WO2010081358A1 - Px oxidation reactor for producing terephthalic acid - Google Patents
Px oxidation reactor for producing terephthalic acid Download PDFInfo
- Publication number
- WO2010081358A1 WO2010081358A1 PCT/CN2009/075384 CN2009075384W WO2010081358A1 WO 2010081358 A1 WO2010081358 A1 WO 2010081358A1 CN 2009075384 W CN2009075384 W CN 2009075384W WO 2010081358 A1 WO2010081358 A1 WO 2010081358A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- reactor
- terephthalic acid
- producing terephthalic
- oxidation reactor
- air
- Prior art date
Links
Classifications
-
- 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
- B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/255—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting
- C07C51/265—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
Definitions
- the invention relates to the field of chemical equipment, and in particular to a PX oxidation reactor for producing terephthalic acid.
- the production process of the purified terephthalic acid (PTA) process is: a mixture of the raw material p-benzoquinone (PX) and the solvent acetic acid (HAC), in the presence of a catalyst, with oxygen in the air at a certain temperature and pressure.
- the oxidation reaction is carried out to form crude terephthalic acid (CTA), and the CTA is further refined to finally produce purified terephthalic acid (PTA).
- PX oxidation reactors are key equipment in this process, and different process oxidation reactors have different structural forms.
- the first type is a stirred bubble column reactor; the second type is a tank reactor with a stirrer, and the oxidation of these two types of structures
- the reactor can be produced.
- the difference is that there is a big difference between the equipment's primary input and long-term energy consumption.
- the reaction conditions it can be divided into three cases: high temperature oxidation process (191 ⁇ 205 °C), Medium temperature oxidation process (185 ⁇ 189 °C) and low temperature oxidation process (160 ⁇ 170 °C).
- PTA production in the world mainly uses high-temperature oxidation process, high-temperature oxidation process has a fast reaction rate, and uses a stirred tank to enhance mass transfer and heat transfer, high productivity per unit volume, large particle size of CTA crystal, and allowable water content in the reaction slurry.
- High the shortage is high PX and HAC, the cost of the agitator and compressor is high, and the equipment manufacturing is difficult; the requirements of the medium temperature oxidation process and the PX and HAC consumption are relatively moderate, and the reactor can be simple in structure.
- Bubbling tower instead of stirred tank, low equipment input and maintenance costs, low energy consumption, separation of CTA It is much easier to process with mother liquor than the low temperature process.
- the object of the present invention is to overcome the defects of the prior art and provide a novel PX oxidation reactor for producing terephthalic acid to save energy, reduce investment, reduce cost, and simple process, and realize large-scale production of parabens.
- the purpose of the acid is to overcome the defects of the prior art and provide a novel PX oxidation reactor for producing terephthalic acid to save energy, reduce investment, reduce cost, and simple process, and realize large-scale production of parabens.
- the reactor housing is provided with a columnar shape, preferably having a height-to-diameter ratio of 2. 8 ⁇ 5 , and the bottom of the reactor housing is provided. There are distributed air intake devices and swirling air intake devices.
- the distributed air intake device may include a plurality of air flow distribution tubes, and the air flow distribution tubes may generally have a circular shape with a center on a vertical center line of the casing, and a plurality of vent holes are provided in the pipe body.
- the air distribution tube may generally include an outer ring air distribution tube and an inner ring air distribution tube, the outer ring air distribution tube is adjacent to an inner wall of the housing, and the inner ring air distribution tube is located at a middle portion of the inner space of the housing. In the horizontal direction, the same below), the outer ring air distribution pipe and the inner ring air distribution pipe are connected with an intake pipe.
- the swirling air intake device may be constituted by a plurality of swirling air intake tubes located below the air flow distributing tubes.
- the number of the swirling intake pipes is plural, it should generally be evenly distributed The periphery of the inner wall of the housing.
- the invention adopts a combined air intake device composed of a distributed air intake device and a swirling air intake device, and pushes the fluid at the bottom of the reactor with an appropriate amount of air to make a rotary motion, and the gas is well dispersed and evenly distributed. Reduce the drift, can meet the needs of solid suspension, the use of the swirling gas distribution tube can effectively eliminate the bottom flow dead zone, keep the material in a normal suspension state, thus ensuring the safe and stable operation of the reactor for many years;
- the shell has a high aspect ratio between the high temperature and low temperature reactors, and the corresponding superficial gas velocity is also between the two, which can ensure good gas-liquid mass transfer and mixing, and can satisfy the uniform suspension of solids.
