CN218047843U - Alkylbenzene apparatus for producing of high-efficient catalysis of hydrogen fluoride and quick separation - Google Patents
Alkylbenzene apparatus for producing of high-efficient catalysis of hydrogen fluoride and quick separation Download PDFInfo
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- CN218047843U CN218047843U CN202222018029.5U CN202222018029U CN218047843U CN 218047843 U CN218047843 U CN 218047843U CN 202222018029 U CN202222018029 U CN 202222018029U CN 218047843 U CN218047843 U CN 218047843U
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- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 title claims abstract description 95
- 150000004996 alkyl benzenes Chemical class 0.000 title claims abstract description 32
- 238000000926 separation method Methods 0.000 title claims abstract description 32
- 229910000040 hydrogen fluoride Inorganic materials 0.000 title abstract description 13
- 238000006555 catalytic reaction Methods 0.000 title abstract description 8
- 238000004519 manufacturing process Methods 0.000 claims abstract description 19
- 238000006243 chemical reaction Methods 0.000 claims abstract description 18
- 238000004581 coalescence Methods 0.000 claims abstract description 18
- 230000008929 regeneration Effects 0.000 claims abstract description 18
- 238000011069 regeneration method Methods 0.000 claims abstract description 18
- 238000000034 method Methods 0.000 claims abstract description 16
- 239000003054 catalyst Substances 0.000 claims abstract description 15
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 66
- 239000002253 acid Substances 0.000 claims description 20
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 17
- 239000000835 fiber Substances 0.000 claims description 13
- 150000001336 alkenes Chemical class 0.000 claims description 10
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 10
- 239000002994 raw material Substances 0.000 claims description 8
- 238000009941 weaving Methods 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 5
- 239000000376 reactant Substances 0.000 claims description 4
- 230000002708 enhancing effect Effects 0.000 claims description 2
- 238000012856 packing Methods 0.000 claims 1
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 7
- 229930195733 hydrocarbon Natural products 0.000 abstract description 2
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 2
- 238000005804 alkylation reaction Methods 0.000 description 10
- 239000000047 product Substances 0.000 description 8
- 230000029936 alkylation Effects 0.000 description 5
- 239000000203 mixture Substances 0.000 description 4
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- 238000003541 multi-stage reaction Methods 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000011541 reaction mixture Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 229910000792 Monel Inorganic materials 0.000 description 1
- 239000003377 acid catalyst Substances 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000003442 catalytic alkylation reaction Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- -1 polytetrafluoroethylene Polymers 0.000 description 1
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 1
- 239000004810 polytetrafluoroethylene Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides an alkylbenzene production device with high-efficiency catalysis and rapid separation of hydrogen fluoride, which comprises a micro mixer, a coalescence separator, a stripping tower and a regeneration tower, wherein a product outlet at the top of the micro mixer is communicated with a coalescer inlet at the left end of the coalescence separator through a pipeline, an alkylate oil outlet at the top of the right end of the coalescence separator is communicated with an alkylate oil inlet of the stripping tower through a pipeline, a hydrofluoric acid outlet at the bottom of the right end of the separator is respectively communicated with a hydrofluoric acid outlet of the regeneration tower and a catalyst inlet of the micro mixer through pipelines, and a regenerated hydrofluoric acid outlet of the regeneration tower is communicated with the catalyst inlet of the micro mixer through a pipeline. The utility model discloses a process flow is short, compact structure, and reaction efficiency is high, and sour hydrocarbon separation is fast, and the separation precision is high, and hydrofluoric acid content is low in the ejection of compact alkylate oil.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to an alkylbenzene production device with efficient catalysis and rapid separation of hydrogen fluoride.
