CN214142143U - Energy recovery device for aromatic dicarboxylic acid production process - Google Patents
Energy recovery device for aromatic dicarboxylic acid production process Download PDFInfo
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- CN214142143U CN214142143U CN202022848918.5U CN202022848918U CN214142143U CN 214142143 U CN214142143 U CN 214142143U CN 202022848918 U CN202022848918 U CN 202022848918U CN 214142143 U CN214142143 U CN 214142143U
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Abstract
The utility model discloses an energy recovery device of aromatic dicarboxylic acid production process, which comprises an oxidation section, a first condensation section, an oxidation crystallization section, a second condensation section, a purification crystallization section, a third condensation section, a flash evaporation section and a steam turbine section; the method comprises the steps of respectively recovering corresponding heat source energy step by step through a first condensation section, a second condensation section and a third condensation section to generate saturated vapor with various different pressures, and sending a plurality of strands of saturated vapor with different pressures to a steam turbine section to generate power or push an air compressor to operate, or directly using the saturated vapor to heat equipment needing to be heated in a heating process. The energy recovery device of the utility model solves the problem that the heat of the low-temperature heat source can not be effectively recycled in the production process of the aromatic dicarboxylic acid, not only reduces the consumed cooling water energy, but also increases the recovery benefit.
Description
Technical Field
The utility model relates to the technical field of aromatic dicarboxylic acid production, in particular to an energy recovery device for an aromatic dicarboxylic acid production process.
Background
Aromatic dicarboxylic acids are generally prepared by oxidizing alkyl or partially oxidized alkyl substituted alkyl aromatic dicarboxylic acids (e.g., P-xylene, m-xylene, o-xylene) in a liquid solution of a lower aliphatic carboxylic acid (e.g., acetic acid) with bromide and heavy metal salts as catalysts, introducing oxygen (e.g., air) to perform an oxidation reaction to obtain a crude aromatic dicarboxylic acid (e.g., terephthalic acid TA) containing impurities such as 4-carboxybenzaldehyde (4-CBA) and P-Toluic acid (P-Toluic acid), mixing the crude aromatic dicarboxylic acid with water to form a slurry, performing a hydrogenation reaction with hydrogen to convert the water insoluble 4-carboxybenzaldehyde (4-CBA) impurities into water soluble P-Toluic acid (P-Toluic acid), crystallizing, separating, etc., separating and washing the aromatic dicarboxylic acid crystals from the impurities, the aromatic dicarboxylic acid is obtained in high purity.
In a typical aromatic dicarboxylic acid process, related heat is usually recovered to save energy consumption, the heat source usually includes three forms of high-temperature pressure condensed water, high-temperature pressure water or solvent-rich condensate in the process, high-temperature pressure water or lower aliphatic carboxylic acid-rich gas (such as nitrogen) stream, and the like, and the conventional heat recovery mainly aims at recycling a heat source with medium-high temperature, and cannot further recycle heat for a low-temperature heat source.
SUMMERY OF THE UTILITY MODEL
In view of the defects of the prior art, the utility model provides an energy recovery device for an aromatic dicarboxylic acid production process to solve the problem that the heat of a low-temperature heat source cannot be effectively recycled in the aromatic dicarboxylic acid production process.
In order to achieve the above purpose, the utility model adopts the technical scheme that:
an energy recovery device of an aromatic dicarboxylic acid production process comprises the following working sections:
an oxidation section for subjecting an alkyl aromatic dicarboxylic acid in a lower aliphatic carboxylic acid solution to a catalytic oxidation reaction with oxygen in the presence of a catalyst to form an aromatic dicarboxylic acid-rich product stream and a lower aliphatic carboxylic acid-water-and non-condensable gas-containing gas stream;
an oxidative crystallization stage for depressurizing said aromatic dicarboxylic acid-rich product stream section by section to form a slurry containing aromatic dicarboxylic acid crystals and hot steam, said slurry containing aromatic dicarboxylic acid crystals being mixed with water to form a crude aromatic dicarboxylic acid slurry;
the purification section comprises a preheater and a hydrogenation reactor, the preheater is arranged in two stages, the heat source of the first stage preheater is from steam rich in water generated by a downstream purification crystallization section, the heat source of the second stage preheater is from high-pressure steam, the preheater is used for preheating the crude aromatic dicarboxylic acid slurry in two stages to form a crude aromatic dicarboxylic acid solution, and the hydrogenation reactor is used for carrying out hydrogenation reaction on the crude aromatic dicarboxylic acid solution to remove impurities and obtain a purified product stream;
a purification crystallization section for depressurizing a purified product stream from said purification section to form a purified slurry containing aromatic dicarboxylic acid crystals and a water-rich vapor;
an energy recovery section for generating saturated steam at different pressures, the energy recovery section being from at least one of the first condensation section, the second condensation section, the third condensation section and the flash section; and
the steam turbine section is used for sending saturated steam generated in the energy recovery section to a steam turbine or a steam turbine directly connected with an air compressor for power generation, or sending the saturated steam to the air compressor to drive the air compressor to operate, or directly used for heating equipment needing to be heated in the process, wherein the saturated steam generated in the energy recovery section is collected together with the same pressure, T strands of the collected saturated steam have different pressures, T is selected from 1-7, and preferably T is selected from 3-5.
