CN220990751U - Cyclohexane oxidation decomposition liquid refining device - Google Patents
Cyclohexane oxidation decomposition liquid refining device Download PDFInfo
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- CN220990751U CN220990751U CN202322423556.9U CN202322423556U CN220990751U CN 220990751 U CN220990751 U CN 220990751U CN 202322423556 U CN202322423556 U CN 202322423556U CN 220990751 U CN220990751 U CN 220990751U
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- separator
- connecting pipe
- pipe
- washing
- liquid
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- 239000007788 liquid Substances 0.000 title claims abstract description 66
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 230000003647 oxidation Effects 0.000 title claims abstract description 25
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 25
- 238000000354 decomposition reaction Methods 0.000 title claims abstract description 23
- 238000007670 refining Methods 0.000 title claims abstract description 19
- 238000005406 washing Methods 0.000 claims abstract description 44
- 238000007127 saponification reaction Methods 0.000 claims abstract description 21
- 239000002699 waste material Substances 0.000 claims description 34
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 34
- 238000004581 coalescence Methods 0.000 claims description 12
- 238000006864 oxidative decomposition reaction Methods 0.000 claims description 11
- 238000004821 distillation Methods 0.000 claims description 8
- 238000002347 injection Methods 0.000 claims description 8
- 239000007924 injection Substances 0.000 claims description 8
- 238000011144 upstream manufacturing Methods 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 5
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 abstract description 14
- 230000009286 beneficial effect Effects 0.000 abstract description 4
- 238000000034 method Methods 0.000 description 19
- 238000000926 separation method Methods 0.000 description 18
- 239000012074 organic phase Substances 0.000 description 13
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 12
- 150000001335 aliphatic alkanes Chemical class 0.000 description 7
- HGCIXCUEYOPUTN-UHFFFAOYSA-N cyclohexene Chemical compound C1CCC=CC1 HGCIXCUEYOPUTN-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 239000003513 alkali Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- WNLRTRBMVRJNCN-UHFFFAOYSA-N adipic acid Chemical compound OC(=O)CCCCC(O)=O WNLRTRBMVRJNCN-UHFFFAOYSA-N 0.000 description 2
- 230000002411 adverse Effects 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- JBKVHLHDHHXQEQ-UHFFFAOYSA-N epsilon-caprolactam Chemical compound O=C1CCCCCN1 JBKVHLHDHHXQEQ-UHFFFAOYSA-N 0.000 description 2
- 230000036571 hydration Effects 0.000 description 2
- 238000006703 hydration reaction Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 159000000000 sodium salts Chemical class 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 239000001361 adipic acid Substances 0.000 description 1
- 235000011037 adipic acid Nutrition 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- KGBXLFKZBHKPEV-UHFFFAOYSA-N boric acid Chemical compound OB(O)O KGBXLFKZBHKPEV-UHFFFAOYSA-N 0.000 description 1
- 239000004327 boric acid Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- FWFSEYBSWVRWGL-UHFFFAOYSA-N cyclohex-2-enone Chemical compound O=C1CCCC=C1 FWFSEYBSWVRWGL-UHFFFAOYSA-N 0.000 description 1
- 125000000113 cyclohexyl group Chemical group [H]C1([H])C([H])([H])C([H])([H])C([H])(*)C([H])([H])C1([H])[H] 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000032050 esterification Effects 0.000 description 1
- 238000005886 esterification reaction Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- -1 organic acid sodium salt Chemical class 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- PAPBSGBWRJIAAV-UHFFFAOYSA-N ε-Caprolactone Chemical compound O=C1CCCCCO1 PAPBSGBWRJIAAV-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present utility model relates to a cyclohexane oxidation decomposition liquid refining device. The cyclohexane oxidation decomposition liquid refining device comprises a saponification separator, a first mixer, a second mixer, a first washing separator, a second washing separator, a cyclone separator and a coalescing separator, wherein a liquid outlet of the saponification separator is connected with a liquid inlet of the first washing separator through a first connecting pipe, the first mixer is arranged on the first connecting pipe, a liquid outlet of the first washing separator is connected with a liquid inlet of the second washing separator through a second connecting pipe, the second mixer is arranged on the second connecting pipe, a liquid outlet of the second washing separator is connected with a liquid inlet of the cyclone separator through a third connecting pipe, and a liquid outlet of the cyclone separator is connected with a liquid inlet of the coalescing separator through a fourth connecting pipe. Compared with the prior art, the cyclohexane oxidation decomposition liquid refining device has high purity, and is beneficial to improving the purity of the tail cyclohexanone product.
