CN213824704U - Built-in micro-interface unit enhanced reaction system for PX production PTA - Google Patents
Built-in micro-interface unit enhanced reaction system for PX production PTA Download PDFInfo
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- CN213824704U CN213824704U CN202020445692.1U CN202020445692U CN213824704U CN 213824704 U CN213824704 U CN 213824704U CN 202020445692 U CN202020445692 U CN 202020445692U CN 213824704 U CN213824704 U CN 213824704U
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 219
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 27
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 claims description 100
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 claims description 82
- LPNBBFKOUUSUDB-UHFFFAOYSA-N p-toluic acid Chemical compound CC1=CC=C(C(O)=O)C=C1 LPNBBFKOUUSUDB-UHFFFAOYSA-N 0.000 claims description 30
- GOUHYARYYWKXHS-UHFFFAOYSA-N 4-formylbenzoic acid Chemical compound OC(=O)C1=CC=C(C=O)C=C1 GOUHYARYYWKXHS-UHFFFAOYSA-N 0.000 claims description 24
- FXLOVSHXALFLKQ-UHFFFAOYSA-N p-tolualdehyde Chemical compound CC1=CC=C(C=O)C=C1 FXLOVSHXALFLKQ-UHFFFAOYSA-N 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 7
- 230000009471 action Effects 0.000 claims description 5
- 239000012295 chemical reaction liquid Substances 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 abstract description 51
- 239000002904 solvent Substances 0.000 abstract description 13
- 238000000034 method Methods 0.000 abstract description 12
- 238000005265 energy consumption Methods 0.000 abstract description 9
- 239000007810 chemical reaction solvent Substances 0.000 abstract description 6
- 239000000463 material Substances 0.000 description 18
- 238000007254 oxidation reaction Methods 0.000 description 17
- 239000007791 liquid phase Substances 0.000 description 11
- 239000000047 product Substances 0.000 description 9
- 239000007788 liquid Substances 0.000 description 8
- 239000000376 reactant Substances 0.000 description 8
- 239000007789 gas Substances 0.000 description 7
- 239000000839 emulsion Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 238000007086 side reaction Methods 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000005728 strengthening Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- BMYNFMYTOJXKLE-UHFFFAOYSA-N 3-azaniumyl-2-hydroxypropanoate Chemical compound NCC(O)C(O)=O BMYNFMYTOJXKLE-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 229940011182 cobalt acetate Drugs 0.000 description 2
- QAHREYKOYSIQPH-UHFFFAOYSA-L cobalt(II) acetate Chemical compound [Co+2].CC([O-])=O.CC([O-])=O QAHREYKOYSIQPH-UHFFFAOYSA-L 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 229940071125 manganese acetate Drugs 0.000 description 2
- UOGMEBQRZBEZQT-UHFFFAOYSA-L manganese(2+);diacetate Chemical compound [Mn+2].CC([O-])=O.CC([O-])=O UOGMEBQRZBEZQT-UHFFFAOYSA-L 0.000 description 2
- HJUGFYREWKUQJT-UHFFFAOYSA-N tetrabromomethane Chemical compound BrC(Br)(Br)Br HJUGFYREWKUQJT-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- -1 p-xylene PX Chemical compound 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000007039 two-step reaction Methods 0.000 description 1
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Abstract
The utility model provides a reaction system is reinforceed to built-in little interface unit of PX production PTA, include: the reactor comprises a reactor and a micro interface unit arranged in the reactor; the reactor comprises a shell, an inner barrel and a circulating heat exchange device, wherein the inner barrel and the part of the inner barrel are arranged inside the shell in a concentric mode, the circulating heat exchange device is arranged outside the shell, the bottom end of the inner barrel is connected to the upper portion of the inner bottom surface of the shell in a closed mode, the top end of the inner barrel is open, the shell and an area between the inner barrels are a first reaction area, a second reaction area and a third reaction area are sequentially arranged inside the inner barrel from top to bottom, and the circulating heat exchange device is respectively connected with the inner barrel and the micro-interface unit. The utility model discloses solved current PX production PTA in-process reaction solvent acetic acid effectively and by a large amount of wastes under high temperature high pressure, can not take out the problem of product TA simultaneously in time, and then reduced the energy consumption widely, saved the acetic acid solvent, promoted reaction efficiency.
