CN217430859U - Device for preparing alpha-methylstyrene by dehydrating 2-phenyl-2-propanol - Google Patents
Device for preparing alpha-methylstyrene by dehydrating 2-phenyl-2-propanol Download PDFInfo
- Publication number
- CN217430859U CN217430859U CN202221520756.5U CN202221520756U CN217430859U CN 217430859 U CN217430859 U CN 217430859U CN 202221520756 U CN202221520756 U CN 202221520756U CN 217430859 U CN217430859 U CN 217430859U
- Authority
- CN
- China
- Prior art keywords
- dehydration catalyst
- catalyst layer
- dehydration
- phase
- reaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- XYLMUPLGERFSHI-UHFFFAOYSA-N alpha-Methylstyrene Chemical compound CC(=C)C1=CC=CC=C1 XYLMUPLGERFSHI-UHFFFAOYSA-N 0.000 title claims abstract description 39
- BDCFWIDZNLCTMF-UHFFFAOYSA-N 2-phenylpropan-2-ol Chemical compound CC(C)(O)C1=CC=CC=C1 BDCFWIDZNLCTMF-UHFFFAOYSA-N 0.000 title claims abstract description 18
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 133
- 230000018044 dehydration Effects 0.000 claims abstract description 114
- 238000006243 chemical reaction Methods 0.000 claims abstract description 67
- 238000004519 manufacturing process Methods 0.000 claims abstract description 24
- 239000003054 catalyst Substances 0.000 claims description 106
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 claims description 93
- 239000012071 phase Substances 0.000 claims description 72
- 238000000066 reactive distillation Methods 0.000 claims description 46
- 238000012856 packing Methods 0.000 claims description 35
- 238000010992 reflux Methods 0.000 claims description 35
- 238000000926 separation method Methods 0.000 claims description 34
- 238000010438 heat treatment Methods 0.000 claims description 32
- 239000007788 liquid Substances 0.000 claims description 32
- 239000002994 raw material Substances 0.000 claims description 23
- 239000007791 liquid phase Substances 0.000 claims description 13
- 239000000463 material Substances 0.000 claims description 11
- 238000005191 phase separation Methods 0.000 claims description 11
- 238000003860 storage Methods 0.000 claims description 5
- 238000009826 distribution Methods 0.000 claims description 3
- 239000002351 wastewater Substances 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 239000008346 aqueous phase Substances 0.000 claims 1
- ARSRBNBHOADGJU-UHFFFAOYSA-N 7,12-dimethyltetraphene Chemical compound C1=CC2=CC=CC=C2C2=C1C(C)=C(C=CC=C1)C1=C2C ARSRBNBHOADGJU-UHFFFAOYSA-N 0.000 abstract description 44
- VFZRZRDOXPRTSC-UHFFFAOYSA-N DMBA Natural products COC1=CC(OC)=CC(C=O)=C1 VFZRZRDOXPRTSC-UHFFFAOYSA-N 0.000 abstract description 44
- 238000000034 method Methods 0.000 abstract description 38
- 230000008569 process Effects 0.000 abstract description 15
- 230000003197 catalytic effect Effects 0.000 abstract description 4
- 208000005156 Dehydration Diseases 0.000 description 88
- 239000007789 gas Substances 0.000 description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 21
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 10
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 8
- 239000000047 product Substances 0.000 description 8
- 238000004458 analytical method Methods 0.000 description 7
- 239000012295 chemical reaction liquid Substances 0.000 description 7
- 239000000243 solution Substances 0.000 description 7
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 6
- 238000005070 sampling Methods 0.000 description 6
- 238000007599 discharging Methods 0.000 description 5
- 239000000945 filler Substances 0.000 description 5
- 230000003647 oxidation Effects 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- XMNIXWIUMCBBBL-UHFFFAOYSA-N 2-(2-phenylpropan-2-ylperoxy)propan-2-ylbenzene Chemical compound C=1C=CC=CC=1C(C)(C)OOC(C)(C)C1=CC=CC=C1 XMNIXWIUMCBBBL-UHFFFAOYSA-N 0.000 description 4
- FRIBMENBGGCKPD-UHFFFAOYSA-N 3-(2,3-dimethoxyphenyl)prop-2-enal Chemical compound COC1=CC=CC(C=CC=O)=C1OC FRIBMENBGGCKPD-UHFFFAOYSA-N 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 4
- XENVCRGQTABGKY-ZHACJKMWSA-N chlorohydrin Chemical compound CC#CC#CC#CC#C\C=C\C(Cl)CO XENVCRGQTABGKY-ZHACJKMWSA-N 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000012808 vapor phase Substances 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- 230000008859 change Effects 0.000 description 2
- 238000010543 cumene process Methods 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000011344 liquid material Substances 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- YZUPZGFPHUVJKC-UHFFFAOYSA-N 1-bromo-2-methoxyethane Chemical compound COCCBr YZUPZGFPHUVJKC-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 239000004721 Polyphenylene oxide Substances 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- SNAAJJQQZSMGQD-UHFFFAOYSA-N aluminum magnesium Chemical compound [Mg].[Al] SNAAJJQQZSMGQD-UHFFFAOYSA-N 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000010533 azeotropic distillation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003729 cation exchange resin Substances 0.000 description 1
- 229940023913 cation exchange resins Drugs 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000005285 chemical preparation method Methods 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 125000002592 cumenyl group Chemical group C1(=C(C=CC=C1)*)C(C)C 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000003631 expected effect Effects 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 229920000570 polyether Polymers 0.000 description 1
- 229920005862 polyol Polymers 0.000 description 1
- 150000003077 polyols Chemical class 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000011973 solid acid Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Images
Abstract
The utility model provides a production device and a production method for preparing alpha-methyl styrene (AMS) by utilizing 2-phenyl-2-propanol (DMBA) to dehydrate. The device is a reaction rectifying tower capable of simultaneously carrying out dehydration reaction and dehydration rectification, can realize the functions of catalytic dehydration, azeotropic rectification and split-phase dehydration of DMBA at the same time, can improve the dehydration efficiency, and can realize that the dehydration conversion rate of DMBA reaches more than 95% under the mild process condition.