Background
At present, in the industrial production process of alkylbenzene, benzene and long-chain olefin are mainly used for preparing alkylate oil through alkylation reaction under the action of an acid catalyst, and then alkylbenzene is obtained through a subsequent purification process. The existing alkylbenzene production process mainly adopts a hydrofluoric acid method, and generally raw materials are input into a static mixer through a feeding system, are conveyed into a reactor after being fully mixed, and react under the action of a catalyst to obtain a reaction mixture. And (3) inputting the reaction mixture into a separation tank for acid-hydrocarbon separation, and then further separating and purifying the reaction product after the acid-hydrocarbon separation to obtain the alkylbenzene. The process mainly involves the equipment and procedures of a feed system, a static mixer, an alkylation reactor, an acid settling tank and the like.
CN202010294860.6 discloses a process for producing long-chain alkylbenzenes with hydrogen fluoride by reacting C 14-24 Olefin and benzene are mixed, added with hydrogen fluoride for alkylation reaction, and then layered, distilled and resolved to obtain C 14-24 An alkylbenzene. The method has high requirements on the purity of the used hydrogen fluoride, generally requires the purity to be higher than 99 percent, and needs liquid hydrogen fluoride, and has high requirements on reaction temperature and pressure and complex flow; CN03113197.2 discloses a liquid hydrogen fluoride catalytic alkylation multistage reaction, which divides the alkylation step into two or more stages, and feeds the stage by stage to carry out multistage reaction. The method solves the problem of high total benzene content in alkylation reaction, but the corresponding multistage reaction improves the load of a reaction system, prolongs the reaction flow and increases the energy consumption.
The method of the patent has the problems of more production devices, large occupied area and low acid-hydrocarbon separation speed.
Disclosure of Invention
In order to solve the defects of the prior art, the invention provides an alkylbenzene production device with high-efficiency catalysis and rapid separation of hydrogen fluoride, which utilizes a micro mixer to replace the traditional static mixer and reactor and a coalescence separator to replace the traditional acid settling tank, so that the mixing and reaction of alkane and olefin and benzene are carried out in the micro mixer, the process flow is shortened, the load and energy consumption of the process are reduced, and the reaction and the acid-hydrocarbon separation efficiency are improved.
In order to achieve the purpose, the invention adopts the following technical scheme:
an alkylbenzene production device with efficient catalysis and rapid separation of hydrogen fluoride comprises a micro mixer, a coalescence separator, a stripping tower and a regeneration tower, wherein the micro mixer is provided with an alkane and olefin raw material inlet, a benzene raw material inlet, a catalyst inlet and a product outlet; the product outlet at the top of the micro mixer is communicated with the coalescer inlet at the left end of the coalescer separator through a pipeline, the alkylate oil outlet at the top of the right end of the coalescer separator is communicated with the alkylate oil inlet of the stripping tower through a pipeline, the hydrofluoric acid outlet at the bottom of the right end of the separator is respectively communicated with the hydrofluoric acid outlet of the regeneration tower and the catalyst inlet of the micro mixer through pipelines, and the regenerated hydrofluoric acid outlet of the regeneration tower is communicated with the catalyst inlet of the micro mixer through a pipeline.
Preferably, the micro mixer comprises a vertical shell, and the shell is internally divided into a feeding section, a mixing section and a reaction section from bottom to top in sequence: a feeding unit is arranged in the feeding section shell and comprises a feeding tee joint, an ejector and a first feeding pipeline, the left port and the right port of the feeding tee joint are respectively connected with the ejector and the first feeding pipeline, the ejector and the first feeding pipeline are respectively used for feeding alkane and olefin and benzene, the side surface of the upper port of the feeding tee joint is connected with a second feeding pipeline, and the second feeding pipeline is used for feeding hydrofluoric acid; a mixer is arranged in the mixing section shell, one end of the mixer is connected with the top port of the feed tee, and the mixer is used for enhancing the mixing of reactants and a catalyst; and a spiral coil is arranged in the shell of the reaction section, the inlet end of the spiral coil is communicated with the other end of the mixer, and the outlet end of the spiral coil extends to the top of the shell of the micro mixer to form a product outlet.