Further, the first condensation section comprises N first heat exchangers, the first heat exchangers are used for condensing the gas flow containing the low-grade aliphatic carboxylic acid, the water and the non-condensable gas step by step, and simultaneously transferring heat to the cooling liquid step by step, so that N saturated steam with different pressures is generated after the cooling liquid is heated; the N is selected from 1-7, and preferably, the N is selected from 3-5.
Furthermore, the second condensation section comprises M second heat exchangers, the second heat exchangers are used for condensing hot steam generated by the oxidation crystallization section step by step and transmitting heat to cooling liquid step by step, and the cooling liquid is heated to generate M saturated water vapors with different pressures; the M is selected from 1-7, preferably, the M is selected from 3-5.
Further, the third condensation section comprises R first buffers and a third heat exchanger connected with each first buffer, the first buffers are used for carrying out multi-stage depressurization on the condensate rich in water after the first-stage preheater to generate R saturated steam rich in water with different pressures and condensate, the saturated steam rich in water is used as a heat source for heating the crude aromatic dicarboxylic acid slurry, and the third heat exchanger is used for further condensing the condensate and simultaneously transferring heat to the cooling liquid so that the cooling liquid generates R saturated steam with different pressures after being heated; r is selected from 1-7, preferably, R is selected from 3-5.
Further, the flash evaporation section comprises P second buffers, and the second buffers are used for carrying out multi-section pressure reduction on the high-pressure condensed water after the second-stage preheater to generate P saturated steam with different pressures; p is selected from 1-7, and preferably, P is selected from 3-5.
Further, the alkyl aromatic dicarboxylic acid is selected from one of p-xylene, m-xylene and o-xylene, preferably p-xylene; the aromatic dicarboxylic acid is selected from one of terephthalic acid, isophthalic acid and phthalic acid, preferably from terephthalic acid; the lower aliphatic carboxylic acid is selected from one of acetic acid, propionic acid and butyric acid, preferably acetic acid; the catalyst comprises bromide and soluble salts of heavy metals, wherein the bromide is selected from one of tetrabromomethane, tetrabromoethane and hydrogen bromide, preferably selected from hydrogen bromide, and the soluble salts of the heavy metals are selected from soluble salts of cobalt and/or manganese, preferably selected from acetate salts of cobalt and/or manganese.
Further, the lowest pressure of the saturated steam generated by the first condensation section, the second condensation section, the third condensation section and the flash evaporation section is 0-0.5 Kg/cm independently2G, preferably, the lowest pressure thereof is independently 0 to 0.3Kg/cm2.G。
In a further technical scheme, the device can further comprise a distillation section or an absorption section, wherein the distillation section or the absorption section is used for separating a liquid stream rich in the lower aliphatic carboxylic acid from the gas stream containing the lower aliphatic carboxylic acid, water and the non-condensable gas, the liquid stream rich in the lower aliphatic carboxylic acid is returned to the oxidation section, the separated gas stream containing the lower aliphatic carboxylic acid, water and the non-condensable gas is further introduced into the first condensation section, or the gas stream containing the lower aliphatic carboxylic acid, water and the non-condensable gas is directly introduced into the first condensation section.