- the device adopts two annular flow distribution tube structures of the outer ring and the inner ring, which cooperate with the swirl flow formed by the swirling intake pipe to ensure effective advancement. And air amount and the distribution of mass transfer, not only simple in structure, and avoid damage to the swirling flow, no dead space, avoiding deposition of crystals produced by the reaction.
- Fig. 1 is a front view showing a PX oxidation reactor for producing terephthalic acid according to the present invention
- Fig. 2 is a plan view showing a bottom cross section of a PX oxidation reactor for producing terephthalic acid according to the present invention.
- a PX oxidation reactor for producing terephthalic acid includes a reactor casing 1 , and a distributed air intake device and a swirling inlet are arranged at the bottom of the reactor casing 1 .
- the reactor housing 1 can be generally in the shape of a tower, and has a height-to-diameter ratio of preferably 2. 8 ⁇ 5 .
- the high-diameter ratio of the superficial gas velocity is between the high-temperature and low-temperature reactors, thereby avoiding the high diameter.
- the uneven distribution phenomenon existing in the large-scale low-temperature reactor is superior to the high-temperature reactor with low power consumption.
- the distributed air intake device may include a plurality of air distribution tubes 2 (such as the outer ring air distribution tube 4 and the inner ring air distribution tube 5 shown in FIG. 2), the air distribution tube 2 is in a circular shape, and its center is at The vertical center line of the casing is provided with a plurality of vent holes 7 on the pipe body.
- the air intake device is provided with a swirling air intake device formed by the swirling air intake pipe 3 below the gas supply and air supply. Coordination can significantly improve the dispersion effect of the gas, ensure uniform air distribution, keep the material in a normal suspension state, avoid damage to the swirl, and avoid dead spots.
- the air distribution tube can generally include an outer ring air distribution tube 4 and an inner ring air distribution tube 5, the outer ring air distribution tube 4 is adjacent to the inner wall of the housing, and the inner ring air distribution tube 5 is located at the middle of the housing.
- the air flow can prevent the annular backflow that occurs when the side wall effect of the reactor is too large; the outer ring air distribution pipe 4 and the inner ring air distribution pipe 5 are connected to the intake pipe 6, and the inner ring distribution pipe 5 is located in the middle of the body, mainly It enhances the mass transfer in the middle of the reactor.
- the height (vertical position) of the inner ring air distribution tube 5 may be the same as the outer ring air distribution tube 4, or may be lower than the outer ring air distribution tube 4 to improve the air supply status at the central portion of the lower portion of the housing. .
- the gas distribution tube 2 can usually be connected to a support member 8.
- the swirling air intake device may be constituted by a plurality of swirling air intake pipes 3, usually below the air flow distributing pipe 2.
- the number of the swirling intake pipes 3 is plural, generally It is evenly distributed around the inner wall of the casing.
- Such a swirling air intake device can form a good swirling flow and, while driving the swirling of the liquid stream, also provides a portion of the amount of air required for the reaction.
- the outlet section of the swirling intake pipe 3 can be inclined by 45 to 60 with respect to the radius of the can body. , in order to form a proper swirl.
- the overall gas holdup rate is increased.
- the upper part of the reactor casing 1 is a gas-liquid separation section, and a packing layer 9 is provided.
- the packing layer 9 is filled with a structured packing 10, which can simultaneously dehydrate, defoam and recover solids.
- the upper part of the packing layer 9 can usually be installed.
- the reflux distributor has a separation space above and below to facilitate separation of TA solids and acetic acid solvent entrained in the ascending air stream.
- the middle portion of the gas-liquid separation section may be provided with a return port 11 and the top portion may be provided with a vapor phase outlet 12.
- the bottom of the reactor housing 1 is a bubbling zone, and the bottom of the reactor housing is preferably a spherical head, and the volume of the head is multi-dimensionally intakeed through a plurality of swirling intake manifolds of the respective hooks.
- the gas-liquid contact is sufficiently uniform, leaving no dead zone, and the liquid has a regular rotating motion, so that the wall is self-cleaning, and the discharge port 13 is opened at the bottom of the head.
- the spherical head can avoid the small diameter transition section of other shape heads such as a dish or an ellipse, which is favorable for the reaction product to be smoothly discharged from the discharge port 13.