Description
Technical Field
The utility model relates to a chemical industry technical field particularly, relates to a reaction system is reinforceed to built-in little interface unit of PX production PTA.
Background
The oxidation reaction process for producing TA (terephthalic acid) from PX (p-xylene) is very complicated, mainly comprising 4 steps, namely p-xylene (PX) → p-Tolualdehyde (TALD) → p-toluic acid (p-TA) → p-carboxybenzaldehyde (4-CBA) → Terephthalic Acid (TA), and the 4 oxidation reactions in the reaction process are series reactions, which generally use acetic acid as a solvent and cobalt acetate, manganese acetate and hydrobromic acid (or tetrabromomethane) as catalysts.
At present, in the existing PTA production technology, 4 main steps in the oxidation reaction process are all carried out in the same reactor, although the reaction rate constants of the 4 steps are different by dozens of times, a mixed reaction process is adopted, different conditions are not given for different reactions, reaction solvent acetic acid is greatly wasted under high temperature and high pressure, and meanwhile, a product TA cannot be taken out in time, so that the energy consumption is high, the acetic acid consumption is large, and the reaction efficiency is low.
Disclosure of Invention
In view of this, the utility model provides a built-in micro-interface unit of PX production PTA reinforces reaction system aims at solving current PX production PTA in-process reaction solvent acetic acid and is wasted by a large amount under high temperature and high pressure, can not take out the problem of product TA in time simultaneously.
The utility model provides a reaction system is reinforceed to built-in little interface unit of PX production PTA, include: the reactor comprises a reactor and a micro interface unit arranged in the reactor; wherein the content of the first and second substances,
the reactor comprises a shell, an inner cylinder concentrically arranged in the shell and a circulating heat exchange device partially arranged outside the shell, the bottom end of the inner cylinder is connected to the inner bottom surface of the shell in a closed mode, the top end of the inner cylinder is open, the area between the shell and the inner cylinder is a first reaction area, a second reaction area and a third reaction area are sequentially arranged in the inner cylinder from top to bottom, and the circulating heat exchange device is respectively connected with the inner cylinder and the micro-interface unit;
the micro-interface unit comprises a first micro-interface generator and a second micro-interface generator, wherein the first micro-interface generator is respectively arranged at the bottoms of the first reaction zone, the second reaction zone and the third reaction zone and used for crushing air serving as a reaction raw material into micro-bubbles with the diameter larger than or equal to 1 mu m and smaller than 1mm, and the second micro-interface generator is arranged at the upper end of the second reaction zone, is opposite to the first micro-interface generator arranged at the bottom of the second reaction zone and used for conveying the unreacted air at the top of the reactor under the power action of the reaction liquid in the second reaction zone under the circulating heat exchange device to be sucked into the interior of the reactor and crushed into the micro-bubbles.
Further, in the built-in micro interface unit enhanced reaction system for producing PTA by PX, the first reaction zone is a reaction zone in which p-xylene is converted into p-tolualdehyde, and p-tolualdehyde is converted into p-toluic acid, the second reaction zone is a reaction zone in which p-toluic acid is converted into p-carboxybenzaldehyde, and the third reaction zone is a reaction zone in which p-carboxybenzaldehyde is converted into terephthalic acid.
Further, in the strengthening reaction system of the built-in micro interface unit for producing PTA by PX, the diameter of the micro bubbles is more than or equal to 1 μm and less than 1 mm.
Further, in the built-in micro interface unit enhanced reaction system for producing PTA by PX, the height of the inner cylinder is 4/5 of the height of the outer shell.
Further, in the built-in micro interface unit enhanced reaction system for producing PTA by PX, the volume of the first reaction zone accounts for 45% of the total reaction volume in the reactor.
Further, in the built-in micro interface unit enhanced reaction system for producing PTA by PX, the volume of the second reaction zone accounts for 53.5% of the total reaction volume in the reactor.
