CN220878795U - Heat exchange structure for initial delivery of hydrogenation catalyst after filling in butanol and octanol production - Google Patents
Heat exchange structure for initial delivery of hydrogenation catalyst after filling in butanol and octanol production Download PDFInfo
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- CN220878795U CN220878795U CN202322456273.4U CN202322456273U CN220878795U CN 220878795 U CN220878795 U CN 220878795U CN 202322456273 U CN202322456273 U CN 202322456273U CN 220878795 U CN220878795 U CN 220878795U
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- crude alcohol
- pipe
- hydrogenation
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- outlet pipe
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 69
- 239000003054 catalyst Substances 0.000 title claims abstract description 41
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 32
- KBPLFHHGFOOTCA-UHFFFAOYSA-N 1-Octanol Chemical compound CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 title description 18
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 title description 18
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 94
- 239000007788 liquid Substances 0.000 claims abstract description 40
- 239000002826 coolant Substances 0.000 claims abstract description 22
- IDYWQONQVXWFQP-UHFFFAOYSA-N butan-1-ol;octan-1-ol Chemical compound CCCCO.CCCCCCCCO IDYWQONQVXWFQP-UHFFFAOYSA-N 0.000 claims abstract description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000000110 cooling liquid Substances 0.000 claims description 57
- 239000000463 material Substances 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 12
- 230000001105 regulatory effect Effects 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 10
- 238000005260 corrosion Methods 0.000 claims description 6
- 230000007797 corrosion Effects 0.000 claims description 6
- 239000010963 304 stainless steel Substances 0.000 claims description 3
- 229910000589 SAE 304 stainless steel Inorganic materials 0.000 claims description 3
- XMVBHZBLHNOQON-UHFFFAOYSA-N 2-butyl-1-octanol Chemical compound CCCCCCC(CO)CCCC XMVBHZBLHNOQON-UHFFFAOYSA-N 0.000 claims 2
- 238000000034 method Methods 0.000 abstract description 11
- 230000008569 process Effects 0.000 abstract description 9
- 230000008859 change Effects 0.000 abstract description 7
- 230000000694 effects Effects 0.000 abstract description 6
- 239000001257 hydrogen Substances 0.000 abstract description 5
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 5
- 230000008676 import Effects 0.000 abstract 2
- 239000002994 raw material Substances 0.000 description 5
- 230000006872 improvement Effects 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 238000007599 discharging Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 description 1
- 239000005751 Copper oxide Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 229910000431 copper oxide Inorganic materials 0.000 description 1
- TVZPLCNGKSPOJA-UHFFFAOYSA-N copper zinc Chemical compound [Cu].[Zn] TVZPLCNGKSPOJA-UHFFFAOYSA-N 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A heat exchange structure for when adding hydrogen catalyst and just throwing fortune after filling in the butanol octanol production, set up the hydrogenation workshop section in butanol octanol production system, this heat exchange structure includes the catalyst heat exchanger, and this catalyst heat exchanger's cold junction import and cold junction export are connected on the thick alcohol groove in hydrogenation workshop section to the pipeline between the prefractionation tower through having crude alcohol feed liquor pipe and crude alcohol drain pipe of valve respectively, and this catalyst heat exchanger's hot junction import and hot junction export are connected on the coolant liquid input pipe of hydrogenation reactor in the hydrogenation workshop section through having coolant liquid feed liquor pipe and coolant liquid drain pipe of valve respectively. According to the method, the high temperature generated in the initial operation process of the hydrogenation catalyst in the hydrogenation reactor can be reduced, so that the activity of the catalyst is protected, and meanwhile, the temperature of the crude alcohol entering the pre-rectifying tower can be increased, so that the usage amount of steam in the pre-rectifying tower is reduced, and the influence of the change of the passing amount of the crude alcohol on the temperature of a sensitive plate of the pre-rectifying tower can be reduced.
Description
Technical Field
The utility model relates to a butanol-octanol production process, in particular to a heat exchange structure used for initial delivery after filling a hydrogenation catalyst in butanol-octanol production.