Description
Technical Field
The utility model belongs to the technical field of organic synthesis's process units, concretely relates to preparation facilities of alpha-methylstyrene.
Background
Propylene Oxide (PO) is an important chemical raw material. The propylene oxide can be used for preparing polyether polyol and occupies an important position in the field of fine chemical engineering. The chemical preparation method of the propylene oxide comprises a chlorohydrin method, an electrochemical chlorohydrin method, an ethylbenzene indirect oxidation method, a hydrogen peroxide direct oxidation method, a cumene oxidation method and the like. Among them, the chlorohydrin method and electrochemical chlorohydrin method can produce a large amount of chlorine-containing wastewater, and the pollution is serious; the ethylbenzene indirect oxidation method has more byproducts; the direct hydrogen peroxide oxidation method needs a large amount of hydrogen peroxide as a raw material, and the current process for preparing high-concentration hydrogen peroxide in China still has a plurality of defects. Compared with the above methods for preparing propylene oxide, the cumene method has the advantages of environmental friendliness, low cost, few byproducts and no need of preparing hydrogen peroxide.
In the cumene process, 2-phenyl-2-propanol (DMBA) is an intermediate product in the production of propylene oxide by the cumene process. Cumene and oxygen react to form Cumene Hydroperoxide (CHP), which further reacts with propylene to form 2-phenyl-2-propanol (DMBA) and PO. Currently, there are two main directions for the subsequent processing of DMBA: 1) synthesizing and preparing dicumyl peroxide (DCP) to form PO and DCP for co-production: CN103212437, CHP and DMBA are condensed and dehydrated to generate DCP. However, the method has the defects of small production scale, low CHP conversion rate and the like. 2) And (3) preparing the cumene by hydrogenation after preparing the AMS for recycling. In this direction, alpha-methyl styrene monomer (AMS) is produced by dehydration, and then the AMS is hydrogenated to produce cumene for recycling.
There are two common methods used to prepare AMS:
one is high temperature decomposition, adding the mixture of DMBA and isopropyl benzene into a reactor, heating to 200 deg.C, and the pressure is above 0.5MPa, the DMBA is decomposed and dehydrated, the conversion rate can reach 80%, the cost of the process equipment is high, the by-products are more, and the part of AMS generated at high temperature can be converted into ethylbenzene.
The other method is a catalytic dehydration process, a dehydration catalyst is adopted, the mixed solution of DMBA and cumene is heated to 160 ℃, and is added into a reactor filled with the catalyst for processing for 4-8 hours, the dehydration of the DMBA can be realized, and the conversion rate of the DMBA can reach 90%. WO0248126 mentions this process, which has a lower dehydration temperature. However, the patent does not separate the water generated in the reaction as soon as possible, which results in long reaction period and low efficiency.
SUMMERY OF THE UTILITY MODEL
To solve these problems, the present invention provides a production apparatus for preparing alpha-methylstyrene (AMS) by dehydrating 2-phenyl-2-propanol (DMBA), and a method for producing alpha-methylstyrene (AMS) using the same.
The utility model discloses a first aspect provides a production facility of preparation alpha-methylstyrene (AMS) by 2-phenyl-2-propanol (DMBA) dehydration.
The device comprises a reaction rectification device, a condensation device and a phase separation device; a dehydration catalyst layer is arranged in the reaction rectification device, and a separation packing layer is arranged above the dehydration catalyst layer; the reaction rectifying device is characterized in that a feed port is arranged below the separation packing layer, and a gas phase discharge port is arranged above the separation packing layer. The condensing device is connected with a gas phase discharge port of the reaction rectifying device through a pipeline, and the phase separation device is connected with the condensing device through a pipeline.
In one embodiment of the present invention, the reactive distillation apparatus is a reactive distillation column. According to the present invention, the height-diameter ratio of the reactive distillation column is in the range of 5:1 to 10:1, for example, 5.5:1, 5.6:1, 5.7:1, 5.8:1, 5.9:1, 6:1, 6.1:1, 6.2:1, 6.3:1, 6.4:1, 6.5:1, 6.6:1, 6.7:1, 6.8:1, 6.9:1, 7:1, 7.5:1, 8:1, 8.5:1, 9:1, 9.5: 1.
In one embodiment of the present invention, the aspect ratio of the separation packing layer is 0.8:1 to 2:1, for example, 0.9:1, 1:1, 1.1:1, 1.2:1, 1.3:1, 1.4:1, 1.5:1, 1.6:1, 1.7:1, 1.8:1, 1.9: 1.
In one embodiment of the present invention, the dehydration catalyst layer has a height to diameter ratio of 2:1 to 4:1, for example, 2:1, 2.1:1, 2.2:1, 2.3:1, 2.4:1, 2.5:1, 2.6:1, 2.7:1, 2.8:1, 2.9:1, 3:1, 3.1:1, 3.2:1, 3.3:1, 3.4:1, 3.5:1, 3.6:1, 3.7:1, 3.8:1, 3.9: 1. According to the utility model discloses, the dehydration catalyst layer can be divided into one section or multistage setting. In any arrangement form, the height-diameter ratio of the total dehydration catalyst layer is 2: 1-4: 1.
In the utility model, the dehydration catalyst layer arranged in a multi-section mode is sequentially called as an upper section dehydration catalyst layer and a lower section dehydration catalyst layer from top to bottom according to the position of each section in the reaction rectifying device; or a first dehydration catalyst layer, a second dehydration catalyst layer, a third dehydration catalyst layer, and so on.