Preferably, the ejector comprises a cylindrical ejector shell with an opening at one side and a hemispherical structure at the other side, and a supporting structure, a flow guide structure and a thimble structure are sequentially arranged in the ejector shell; the supporting structure comprises a cylindrical supporting rod and a supporting frame which is radially connected with the supporting rod and the inner wall of the ejector shell; the flow guide structure comprises an integrally formed cylindrical flow guide body and a conical flow guide body with equal excircles; the bottom of the cylindrical flow guide body is connected with a support rod; the thimble structure is a cylinder arranged at the tip end of the conical flow deflector; the ejector comprises an ejector shell, and is characterized in that a hemispherical structure of the ejector shell is provided with a jet orifice, and the jet orifice is over against the ejector pin structure and is 1-10 mm away from the ejector pin structure.
Preferably, be equipped with the blender in the mixing section casing, the blender includes the cylindric casing of vertical setting, is equipped with the mixing unit of a plurality of grades of range repeatedly in the cylindric casing, mixing unit is including the first helical structure, interlude and the second helical structure that set gradually, the central part of interlude is equipped with cylindrical support body, first helical structure and second helical structure are connected on cylindrical support body, are revolved to opposite helical blade and constitute.
Preferably, the lengths of the first spiral structure and the second spiral structure are both 1/8 to 1/2 of the length of the mixing unit.
Preferably, the coalescer separator comprises a coalescer housing, one end of the coalescer housing is provided with a coalescer inlet, and a rectifier, a first enhanced settling module, a coalescing separation module and a second enhanced settling module are sequentially arranged in the coalescer housing along the coalescer inlet and backwards; the top of the other end of the coalescer shell is provided with an oil pocket, the bottom of the coalescer shell is provided with an acid pocket, and the oil pocket and the acid pocket are respectively used for discharging the alkylate oil and the hydrofluoric acid after coalescence and separation.
Preferably, the rectifier is a circular disc with uniformly arranged circular holes or square holes, and the aperture ratio of the rectifier is 40-80%.
Preferably, the first reinforced sedimentation module and the second reinforced sedimentation module are both composed of corrugated plate coalescing filler filled in the coalescer housing.
Preferably, the coalescence-separation module is formed by mixing and weaving oleophylic fibers and hydrophilic fibers by an omega-type weaving method, wherein the proportion of the oleophylic fibers is 60-80%.
The invention has the beneficial effects that:
1. the invention provides an alkylbenzene production device with high-efficiency catalysis and rapid separation of hydrogen fluoride, which comprises a micro-mixer, a coalescence separator, a stripping tower and a regeneration tower, wherein the mixing and reaction of alkane, benzene and hydrofluoric acid are carried out in the micro-mixer, and the reaction efficiency is high; the target product alkylbenzene generated by the reaction is separated from the unreacted alkane, benzene and hydrofluoric acid in the coalescence separator, the acid and hydrocarbon separation speed is high, the separation precision is high, and the content of hydrofluoric acid in the discharged alkylate oil is low.
2. The coalescence separator has high separation efficiency, and the occupied area of the device is greatly reduced compared with the prior acid settling tank. Under the conditions of same inlet cross-section flow rate and separation effect of hydrofluoric acid content in alkylate oil lower than 1%, the raw acid settler is used for gravity settling separation only, and the volume of the raw acid settler is required to be up to
The inventive coalescer may be of a volume of
The ratio of the length to the diameter can be 2.17, greatly reducing the floor area of the device.
Drawings
FIG. 1 is a schematic view of the structure of an alkylbenzene production apparatus according to the present invention;
FIG. 2 is a schematic structural diagram of a micro mixer according to the present invention;
FIG. 3 is a schematic view showing a structure of a feed unit and a mixer of the micro mixer of the present invention;
FIG. 4 is a schematic structural view of the ejector of the present invention;
FIG. 5 is a schematic structural view of a support structure of the injector of the present invention;
FIG. 6 is a schematic structural view of a mixer of the present invention;
FIG. 7 is a schematic of the coalescer according to the invention.