Background
At present, most hydrogenation catalysts used in butanol and octanol production processes are copper-zinc catalysts, and the main components of the hydrogenation catalysts are copper oxide and zinc oxide, wherein the catalysis is reduced copper. The hydrogenation catalyst has a high hot spot temperature at the initial stage of use, and has a risk of overtemperature, which is very unfavorable for maintaining the activity of the catalyst. In addition, the temperature of the crude alcohol discharged from the crude alcohol tank is lower than the pre-rectifying temperature, so that the steam consumption of the pre-rectifying tower is larger, and the influence of the change of the passing amount of the crude alcohol on the temperature of a sensitive plate of the pre-rectifying tower is larger.
Therefore, how to solve the problem of high temperature of the hydrogenation catalyst in the initial hot spot of use and simultaneously reduce the temperature difference when the crude alcohol enters the prefractionator has become one of the technical problems to be solved by those skilled in the art.
Disclosure of utility model
The technical scheme aims to solve the technical problems that how to reduce the high temperature generated by a hydrogenation catalyst in the initial use stage in a butanol and octanol production system and simultaneously improve the temperature of crude alcohol discharged through a crude alcohol tank, so that the activity of the hydrogenation catalyst is maintained, the usage amount of steam of a pre-rectifying tower is saved, and the influence of the change of the material passing amount of the crude alcohol on the temperature of a sensitive plate of the pre-rectifying tower is reduced.
In order to solve the technical problems, the technical scheme provides a heat exchange structure for initial delivery of a hydrogenation catalyst after filling in butanol and octanol production, wherein the heat exchange structure is arranged in a hydrogenation section of a butanol and octanol production system; the hydrogenation section comprises: the device comprises a gas-phase hydrogenation evaporator, a hydrogenation reactor, a plurality of coolers and a crude alcohol tank, wherein the feed end of the gas-phase hydrogenation evaporator is connected with a gas-liquid separator of the previous section through a pipeline, the discharge end of the gas-phase hydrogenation evaporator is connected with the feed end of the bottom of the hydrogenation reactor through a pipeline and the coolers, the bottom of the gas-phase hydrogenation evaporator is also connected with a hydrogen gas supply pipeline, the hydrogenation reactor is provided with a cooling device, the inlet end and the outlet end of the cooling device are respectively connected with a cooling liquid input pipe and a cooling liquid output pipe with valves, the discharge end of the top of the hydrogenation reactor is connected with the feed end of the crude alcohol tank through a pipeline and the coolers, and the discharge end of the crude alcohol tank is connected with a pre-rectifying tower of the subsequent section through a pipeline; the heat exchange structure of this technical scheme includes: the cold end inlet and the cold end outlet of the catalyst heat exchanger are respectively connected to a pipeline between the crude alcohol tank and the pre-rectifying tower through a crude alcohol liquid inlet pipe and a crude alcohol liquid outlet pipe with valves, and the hot end inlet and the hot end outlet of the catalyst heat exchanger are respectively connected to a cooling liquid input pipe through a cooling liquid inlet pipe and a cooling liquid outlet pipe with valves. According to the technical scheme, the heat exchange structure can introduce the cooling liquid (usually the steam condensate water with the temperature of about 90 ℃ generated in other working sections) input through the cooling liquid input pipe as a heat source, and introduce the crude alcohol discharged through the crude alcohol tank as a cold source, so that the heat source and the cold source conduct and exchange temperature energy in the heat exchange structure, thereby improving the discharging temperature of the crude alcohol and further reducing the temperature of the cooling liquid. And then the cooling liquid subjected to further cooling enters a cooling device of the hydrogenation reactor to absorb high-temperature heat generated in the initial operation process of the hydrogenation catalyst. Through the heat exchange process, the temperature difference of the crude alcohol entering the pre-rectifying tower can be effectively reduced, so that the use amount of steam of the pre-rectifying tower is saved, and the influence of the change of the material passing amount of the crude alcohol on the temperature of a sensitive plate of the pre-rectifying tower can be further reduced; in addition, the cooling liquid with further temperature reduction can more effectively absorb high-temperature heat generated in the initial operation process of the hydrogenation catalyst so as to maintain the activity of the catalyst.
