CN218047830U - Hydrodecarbonylation system for fatty alcohol refining - Google Patents
Hydrodecarbonylation system for fatty alcohol refining Download PDFInfo
- Publication number
- CN218047830U CN218047830U CN202220881693.XU CN202220881693U CN218047830U CN 218047830 U CN218047830 U CN 218047830U CN 202220881693 U CN202220881693 U CN 202220881693U CN 218047830 U CN218047830 U CN 218047830U
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- CN
- China
- Prior art keywords
- pipe
- fatty alcohol
- heater
- heat exchanger
- hydrogen
- 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.)
- Expired - Fee Related
Links
- 150000002191 fatty alcohols Chemical class 0.000 title claims abstract description 32
- 238000007670 refining Methods 0.000 title claims description 10
- 239000001257 hydrogen Substances 0.000 claims abstract description 33
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 33
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 230000006324 decarbonylation Effects 0.000 claims abstract description 19
- 238000006606 decarbonylation reaction Methods 0.000 claims abstract description 19
- 239000007789 gas Substances 0.000 claims abstract description 19
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 8
- DNIAPMSPPWPWGF-GSVOUGTGSA-N (R)-(-)-Propylene glycol Chemical compound C[C@@H](O)CO DNIAPMSPPWPWGF-GSVOUGTGSA-N 0.000 claims abstract description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 20
- 230000001105 regulatory effect Effects 0.000 claims description 7
- 239000000498 cooling water Substances 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- 239000000047 product Substances 0.000 description 11
- 239000003921 oil Substances 0.000 description 9
- 229910001873 dinitrogen Inorganic materials 0.000 description 8
- 239000000463 material Substances 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000001035 drying Methods 0.000 description 5
- 238000007599 discharging Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000005262 decarbonization Methods 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 239000002216 antistatic agent Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- -1 carbonyl alcohol Chemical compound 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000000271 synthetic detergent Substances 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
Images
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model provides a refined hydrogenation decarbonylation system of aliphatic alcohol, include: the device comprises a heater, a heat exchanger and a gas circulator, wherein one end of the heater is connected with a hydrogen feeding pipe, and the other end of the heater is connected with a decarbonylation tower; one end of the heat exchanger is connected with a fatty alcohol feeding pipe, the outlet of the heat exchanger is connected with the inlet of the heater through a pipeline, the hydrogen feeding pipe is communicated with the pipeline, and the other end of the heat exchanger is connected with the cooler; one end of the gas circulator is connected with a separated gas emptying pipe connected with the cooler, and the other end of the gas circulator is connected with a fatty alcohol feeding pipe connected with the heat exchanger.
Description
Technical Field
The utility model belongs to the technical field of fatty alcohol hydrogenation decarbonylation, concretely relates to fatty alcohol refining hydrogenation decarbonylation system.
Background
The fatty alcohol refers to an alcohol with hydroxyl group connected with fatty alkyl, is used for manufacturing synthetic detergents, cosmetics and medicines, is also used as an additive of lubricating oil and an antistatic agent of textiles, is industrially prepared by oxo synthesis or a grease hydrogenation method, and in the existing fatty alcohol hydrogenation decarbonylation system, a large amount of nitrogen is needed for supplement and discharge in a start preheating stage and a stop drying stage, the start heating and the drying of a catalyst are increased by using the nitrogen carrying heat energy, the start heating is slow, and the stop drying time is long.
SUMMERY OF THE UTILITY MODEL
The utility model aims at solving the problems existing in the prior art, and provides a hydrogenation and decarbonylation system for refining fatty alcohol.
The utility model provides a following technical scheme:
a fatty alcohol refining hydrodecarbonylation system, comprising:
one end of the heater is connected with a hydrogen feeding pipe, and the other end of the heater is connected with a decarbonylation tower;
one end of the heat exchanger is connected with a fatty alcohol feeding pipe, the outlet of the heat exchanger is connected with the inlet of the heater through a pipeline, the hydrogen feeding pipe is communicated with the pipeline, and the other end of the heat exchanger is connected with the cooler;
and one end of the gas circulator is connected with a separated gas emptying pipe connected with the cooler, and the other end of the gas circulator is connected with a fatty alcohol feeding pipe connected with the heat exchanger.
Further, install pressure regulating valve on the hydrogen inlet pipe, make hydrogen pressure keep certain in the hydrogen inlet pipe through pressure regulating valve, the decarbonylation tower other end with heat exchanger connects, decarbonylation tower one side has connect the evacuation house steward, installs the emission control valve on the evacuation house steward, through emission control valve adjustment hydrogen purity.