Detailed Description
The present invention will be described in further detail with reference to examples. It is to be understood that the following examples are for illustrative purposes only and are not to be construed as limiting the scope of the present invention, and that certain insubstantial modifications and adaptations of the invention may be made by those skilled in the art based on the teachings herein.
Example 1
This example provides an alkylbenzene production device with high catalytic efficiency and rapid separation of hydrogen fluoride, as shown in fig. 1, comprising a micromixer 1, a coalescer 2, a stripping tower 3 and a regeneration tower 4. The micro mixer 1 is provided with an alkane and olefin raw material inlet, a benzene raw material inlet, a catalyst inlet and a product outlet, the coalescence separator 2 is provided with a coalescence device inlet 22, an alkylate oil outlet and a hydrofluoric acid outlet, the stripping tower 3 is provided with an alkylate oil inlet, a benzene outlet and an alkylbenzene outlet, and the regeneration tower 4 is provided with a hydrofluoric acid inlet, a regenerated hydrofluoric acid outlet and a tar outlet; the resultant outlet at the top of the micro mixer 1 is communicated with the coalescer inlet 22 at the left end of the coalescer separator 2 through a pipeline, the alkylate oil outlet at the top of the right end of the coalescer separator 2 is communicated with the alkylate oil inlet of the stripping tower 3 through a pipeline, the hydrofluoric acid outlet at the bottom of the right end of the separator 2 is respectively communicated with the hydrofluoric acid outlet of the regeneration tower 4 and the catalyst inlet of the micro mixer 1 through pipelines, and the regenerated hydrofluoric acid outlet of the regeneration tower 4 is communicated with the catalyst inlet of the micro mixer 1 through a pipeline.
Referring to fig. 2 to 6, the micro mixer 1 is a vertical mixer, and includes a housing, and the housing is divided into a feeding section, a mixing section and a reaction section from bottom to top.
As shown in fig. 3, a feeding unit 11 is arranged in the feeding section shell, the feeding unit 11 comprises a feeding tee 14, an ejector 15 and a first feeding pipeline 16, the feeding tee 14 is provided with a first port 141, a second port 142 and a third port 143, the third port 143 is vertically arranged, and the side surface of the third port 143 is connected with a second feeding pipeline 19; the discharge end of the ejector 15 is inserted into the first port 141, and the feed end extends out of the side wall of the shell for feeding alkane and olefin; the first feed line 16 has one end connected to the second port 142 and the other end extending beyond the side wall of the housing for feeding benzene, and the second feed line 19 has one end connected to the third port 143 and the other end extending beyond the side wall of the housing for feeding hydrofluoric acid.
As shown in fig. 4, the injector 15 includes a cylindrical injector housing 151 with one side open and the other side having a hemispherical structure, and a support structure 152, a flow guiding structure 153 and an ejector pin structure 154 are sequentially disposed in the injector housing 151. As shown in fig. 5, the support structure 152 includes a cylindrical support rod 155 and a cross-shaped support bracket 156 radially connecting the support rod 155 and the inner wall of the injector housing 151; the flow guide structure 153 comprises a cylindrical flow guide body 157 and a conical flow guide body 158 which are integrally formed and have equal outer circles; the bottom surface of the cylindrical flow guiding body 157 is connected with the cylindrical supporting rod 155, the top surface is connected with the conical flow guiding body 158, and the thimble structure 154 is a cylinder arranged at the center of the top surface of the conical flow guiding body 158; the semi-spherical structure of the ejector shell 151 is provided with an injection port 159, and the injection port 159 is opposite to the thimble structure 154 and has a distance of 1-10 mm from the thimble structure 154. The reactant alkane and olefin are fed from the open end of the injector 16, pass through the supporting structure 152, are guided by the guide structure 153, are subjected to shearing and crushing between the ejector pin structure 154 and the injector shell 151, are ejected from the injection port 159, are contacted with the reactant benzene fed from the first feeding pipeline 16, are preliminarily mixed in the feeding tee joint 14, are mixed with the hydrofluoric acid fed from the second feeding pipeline 19, and are discharged from the third port 143 to enter the mixing section.