Preferably, a space is provided between the separation packing layer and the dehydration catalyst layer. When the dehydration catalyst layers are provided in multiple stages, there are spaces between the dehydration catalyst layers in the respective stages.
In some embodiments of the present invention, a liquid distribution member is provided between the separation packing layer and the dehydration catalyst layer, and/or between the dehydration catalyst layers in each stage, to achieve the purpose of uniformly distributing the liquid material.
The utility model discloses an in an embodiment, dehydration catalyst layer sets up the form for the multistage, and the feed inlet setting is in the dehydration catalyst layer top of the top section, sets up the liquid phase discharge port in the below of bottom section dehydration catalyst layer.
Preferably, a heating member is installed between every two adjacent dehydration catalyst layers, and when the temperature of the mixed liquid passing through the previous dehydration catalyst layer is lowered to a temperature unsuitable for dehydration reaction, the heating member may be turned on to heat the mixed liquid. In an embodiment of the invention, the heating element is a heating coil.
Preferably, gas phase channels are distributed in the dehydration catalyst layer other than the lowermost stage. In the dehydration catalyst layer with the gas phase channel, the gas phase channel in the dehydration catalyst layer can be one or more, and the total cross-sectional area of the gas phase channel is not more than 15% of the internal cross-sectional area of the reactive distillation column, preferably 2% -10% of the internal cross-sectional area of the reactive distillation column.
In one embodiment of the present invention, the dehydration catalyst layer is provided in two stages. The feed inlet is arranged above the upper dehydration catalyst layer, and the liquid phase discharge outlet is arranged below the lower dehydration catalyst layer. Heating elements (e.g., heating coils) are installed in the space between the two dehydration catalyst layers. Gas phase channels are distributed in the upper dehydration catalyst layer, the number of the gas phase channels is one or more, the total cross-sectional area of the gas phase channels is not more than 15% of the internal cross-sectional area of the reactive distillation column, and the total cross-sectional area of the gas phase channels is preferably 2% -10% of the internal cross-sectional area of the reactive distillation column.
In another embodiment of the present invention, the dehydration catalyst layer is a section of setting form, the feed inlet is disposed below the dehydration catalyst layer, and a liquid phase discharge port is disposed between the separation packing layer and the dehydration catalyst layer.
According to the utility model, the water phase discharge port of the phase separation device is connected with a device for storing or treating waste water through a pipeline. In some embodiments of the present invention, the phase separation device is a phase separator. Preferably, the aspect ratio of the phase separator is 1.5:1 to 3:1, such as 1.6:1, 1.7:1, 1.8:1, 1.9:1, 2:1, 2.1:1, 2.2:1, 2.3:1, 2.4:1, 2.5:1, 2.6:1, 2.7:1, 2.8:1, 2.9: 1.
According to the utility model discloses, the device still includes raw materials heating device. The raw material heating device is connected with the feed inlet of the reaction rectifying device through a pipeline.
According to the utility model discloses, the device still includes raw materials storage device. The raw material storage device is connected with the raw material heating device through a pipeline.
According to the utility model discloses, the device still includes backward flow isopropyl benzene heating device. The refluxing cumene heating device is connected with an oil phase discharge port of the phase separation device through a pipeline. In one embodiment of the present invention, the refluxing cumene heating device is a refluxing heater.
According to the utility model discloses, backward flow cumene heating device's discharge gate passes through the pipeline and is connected with the backward flow material feed inlet of reaction rectification device, separation packing layer top is located to the backward flow material feed inlet.
According to the utility model discloses, raw materials heating device and backward flow cumene heating device all can adopt the various heating device that the field is commonly used, including but not limited to tube heat exchanger etc..
According to the present invention, the separation packing in the separation packing layer may use any packing known in the art and forms thereof, including but not limited to wire mesh packing, structured plate corrugated packing, random packing such as raschig rings, pall rings, etc.
According to the present invention, the dehydration catalyst is a dehydration catalyst commonly used in the art, and is selected from common solid acid catalysts, including but not limited to cation exchange resins (such as Amberlyst15), zeolites, magnesium aluminum silicate molecular sieves, or alumina, and the like, preferably gamma-A1 2 O 3 . In the specific embodiment of the present invention, gamma-A1 is adopted 2 O 3 Preferably, the bulk density is 0.3 to 1.0g/mL, for example, 0.5g/mL, 0.6g/mL, 0.7g/mL, 0.8g/mL, 0.9 g/mL. Such as spherical gamma-A1 2 O 3 。
The second aspect of the present invention is to provide a method for preparing alpha-methylstyrene by dehydrating 2-phenyl-2-propanol (DMBA) using the apparatus of the first aspect of the present invention. The method comprises the following steps: the mixed liquid of the 2-phenyl-2-propanol and the isopropylbenzene enters a reaction rectifying device, the 2-phenyl-2-propanol carries out dehydration reaction in the reaction rectifying device in the presence of a dehydration catalyst for catalyzing dehydration reaction, the isopropylbenzene and water generated by the dehydration reaction are discharged from the reaction rectifying device in a gas phase form, and the generated alpha-methyl styrene is discharged from the reaction rectifying device in a liquid phase form.
The mass fraction of 2-phenyl-2-propanol in the mixed solution of 2-phenyl-2-propanol and cumene is 10% to 80%, preferably 30% to 60%, for example, 35%, 40%, 45%, 46%, 47%, 48%, 49%, 50%, 51%, 52%, 53%, 54%, 55%, 56%, 57%, 58%, 59%, etc.
In the process, water and cumene are preferably discharged from the reactive distillation unit in the form of an azeotrope. In one embodiment of the present invention, water and cumene in vapor phase are withdrawn from the top of the reactive distillation unit.