Description
Technical Field
The utility model belongs to the technical field of cyclohexane oxidation liquid refining, and particularly relates to a cyclohexane oxidation decomposition liquid refining device.
Background
Cyclohexanone is an important monomer for the production of caprolactam, adipic acid and caprolactone, and is a solvent for various paint products. As an important organic chemical product, the application is becoming wider and wider, and the demand is expanding. The industrial production process of cyclohexanone mainly comprises a phenol hydrogenation method, a cyclohexane oxidation method, a boric acid esterification method and a cyclohexene hydration method. Among them, cyclohexene hydration method has a market ratio increasing year by virtue of a higher carbon resource utilization rate, but the price of an expensive catalyst has been limited. From the domestic cyclohexanone production process, the cyclohexane oxidation method is mature in technology, stable in raw material source and still the most extensive process route for producing cyclohexanone at present, in particular to a cyclohexane non-catalytic oxidation method. During the decomposition of cyclohexane oxidation process, a large amount of waste lye (about 40% of solid mass fraction, mainly sodium carbonate, organic acid sodium salt and a small amount of free sodium hydroxide) is generated due to the addition of sodium hydroxide aqueous solution. If the waste alkali in the oxidative decomposition liquid is not thoroughly removed and is brought into the alkane distillation tower, the reboiler of the alkane distillation tower is coked, the material consumption is increased, and the driving period of the alkane distillation tower is greatly shortened. Therefore, it is necessary to provide a device for purifying a cyclohexane oxidation decomposition solution.
Disclosure of utility model
In order to achieve the above object, the present utility model provides a cyclohexane oxidation decomposition liquid refining apparatus.
The technical scheme of the cyclohexane oxidation decomposition liquid refining device is as follows:
the utility model provides a cyclohexane oxidation decomposition liquid refining plant, includes saponification separator, first blender, second blender, one wash the separator, two wash the separator, cyclone and coalescence separator, the liquid outlet of saponification separator pass through first connecting pipe with the inlet of one wash the separator is connected, first blender sets up on the first connecting pipe, the liquid outlet of one wash the separator pass through the second connecting pipe with the inlet of two wash the separator is connected, the second blender sets up on the second connecting pipe, the liquid outlet of two wash the separator pass through the third connecting pipe with the inlet of cyclone is connected, the liquid outlet of cyclone pass through the fourth connecting pipe with the inlet of coalescence separator is connected.
Further, a liquid inlet pipe for the cyclohexane oxidative decomposition liquid to enter is arranged on the saponification separator, and a liquid outlet pipe for feeding liquid to the alkane distillation tower is arranged on the coalescence separator.
Further, a first water injection pipe positioned at the upstream of the first mixer is arranged on the first connecting pipe, and a second water injection pipe positioned at the upstream of the second mixer is arranged on the second connecting pipe.
Further, the second washing separator is connected with the first mixer through a fifth connecting pipe.
Further, the cyclohexane oxidation decomposition liquid refining device comprises a sixth connecting pipe, the waste discharge port of the saponification separator is connected with the sixth connecting pipe through a first waste discharge pipe, the waste discharge port of the one-wash separator is connected with the sixth connecting pipe through a second waste discharge pipe, the waste discharge port of the cyclone separator is connected with the sixth connecting pipe through a third waste discharge pipe, the waste discharge port of the coalescence separator is connected with the sixth connecting pipe through a fourth waste discharge pipe, one end of the sixth connecting pipe is connected with the decomposition kettle or the evaporation kettle, and the other end of the sixth connecting pipe is connected with the outer discharge pipe.