As another implementation of the technical scheme, the crude alcohol liquid inlet pipe and the crude alcohol liquid outlet pipe are respectively connected to a pipe section between the crude alcohol tank and the pre-rectifying tower, which is close to the crude alcohol tank, and a pipe section between the crude alcohol liquid inlet pipe and the crude alcohol liquid outlet pipe, which is close to the pre-rectifying tower, and a valve is arranged on the pipe section between the crude alcohol liquid inlet pipe and the crude alcohol liquid outlet pipe. The flow direction and the flow rate of the crude alcohol can be controlled by opening and closing the valve and operating the opening.
As another implementation of the technical scheme, the cooling liquid inlet pipe and the cooling liquid outlet pipe are respectively connected to a pipe section between the valve on the cooling liquid input pipe and the inlet end, which is close to the valve, and a pipe section between the cooling liquid inlet pipe and the cooling liquid outlet pipe, which is close to the inlet end, and are provided with valves. The flow direction and the flow rate of the cooling liquid can be controlled by opening and closing the valve and operating the opening.
As another implementation of the technical scheme, temperature indicators are arranged at positions, close to the inlet end, on the crude alcohol outlet pipe and the cooling liquid input pipe. Therefore, the temperature change of the cold source and the heat source can be intuitively known, and the adjustment of the heat exchange structure can be conveniently assisted.
As another implementation of the technical scheme, the butanol and octanol production system is provided with a central control unit, wherein the cooling liquid input pipe, the cooling liquid output pipe, the crude alcohol liquid inlet pipe, the crude alcohol liquid outlet pipe, the cooling liquid outlet pipe and a valve arranged on a pipeline section between the crude alcohol liquid inlet pipe and the crude alcohol liquid outlet pipe and a valve arranged on a pipeline section between the cooling liquid inlet pipe and the cooling liquid outlet pipe are electric cut-off valves or electric regulating valves, the electric cut-off valves or the electric regulating valves and the temperature indication meters are respectively electrically connected with the central control unit, and the central control unit can control the opening and the switching sequence of the electric cut-off valves or the electric regulating valves according to the temperature data of the crude alcohol and/or the cooling liquid monitored by the temperature indication meters. Therefore, the automatic operation of the heat exchange structure is realized, and the investment of labor cost can be saved.
As another implementation of the technical scheme, the catalyst heat exchanger is made of a corrosion-resistant material, so that the catalyst heat exchanger does not react with the crude alcohol solution. Further, the corrosion-resistant material is 304 stainless steel.
Drawings
FIG. 1 is a connection block diagram of an improved butanol-octanol production system of this utility model;
FIG. 2 is a connection structure diagram of the heat exchange structure of the utility model used in the initial operation after loading the hydrogenation catalyst in the butanol-octanol production. Symbol description in the drawings: 100 butanol and octanol production system; 10 raw material production sections; 20 hydrogenation working sections; 1a gas phase hydrogenation evaporator; 11 hydrogen supply pipeline; 2, a hydrogenation reactor; 21 a cooling liquid input pipe; 22 a coolant outlet pipe; 3a cooler; 4, a crude alcohol tank; 5 a catalyst heat exchanger; 51 crude alcohol feed pipe; 52 crude alcohol outlet pipe; 53 a cooling liquid inlet pipe; 54 a cooling liquid outlet pipe; 6, a temperature indicating instrument; 30 separation and purification section.
Detailed Description
The detailed description and technical content of the present utility model are described below with reference to the drawings, which are, however, provided for reference and illustration only and are not intended to limit the present utility model.
Any two or more embodiments of the utility model may be combined in any desired manner within the context of this specification, and the resulting solution is part of the original disclosure of this specification, while still falling within the scope of the utility model.
As shown in fig. 1, for the connection structure of the improved butanol-octanol production system 100 of this utility model, the butanol-octanol production system 100 may be divided into three sections according to the butanol-octanol production process: a raw material production section 10, a hydrogenation section 20 and a separation and purification section 30. The heat exchange structure (hereinafter referred to as heat exchange structure) for initial operation after loading the hydrogenation catalyst in butanol and octanol production of the present utility model is disposed in the hydrogenation section 20. Since the butanol-octanol production process and production system are already mature technologies, the present utility model only describes the hydrogenation section 20 related to the structural improvement in detail, and the specific construction of the raw material production section 10 and the separation and purification section 30 not subjected to the structural improvement will not be described in detail. It will be apparent to those skilled in the art that the connection structure of the butanol-octanol production system 100 can be understood from the expert knowledge of the person himself and the existing process technology even without detailed description of the whole butanol-octanol production system 100, and that improvements and the resulting advantageous technical effects of the present utility model can be understood.