Furthermore, one side of the heater is connected with a heat conduction oil inlet pipe, the other side of the heater is connected with a heat conduction oil outlet pipe, a temperature controller is installed on the heat conduction oil inlet pipe, and the temperature of the heater is controlled to be 90-150 ℃ through the temperature controller.
Furthermore, cooler one side has connect the flash tank, and the flash tank opposite side has connect the product discharging pipe, install the product delivery pump on the product discharging pipe, the cooler top has connect the separation gas evacuation pipe.
Furthermore, a cooling water inlet pipe and a cooling water outlet pipe are connected to the cooler.
Further, install feed pump and batch meter on the aliphatic alcohol inlet pipe, feed pump department installs the pipe-line filter, install the nitrogen gas intake pipe on the aliphatic alcohol inlet pipe, the nitrogen gas intake pipe is located between batch meter and the heat exchanger.
The utility model has the advantages that:
the gas circulator is added in the system, and in the processes of starting, warming, preheating and stopping catalyst drying, the nitrogen in the system is subjected to closed circulating flow by using the circulator without emission, so that the starting, warming and stopping drying speeds are increased, the time is shortened, and the consumption of the nitrogen is saved; because the purity of the hydrogen is reduced after the hydrogen participates in the reaction for a long time, a discharge control valve is installed on a hydrogen pipeline, and hydrogen discharge replacement is performed periodically.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention, and together with the description serve to explain the invention and not to limit the invention. In the drawings:
fig. 1 is a schematic view of the structure of the present invention.
Detailed Description
As shown in figure 1, in the fatty alcohol refining hydrodecarbonylation system, one end of a heater 13 is connected with a hydrogen feeding pipe 18, and the other end of the heater 13 is connected with a decarbonylation tower 12; install pressure regulating valve 20 on the hydrogen inlet pipe 18, make hydrogen pressure in the hydrogen inlet pipe 18 keep certain through pressure regulating valve 20, the decarbonization tower 12 other end with heat exchanger 14 is connected, decarbonization tower 12 one side has connect evacuation house steward 11, installs emission control valve 21 on the evacuation house steward 11, adjusts the hydrogen purity through emission control valve 21.
One end of the heat exchanger 14 is connected with a fatty alcohol feeding pipe 15, a feeding pump 17 and a metering gauge 19 are installed on the fatty alcohol feeding pipe 15, a pipeline filter 18 is installed at the position of the feeding pump 17, the feeding pump 17 has a pressurization function, the outlet of the heat exchanger 14 is connected with the inlet of the heater 13 through a pipeline, the hydrogen feeding pipe 18 is communicated with the pipeline, and the other end of the heat exchanger 14 is connected with the cooler 4; one side of the heater 13 is connected with a heat-conducting oil inlet pipe 10, the other side of the heater 13 is connected with a heat-conducting oil outlet pipe 9, a temperature controller 22 is installed on the heat-conducting oil inlet pipe 10, and the temperature of the heater is controlled to be 90-150 ℃ through the temperature controller 22.
Cooler 4 one side has connect flash tank 3, and flash tank 3 opposite side has connect product discharging pipe 2, install product delivery pump 1 on the product discharging pipe 2, cooler 4 top termination has separation gas evacuation pipe 5, has connect cooling water inlet tube 6 and cooling water outlet pipe 7 on the cooler 4.
Install nitrogen gas intake pipe 8 on fatty alcohol inlet pipe 15, nitrogen gas intake pipe 8 is located between metrological 19 and heat exchanger 14, and gas circulator 16 one end is connected with the separation gas evacuation pipe 5 that cooler 4 meets, the fatty alcohol inlet pipe 15 that the other end and heat exchanger 14 of gas circulator 16 meet is connected.