The utility model also provides an energy recovery method for the production process of the aromatic dicarboxylic acid, which comprises the following steps:
in the oxidation section, alkyl aromatic dicarboxylic acid in a lower aliphatic carboxylic acid solution is subjected to catalytic oxidation reaction with oxygen under the action of a catalyst to form a product stream rich in aromatic dicarboxylic acid and a gas stream containing lower aliphatic carboxylic acid, water and non-condensable gas;
depressurizing said aromatic dicarboxylic acid-rich product stream section by section in an oxidative crystallization section to form a slurry of aromatic dicarboxylic acid-containing crystals and hot steam, said slurry of aromatic dicarboxylic acid-containing crystals being combined with water to form a crude aromatic dicarboxylic acid slurry;
in the purification section, the crude aromatic dicarboxylic acid slurry is preheated in two stages by two stages of preheaters to form a crude aromatic dicarboxylic acid solution, wherein the heat source of the first stage preheater is from steam rich in water generated in a downstream purification crystallization section, and the heat source of the second stage preheater is from high-pressure steam; subjecting the crude aromatic dicarboxylic acid solution to a hydrogenation reaction in a hydrogenation reactor to remove impurities and obtain a purified product stream;
in a purification crystallization section, depressurizing a purified product stream from said purification section to form a purified slurry containing aromatic dicarboxylic acid crystals and a water-rich vapor;
in the energy recovery section, saturated steam with different pressures is generated through at least one of the first condensation section, the second condensation section, the third condensation section and the flash evaporation section; and
in the steam turbine section, saturated steam from the energy recovery section is sent to a steam turbine or a steam turbine directly connected with an air compressor for power generation, or sent to the air compressor to drive the air compressor to operate, or directly used for heating equipment in the heating process; the saturated steam generated in the energy recovery section is gathered together with the same pressure, T strands of the gathered saturated steam have different pressures, T is selected from 1-7, and preferably T is selected from 3-5;
in the first condensation section, the gas flow containing the low-grade aliphatic carboxylic acid, water and non-condensable gas is gradually condensed through N first heat exchangers, and meanwhile, heat is gradually transmitted to cooling liquid, so that N saturated steam with different pressures is generated after the cooling liquid is heated;
in a second condensation section, gradually condensing hot steam generated in the oxidation crystallization section through M second heat exchangers, and simultaneously gradually transmitting heat to cooling liquid, so that the cooling liquid generates M saturated water vapors with different pressures after being heated;
in a third condensation section, carrying out multistage depressurization on the steam rich in water after the first-stage preheater through R first buffers to generate R kinds of saturated steam rich in water and condensate with different pressures, wherein the saturated steam rich in water is used as a heat source to heat the crude aromatic dicarboxylic acid slurry, and the condensate is further condensed through a third heat exchanger, and simultaneously, heat is transferred to a cooling liquid, so that the cooling liquid generates R kinds of saturated steam with different pressures after being heated;
and in the flash evaporation section, the high-pressure condensate water after the second-stage preheater is subjected to multi-stage depressurization through P second buffers to generate P kinds of saturated steam with different pressures.
Go toStep one, the reaction pressure of the catalytic oxidation reaction is 10-19 Kg/cm2G, the reaction temperature is 95-260 ℃.
Further, the reaction pressure of the hydrogenation reaction is 69-91 Kg/cm2G, the reaction temperature is 270-300 ℃.
Further, the lowest pressure of the saturated steam generated by the first condensation section, the second condensation section, the third condensation section and the flash evaporation section is 0-0.5 Kg/cm independently2G, preferably, the lowest pressure thereof is independently 0 to 0.3Kg/cm2.G。
Further, the gas flow containing the lower aliphatic carboxylic acid, water and the non-condensable gas passes through a distillation section or an absorption section to separate a liquid flow rich in the lower aliphatic carboxylic acid, the liquid flow rich in the lower aliphatic carboxylic acid is returned to the oxidation section, and the separated gas flow containing the lower aliphatic carboxylic acid, the water and the non-condensable gas enters a first condensation section.
The utility model has the advantages that:
the utility model changes the existing aromatic dicarboxylic acid production process into low-temperature heat source (such as water vapor, condensate rich in water or solvent, gas rich in water or solvent) which is condensed by cooling water energy and recovered to the process because of low temperature and no recovery benefit, and changes the low-temperature heat source into pressure reduction flash evaporation or heating water by the heat to generate low-pressure saturated water vapor (the lowest pressure is about 0-0.3 Kg/cm)2G) and sending the energy to a steam turbine (or a steam turbine of a direct-connection air compressor) for generating power (or pushing the air compressor to operate) or directly used for heating equipment in the process for recovering the energy, thereby not only reducing the consumed cooling water energy, but also increasing the recovery benefit.