In the method, preferably, the azeotrope is further condensed into a liquid state to form a condensate.
In the method, the dehydration reaction temperature is 120-200 ℃, preferably 130-185 ℃, such as 150-165 ℃, 150-175 ℃ and 160-185 ℃.
In the method, the dehydration reaction pressure is 0.1 to 0.4MPa, preferably 0.15 to 0.3MPa, for example, 0.15MPa, 0.2MPa, 0.21MPa, 0.22MPa, 0.23MPa, 0.24MPa, 0.25MPa, 0.26MPa, 0.27MPa, 0.28MPa, 0.29MPa, 0.3MPa or the like.
According to the present invention, preferably, while the dehydration reaction is carried out, the generated water is rectified out in the form of an azeotrope with cumene, so that the water is separated from the generated alpha-methylstyrene.
In the method, the feeding amount is controlled at the liquid hourly space velocity of 0.2-2.0h -1 Preferably 0.3-1.0h -1 . For example, 0.3h -1 ，0.4h -1 ，0.5h -1 ，0.6h -1 ，0.7h -1 ，0.8h -1 ，0.9h -1 。
In the method, preferably, the gas phase condensate is subjected to phase separation treatment to be divided into an oil phase and a water phase, the water phase is discharged to a wastewater treatment unit, and the oil phase is cumene. In one embodiment of the invention, the phase separation of the gas phase condensate is carried out using a phase separator, the residence time of the condensate in the phase separator being 5-60min, preferably 10-20 min.
In the method, the catalytic dehydration reaction is preferably completed by controlling the time of contacting the DMBA with the catalyst.
In the method, preferably, the separated cumene is further fed into the reaction rectifying device again for reflux. In one embodiment of the present invention, the refluxed cumene is heated and then enters the reactive distillation apparatus. The refluxed cumene is heated to a temperature of 100-140 deg.C, preferably 120-135 deg.C, such as 120 deg.C, 121 deg.C, 122 deg.C, 123 deg.C, 124 deg.C, 125 deg.C, 126 deg.C, 127 deg.C, 128 deg.C, 129 deg.C, 130 deg.C, 131 deg.C, 132 deg.C, 134 deg.C, 135 deg.C.
According to the utility model discloses, from last to arranging separation packing layer and dehydration catalyst layer down in proper order in the reaction rectification device.
In some embodiments of the present invention, the reactive distillation apparatus is a reactive distillation column. According to the present invention, the height-diameter ratio of the reactive distillation column is in the range of 5:1 to 10:1, for example, 5.5:1, 5.6:1, 5.7:1, 5.8:1, 5.9:1, 6:1, 6.1:1, 6.2:1, 6.3:1, 6.4:1, 6.5:1, 6.6:1, 6.7:1, 6.8:1, 6.9:1, 7:1, 7.5:1, 8:1, 8.5:1, 9:1, 9.5: 1.
In some embodiments of the present invention, the aspect ratio of the separation packing layer is 0.8:1 to 2:1, such as 0.9:1, 1:1, 1.1:1, 1.2:1, 1.3:1, 1.4:1, 1.5:1, 1.6:1, 1.7:1, 1.8:1, 1.9: 1.
In some embodiments of the present invention, the dehydration catalyst layer has a height to diameter ratio of 1.9:1 to 4:1, such as 2:1, 2.1:1, 2.2:1, 2.3:1, 2.4:1, 2.5:1, 2.6:1, 2.7:1, 2.8:1, 2.9:1, 3:1, 3.1:1, 3.2:1, 3.3:1, 3.4:1, 3.5:1, 3.6:1, 3.7:1, 3.8:1, 3.9: 1. In one embodiment of the present invention, the dehydration catalyst layer is one-stage. In another embodiment of the present invention, the dehydration catalyst layer is two or more segments. No matter the dehydration catalyst layer is one section or multiple sections, the height-diameter ratio of the total dehydration catalyst layer is 2: 1-4: 1.
In some embodiments of the present invention, a liquid distribution member is provided between the separation packing layer and the dehydration catalyst layer, and/or between the dehydration catalyst layers in each stage, to achieve the purpose of uniformly distributing the liquid material.
In one embodiment of the present invention, the mixed liquid of 2-phenyl-2-propanol and cumene enters the apparatus from the middle part of the reactive distillation apparatus and flows downwards in the apparatus through a dehydration catalyst layer arranged below the feeding position; discharging the generated alpha-methyl styrene from the lower part of the reaction rectification device in a liquid phase form; the cumene and the generated water pass upwards through a separation packing layer and are discharged from the top of the reaction rectifying device in a gas phase form.
Preferably, the dehydration catalyst layer is two or more layers that are spaced apart.
Preferably, the mixed liquid is heated when the temperature of the mixed liquid is lowered to a temperature unsuitable for the dehydration reaction after flowing down through the dehydration catalyst layer. The utility model discloses an in the embodiment, install the heater block between per two adjacent dehydration catalyst layers, when the temperature of mixed liquid after the last section dehydration catalyst layer of flowing through reduces to the temperature that is not suitable for the dehydration reaction, can open the heater block, heat mixed liquid. In an embodiment of the invention, the heating element is a heating coil.
Preferably, a gas phase passage is provided in the dehydration catalyst layer other than the lowermost stage so as to allow cumene and water in the gas phase to rise. In the catalyst layer with the gas phase channel, the gas phase channel in the dehydration catalyst layer can be one or more, and the total cross-sectional area of the gas phase channel is not more than 15% of the internal cross-sectional area of the reactive distillation column, preferably 2% -10% of the internal cross-sectional area of the reactive distillation column.