As shown in fig. 6, a mixer 12 is arranged in the mixing section shell, the mixer 12 includes a vertically arranged cylindrical shell, a plurality of mixing units 121 arranged repeatedly are arranged in the cylindrical shell, and the number of the mixing units 121 is the number of mixing stages; the mixing unit 121 includes a first helical structure 122, an intermediate section 123 and a second helical structure 124 which are sequentially arranged, the central portion of the intermediate section 123 is provided with a cylindrical support body 125, two ends of the cylindrical support body 125 respectively extend to the first helical structure 122 and the second helical structure 124, the first helical structure 122 and the second helical structure 124 are formed by helical blades which are connected to the cylindrical support body 125 and have opposite rotation directions, and the helical blades of the first helical structure 122 and the second helical structure 124 are in contact with the inner wall of the shell of the mixer 12.
The length of the mixing unit 121 is L, and the lengths of the first spiral structure 122 and the second spiral structure 124 are L respectively 1 And L 3 ，L 1 ＝L 3 ＝1/8～1/2L。
One end of the mixer 12 is connected with the third port 143 through a flange, the other end is communicated with a spiral coil 13 arranged in the shell of the reaction section, the spiral coil 13 spirally rises along the inner wall of the shell of the micro mixer 1, and the top of the shell stretches out to form a discharge port. The alkane, the benzene and the hydrofluoric acid mixed by the mixer 12 are subjected to alkylation reaction in the spiral coil pipe 13, and a target product, namely alkylbenzene, and unreacted alkane, benzene and hydrofluoric acid generated by the reaction are discharged from a discharge hole and enter the coalescence separator 2. The heat exchange medium flows in the shell of the micro mixer 1, the shell of the micro mixer 1 is provided with a shell pass inlet 17 and a shell pass outlet 18 for the heat exchange medium to enter and exit, and the flow of the heat exchange medium and the flow of the reaction system are in counter flow.
As shown in fig. 7, the coalescer separator 2 comprises a coalescer housing 21, one end of the coalescer housing 21 is provided with a coalescer inlet 22, and the coalescer inlet 22 is communicated with the discharge port of the micromixer 1 through a pipeline; a rectifier 25, a first enhanced settling module 26, a coalescing separation module 27 and a second enhanced settling module 28 are sequentially arranged in the coalescer housing 21 along the coalescer inlet 22 backwards; the other end of the coalescer shell 21 is provided with an oil pocket 23 at the top and an acid pocket 24 at the bottom, which are respectively used for separating and discharging the alkylate oil and the hydrofluoric acid after coalescence and separation.
The rectifier 25 is a disc uniformly provided with round holes or square holes, and the aperture ratio is 40-80%, so that the alkylated mixture after reaction is uniformly distributed along the radial section; the first enhanced settling module 26 and the second enhanced settling module 28 have substantially the same structure, and are formed by corrugated plate coalescing fillers filled in the coalescer housing 21, oil drops and acid drops are rapidly concentrated on the upper surface and the surface of the corrugated plate in the up-down cross flow flowing process of the corrugated plate, an oil film and an acid film are formed, the oil drops entrained in the acid are rapidly combined with the oil film, the acid drops entrained in the oil are rapidly combined with the acid film, and large oil drops and large acid drops are formed when the oil drops are separated from the corrugated plate.
The coalescence-separation module 27 is formed by mixing and weaving oleophylic fibers and hydrophilic fibers by an omega-type weaving method, wherein the proportion of the oleophylic fibers is 60-80%, the omega-type weaving method is the weaving method disclosed in CN201410211201.6, the coalescence-separation module 27 can provide a great specific surface area, improve the purity of liquid phase separation, and can realize deep separation while keeping low pressure drop. The oleophilic fibers are preferably polytetrafluoroethylene fibers, and the hydrophilic fibers are preferably Monel fibers.