The utility model discloses when using, fatty alcohol that is located the holding vessel district gets into the entry of feed pump 17 through fatty alcohol inlet pipe 15, carry to in heat exchanger 14 after the pressurization of feed pump 17, the flow of fatty alcohol in the fatty alcohol inlet pipe 15 is controlled to the meter 19 this moment, nitrogen gas gets into in heat exchanger 14 from nitrogen gas intake pipe 8, after the heat transfer of fatty alcohol and nitrogen gas reaction resultant, continue to flow to heater 13, hydrogen gets into in heater 13 through hydrogen inlet pipe 18 this moment, fatty alcohol and nitrogen gas reaction resultant mix with hydrogen again after the heat transfer, get into heating to reaction temperature (90 ℃ -150 ℃) in heater 13 after mixing, pressure in hydrogen inlet pipe 18 is controlled through pressure regulating valve 20, guarantee that hydrogen pressure keeps certain, in conventional conditions, pressure keeps 0.8Mpa-2.5Mpa, pressure is according to the variety and catalyst activity difference and decides, the conduction oil gets into in heater 13 through oil inlet pipe 10, adjust the temperature on the heat conduction oil pipeline through temperature controller 22 at this moment, make its temperature between 90 ℃, material after reaching reaction temperature dissolves certain hydrogen under pressure and gets into in decarbonylation tower 12 by upper portion, this hydrogen decarbonylation tower takes part of the periodic emission, therefore the hydrogen gas control can be gone down through the long-term control, the decarbonylation tower, the process is installed and can be carried out the control and can be located for a long-term;
the material flows through a catalyst bed layer after being uniformly distributed by a distributor at the top of the tower, a small amount of carbonyl alcohol and hydrogen carry out reduction reaction on the surface of a catalyst, the material after hydrogenation purification flows into a material temporary storage space at the bottom of the tower, the liquid level of a decarbonylation tower 12 is controlled by a liquid level controller arranged at the outlet of a cooler 4, the material after liquid level control leaves the decarbonylation tower 12, the material exchanges heat with raw materials in a heat exchanger 14 and then enters the cooler 4 for cooling, the cooled fatty alcohol product enters a flash tank 3 for flash evaporation to dissolve hydrogen, gas-liquid separation is realized in the flash tank 3, the gas is discharged through a separated gas emptying pipe 5, and the product is conveyed into a product storage tank from a product discharge pipe 2 through a product conveying pump 1.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described in the foregoing embodiments, or equivalents may be substituted for elements thereof. 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 (6)
1. A fatty alcohol refining hydrodecarbonylation system is characterized by comprising:
one end of the heater is connected with a hydrogen feeding pipe, and the other end of the heater is connected with a decarbonylation tower;
one end of the heat exchanger is connected with a fatty alcohol feeding pipe, the outlet of the heat exchanger is connected with the inlet of the heater through a pipeline, the hydrogen feeding pipe is communicated with the pipeline, and the other end of the heat exchanger is connected with the cooler;
and one end of the gas circulator is connected with a separated gas emptying pipe connected with the cooler, and the other end of the gas circulator is connected with a fatty alcohol feeding pipe connected with the heat exchanger.
2. The aliphatic alcohol refining hydrodecarbonylation system according to claim 1, wherein a pressure regulating valve is installed on the hydrogen feeding pipe, the pressure of hydrogen in the hydrogen feeding pipe is kept constant by the pressure regulating valve, the other end of the decarbonylation tower is connected with the heat exchanger, an evacuation main pipe is connected to one side of the decarbonylation tower, a discharge control valve is installed on the evacuation main pipe, and the purity of hydrogen is adjusted by the discharge control valve.
3. The system for the refined hydrogenation and decarbonylation of fatty alcohol according to claim 2, wherein one side of the heater is connected with a heat transfer oil inlet pipe, the other side of the heater is connected with a heat transfer oil outlet pipe, a temperature controller is installed on the heat transfer oil inlet pipe, and the temperature of the heater is controlled to be 90-150 ℃ through the temperature controller.
4. The system of claim 1, wherein a flash tank is connected to one side of the cooler, a product discharge pipe is connected to the other side of the flash tank, a product delivery pump is installed on the product discharge pipe, and a separated gas emptying pipe is connected to the top end of the cooler.
5. The fatty alcohol refining hydrodecarbonylation system of claim 4, wherein the cooler is connected with a cooling water inlet pipe and a cooling water outlet pipe.
6. The fatty alcohol refining hydrodecarbonylation system of claim 1, wherein the fatty alcohol feeding pipe is provided with a feeding pump and a metering gauge, the feeding pump is provided with a pipeline filter, the fatty alcohol feeding pipe is provided with a nitrogen inlet pipe, and the nitrogen inlet pipe is positioned between the metering gauge and the heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220881693.XU CN218047830U (en) | 2022-04-13 | 2022-04-13 | Hydrodecarbonylation system for fatty alcohol refining |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220881693.XU CN218047830U (en) | 2022-04-13 | 2022-04-13 | Hydrodecarbonylation system for fatty alcohol refining |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218047830U true CN218047830U (en) | 2022-12-16 |
Family
ID=84417030
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202220881693.XU Expired - Fee Related CN218047830U (en) | 2022-04-13 | 2022-04-13 | Hydrodecarbonylation system for fatty alcohol refining |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN218047830U (en) |
-
2022
- 2022-04-13 CN CN202220881693.XU patent/CN218047830U/en not_active Expired - Fee Related
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20221216 |