In one embodiment of the present invention, the mixed liquid of 2-phenyl-2-propanol and cumene enters the apparatus from the lower part of the reactive distillation apparatus, and flows upwards through the dehydration catalyst layer arranged above the feeding position in the apparatus; discharging the generated alpha-methyl styrene from the middle part of the reaction rectifying device in a liquid phase form; the cumene and the generated water pass upwards through a separation packing layer and are discharged from the top of the reaction rectifying device in a gas phase form.
Preferably, the dehydration catalyst layer is one-stage.
In one embodiment of the present invention, the refluxing cumene enters the reactive distillation device from the top of the separation packing layer.
In one embodiment of the present invention, the heated aqueous cumene is used to raise the temperature in the reactive distillation apparatus to the dehydration reaction temperature prior to feeding the mixed liquid of 2-phenyl-2-propanol and cumene. The water content of the hydrous cumene is 5 to 15%, for example, 6%, 7%, 8%, 9%, 10%, 11%, 12%, 13%, 14%.
The utility model discloses following beneficial effect has:
1. by adopting the reaction rectification device with dehydration reaction and dehydration rectification, the function of removing water generated by reaction in real time while carrying out catalytic dehydration reaction on DMBA in one device can be realized. The inventors have found that controlling the water content in the reaction system to be always kept at a low level allows the dehydration reaction to proceed continuously and rapidly. Correspondingly, the industrial practice of dehydration after reaction leads to low efficiency and long time consumption of dehydration reaction.
2. The utility model discloses a dehydration mode adopts the mode of azeotropic distillation, can improve dehydration efficiency by a wide margin, reduces the energy consumption, reduces the equipment investment.
3. The process has mild reaction conditions, the dehydration conversion rate of DMBA reaches more than 95 percent, can realize continuous operation, is easy for industrial amplification and has great commercial value.
In the present invention, the height-diameter ratio refers to the length ratio of the height and diameter of the corresponding structure or device. Aspect ratio refers to the ratio of the length to the diameter of the corresponding structure or device.
In the present invention, the pressure is gauge pressure unless otherwise specified.
Drawings
Fig. 1 is a schematic diagram of an embodiment of the apparatus and process of the present invention, wherein a: a material tank, B: a feed pump, C: raw material heater, D: reactive rectification column, D1: separation packing layer, D2: one-stage dehydration catalyst layer, D3: two-stage dehydration catalyst layer, D4: gas phase channel, D5: heating coil, E: a condenser, F: phase separator, G: reflux pump, H: reflux heater
Fig. 2 is a schematic diagram of another embodiment of the apparatus and process of the present invention, wherein a: a material tank, B: a feed pump, C: raw material heater, D: reactive rectification column, D1: separation packing layer, D4: dehydration catalyst layer, E: a condenser, F: phase separator, G: reflux pump, H: reflux heater
Detailed Description
Fig. 1 illustrates one embodiment of the apparatus and process of the present invention. In the reactive distillation column D, two dehydration catalyst layers are arranged, namely a first dehydration catalyst layer D2 and a second dehydration catalyst layer D3, and D3 is arranged below D2. A separation filler layer D1 is provided above the first stage dehydration catalyst layer D2. The feed inlet was placed below D1, the vapor phase discharge outlet was placed above D1, and the liquid phase discharge outlet was placed below D3. A gas phase channel D4 is arranged in D2, and a heating coil D5 is arranged between D2 and D3.
The gas phase discharge port of the reactive distillation column D is connected with a condenser E through a pipeline, the E is connected with a phase separator F through a pipeline, the oil phase discharge port of the F is connected with a reflux pump G through a pipeline, and the G is connected with a reflux heater H through a pipeline. H is connected with a reflux feed inlet positioned above D1 through a pipeline.
The charging bucket A is a raw material storage device and is used for storing raw materials for reaction, the A is connected with a feed pump B through a pipeline, the B is connected with a raw material heater C through a pipeline, and the C is connected with a feed inlet of a reaction rectifying tower D through a pipeline.
The mixed liquid of 2-phenyl-2-propanol and cumene (hereinafter also referred to as "reaction liquid") is stored in a charging bucket A, sent to a raw material heater C through a feeding pump B, heated to a temperature suitable for reaction, and sent to a reaction rectifying tower D through a feeding hole. After passing through the primary dehydration catalyst layer D2, the reaction solution was appropriately heated by the heating coil D5 and then passed through the secondary dehydration catalyst layer D3.
And after a reaction product passes through a separation filler layer D1, an azeotrope (gas phase) of water and cumene is discharged from a gas phase discharge port at the top of the D and is sent to a condenser E, the condensed product is sent to a phase separator F, the oil-phase cumene and the water phase are separated in the phase separator F, the water phase is discharged to a wastewater treatment device, the oil phase is sent to a reflux heater H through a reflux pump G, and the heated product is refluxed and enters a reaction rectifying tower D.
The liquid phase in the reaction product is discharged from the bottom of the reactive distillation column, and is a mixture of cumene and AMS.
In the embodiment of the present invention, a liquid distributor may be further installed between D1 and D2, and between D2 and D3.
Fig. 2 illustrates another embodiment of the apparatus and process of the present invention. In the reactive distillation column D, a dehydration catalyst layer D4 is provided in a one-stage form, and a separation filler layer D1 is provided above D4. The feed inlet was placed below D4, the vapor phase discharge port was placed above D1, and the liquid phase discharge port was placed above D4.
The gas phase discharge port of the reactive distillation column D is connected with a condenser E through a pipeline, the E is connected with a phase separator F through a pipeline, the oil phase discharge port of the F is connected with a reflux pump G through a pipeline, and the G is connected with a reflux heater H through a pipeline.
The charging bucket A is used for storing raw materials for reaction, the A is connected with a feed pump B through a pipeline, the B is connected with a raw material heater C through a pipeline, and the C is connected with a feed inlet of a reaction rectifying tower D through a pipeline.