Drawings
FIG. 1 is a schematic view of an energy recovery apparatus for the production process of aromatic dicarboxylic acid according to the present invention.
Detailed Description
The following description is presented to disclose the invention so as to enable any person skilled in the art to practice the invention.
Examples
As shown in fig. 1, the energy recovery device of the aromatic dicarboxylic acid production process of the present embodiment includes an oxidation section, a distillation section (or an absorption section), a first condensation section, an oxidation crystallization section, a second condensation section, a purification crystallization section, a third condensation section, a flash evaporation section, and a steam turbine section.
In the oxidation section, adding an aqueous acetic acid solution, p-xylene and a catalyst into an oxidation reactor 1, uniformly mixing, and introducing air (a raw material liquid and an air pipeline are not shown), so that the p-xylene in the aqueous acetic acid solution and oxygen in the air perform catalytic oxidation reaction under the action of the catalyst to form a product stream 1a rich in terephthalic acid and a gas stream 1b containing lower aliphatic carboxylic acid, water and non-condensable gas; the catalyst comprises a mixed solution composed of hydrogen bromide and cobalt acetate; wherein the reaction pressure of the catalytic oxidation reaction is 10-19 Kg/cm2G, the reaction temperature is 95-260 ℃. A gas stream 1b containing a lower aliphatic carboxylic acid, water and a non-condensable gas is sent from the oxidation reactor 1 to a distillation section (or absorption section) 8 to perform a distillation operation to obtain a gas stream 8a rich in water and a liquid stream 8c rich in an organic solvent, the liquid stream 8c rich in the organic solvent is refluxed from the distillation section (or absorption section) 8 to the oxidation reactor 1, and the gas stream 8a rich in water is sent to a first condensation section. The distillation section (or absorption section) 8 may be omitted, and if the distillation section (or absorption section) 8 is not provided, the gas stream 1b containing the lower aliphatic carboxylic acid, water and the noncondensable gas is directly sent from the oxidation reactor 1 to the first condensation section.
Alternatively, the alkyl aromatic dicarboxylic acid is selected from m-xylene or o-xylene, and the aromatic dicarboxylic acid produced by the reaction is isophthalic acid or phthalic acid; the acetic acid aqueous solution can be replaced by propionic acid and butyric acid; the hydrogen bromide can be replaced by one of tetrabromomethane and tetrabromoethane, and the soluble salt of heavy metal can be soluble salt containing cobalt and manganese (such as acetate), or manganese-containing acetate, preferably cobalt and/or manganese acetate.
In the first condensation stage, the water-rich gas stream is passed through a first heat exchanger (this heat exchanger may be 1 or more), as shown in FIG. 1, 5, through a plurality of first heat exchangersAnd 8a, gradually condensing, and simultaneously gradually transmitting heat to the cooling liquid, so that the cooling liquid generates 5 saturated water vapors with different pressures after being heated. Specifically, the water-rich gas stream 8a is passed directly to a first condenser 9 or from the distillation section (or absorption section) 8 to the first condenser 9 and partially condensed by heat exchange with a cooling liquid 9a (preferably water, with cooling liquids 10a, 11a, 12a, 13a also preferably water), the cooling liquid 9a being heated to a pressure of about 6.5 to 10 Kg/cm2G and sent to the equipment in the process that needs to be heated as a heating source or to a steam turbine (or a steam turbine combined with an air compressor) 21 to generate electricity (or drive the air compressor to operate). The uncondensed water-rich gas 9c is sent to a second condenser 10 and partially condensed by heat exchange with a cooling liquid 10a, the cooling liquid 10a is heated to a pressure of about 4 to 6.5 Kg/cm2G and sent to the equipment requiring heating in the process as a heating source or to a steam turbine (or a steam turbine combined with an air compressor) 21 to generate electricity (or drive the air compressor to operate). The uncondensed water-rich gas 10c is sent to a third condenser 11 and partially condensed by heat exchange with a cooling liquid 11a, the cooling liquid 11a being heated to a pressure of about 1.5 to 4 Kg/cm2G and sent to the equipment in the process that needs to be heated as a heating source or to a steam turbine (or a steam turbine combined with an air compressor) 21 to generate electricity (or drive the air compressor to operate). The uncondensed water-rich gas 11c is sent to a fourth condenser 12 and partially condensed by heat exchange with a cooling liquid 12a, the cooling liquid 12a being heated to a pressure of about 0.5 to 1.5 Kg/cm2G and sent to the equipment in the process that needs to be heated as a heating source or to a steam turbine (or a steam turbine combined with an air compressor) 21 to generate electricity (or drive the air compressor to operate). The uncondensed water-rich gas 12c is sent to a fifth condenser 13 and partially condensed by heat exchange with a cooling liquid 13a, the cooling liquid 13a is heated to a pressure of about 0 to 0.5Kg/cm2G and sent to the plant to be heated in the process as a heating source or to a turbine (or a turbine combined with an air compressor) 21 to generate electricity (or to drive the air compressor to operate), without any need for any further heating of the plantThe condensed water-rich gas 13c is sent to be treated elsewhere in the process.