Further, in the built-in micro-interface unit enhanced reaction system for producing PTA by PX, the volume of the third reaction zone accounts for 1.5% of the total reaction volume in the reactor.
Further, in the built-in micro-interface unit enhanced reaction system for producing PTA by PX, the first micro-interface generator is pneumatic, and the second micro-interface generator is hydraulic.
Further, in the built-in micro-interface unit enhanced reaction system for producing PTA by PX, the circulating heat exchange device includes a heat exchanger for exchanging heat and a pressure pump connected to the heat exchanger for providing power.
Further, in the strengthening reaction system of the built-in micro interface unit for producing PTA by PX, a wave-proof grid is arranged between the second reaction zone and the third reaction zone.
Compared with the prior art, the beneficial effects reside in that, the utility model provides a reaction system is reinforceed to PX production PTA's built-in micro-interface unit, consider the rate difference of PX production PTA's four-step reaction, adopt the reaction theory of sectional type, set up the reactor inside into the reaction zone of three difference, the different reaction step in each reaction zone, realized giving different conditions to different reaction stages in same reactor, especially solved the contradiction that the acetic acid solvent can not bear the high temperature oxidation condition, and utilize water as p-TA oxidation reaction's solvent, it is extravagant by a large amount at high temperature high pressure to have solved current PX production PTA in-process reaction solvent acetic acid effectively, can not take out the problem of product TA simultaneously in time, and then reduced the energy consumption widely, the acetic acid solvent has been saved, the reaction efficiency has been promoted.
Especially, the utility model discloses a reaction system is reinforceed to built-in little interface unit of PX production PTA, through set up little interface generator in each reaction zone inside the reactor, carry out the breakage to the air inside each reactor, make its breakage be diameter more than or equal to 1 mu m, be less than 1 mm's microbubble, form the emulsion with the liquid phase material, mass transfer area between air and the liquid phase material has been increased effectively, reduce liquid film thickness, reduce mass transfer resistance, and then reduced the energy consumption effectively, the reaction efficiency has been promoted.
Further, the utility model discloses a reaction system is reinforceed to built-in micro-interface unit of PX production PTA, through setting up circulation heat transfer device, the in-process effective control that goes on at the reaction temperature in the reaction process, the degree of consistency of mixing between inside each reaction material of reactor has been ensured simultaneously, each reactant can be abundant participate in the reaction has been ensured, and then the utilization ratio of reactant has greatly been promoted, the emergence of the while because of the uneven side reaction that causes of local temperature has been prevented, the quality of result has been promoted to a certain extent.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
fig. 1 is a schematic structural diagram of a built-in micro-interface unit enhanced reaction system for producing PTA by PX according to an embodiment of the present invention.
In the figure: 10 is a shell, 11 is an inner cylinder, 13 is a first reaction zone, 14 is a second reaction zone, 15 is a third reaction zone, 16 is a pipeline, 17 is a wave-proof grid, 18 is a defoaming net, 19 is a gas-guide tube, 20 is a first micro-interface generator, 21 is a second micro-interface generator, 121 is a heat exchanger, and 122 is a pressure pump 122.