The utility model provides a cyclohexane oxidation decomposition liquid refining device, which has the beneficial effects that compared with the prior art:
When the cyclohexane oxidative decomposition liquid refining device is used, cyclohexane oxidative decomposition liquid firstly enters a saponification separator for primary alkali-water separation. The upper organic phase is fully mixed with the process water after exiting the saponification separator through a first mixer, and then enters a washing separator to complete oil-water separation. The organic phase at the upper layer of the first-washing separator is fully mixed with the process water again through the second mixer after exiting the separator, and then enters the second-washing separator to complete oil-water separation. The organic phase from the second washing separator enters the cyclone separator, and after mixed mass transfer and cyclone separation, the organic phase enters the coalescence separator to perform filter element coalescence separation, so that alkaline water in the material is further reduced, the organic phase enters the alkane distillation tower, and the bottom waste alkali solution returns to the decomposing kettle or is discharged. In the saponification alkaline washing separation process, if the water consumption of the water washing process is increased, the dissolution of sodium salt can be promoted, and the entrainment of Na+ in the organic phase can be greatly reduced. However, increasing the water content only to improve the separation effect brings adverse effects such as increased process water consumption, large amount of waste lye generation, large amount of steam consumption in the evaporation concentration process, and increased operation cost. Therefore, the water separated by the secondary water-washing separator is totally returned to the mixer in front of the primary water-washing separator and is re-injected into the primary water-washing separator, and the water quantity of the water-washing separator is increased under the condition of not increasing the process water loss by reasonably arranging the circulating water-washing separation step, so that the separation efficiency of Na+ in the organic phase is greatly improved. Compared with the prior art, the cyclohexane oxidation decomposition liquid refining device has high purity, and is beneficial to improving the purity of the tail cyclohexanone product.
Drawings
FIG. 1 is a schematic view of a device for purifying a cyclohexane oxidation decomposition solution according to the present utility model.
In the figure: 1. a saponification separator; 2. a wash separator; 3. a first mixer; 4. a second washing separator; 5. a second mixer; 6. a cyclone separator; 7. a coalescing separator; 8. a liquid inlet pipe; 9. a liquid outlet pipe; 10. a first connection pipe; 11. a second connection pipe; 12. a third connection pipe; 13. a fourth connection pipe; 14. a first water injection pipe; 15. a second water injection pipe; 16. a fifth connection pipe; 17. a sixth connection pipe; 18. a first waste pipe; 19. a second waste pipe; 20. a third waste pipe; 21. and a fourth waste discharge pipe.
Detailed Description
The utility model is described in further detail below with reference to the attached drawings and detailed description:
As shown in figure 1, the specific embodiment of the cyclohexane oxidation decomposition liquid refining device comprises a saponification separator 1, a first mixer 3, a second mixer 5, a first washing separator 2, a second washing separator 4, a cyclone separator 6 and a coalescing separator 7, wherein a liquid outlet of the saponification separator 1 is connected with a liquid inlet of the first washing separator 2 through a first connecting pipe 10, the first mixer 3 is arranged on the first connecting pipe 10, a liquid outlet of the first washing separator 2 is connected with a liquid inlet of the second washing separator 4 through a second connecting pipe 11, the second mixer 5 is arranged on the second connecting pipe 11, a liquid outlet of the second washing separator 4 is connected with a liquid inlet of the cyclone separator 6 through a third connecting pipe 12, and a liquid outlet of the cyclone separator 6 is connected with a liquid inlet of the coalescing separator 7 through a fourth connecting pipe 13.
The saponification separator 1 is provided with a liquid inlet pipe 8 for the cyclohexane oxidative decomposition liquid to enter, and the coalescence separator 7 is provided with a liquid outlet pipe 9 for the liquid to enter the alkane distillation tower. The first connecting pipe 10 is provided with a first water injection pipe 14 positioned upstream of the first mixer 3, and the second connecting pipe 11 is provided with a second water injection pipe 15 positioned upstream of the second mixer 5. The two-wash separator 4 is connected to the first mixer 3 via a fifth connection pipe 16.
The cyclohexane oxidation decomposition liquid refining device comprises a sixth connecting pipe 17, wherein the waste discharge port of the saponification separator 1 is connected with the sixth connecting pipe 17 through a first waste discharge pipe 18, the waste discharge port of the first washing separator 2 is connected with the sixth connecting pipe 17 through a second waste discharge pipe 19, the waste discharge port of the cyclone separator 6 is connected with the sixth connecting pipe 17 through a third waste discharge pipe 20, the waste discharge port of the coalescing separator 7 is connected with the sixth connecting pipe 17 through a fourth waste discharge pipe 21, one end of the sixth connecting pipe 17 is connected with a decomposition kettle or an evaporation kettle, and the other end of the sixth connecting pipe 17 is connected with an external discharge pipe.