Specifically, referring to fig. 2, the hydrogenation section 20 mainly includes a gas phase hydrogenation evaporator 1, a hydrogenation reactor 2, a plurality of coolers 3 and a crude alcohol tank 4, wherein a feed end of the gas phase hydrogenation evaporator 1 is connected with a gas-liquid separator (not shown) of a previous section (raw material production section) through a pipeline, a discharge end of the gas phase hydrogenation evaporator 1 is connected with a feed end at a bottom of the hydrogenation reactor 2 through a pipeline and one of the coolers 3, the bottom of the gas phase hydrogenation evaporator 1 is further connected with a hydrogen supply pipeline 11, and in order to enable hydrogen entering the gas phase hydrogenation evaporator 1 to be better mixed with raw materials, the hydrogen can be used as a cold source for carrying out temperature energy exchange on a discharge of the hydrogenation reactor 2 flowing through the one of the coolers 3 arranged at the discharge end of the hydrogenation reactor 2 before entering the gas phase hydrogenation evaporator 1 to raise the temperature, and then enters the gas phase hydrogenation evaporator 1. The hydrogenation reactor 2 is provided with a cooling device (not shown in the figure), the inlet end and the outlet end of the cooling device are respectively connected with a cooling liquid input pipe 21 and a cooling liquid output pipe 22 with valves, the discharge end at the top of the hydrogenation reactor 2 is connected with the feed end of the crude alcohol tank 4 through a pipeline and a cooler 3 (two are shown in the figure because of the technological requirement), and the discharge end of the crude alcohol tank 4 is connected with a pre-rectifying tower (not shown in the figure) of the subsequent section (separation and purification section) through a pipeline. The heat exchange structure is realized by adding the catalyst heat exchanger 5 between the hydrogenation reactor 2 and the discharging of the crude alcohol tank 4, wherein the catalyst heat exchanger 5 can be made of a corrosion-resistant material to prevent the catalyst heat exchanger 5 from being corroded and damaged by the crude alcohol solution, and the corrosion-resistant material can be 304 stainless steel. The specific structural improvement of the utility model is as follows: the cold end inlet and the cold end outlet of the catalyst heat exchanger 5 are respectively connected to a pipeline between the crude alcohol tank 4 and the pre-rectifying tower through a crude alcohol liquid inlet pipe 51 and a crude alcohol liquid outlet pipe 52 with valves, and the hot end inlet and the hot end outlet of the catalyst heat exchanger 5 are respectively connected to the cooling liquid input pipe 21 through a cooling liquid inlet pipe 53 and a cooling liquid outlet pipe 54 with valves. The coolant used in the butanol-octanol production system 100 is typically steam condensate at a temperature of about 90 degrees celsius produced by other stations. Crude alcohol tank
Further, the crude alcohol liquid inlet pipe 51 and the crude alcohol liquid outlet pipe 52 are respectively connected to a pipe section between the crude alcohol tank 4 and the pre-rectifying tower, which is close to the crude alcohol tank 4, and a pipe section between the crude alcohol liquid inlet pipe 51 and the crude alcohol liquid outlet pipe 52, which is close to the pre-rectifying tower, and valves are provided on the pipe sections. The coolant inlet pipe 53 and the coolant outlet pipe 54 are connected to a pipe section between the valve on the coolant inlet pipe 21 and the inlet end near the valve and a pipe section near the inlet end, respectively, and a valve is provided on a pipe section between the coolant inlet pipe 53 and the coolant outlet pipe 54. The flow direction and the flow rate of the crude alcohol and the cooling liquid can be controlled by the opening and closing of the valve and the opening operation. Furthermore, the temperature indicator 6 can be installed on the crude alcohol outlet pipe 52 and the cooling liquid inlet pipe 21 near the inlet end, so as to intuitively understand the temperature changes of the cold source and the heat source, and further facilitate the adjustment of the heat exchange structure.