The mixed liquid of 2-phenyl-2-propanol and cumene (hereinafter also referred to as "reaction liquid") is stored in a charging bucket A, sent to a raw material heater C through a feeding pump B, heated to a temperature suitable for reaction, and sent to a reaction rectifying tower D through a feeding hole. The reaction solution was dehydrated through the dehydration catalyst layer D4.
And after a reaction product passes through a separation packing layer D1, discharging an azeotrope of water and cumene from a gas phase discharge port at the top of the D, sending the azeotrope to a condenser E, condensing the azeotrope, sending the condensed azeotrope to a phase separator F, separating the condensed azeotrope into oil-phase cumene and a water phase in the phase separator F, discharging the water phase to a wastewater treatment device, sending the oil phase to a reflux heater H through a reflux pump G, heating the oil phase, and refluxing the oil phase to enter a reaction rectifying tower.
The liquid phase in the reaction product was withdrawn from above D4 as a mixture of cumene and AMS.
In the specific embodiment of the present invention, a liquid distributor may be further installed between D1 and D4.
The expected effect can be achieved by both the apparatus and the process shown in fig. 1 and fig. 2, wherein the apparatus and the process represented by fig. 2 have stronger practicability and simpler equipment than those of fig. 1.
Example 1:
a reaction apparatus was set up in the apparatus and process flow sequence of FIG. 1, wherein: the diameter of the reactive distillation column D is 0.5m, the total height is 3.3m, the dehydration catalyst layer in the reactive distillation column is divided into two sections, namely a first section dehydration catalyst layer D2 and a second section dehydration catalyst layer D3, each section is 0.5m, and a DN100 gas phase channel is reserved in the first section dehydration catalyst layer D2. The separating filler layer D1 above D2 in the upper part of the reactive distillation column was packed with MELPACK 252 packing of 0.6m height. Liquid distributors are arranged in the reactive distillation column between D1 and D2 and between D2 and D3, and the design of the liquid distributors is the same as that of a conventional column. The adopted catalyst is spherical, and the main component is gamma-A1 2 O 3 The diameter is 4-8 mm, and the bulk density is about 0.7 g/mL. The raw material heater C and the reflux heater H are bothIs a tubular heat exchanger, and the heat exchange area of C is 0.66m 2 H heat exchange area 0.52m 2 . The heating coil D5 at the middle part of the reactive distillation tower is a coil with the diameter DN20 and the heat exchange area is 0.26m 2 . Phase separator F volume 15L, aspect ratio 2: 1; the feed pump B and the reflux pump G are metering pumps, and the flow range is 50-200L/h; bucket A has a volume of 200L.
Safety check of the whole device 2 After purging and replacement, firstly cumene containing 10 percent of moisture is added into the system, and the temperature is raised through a raw material heat exchanger C and a reflux heater H, so that the temperature in the reactive distillation tower is raised to 160-165 ℃, and the pressure is controlled at 0.2 MPa. Then according to the liquid hourly space velocity of 0.5h -1 To the reactive distillation column, a cumene solution of 50% DMBA (hereinafter also referred to as "reaction liquid") was added. The feed temperature was controlled to 160 ℃ and the reflux temperature to 125 ℃ by controlling the flow rate of steam. After the reaction liquid passes through the first-stage dehydration catalyst layer D2, the temperature is reduced from 160 ℃ to about 150 ℃, the reaction liquid is heated to 158-160 ℃ through the heating coil D5 and enters the second-stage dehydration catalyst layer D3, and the discharge temperature of the tower bottom is 153 ℃. And sampling from the bottom of the tower to analyze the content of DMBA. The change in concentration of DMBA, AMS and impurities was determined by gas chromatography. The conversion was calculated from the change in the area of the peak of DMBA. The selectivity of AMS was calculated from the ratio of the peak area of the product AMS to the sum of the peak areas of the product AMS and the impurity. The conversion rate of DMBA is 98.2 percent through measurement and analysis. The AMS selectivity was greater than 99.6%.
Example 2:
the feed rate was adjusted so that the liquid hourly space velocity was 0.4h -1 Otherwise, samples were taken from the bottom of the column under the same conditions as in example 1 for the DMBA content. The analysis revealed that the conversion of DMBA was 99.1%. The AMS selectivity was greater than 99.6%.
Example 3:
the feed flow is adjusted to ensure that the liquid hourly space velocity is 0.6h -1 Otherwise, samples were taken from the bottom of the column under the same conditions as in example 1 for the DMBA content. The analysis revealed that the conversion of DMBA was 97.3%. The AMS selectivity was greater than 99.6%.
Example 4:
the feed flow is adjusted to ensure that the liquid hourly space velocity is 0.8h -1 Otherwise, samples were taken from the bottom of the column under the same conditions as in example 1 for the DMBA content. The analysis revealed that the conversion of DMBA was 92.8%. The AMS selectivity was greater than 99.6%.
Example 5:
the apparatus and conditions of example 1 were as described except that the temperature in the reactive distillation column was raised to 185 ℃ by the feed heat exchanger C and the reflux heater H, and the pressure was controlled to 0.25 MPa. Then according to the liquid hourly space velocity of 0.6h -1 Adding 50 percent of DMBA cumene solution into the reaction rectifying tower. The feeding temperature is controlled to be 180 ℃ by controlling the flow rate of steam, and the reflux temperature is controlled to be 130 ℃. After the reaction liquid passes through a section of dehydration catalyst layer D2, the temperature is reduced from 180 ℃ to about 169 ℃ without opening a heating coil D5, and the discharging temperature of the tower bottom is 163 ℃. And sampling from the bottom of the tower to analyze the content of DMBA. The analysis revealed that the conversion of DMBA was 99.3%. The AMS selectivity was greater than 99.4%.