Depressurizing said terephthalic acid-rich product stream 1a section by section in an oxidative crystallization section and a second condensation section to form a slurry containing terephthalic acid crystals and a hot vapor; mixing said slurry containing terephthalic acid crystals with water to form a crude terephthalic acid slurry; in addition, through 3 second heat exchangers, the hot steam that produces the oxidation crystallization section is condensed step by step, simultaneously passes heat to the coolant liquid step by step, makes the coolant liquid produce 3 kinds of saturated vapor of different pressures after being heated. Specifically, the terephthalic acid-rich product stream 1a is sent to a first crystallizer 2 for a pressure-reducing flash operation, the hot vapor 2b produced after the flash evaporation is sent to a sixth condenser 3 and condensed by heat exchange with a cooling liquid 3a, the condensate 3c is removed for further treatment or is partially recycled to the first crystallizer 2, and the cooling liquid 3a (preferably water, and the cooling liquids 5a and 7a are also preferably water) is heated to produce 1.5 to 4 Kg/cm2G and sent to the equipment in the process that needs to be heated as a heating source or to a steam turbine (or a steam turbine combined with an air compressor) 21 to generate electricity (or drive the air compressor to run). The product stream 2a is conveyed to a second crystallizer 4 for flash evaporation, hot vapor 4b generated after flash evaporation is conveyed to a seventh condenser 5 and condensed through heat exchange with cooling liquid 5a, condensate 5c is removed for further treatment or is partially circulated to the second crystallizer 4, and the cooling liquid 5a is heated to generate 0.5-1.5 Kg/cm2G and sent to the equipment in the process that needs to be heated as a heating source or to a steam turbine (or a steam turbine combined with an air compressor) 21 to generate electricity (or to drive the air compressor to operate). The product stream 4a is sent to a third crystallizer 6 for flash evaporation, the hot vapor 6b produced after flash evaporation is sent to an eighth condenser 7, and the condenser outlet stream 7c is removed for further treatment or is partially recycled to the third crystallizer 6 and condensed by heat exchange with a cooling liquid 7a, the cooling liquid 7a is heated to generate 0-0.5 Kg/cm2G and sent to the plant to be heated in the process as heating source or to a steam turbine (or a steam turbine combined with an air compressor)Machine) 21 to generate electricity (or drive the air compressor to operate), product stream 6a being a slurry containing terephthalic acid crystals; the slurry containing terephthalic acid crystals is mixed with water to form a crude terephthalic acid slurry.
In the purification section, the crude terephthalic acid slurry is preheated by two stages through preheaters arranged in two stages to form a crude terephthalic acid solution, wherein the heat source of the first stage preheater is from steam rich in water generated in a downstream purification crystallization section, and the heat source of the second stage preheater is from high-pressure steam; the crude terephthalic acid solution is subjected to a hydrogenation reaction in a hydrogenation reactor 19 to remove impurities and obtain a purified product stream; wherein the reaction pressure of the hydrogenation reaction is 69-91 Kg/cm2G, the reaction temperature is 270-300 ℃; in the purification crystallization section, the purified product stream from the purification section is flashed under reduced pressure to form a purified slurry containing terephthalic acid crystals and a water-rich vapor. Specifically, the crude terephthalic acid slurry stream 14c is sent to a first stage preheater 14 (the number of the first stage preheater 14 may be 1 or more), and is increased in temperature by heat exchange with a water-rich vapor 20b produced by flashing a crystallizer 20 (the number of the crystallizer 20 may be 1 or more), and the condensed water-rich condensate 14b is sent to a first buffer 15 for collection. Heated slurry stream 14a is sent to second stage preheater 17 and is raised in temperature by heat exchange with steam 17c, and steam condensate 17b is sent to second buffer 18 for collection. The product stream 17a heated to a crude terephthalic acid solution is sent to a hydrogenation reactor 19, and hydrogenation is carried out using a palladium metal catalyst supported on carbon in the hydrogenation reactor 19. The purified terephthalic acid solution 19a after hydrogenation is fed to a fourth crystallizer 20 (which crystallizer 20 can be 1 or more) for flashing, and the water-rich vapor 20b produced by flashing is fed to the first stage preheater 14 as a heat source for the crude terephthalic acid slurry. The purified slurry 20a containing terephthalic acid crystals precipitated by crystallization is sent downstream for separation treatment.