As another embodiment of the present utility model, the cooling liquid input pipe 21, the cooling liquid output pipe 22, the crude alcohol liquid inlet pipe 51, the crude alcohol liquid outlet pipe 52, the cooling liquid inlet pipe 53 and the cooling liquid outlet pipe 54, and the valves disposed on the pipe sections between the crude alcohol liquid inlet pipe 51 and the crude alcohol liquid outlet pipe 52 and the valves disposed on the pipe sections between the cooling liquid inlet pipe 53 and the cooling liquid outlet pipe 54 may be electric shut-off valves or electric regulating valves, and the electric shut-off valves or electric regulating valves and the temperature indicators 6 in the above-mentioned pipes may be electrically connected to a central control unit (not shown) in the butanol-octanol production system 100, respectively, and the central control unit may control the opening and switching sequence of the above-mentioned electric shut-off valves or electric regulating valves according to the temperature data of the crude alcohol and/or the cooling liquid monitored by the temperature indicators 6, so as to realize the automatic operation of the heat exchange structure and save the investment of labor costs. In the present embodiment, the electric cut-off valve or the electric regulating valve and the instrument control component such as the temperature indicator in the newly added pipeline are electrically connected to the self central control unit of the butanol-octanol production system, and the central control unit may be formed by a Programmable Logic Control (PLC) or a central control circuit, a central control system or an upper computer, etc., whereas the present application central control unit is a very wide and common control method applied in the field of automation control in view of the fact that the present application central control unit controls the operation state of each mechanism or component according to the input or written instruction, that is, the present control technology, so the present application central control unit does not need to describe the operation process of the electric cut-off valve or the electric regulating valve.
The heat exchange structure of the utility model firstly opens the valve on the pipeline section between the crude alcohol liquid inlet pipe 51 and the crude alcohol liquid outlet pipe 52 and closes to throw cold materials, namely crude alcohol is discharged, then gradually opens the valve on the pipeline section between the cooling liquid inlet pipe 53 and the cooling liquid outlet pipe 54 and closes to throw hot materials, namely cooling liquid flowing in through the cooling liquid input pipe 21, and the hot materials should be thrown slowly, and the temperature change of the cold and hot materials is concerned at any time so as to adjust the steam of the prefractionator in time. After the hydrogenation catalyst runs stably after the initial period of operation (i.e. no high temperature heat is released), the valves on the pipe sections between the crude alcohol liquid inlet pipe 51 and the crude alcohol liquid outlet pipe 52 can be closed and opened, and the valves on the pipe sections between the cooling liquid inlet pipe 53 and the cooling liquid outlet pipe 54 can be slowly closed and opened so as to stop the operation of the heat exchange structure.
In summary, the heat exchange structure of the utility model can introduce the cooling liquid input through the cooling liquid input pipe as a heat source, and introduce the crude alcohol discharged through the crude alcohol tank as a cold source, so that the heat source and the cold source conduct and exchange temperature energy in the heat exchange structure, thereby increasing the discharging temperature of the crude alcohol and further reducing the temperature of the cooling liquid. And then the cooling liquid subjected to further cooling enters a cooling device of the hydrogenation reactor to absorb high-temperature heat generated in the initial operation process of the hydrogenation catalyst. Through the heat exchange process, the temperature difference of the crude alcohol entering the pre-rectifying tower can be effectively reduced, so that the use amount of steam of the pre-rectifying tower is saved, and the influence of the change of the material passing amount of the crude alcohol on the temperature of a sensitive plate of the pre-rectifying tower can be further reduced; in addition, the cooling liquid with further temperature reduction can more effectively absorb high-temperature heat generated in the initial operation process of the hydrogenation catalyst so as to maintain the activity of the catalyst.
The foregoing description of the preferred embodiments of the present utility model is not intended to limit the scope of the utility model, and other equivalent variations using the inventive concepts are intended to fall within the scope of the utility model.