Detailed Description
Exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. While exemplary embodiments of the present disclosure are shown in the drawings, it should be understood that the present disclosure may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the disclosure to those skilled in the art. It should be noted that, in the present invention, the embodiments and features of the embodiments may be combined with each other without conflict. The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
Referring to fig. 1, a built-in micro interface unit enhanced reaction system for PX production PTA according to an embodiment of the present invention includes: the reactor comprises a reactor and a micro interface unit arranged in the reactor; wherein the content of the first and second substances,
the reactor comprises: the heat exchanger comprises a shell 10, an inner cylinder 11 arranged in the shell 10 and a circulating heat exchange device; the bottom end of the inner cylinder 11 is connected to the inner bottom surface of the shell 10, and the top end is open; the area between the outer shell 10 and the inner cylinder 11 is a first reaction zone 13, the first reaction zone 13 is a reaction zone for converting p-xylene into p-tolualdehyde and p-tolualdehyde into p-toluic acid (i.e. the first two-step oxidation reaction for PX producing PTA), the inner cylinder 11 is sequentially provided with a second reaction zone 14 and a third reaction zone 15 from top to bottom, the second reaction zone 14 is a reaction zone for converting p-toluic acid into p-carboxybenzaldehyde (i.e. the third-step oxidation reaction for PX producing PTA), and the third reaction zone 15 is a reaction zone for converting p-carboxybenzaldehyde into terephthalic acid (i.e. the fourth-step oxidation reaction for PX producing PTA); the circulating heat exchange device is respectively connected with the inner cylinder 11 and the micro-interface unit, is formed by connecting a heat exchanger 121 and a pressure pump 122 through a pipeline 16, is used for effectively controlling the temperature in the reaction process, simultaneously ensures the mixing uniformity among all reaction materials in the reactor, ensures that all reactants can fully participate in the reaction, further greatly improves the utilization rate of the reactants, simultaneously prevents the occurrence of side reactions caused by uneven local temperature, and improves the quality of products to a certain extent. In addition, the top end of the housing 10 is further opened with a tail gas channel, and the bottom is provided with a mixed material for taking out the reaction product terephthalic acid in the third reaction zone 15. It can be understood that, in the invention, the rate difference of the four-step reaction for producing PTA by PX is considered, a sectional type reaction concept is adopted, the reactor is internally provided with a first reaction area, a second reaction area and a third reaction area which are different, different reaction steps are carried out in each reaction area, the purpose of giving different conditions to different reaction stages in the same reactor is effectively realized, especially the contradiction that an acetic acid solvent cannot bear high-temperature oxidation conditions is solved, water is used as a solvent of p-TA oxidation reaction, the problems that a large amount of acetic acid which is a reaction solvent in the existing PX production PTA process is wasted at high temperature and high pressure and a product TA cannot be taken out in time are effectively solved, the energy consumption is greatly reduced, the acetic acid solvent is saved, and the reaction efficiency is improved.
In this embodiment, a shell 10, an inner tube 11 concentrically disposed inside the shell 10, and a circulating heat exchange device partially disposed outside the shell 10, the inner tube 11 is connected to the inner bottom surface of the shell 10 in a closed manner at the bottom end, has an open top end, and extends upwards to 4/5 of the height of the shell 10 along the axial direction of the reactor, the annular region between the shell 10 and the inner tube 11 is a first reaction zone 13 for performing the first two-step oxidation reaction for PX to produce PTA, the volume of the first reaction zone is 45% of the total reaction volume in the reactor, the interior of the inner tube 11 is sequentially from top to bottom a second reaction zone 14 for performing the third-step oxidation reaction for PX to produce PTA and a third reaction zone 15 for performing the fourth-step oxidation reaction for PX to produce PTA, the volume of the second reaction zone is 53.5% of the total reaction volume in the reactor, the volume of the third reaction zone accounts for 1.5 percent of the total reaction volume in the reactor, and a wave-proof grating 17 is arranged between the third reaction zone and the third reaction zone; the circulating heat exchange device is respectively connected with the inner cylinder 11 and the micro-interface unit and is formed by connecting a heat exchanger 121 and a pressure pump 122 through a pipeline 16, so that the temperature in the reaction process is effectively controlled in the reaction process, power is provided for a second micro-interface generator connected with the circulating heat exchange device, the mixing uniformity of all reaction materials in the reactor is ensured, the reactants can fully participate in the reaction, the utilization rate of the reactants is greatly improved, meanwhile, the occurrence of side reaction caused by uneven local temperature is prevented, and the quality of products is improved to a certain extent. In addition, the upper part of the shell 10 is also provided with a defoaming net 18, the top end part is also provided with a tail gas channel, and the bottom part is provided with a mixed material for taking out the reaction product terephthalic acid in the third reaction zone 15. It can be understood that, in the embodiment, in consideration of the rate difference of the four-step reaction for producing PTA by PX, a sectional reaction concept is adopted, the reactor is internally provided with three different reaction regions, and different reaction steps of each reaction region realize that different conditions are applied to different reaction stages in the same reactor, and particularly, the reaction volume of each reaction region is determined according to the reaction difficulty or the reaction time of different reaction stages, so that each reaction in the process of producing PTA by PX can be sufficiently performed, further, the reaction efficiency of each reaction region is greatly improved while the contradiction that an acetic acid solvent cannot bear high-temperature oxidation conditions is solved, and finally, the yield of products is effectively improved.