Example 6:
set up the reaction apparatus according to the apparatus and process flow sequence of figure 2, wherein: the diameter of the reactive distillation column D is 0.5m, the total height is 3.3m, and the height of a dehydration catalyst layer D4 in the reactive distillation column is 1.2 m. The separating filler layer D1 above D4 in the upper part of the reactive distillation column was packed with MELPACK 252 packing of 0.6m height. A liquid distributor is arranged between D1 and D4 in the reactive distillation column, and the design of the liquid distributor is the same as that of a conventional column. The adopted catalyst is spherical, and the main component is gamma-A1 2 O 3 The diameter is 4-8 mm, and the bulk density is about 0.7 g/mL. The raw material heater C and the reflux heater H are both tube-type heat exchangers, and the heat exchange area of C is 0.66m 2 H heat exchange area is 0.52m 2 . Phase separator F volume 15L, aspect ratio 2: 1; the feed pump B and the reflux pump G are metering pumps, and the flow range is 50-200L/h; bucket A has a volume of 200L.
Safety check of the whole device 2 After purging and replacement, cumene containing 10 percent of moisture is added into the system, and the temperature is raised through a raw material heat exchanger C and a reflux heater H, so that the temperature in the reactive distillation column reaches 180 ℃ and 185 ℃, and the pressure is controlled at 0.25 MPa. Then according to the liquid hourly space velocity of 0.6h -1 Adding 50 percent of DMBA cumene solution into the reaction rectifying tower at the speed of (1). By controlling steamThe flow control of (3) is that the feeding temperature is 180 ℃, and the reflux temperature is 130 ℃. After the reaction solution passed through the dehydration catalyst layer D4, the temperature was decreased from 180 ℃ to about 162 ℃. And (3) extracting a product material from the upper part of the dehydration catalyst layer D4 through the liquid level control in the tower, and sampling to analyze the content of DMBA. The analysis revealed that the conversion of DMBA was 99.6%. The AMS selectivity was greater than 99.6%.
Example 7
The apparatus and conditions of example 6 were as described except that the temperature in the reactive distillation column was raised to 175 ℃ by the feed heat exchanger C and the reflux heater H, and the pressure was controlled to 0.2 MPa. Then according to the liquid hourly space velocity of 0.6h -1 Adding 50 percent of DMBA cumene solution into the reaction rectifying tower at the speed of (1). The feeding temperature is controlled to be 170 ℃ by controlling the flow of steam, and the reflux temperature is controlled to be 125 ℃. After the reaction liquid passes through the dehydration catalyst D4, the temperature is reduced from 170 ℃ to about 153 ℃. And (3) extracting a product material from the upper part of the dehydration catalyst layer D4 through the liquid level control in the tower, and sampling to analyze the content of DMBA. The analysis revealed that the conversion of DMBA was 98.5%. The AMS selectivity was greater than 99.5%.
Example 8
The apparatus and conditions of example 7 were followed except that the height of the separation packing layer was reduced from 0.6m to 0.4 m. And (3) after the dehydration reaction and separation, extracting a product material from the upper part of the dehydration catalyst layer D4, and sampling and analyzing the content of DMBA to obtain: the conversion of DMBA was 98.6% and the AMS selectivity was greater than 99.5%.
Example 9
The apparatus and conditions of example 1 were followed except that the height of the separation packing layer was increased from 0.6m to 1m, and the reaction conditions were kept the same as those of example 1. After the dehydration reaction and separation, the material discharged from the tower bottom is sampled and analyzed to obtain the DMBA content: the conversion of DMBA was 98.3% and the AMS selectivity was greater than 99.5%.
Example 10
The equipment set-up and conditions of example 6 were followed except that the height of the packing layer was decreased from 0.6m to 0.4m and the height of the dehydration catalyst layer D4 was increased from 1.2m to 1.8m, and the reaction conditions were kept the same as in example 6. And (3) after the dehydration reaction and separation, extracting a product material from the upper part of the catalyst layer D4, and sampling and analyzing the content of DMBA to obtain: the conversion of DMBA was 99.7% and the AMS selectivity was greater than 99.5%.
The embodiments of the present invention have been described above. However, the present invention is not limited to the above embodiment. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (15)
1. A production device for preparing alpha-methyl styrene by dehydrating 2-phenyl-2-propanol is characterized by comprising a reaction rectification device, a condensation device and a phase separation device; a dehydration catalyst layer is arranged in the reaction rectification device, and a separation packing layer is arranged above the dehydration catalyst layer; a feed inlet of the reaction rectifying device is arranged below the separation packing layer, and a gas phase discharge outlet is arranged above the separation packing layer of the reaction rectifying device; the condensing device is connected with a gas-phase discharge port of the reaction rectifying device through a pipeline; the phase separation device is connected with the condensing device through a pipeline;
the reactive distillation device is a reactive distillation tower, and the height-diameter ratio of the reactive distillation tower is 5: 1-10: 1; the height-diameter ratio of the separation packing layer is 0.8: 1-2: 1; the height-diameter ratio of the dehydration catalyst layer is 2: 1-4: 1.
2. The production device of claim 1, wherein the dehydration catalyst layer is a segment.
3. The production device according to claim 1, wherein the dehydration catalyst layer is two or more pieces.
4. The production apparatus according to claim 3, wherein the feed port is provided above the uppermost dehydration catalyst layer, and a liquid phase discharge port is provided below the lowermost dehydration catalyst layer.
5. The production apparatus according to claim 3, wherein a heating member is provided between each two adjacent dehydration catalyst layers.
6. The production apparatus according to claim 3, wherein gas phase passages are distributed in the dehydration catalyst layer other than the lowermost layer, and in the dehydration catalyst layer having the gas phase passages, the gas phase passages in the dehydration catalyst layer are one or more, and the total cross-sectional area of the gas phase passages is not more than 15% of the internal cross-sectional area of the reactive distillation column.