When the cyclohexane oxidative decomposition liquid refining device is used, cyclohexane oxidative decomposition liquid firstly enters a saponification separator 1 for primary alkali water separation. The upper organic phase is discharged from the saponification separator 1, fully mixed with the process water through the first mixer 3, then enters the primary washing separator 2 and is subjected to oil-water separation. The organic phase at the upper layer of the first-washing separator 2 is fully mixed with the process water again through the second mixer 5 after exiting the separator, and then enters the second-washing separator 4 to complete oil-water separation. The organic phase from the second washing separator 4 enters the cyclone separator 6, and after mixed mass transfer and cyclone separation, enters the coalescence separator 7 to perform filter element coalescence separation, so that the alkaline water in the material is further reduced, then the organic phase enters the alkane distillation tower, and the bottom waste alkaline liquid returns to the decomposing kettle or is discharged. In the saponification alkaline washing separation process, if the water consumption of the water washing process is increased, the dissolution of sodium salt can be promoted, and the entrainment of Na+ in the organic phase can be greatly reduced. However, increasing the water content only to improve the separation effect brings adverse effects such as increased process water consumption, large amount of waste lye generation, large amount of steam consumption in the evaporation concentration process, and increased operation cost. Therefore, the water separated by the secondary water-washing separator is totally returned to the mixer in front of the primary water-washing separator and is re-injected into the primary water-washing separator, and the water quantity of the water-washing separator is increased under the condition of not increasing the process water loss by reasonably arranging the circulating water-washing separation step, so that the separation efficiency of Na+ in the organic phase is greatly improved. Compared with the prior art, the cyclohexane oxidation decomposition liquid refining device has high purity, and is beneficial to improving the purity of the tail cyclohexanone product.
The foregoing is only illustrative of the present utility model and is not to be construed as limiting thereof, but rather as various modifications, equivalent arrangements, improvements, etc., within the spirit and principles of the present utility model.
Claims (5)
1. The utility model provides a cyclohexane oxidation decomposition liquid refining plant, its characterized in that includes saponification separator, first blender, second blender, a washing separator, two washing separators, cyclone and coalescence separator, the liquid outlet of saponification separator pass through first connecting pipe with the inlet of a washing separator is connected, first blender sets up on the first connecting pipe, the liquid outlet of a washing separator pass through the second connecting pipe with the inlet of two washing separators is connected, the second blender sets up on the second connecting pipe, the liquid outlet of two washing separators pass through the third connecting pipe with cyclone's inlet is connected, cyclone's liquid outlet pass through the fourth connecting pipe with coalescence separator's inlet is connected.
2. The apparatus for purifying a cyclohexane oxidative decomposition liquid according to claim 1, wherein a liquid inlet pipe for introducing a cyclohexane oxidative decomposition liquid is provided in the saponification separator, and a liquid outlet pipe for introducing a liquid into the distillation column is provided in the coalescence separator.
3. The apparatus for purifying a cyclohexane oxidation decomposition liquid according to claim 1, wherein a first water injection pipe located upstream of the first mixer is provided to the first connection pipe, and a second water injection pipe located upstream of the second mixer is provided to the second connection pipe.
4. The apparatus for purifying a cyclohexane oxidation decomposition liquid according to claim 1, wherein the second washing separator is connected to the first mixer through a fifth connection pipe.
5. The apparatus for purifying a cyclohexane oxidative decomposition liquid according to claim 1, wherein the apparatus for purifying a cyclohexane oxidative decomposition liquid comprises a sixth connecting pipe, a waste discharge port of the saponification separator is connected to the sixth connecting pipe through a first waste discharge pipe, a waste discharge port of the one-wash separator is connected to the sixth connecting pipe through a second waste discharge pipe, a waste discharge port of the cyclone separator is connected to the sixth connecting pipe through a third waste discharge pipe, a waste discharge port of the coalescing separator is connected to the sixth connecting pipe through a fourth waste discharge pipe, one end of the sixth connecting pipe is connected to a decomposing tank or an evaporating tank, and the other end of the sixth connecting pipe is connected to an outer drain pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322423556.9U CN220990751U (en) | 2023-09-07 | 2023-09-07 | Cyclohexane oxidation decomposition liquid refining device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322423556.9U CN220990751U (en) | 2023-09-07 | 2023-09-07 | Cyclohexane oxidation decomposition liquid refining device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220990751U true CN220990751U (en) | 2024-05-24 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322423556.9U Active CN220990751U (en) | 2023-09-07 | 2023-09-07 | Cyclohexane oxidation decomposition liquid refining device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220990751U (en) |
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2023
- 2023-09-07 CN CN202322423556.9U patent/CN220990751U/en active Active
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