The micro-interface unit includes: the first micro-interface generator 20 is arranged at the bottom of the first reaction zone 13, the second reaction zone 14 and the third reaction zone 15, and is used for crushing air serving as a reaction raw material into micro-bubbles with the diameter of more than or equal to 1 micrometer and less than 1mm in each reactor zone inside the reactor so as to provide the reaction raw material for reactions in different stages; the second micro-interface generator 21 is disposed at the upper end of the second reaction zone 14, is opposite to the first micro-interface generator 20 disposed at the bottom of the second reaction zone 14, and is used for sucking the unreacted air collected at the top of the reactor into the interior of the reactor under the power of the reaction liquid in the second reaction zone 14 conveyed by the circulating heat exchange device to be broken into the micro-bubbles. The specific structure of the micro-interfacial surface generator is disclosed in the prior patent of the present invention, such as the patent with the publication number 106215730a, the core of the micro-interfacial surface generator is the bubble breaking, which is not described in detail. The reaction mechanism and the control method of the micro-interface generator 4 are disclosed in the prior patent CN107563051B, and are not described in detail. It can be understood that in the invention, through arranging the micro-interface generator in each reaction zone in the reactor, the air is crushed in each reaction zone to be crushed into micro-bubbles with the diameter of more than or equal to 1 μm and less than 1mm, and the micro-bubbles and the liquid-phase material form emulsion, so that the mass transfer area between the air and the liquid-phase material is effectively increased, the thickness of the liquid film is reduced, the mass transfer resistance is reduced, the energy consumption is effectively reduced, and the reaction efficiency is improved.
In this embodiment, the first micro-interface generator 20 and the second micro-interface generator 21, the first micro-interface generator 20 is a pneumatic micro-interface generator, which is respectively disposed at the bottom of the first reaction zone 13, the second reaction zone 14 and the third reaction zone 15, and is used to break air as a reaction raw material into micro-bubbles with a diameter of 1 μm or more and less than 1mm in each reactor zone inside the reactor, so as to provide the reaction raw material for different stages of reactions; the second micro-interface generator 21 is a hydraulic micro-interface generator, is arranged at the upper end of the second reaction zone 14, is opposite to the first micro-interface generator 20 arranged at the bottom of the second reaction zone 14, and is used for sucking unreacted air collected at the top of the reactor into the interior of the second reaction zone 14 under the power action of the reaction liquid in the second reaction zone and conveyed by the circulating heat exchange device to be broken into the micro-bubbles. It can be understood that, in the embodiment, the micro interface generator is arranged in each reaction zone in the reactor, and the air is crushed in each reaction zone to be crushed into micro bubbles with the diameter of more than or equal to 1 μm and less than 1mm, so as to form emulsion with the liquid-phase material, thereby effectively increasing the mass transfer area between the air and the liquid-phase material, reducing the thickness of the liquid film, reducing the mass transfer resistance, further effectively reducing the energy consumption and improving the reaction efficiency.
