120 ℃.
The PTA refined mother liquor with PX removed enters the middle part of a rectifying tower 3, the rectifying tower 3 concentrates the PTA refined mother liquor through rectification operation, separation of water and heavy component impurities is realized in the rectifying tower 3, COD in purified water is further reduced, high-purity purified water is obtained at the top of the rectifying tower 3, and concentrated refined mother liquor residual liquid is extracted from a tower kettle of the rectifying tower 3 and is sent to a wastewater treatment device. Wherein the operating pressure of the rectifying tower 3 is-0.04 MPaG to-0.06 MPaG, the operating temperature of the rectifying tower 3 is 50-90 ℃, and the compression ratio of the heat pump compressor 4 is 1.5-2.5.
The purification device adopts raw material PX as solvent to extract the p-toluic acid in the wastewater, can return PX and the p-toluic acid to an oxidation reactor together, can convert the p-toluic acid into product PTA through deep oxidation, saves the regeneration step of PX, reduces the extraction cost, can purify PTA wastewater on one hand, returns the PTA wastewater to a hydrorefining process to be recycled as solvent water, and can also recover the p-toluic acid. In addition, the heat pump rectification is realized through the rectifying tower 3, the heat pump compressor 4 and the tower kettle reboiler 5, the refined mother liquor with the p-toluic acid and PX removed is refined, high-quality purified water is obtained on the premise of not consuming steam, the recycling of most of water is realized, the energy consumption is reduced, and the water resource is saved. In addition, after separation of heat pump rectification, most of refined mother liquor is extracted from the standby cooler 6 in the form of purified water and is recycled to the oxidation working section of the PTA device, and only a small amount of concentrated solution is extracted from the tower kettle of the rectification tower 3 and is sent to a wastewater treatment device, so that the wastewater treatment capacity is reduced, and the wastewater treatment cost is saved.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. A purification method of PTA refining mother liquor is characterized in that: the method comprises the following steps:
step a: extracting p-toluic acid in PTA refined mother liquor by PX in an extraction tower, collecting PX containing p-toluic acid at the top of the extraction tower, and collecting refined mother liquor from which p-toluic acid is removed from the tower kettle of the extraction tower;
step b: sending the refined mother liquor without the p-toluic acid to a stripping tower for stripping, extracting mixed steam of PX and water from the top of the stripping tower, and extracting the refined mother liquor without the PX from a tower kettle of the stripping tower;
step c: and (3) sending the refined mother liquor without PX to a rectifying tower for rectification, extracting purified water from the top of the rectifying tower, and sending the concentrated solution extracted from the tower kettle of the rectifying tower to a wastewater treatment device.
2. The utility model provides a purifier of PTA refined mother liquor which characterized in that: comprises that
The extraction tower is used for extracting the p-toluic acid in the PTA refining mother liquor through PX;
the stripping tower is used for stripping the PTA refined mother liquor from which the p-methylbenzoic acid is removed and removing PX in the PTA refined mother liquor;
the rectifying tower is used for rectifying the PTA refined mother liquor from which PX is removed and concentrating the PTA refined mother liquor;
the PTA refined mother liquor with PX removed enters the middle part of the rectifying tower, the top of the rectifying tower is connected with a heat pump compressor through a pipeline, a tower kettle of the rectifying tower is connected with a tower kettle reboiler through a pipeline, the heat pump compressor is used for heating a gas phase from the rectifying tower, and the tower kettle reboiler is used for heating a liquid phase from the rectifying tower by using the heated gas phase as a heat source.
3. The purification apparatus of PTA refining mother liquor according to claim 2, wherein: a backup cooler is included for cooling the gas phase withdrawn from the kettle reboiler.
4. The purification apparatus of PTA refining mother liquor according to claim 2, wherein: the mass transfer element in the extraction tower is an anti-clogging filler or an anti-clogging tower tray, the operating pressure of the extraction tower is 0.2 MPaG-2.0 MPaG, and the operating temperature of the extraction tower is 50-170 ℃; PX and PTA refined mother liquor are in countercurrent contact in the extraction tower.
5. The purification apparatus of PTA refining mother liquor according to claim 2, wherein: the mass transfer element of the stripping tower is a filler or a tower tray, the operating pressure of the stripping tower is 0.02 MPaG-0.2 MPaG, and the operating temperature of the stripping tower is 105-120 ℃.
6. The purification apparatus of PTA refining mother liquor according to claim 2, wherein: the operating pressure of the rectifying tower is-0.04 MPaG to-0.06 MPaG, and the operating temperature of the rectifying tower is 50-90 ℃.
7. The purification apparatus of PTA refining mother liquor according to claim 2, wherein: the compression ratio of the heat pump compressor is 1.5-2.5.
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| CN114507128A (en) * | 2022-02-17 | 2022-05-17 | 吴桥县六合德利化工有限责任公司 | Refining process of p-toluic acid |
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| CN106866412A (en) * | 2017-02-17 | 2017-06-20 | 福州大学 | The group technology of organic matter in a kind of recovery PTA refined wastewaters |
| CN111635293A (en) * | 2020-05-14 | 2020-09-08 | 天津市汇筑恒升科技有限公司 | Sodium methoxide production device and method |
| CN214299725U (en) * | 2021-01-25 | 2021-09-28 | 天津市汇筑恒升科技有限公司 | Purification device for PTA (purified terephthalic acid) refining mother liquor |
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| CN114507128A (en) * | 2022-02-17 | 2022-05-17 | 吴桥县六合德利化工有限责任公司 | Refining process of p-toluic acid |
| CN114507128B (en) * | 2022-02-17 | 2023-10-03 | 吴桥县六合德利化工有限责任公司 | Process for refining p-methylbenzoic acid |
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