Claims (7)
1. A hydrogenation workshop section that is arranged in butyl octanol production system is put into operation to heat transfer structure that is arranged in the production of butyl octanol hydrogenation catalyst to load the back time, hydrogenation workshop section includes: the hydrogenation device comprises a gas phase hydrogenation evaporator, a hydrogenation reactor, a plurality of coolers and a crude alcohol tank, wherein the feed end of the gas phase hydrogenation evaporator is connected with a gas-liquid separator of a previous working section through a pipeline, the discharge end of the gas phase hydrogenation evaporator is connected with the feed end of the bottom of the hydrogenation reactor through a pipeline and the coolers, the bottom of the gas phase hydrogenation evaporator is also connected with a hydrogen gas supply pipeline, the hydrogenation reactor is provided with a cooling device, the inlet end and the outlet end of the cooling device are respectively connected with a cooling liquid input pipe and a cooling liquid output pipe with valves, the discharge end of the top of the hydrogenation reactor is connected with the feed end of the crude alcohol tank through a pipeline and the coolers, and the discharge end of the crude alcohol tank is connected with a pre-rectifying tower of a subsequent working section through a pipeline, and the hydrogenation device is characterized in that: the cold end inlet and the cold end outlet of the catalyst heat exchanger are respectively connected to a pipeline between the crude alcohol tank and the pre-rectifying tower through a crude alcohol liquid inlet pipe and a crude alcohol liquid outlet pipe with valves, and the hot end inlet and the hot end outlet of the catalyst heat exchanger are respectively connected to the cooling liquid input pipe through a cooling liquid inlet pipe and a cooling liquid outlet pipe with valves.
2. The heat exchange structure according to claim 1, wherein the crude alcohol liquid inlet pipe and the crude alcohol liquid outlet pipe are respectively connected to a pipe section between the crude alcohol tank and the pre-rectifying tower, which is close to the crude alcohol tank, and a pipe section between the crude alcohol liquid inlet pipe and the crude alcohol liquid outlet pipe, which is close to the pre-rectifying tower, and a valve is provided on the pipe section between the crude alcohol liquid inlet pipe and the crude alcohol liquid outlet pipe.
3. The heat exchange structure according to claim 2, wherein the coolant inlet pipe and the coolant outlet pipe are connected to a pipe section between the valve on the coolant inlet pipe and the inlet end and a pipe section near the inlet end, respectively, and a valve is provided on the pipe section between the coolant inlet pipe and the coolant outlet pipe.
4. A heat exchange structure according to claim 3, wherein the crude alcohol outlet pipe and the cooling liquid inlet pipe are provided with temperature indicators at positions adjacent to the inlet end.
5. The heat exchange structure according to claim 4, wherein the butanol-octanol production system has a central control unit, the coolant inlet pipe, the coolant outlet pipe, the crude alcohol inlet pipe, the crude alcohol outlet pipe, the coolant outlet pipe, and valves provided on the coolant inlet pipe and on a pipe section between the crude alcohol inlet pipe and the crude alcohol outlet pipe, and valves provided on a pipe section between the coolant inlet pipe and the coolant outlet pipe are electric shut-off valves or electric regulating valves, and the electric shut-off valves or electric regulating valves and the temperature indicators are electrically connected to the central control unit, respectively, and the central control unit controls the opening and the switching sequence of the electric shut-off valves or the electric regulating valves according to the temperature of the crude alcohol and/or the coolant monitored by the temperature indicators.
6. The heat exchange structure of claim 1, wherein the catalyst heat exchanger is made of a corrosion resistant material.
7. The heat exchange structure of claim 6 wherein the corrosion resistant material is 304 stainless steel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322456273.4U CN220878795U (en) | 2023-09-11 | 2023-09-11 | Heat exchange structure for initial delivery of hydrogenation catalyst after filling in butanol and octanol production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322456273.4U CN220878795U (en) | 2023-09-11 | 2023-09-11 | Heat exchange structure for initial delivery of hydrogenation catalyst after filling in butanol and octanol production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220878795U true CN220878795U (en) | 2024-05-03 |
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ID=90875210
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322456273.4U Active CN220878795U (en) | 2023-09-11 | 2023-09-11 | Heat exchange structure for initial delivery of hydrogenation catalyst after filling in butanol and octanol production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220878795U (en) |
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2023
- 2023-09-11 CN CN202322456273.4U patent/CN220878795U/en active Active
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