Please refer to fig. 1, the working process of the strengthening reaction system of the built-in micro interface unit for PX production PTA of the present embodiment is:
firstly, a mixture of raw materials of p-xylene, acetic acid and a catalyst (cobalt acetate, manganese acetate and hydrobromic acid) enters a first reaction zone 13 between a shell 10 and an inner cylinder 11 of a reactor through the lower end of the reactor (the volume of the zone accounts for 45% of the total reaction volume in the reactor, the setting is that the time for the first two-step reaction for producing PTA by PX is about 45% of the total time of all four-step reaction), meanwhile, air enters a first micro-interface generator 20 at the bottom of the first reaction zone 13 in the reactor, is crushed into micro-bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, and is mixed with liquid-phase materials in the zone to form emulsion, so that the contact area between the air and the liquid-phase reaction materials is effectively increased, and the reaction in the zone is promoted. Two reactions before PX produces PTA occur in the area, namely, p-xylene is converted into p-tolualdehyde, p-tolualdehyde is converted into p-toluic acid, and overflows to the inner barrel, and unreacted gas leaves the liquid level (wave line), passes through the defoaming net 18 and rises to the upper part of the reactor. In this region, the fluid is in a steady plug flow, completing primarily the first reaction PX → TALD and the second reaction TALD → p-TA.
Then, air broken into the micro-bubbles is introduced into the region through a first micro-interface generator arranged at the bottom of a second reaction zone at the upper part of the inner cylinder, the air is mixed with liquid-phase materials in the region to form emulsion and reacts with p-toluic acid in the mixed solution under the action of the catalyst to generate p-carboxybenzaldehyde, wherein unreacted gas leaves the liquid level (wave line), passes through a defoaming net 18, rises to the upper part of the reactor, and the unreacted air leaves the liquid level to rise to the upper part of the reactor, is sent to the bottom of the second reaction zone 14 at the upper part of the inner cylinder 11 through a gas guide pipe 19 under the power of a circulating heat exchange device and is sent to the bottom of the second reaction zone 14 at the upper part of the inner cylinder 11 under the entrainment action of the second micro-interface generator to continuously participate in the reaction, after multiple cycles, under the pressure pushing, the tail gas enters the tail gas treatment unit from the top outlet of the reactor, so that the utilization rate of oxygen in the air can be improved. In this region, two micro-interfacial generators (the first micro-interfacial generator 20 and the second micro-interfacial generator 21) opposed up and down are used to generate a vigorous and complete mixed flow to perform the third step of reaction p-TA → 4-CBA (this step has the slowest reaction speed, so the effect of complete mixed flow is to be made to enhance the mass transfer and accelerate the reaction at the same time, this region occupies 53.5% of the total reaction volume in the reactor for the same reason). Meanwhile, the temperature of the materials in the region is controlled by a circulating heat exchange device outside the reactor, the bubbles generated by the second micro-interface generator 21 in the second reaction zone 14 move downwards, the bubbles generated by the first micro-interface generator 20 move upwards, and the bubbles are violently collided, so that the turbulence of the fluid is strengthened, smaller bubbles can be generated, the gas-liquid two-phase contact area is further increased, and the mass transfer and reaction are accelerated.
Finally, the product in the second reaction zone 14 passes through the wave grating 17 into the third reaction zone 15 (this zone has a volume of 1.5% of the total reaction volume in the reactor for the same reason), which is turned into a plug flow by the wave grating 17, and the fourth reaction step 4-CBA → TA is carried out, i.e., the conversion of p-carboxybenzaldehyde into terephthalic acid. Air enters the reaction zone through a first micro-interface generator 20 at the bottom of the reaction zone to perform the oxidation reaction. And discharging a reaction product (terephthalic acid TA) together with unreacted p-xylene PX, the solvent, the catalyst, byproducts and the like through an outlet pipeline below the reactor, and entering a subsequent separation and refining section.
It can obviously be reachd, the utility model provides a built-in micro-interface unit of PX production PTA reinforces reaction system, the rate difference of the four-step reaction of PX production PTA is considered, adopt the reaction theory of sectional type, set up the reactor inside into the reaction zone of three difference, the different reaction step of each reaction zone, it gives different conditions to different reaction stages in same reactor to have realized, especially, the contradiction that the acetic acid solvent can not bear the high temperature oxidation condition has been solved, and utilize water as the solvent of p-TA oxidation reaction, it is extravagant by a large amount at high temperature high pressure to have solved current PX production PTA in-process reaction solvent acetic acid effectively, can not take out the problem of product TA simultaneously in time, and then reduced the energy consumption widely, saved the acetic acid solvent, the reaction efficiency has been promoted.