Preferably, the ratio of the height to the diameter of the micromixer 1 is (1 to 3): 1, the length-diameter ratio of the coalescer separator 2 is (1-3): 1.
the production device of the utility model is used for the production of alkylbenzene:
(1) Alkane and benzene respectively enter the micro mixer 1 through a raw material inlet, hydrofluoric acid enters the micro mixer 1 through a catalyst inlet, and the alkane and the benzene are subjected to alkylation reaction in the micro mixer 1 under the catalysis of the hydrofluoric acid to generate an alkylation mixture which is discharged from a product outlet of the micro mixer 1, wherein the alkylation mixture comprises a target product, namely alkylbenzene and unreacted alkane, benzene and hydrofluoric acid.
(2) Conveying the alkylation mixture discharged in the step (1) into a coalescer inlet 22 of a coalescer separator 2 through a pipeline, carrying out acid-hydrocarbon separation in the coalescer separator 2, discharging separated alkylate oil from an alkylate oil outlet at the top of the coalescer separator 2, and discharging hydrofluoric acid from a hydrofluoric acid outlet at the bottom of the coalescer separator 2, wherein the alkylate oil comprises alkylbenzene and unreacted alkane and benzene;
(3) Conveying the alkylate discharged in the step (2) to an alkylate inlet of a stripping tower 3 through a pipeline, evaporating benzene containing acid from the top of the tower, and separating alkylbenzene and unreacted alkane from the bottom of the tower;
(4) Most of hydrofluoric acid discharged from the bottom of the coalescence separator 2 is returned to the micro mixer 1 as circulating acid for recycling, in order to maintain the purity of the circulating acid, the residual small amount of hydrofluoric acid is conveyed to the regeneration tower 4 for regeneration, and the hydrofluoric acid purified by the regeneration tower 4 is returned to the micro mixer 1 from a side discharge for recycling.
Claims (9)
1. The alkylbenzene production device is characterized by comprising a micro mixer (1), a coalescence separator (2), a stripping tower (3) and a regeneration tower (4), wherein the micro mixer (1) is provided with an alkane and olefin raw material inlet, a benzene raw material inlet, a catalyst inlet and a resultant outlet, the coalescence separator (2) is provided with a coalescence device inlet (22), an alkylate oil outlet and a hydrofluoric acid outlet, the stripping tower (3) is provided with an alkylate oil inlet, a benzene outlet and an alkylbenzene outlet, and the regeneration tower (4) is provided with a hydrofluoric acid inlet, a regenerated hydrofluoric acid outlet and a tar outlet; a resultant outlet at the top of the micro mixer (1) is communicated with a coalescer inlet (22) at the left end of the coalescer separator (2) through a pipeline, an alkylate oil outlet at the top of the right end of the coalescer separator (2) is communicated with an alkylate oil inlet of the stripping tower (3) through a pipeline, a hydrofluoric acid outlet at the bottom of the right end of the separator (2) is respectively communicated with a hydrofluoric acid outlet of the regeneration tower (4) and a catalyst inlet of the micro mixer (1) through pipelines, and a regenerated hydrofluoric acid outlet of the regeneration tower (4) is communicated with a catalyst inlet of the micro mixer (1) through a pipeline.