In the third condensation stage, the water-rich condensate 14b after the first preheater is subjected to a multistage pressure-reducing flash distillation via at least 1 first buffer 15, producing a saturated steam 15b rich in water andthe condensate 15a and the saturated steam 15b rich in water are used as a heat source for heating the crude terephthalic acid slurry, the condensate 15a is condensed again by a third heat exchanger 16, and simultaneously the heat is transferred to a cooling liquid 16b (preferably water), so that the lowest pressure generated after the cooling liquid 16b is heated is 0-0.5 Kg/cm2G saturated water vapor 16 c; the saturated steam 16c is sent to the equipment to be heated in the process as a heating source or sent to a steam turbine (or a steam turbine of a direct air compressor) 21 to generate electricity (or drive the air compressor to operate), and the condensate 16a is recycled to the process for use.
In the flash evaporation section, the high-pressure condensed water 17b after the second-stage preheater 17 is subjected to pressure reduction flash evaporation through at least 1 second buffer 18 to generate the lowest pressure of 0-0.5 Kg/cm2G saturated steam 18b and condensate 18a, the saturated steam 18b may be sent to equipment requiring heating in the process as a heating source or to a steam turbine (or a steam turbine of a direct coupled air compressor) 21 to generate electricity (or to drive the air compressor to operate), and the condensate 18a may be recycled to the process for use.
In the steam turbine section, saturated steam (3 b, 5b, 7b, 9b, 10b, 11b, 12b, 13b, 18b, 16 c) from the first condensation section, the second condensation section, the third condensation section and the flash evaporation section respectively is sent to a steam turbine or a steam turbine 21 directly connected with an air compressor for power generation, or sent to the air compressor to drive the air compressor to operate or directly used for equipment needing heating in the heating process. The pressure of the saturated steam (3 b, 5b, 7b, 9b, 10b, 11b, 12b, 13b, 18b, 16 c) transmitted to the turbine 21 of the turbine or the straight-joint air compressor for generating power (or driving the air compressor to operate) is independently selected from 1 to 7 strands, more preferably from 3 to 5 strands, and the pressure is 6.5 to 10 Kg/cm in sequence2.G、4~6.5 Kg/cm2.G、1.5~4 Kg/cm2.G、0.5~1.5 Kg/cm2.G、0~0.5 Kg/cm2.G。
In at least one embodiment, the number of the first heat exchanger, the second heat exchanger, the third heat exchanger, the first buffer 15 and the second buffer 18 is independently selected from 1 to 7, more preferably from 3 to 5.
Through the technology of the above embodimentsThe technical proposal can recover the lowest pressure of heat production in the process from about 0 to 0.5Kg/cm2G, low pressure saturated steam, and for turbine (or direct steam turbine) power generation; in addition, three or four or five saturated steam streams can enter a steam turbine (or an air compressor of a direct-connection steam turbine) at the same time to generate power or push the air compressor to operate or be directly used for heating equipment in the heating process; thereby not only reducing the cooling water energy consumed in the prior aromatic dicarboxylic acid process, but also increasing the recovery benefit of the whole production process.
The foregoing shows and describes the general principles, essential features, and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the above embodiments, and that the principles of the present invention may be applied to any other embodiment without departing from the spirit and scope of the present invention.