Especially, the utility model discloses a reaction system is reinforceed to built-in little interface unit of PX production PTA, through set up little interface generator in each reaction zone inside the reactor, carry out the breakage to the air inside each reactor, make its breakage be diameter more than or equal to 1 mu m, be less than 1 mm's microbubble, form the emulsion with the liquid phase material, mass transfer area between air and the liquid phase material has been increased effectively, reduce liquid film thickness, reduce mass transfer resistance, and then reduced the energy consumption effectively, the reaction efficiency has been promoted.
Further, the utility model discloses a reaction system is reinforceed to built-in micro-interface unit of PX production PTA, through setting up circulation heat transfer device, the in-process effective control that goes on at the reaction temperature in the reaction process, the degree of consistency of mixing between inside each reaction material of reactor has been ensured simultaneously, each reactant can be abundant participate in the reaction has been ensured, and then the utilization ratio of reactant has greatly been promoted, the emergence of the while because of the uneven side reaction that causes of local temperature has been prevented, the quality of result has been promoted to a certain extent.
It will be apparent to those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (8)
1. A built-in micro-interface unit intensified reaction system for producing PTA by PX is characterized by comprising: the reactor comprises a reactor and a micro interface unit arranged in the reactor; wherein the content of the first and second substances,
the reactor comprises a shell, an inner cylinder concentrically arranged in the shell and a circulating heat exchange device partially arranged outside the shell, the bottom end of the inner cylinder is connected to the inner bottom surface of the shell in a closed mode, the top end of the inner cylinder is open, the area between the shell and the inner cylinder is a first reaction area, a second reaction area and a third reaction area are sequentially arranged in the inner cylinder from top to bottom, and the circulating heat exchange device is respectively connected with the inner cylinder and the micro-interface unit;
the micro-interface unit comprises a first micro-interface generator and a second micro-interface generator, wherein the first micro-interface generator is pneumatic, and the second micro-interface generator is hydraulic;
the first micro-interface generator is respectively arranged at the bottoms of the first reaction zone, the second reaction zone and the third reaction zone and is used for crushing air serving as a reaction raw material into micro-bubbles, and the second micro-interface generator is arranged at the upper end of the second reaction zone, is opposite to the first micro-interface generator arranged at the bottom of the second reaction zone and is used for sucking unreacted air collected at the top of the reactor into the interior of the reactor under the power action of the reaction liquid in the second reaction zone conveyed by the circulating heat exchange device and crushing the unreacted air into the micro-bubbles;
the first reaction zone is for carrying on the reaction zone that p-xylene turned into p-tolualdehyde, p-tolualdehyde turned into p-toluic acid, the second reaction zone is the reaction zone that p-toluic acid turned into p-carboxybenzaldehyde, the third reaction zone is the reaction zone that p-carboxybenzaldehyde turned into terephthalic acid.
2. The system of claim 1, wherein the diameter of the micro-bubbles is greater than or equal to 1 μm and less than 1 mm.
3. The built-in micro-interface unit enhanced reaction system for PX production PTA of claim 2, wherein the height of the inner barrel is 4/5 of the housing height.
4. The built-in micro-interface unit enhanced reaction system for PX production PTA as claimed in claim 3, wherein the volume of said first reaction zone is 45% of the total reaction volume in said reactor.
5. The built-in micro-interface unit enhanced reaction system for PX production PTA as claimed in claim 3, wherein the volume of said second reaction zone is 53.5% of the total reaction volume in said reactor.
6. The built-in micro-interface unit enhanced reaction system for PX production PTA as claimed in claim 3, wherein the volume of said third reaction zone is 1.5% of the total reaction volume in said reactor.
7. The system of claim 1, wherein the circulating heat exchange device comprises a heat exchanger for exchanging heat and a pressure pump connected to the heat exchanger for providing power.
8. The built-in micro-interface unit enhanced reaction system for PTA production in claim 1, wherein a wave-proof grating is disposed between the second reaction zone and the third reaction zone.
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