2. The alkylbenzene production device according to claim 1, wherein the micromixer (1) comprises a vertical shell, and the shell is internally divided into a feeding section, a mixing section and a reaction section from bottom to top in sequence: a feeding unit is arranged in the feeding section shell and comprises a feeding tee joint (14), an ejector (15) and a first feeding pipeline (16), the left port and the right port of the feeding tee joint (14) are respectively connected with the ejector (15) and the feeding pipeline (16), the ejector (15) and the first feeding pipeline (16) are respectively used for feeding alkane and olefin and benzene, the side surface of the upper port of the feeding tee joint (14) is connected with a second feeding pipeline (19), and the second feeding pipeline (19) is used for feeding hydrofluoric acid; a mixer (12) is arranged in the mixing section shell, one end of the mixer (12) is connected with the top port of the feed tee (14), and the mixer (12) is used for enhancing the mixing of reactants and a catalyst; a spiral coil (13) is arranged in the shell of the reaction section, the inlet end of the spiral coil (13) is communicated with the other end of the mixer (12), and the outlet end extends to the top of the shell of the micro mixer to form a product outlet.
3. The alkylbenzene production device according to claim 2, wherein the injector (15) comprises a cylindrical injector housing (151) having an opening at one side and a hemispherical structure at the other side, and a support structure (152), a flow guide structure (153) and a thimble structure (154) are sequentially arranged in the injector housing (151); the support structure (152) comprises a cylindrical support rod (155) and a support frame (156) radially connecting the support rod (155) and the injector housing; the flow guide structure (153) comprises a cylindrical flow guide body (157) and a conical flow guide body (158) which are integrally formed and have equal excircles; the bottom of the cylindrical flow guide body (157) is connected with a support rod (155); the thimble structure (154) is a cylinder arranged at the tip end of the conical flow guide body (158); and a jet orifice (159) is arranged on the hemispherical structure of the ejector shell, and the jet orifice (159) is over against the thimble structure (154) and is 1-10 mm away from the thimble structure.
4. The alkylbenzene production device according to claim 1, wherein the mixer (12) is arranged in the mixing section shell, the mixer (12) comprises a vertically arranged cylindrical shell, the mixing unit (121) is arranged in the cylindrical shell in a plurality of stages, the mixing unit (121) comprises a first helical structure (122), an intermediate section (123) and a second helical structure (124) which are sequentially arranged, a cylindrical support body (125) is arranged at the center of the intermediate section (123), and the first helical structure (122) and the second helical structure (124) are formed by helical blades which are connected to the cylindrical support body (125) and have opposite rotation directions.
5. The alkylbenzene production apparatus according to claim 4, wherein the lengths of the first helical structure (122) and the second helical structure (124) are each 1/8 to 1/2 of the length of the mixing unit (121).
6. The alkylbenzene production device according to claim 1, wherein the coalescer separator (2) comprises a coalescer housing (21), one end of the coalescer housing (21) is provided with a coalescer inlet (22), and a rectifier (25), a first enhanced settling module (26), a coalescing separation module (27) and a second enhanced settling module (28) are sequentially arranged in the coalescer housing (21) along the coalescer inlet; the top of the other end of the coalescer shell (21) is provided with an oil pocket, the bottom of the coalescer shell is provided with an acid pocket, and the oil pocket and the acid pocket are respectively used for discharging the alkylate oil and the hydrofluoric acid after coalescence and separation.
7. The apparatus for producing alkylbenzene as claimed in claim 6, wherein the rectifier (25) is a circular disk with uniformly formed circular or square holes, and has an opening ratio of 40% to 80%.
8. The alkylbenzene production device according to claim 6, characterised in that the first and second enhanced settling modules (26, 28) are each constituted by corrugated sheet coalescing packing filled in a coalescer housing (21).
9. The alkylbenzene production device according to claim 6, wherein the coalescence-separation module (27) is formed by co-weaving oleophilic fibers and hydrophilic fibers by an omega-weaving method, wherein the proportion of oleophilic fibers is 60% to 80%.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222018029.5U CN218047843U (en) | 2022-08-02 | 2022-08-02 | Alkylbenzene apparatus for producing of high-efficient catalysis of hydrogen fluoride and quick separation |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222018029.5U CN218047843U (en) | 2022-08-02 | 2022-08-02 | Alkylbenzene apparatus for producing of high-efficient catalysis of hydrogen fluoride and quick separation |
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