- the middle part of the reactor casing 1 is a heterogeneous reaction section, wherein the lower part is provided with a feed port 14, and the reaction material and the catalyst are thoroughly mixed and then fed into the reactor from the feed port 14 to be in full contact with the air rising from the bottom. Oxidation reaction.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
RU2011133892/04A RU2505524C2 (en) | 2009-01-15 | 2009-12-08 | Reactor of paraxylol oxidation for obtaining terephthalic acid |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN200910076703.1 | 2009-01-15 | ||
CN200910076703A CN100594972C (en) | 2009-01-15 | 2009-01-15 | PX oxidizing reactor for producing terephthalic acid |
Publications (1)
Publication Number | Publication Date |
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WO2010081358A1 true WO2010081358A1 (en) | 2010-07-22 |
Family
ID=41038314
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/CN2009/075384 WO2010081358A1 (en) | 2009-01-15 | 2009-12-08 | Px oxidation reactor for producing terephthalic acid |
Country Status (3)
Country | Link |
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CN (1) | CN100594972C (en) |
RU (1) | RU2505524C2 (en) |
WO (1) | WO2010081358A1 (en) |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN100594972C (en) * | 2009-01-15 | 2010-03-24 | 中国纺织工业设计院 | PX oxidizing reactor for producing terephthalic acid |
CN101817744B (en) * | 2010-04-30 | 2013-07-10 | 中国石油天然气集团公司 | Oxidizing and crystallizing device of paraxylene |
CN110013814A (en) * | 2019-04-15 | 2019-07-16 | 嘉兴石化有限公司 | A kind of large capacity oxidation reactor gas handling system and its application method |
CN111389314B (en) * | 2020-03-31 | 2020-12-11 | 南京延长反应技术研究院有限公司 | Built-in micro-interface unit enhanced reaction system and process for producing PTA (purified terephthalic acid) by PX (para-xylene) |
CN111569799B (en) * | 2020-03-31 | 2023-03-10 | 南京延长反应技术研究院有限公司 | External micro-interface unit enhanced reaction system and process for producing PTA (pure terephthalic acid) by PX (para-xylene) |
CN113694837A (en) * | 2020-05-21 | 2021-11-26 | 中国石油化工股份有限公司 | Kettle type reactor and method for unsaturated polymer hydrogenation and nitrile rubber hydrogenation method |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3660476A (en) * | 1968-10-30 | 1972-05-02 | Teijin Ltd | Method for the preparation of terephthalic acid |
CN1634848A (en) * | 2004-10-19 | 2005-07-06 | 浙江大学 | Process for producing terephthalic acid and device therefor |
US20060047159A1 (en) * | 2004-09-02 | 2006-03-02 | Wonders Alan G | Optimized liquid-phase oxidation |
CN1806906A (en) * | 2005-01-18 | 2006-07-26 | 中国石化上海石油化工股份有限公司 | Oxidizing reaction device for preparation of terephthalic acid by air current agitation |
CN101513601A (en) * | 2009-01-15 | 2009-08-26 | 中国纺织工业设计院 | PX oxidation reactor for producing terephthalic acid |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU2363534C2 (en) * | 2004-09-02 | 2009-08-10 | Истман Кемикал Компани | Optimised liquid-phase oxidation in bubble reactor |
-
2009
- 2009-01-15 CN CN200910076703A patent/CN100594972C/en active Active
- 2009-12-08 RU RU2011133892/04A patent/RU2505524C2/en active
- 2009-12-08 WO PCT/CN2009/075384 patent/WO2010081358A1/en active Application Filing
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3660476A (en) * | 1968-10-30 | 1972-05-02 | Teijin Ltd | Method for the preparation of terephthalic acid |
US20060047159A1 (en) * | 2004-09-02 | 2006-03-02 | Wonders Alan G | Optimized liquid-phase oxidation |
CN1634848A (en) * | 2004-10-19 | 2005-07-06 | 浙江大学 | Process for producing terephthalic acid and device therefor |
CN1806906A (en) * | 2005-01-18 | 2006-07-26 | 中国石化上海石油化工股份有限公司 | Oxidizing reaction device for preparation of terephthalic acid by air current agitation |
CN101513601A (en) * | 2009-01-15 | 2009-08-26 | 中国纺织工业设计院 | PX oxidation reactor for producing terephthalic acid |
Also Published As
Publication number | Publication date |
---|---|
RU2011133892A (en) | 2013-02-20 |
CN101513601A (en) | 2009-08-26 |
CN100594972C (en) | 2010-03-24 |
RU2505524C2 (en) | 2014-01-27 |
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