7. The production apparatus as claimed in claim 6, wherein the total cross-sectional area of the gas phase channels is 2 to 10% of the internal cross-sectional area of the reactive distillation column.
8. The production device according to claim 3, wherein the dehydration catalyst layer is provided in two stages; the feed inlet is arranged above the upper-section dehydration catalyst layer, and the liquid-phase discharge outlet is arranged below the lower-section dehydration catalyst layer; a heating component is arranged between the two sections of dehydration catalyst layers; gas phase channels are distributed in the upper dehydration catalyst layer, the number of the gas phase channels is one or more, and the total cross-sectional area of the gas phase channels does not exceed 15 percent of the internal cross-sectional area of the reactive distillation column.
9. The production apparatus as claimed in claim 8, wherein the total cross-sectional area of the gas phase passage is 2 to 10% of the internal cross-sectional area of the reactive distillation column.
10. The production apparatus according to claim 2, wherein the dehydration catalyst layer is provided in a single stage, the feed port is provided below the dehydration catalyst layer, and the discharge port for the liquid phase is provided between the separation packing layer and the dehydration catalyst layer.
11. The production plant according to any one of claims 1 to 10, further comprising a refluxing cumene heating unit connected to the oil phase discharge port of the phase separation unit through a pipeline; the discharge hole of the reflux cumene heating device is connected with the reflux material feed inlet of the reaction rectifying device through a pipeline, and the reflux material feed inlet is arranged above the separation packing layer.
12. The production apparatus as claimed in any one of claims 1 to 10, wherein the aqueous phase discharge port of the phase separation apparatus is connected to a waste water storage or treatment apparatus via a pipeline.
13. The production apparatus according to any one of claims 1 to 10, wherein a liquid distribution member is provided between the separation packing layer and the dehydration catalyst layer, and/or between the respective dehydration catalyst layers.
14. The production apparatus according to any one of claims 1 to 10, further comprising a raw material heating apparatus connected to the feed port of the reactive distillation apparatus through a pipeline.
15. The production apparatus according to any one of claims 1 to 10, further comprising a raw material storage device connected to the raw material heating device through a pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221520756.5U CN217430859U (en) | 2022-06-16 | 2022-06-16 | Device for preparing alpha-methylstyrene by dehydrating 2-phenyl-2-propanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221520756.5U CN217430859U (en) | 2022-06-16 | 2022-06-16 | Device for preparing alpha-methylstyrene by dehydrating 2-phenyl-2-propanol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN217430859U true CN217430859U (en) | 2022-09-16 |
Family
ID=83224021
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202221520756.5U Active CN217430859U (en) | 2022-06-16 | 2022-06-16 | Device for preparing alpha-methylstyrene by dehydrating 2-phenyl-2-propanol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN217430859U (en) |
-
2022
- 2022-06-16 CN CN202221520756.5U patent/CN217430859U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR101104106B1 (en) | Process for preparing isobutene from tert-butanol | |
| CN106957221A (en) | The device and method of polymethoxy dimethyl ether is produced in a kind of methanol oxidation | |
| CN1830934A (en) | Method for producing dimethyl ether using methanol as raw material | |
| CN110467595A (en) | A kind of no sulfuric acid process metaformaldehyde synthesizer and its synthesis route | |
| CN111153782A (en) | Method for preparing high-carbon aldehyde by hydroformylation of high-carbon olefin | |
| CN108002995A (en) | A kind of method and its equipment of acetone two-step method synthesizing methyl isobutyl ketone | |
| CN1291968C (en) | Improved production of aminomethane | |
| CN217430859U (en) | Device for preparing alpha-methylstyrene by dehydrating 2-phenyl-2-propanol | |
| CN109748791B (en) | Energy-saving method for producing dimethyl adipate | |
| CN109748790B (en) | Method for producing dimethyl adipate | |
| CN101205163A (en) | Preparation method of cyclohexane | |
| CN114874066B (en) | Method and device for preparing alpha-methylstyrene by dehydrating 2-phenyl-2-propanol | |
| CN106588828A (en) | Separation and purification method of THF (tetrahydrofuran) distillation waste liquid | |
| CN102276452B (en) | Production equipment for sec-butyl acetate | |
| CN100366597C (en) | Process for preparing dimethyl ether | |
| CN109134217B (en) | Oxidation device and oxidation process improvement method in cyclohexanone production process by cyclohexane oxidation method | |
| CN101898930A (en) | Device for producing cyclohexane by adding hydrogen in benzene and synthesis process | |
| CN114984866B (en) | System and method for preparing dimethyl maleate | |
| CN103965005B (en) | The acid stripping method of butylene oxidation-dehydrogenation product | |
| CN109232516B (en) | Multifunctional membrane synthesis trioxymethylene and DMM 3-8 Apparatus and method of (2) | |
| CN109180636B (en) | Device and method for synthesizing trioxymethylene by coupling extraction and catalysis technology | |
| CN210261603U (en) | N-methyldiethanolamine production device | |
| CN1156418C (en) | External coupler of rectifying reaction for preparing cyclohexane by catalyst hydrogenation of benzene and its synthesizing process | |
| CN114247386A (en) | Evaporative isothermal hydrogenation reaction method and evaporative isothermal reaction system | |
| US9738575B2 (en) | Apparatus for producing ethylene and a producing method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: Preparation of 2-phenyl-2-propanol by dehydration a- Device for methylstyrene Granted publication date: 20220916 Pledgee: Shanghai Rural Commercial Bank Co.,Ltd. Shanghai pilot Free Trade Zone Lingang xinpian District sub branch Pledgor: Shanghai Youcheng Gongyi Technology Co.,Ltd. Registration number: Y2024310000119 |