Claims (10)
1. An energy recovery device for an aromatic dicarboxylic acid production process, characterized by comprising:
an oxidation section for subjecting an alkyl aromatic dicarboxylic acid in a lower aliphatic carboxylic acid solution to a catalytic oxidation reaction with oxygen in the presence of a catalyst to form an aromatic dicarboxylic acid-rich product stream and a lower aliphatic carboxylic acid-water-and non-condensable gas-containing gas stream;
an oxidative crystallization section for depressurizing said aromatic dicarboxylic acid-rich product stream section by section to form a slurry containing aromatic dicarboxylic acid crystals and hot vapor;
the purification section comprises a preheater and a hydrogenation reactor, the preheater is arranged in two stages, the heat source of the first stage preheater is from steam rich in water generated by the downstream purification crystallization section, the heat source of the second stage preheater is from high-pressure steam, the preheater is used for preheating the crude aromatic dicarboxylic acid slurry in two stages to form a crude aromatic dicarboxylic acid solution, and the hydrogenation reactor is used for carrying out hydrogenation reaction on the crude aromatic dicarboxylic acid solution to remove impurities and obtain a purified product stream;
a purification crystallization section for depressurizing a purified product stream from said purification section to form a purified slurry containing aromatic dicarboxylic acid crystals and a water-rich vapor;
an energy recovery section for generating saturated steam at different pressures, the energy recovery section being from at least one of the first condensation section, the second condensation section, the third condensation section and the flash section; and
and the steam turbine section is used for sending saturated steam generated in the energy recovery section to a steam turbine or a steam turbine directly connected with an air compressor for power generation, or sending the saturated steam to the air compressor to push the air compressor to operate, or directly used for heating equipment needing to be heated in the process, wherein the saturated steam generated in the energy recovery section is collected together with the same pressure, the collected saturated steam has T strands of different pressures, and T is selected from 1-7.
2. The energy recovery device for an aromatic dicarboxylic acid production process according to claim 1, wherein T is selected from 3 to 5.
3. The apparatus for recovering energy of a process for producing an aromatic dicarboxylic acid according to claim 1, wherein the first condensing section comprises N first heat exchangers for stepwise condensing the gas stream containing the lower aliphatic carboxylic acid, water and noncondensable gases while stepwise transferring heat to a cooling liquid, and the cooling liquid is heated to generate N saturated steam of different pressures; and N is selected from 1-7.
4. The apparatus for recovering energy of a process for producing an aromatic dicarboxylic acid according to claim 1, wherein the second condensing section comprises M second heat exchangers for condensing the hot steam generated in the oxidation-crystallization section step by step while transferring the heat to the cooling liquid step by step, so that the cooling liquid is heated to generate M saturated steam of different pressures; and M is selected from 1-7.
5. The apparatus for recovering energy from an aromatic dicarboxylic acid production process according to claim 1, wherein the third condensing stage comprises R first buffers and a third heat exchanger connected to each first buffer, the first buffers are configured to perform multi-stage depressurization of the water-rich condensate after the first stage preheater to generate R kinds of water-rich saturated steam and condensate of different pressures, the water-rich saturated steam is used as a heat source for heating the crude aromatic dicarboxylic acid slurry, and the third heat exchanger is configured to further condense the condensate while transferring heat to the cooling liquid, so that the cooling liquid is heated to generate R kinds of saturated steam of different pressures; r is selected from 1-7.
6. The energy recovery device for an aromatic dicarboxylic acid production process according to claim 1, wherein the flash evaporation section comprises P second buffers for multi-stage depressurization of the high-pressure condensed water after the second stage preheater to generate P saturated steam of different pressures; and P is selected from 1-7.
7. The energy recovery device for an aromatic dicarboxylic acid production process according to claim 1, wherein the alkyl aromatic dicarboxylic acid is one selected from the group consisting of p-xylene, m-xylene, and o-xylene; the aromatic dicarboxylic acid is selected from one of terephthalic acid, isophthalic acid and phthalic acid; the lower aliphatic carboxylic acid is selected from one of acetic acid, propionic acid and butyric acid.
8. The apparatus for recovering energy from an aromatic dicarboxylic acid production process according to claim 1, wherein the first condensation zone, the second condensation zone, the third condensation zone and the flash evaporation zone generate saturated steam at a minimum pressure of 0 to 0.5Kg/cm independently2.G。
9. The apparatus for recovering energy of a process for producing an aromatic dicarboxylic acid according to claim 1, wherein the first condensation section and the second condensation section are arranged in seriesThe lowest pressure of the saturated steam generated in the section, the third condensation section and the flash evaporation section is 0-0.3 Kg/cm independently2.G。
10. The apparatus for recovering energy of a process for producing an aromatic dicarboxylic acid according to claim 1, further comprising a distillation section or an absorption section for separating a liquid stream rich in a lower aliphatic carboxylic acid from the gas stream containing a lower aliphatic carboxylic acid, water and a non-condensable gas.
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