Hydrogenation reaction heat recycling system

Abstract

The utility model relates to a kind of hydrogenation reaction heat recycling system, through the design of device structure, after the reaction heat from hydrogenation reactor is carried out by water in cooling jacket, part of high-temperature condensed water diversion enters the heat exchanger in refining tower feed heater, for heating the material in refining tower heater, after cooling, water mixes with another part of high-temperature condensed water, and then returns cooling jacket to hydrogenation reactor for circulating cooling;Through this process, the temperature control in hydrogenation reactor is more stable, the refining tower feed heater does not need to use steam or other heat source to provide heat to heat the material, the reaction heat of hydrogenation reactor is fully utilized, the heat energy utilization rate is improved, and the jacket water does not have to be cooled by jacket water cooler, reducing the consumption of cooling water, improving the operation economic benefit of device.

Description

Technical Field

[0001] This utility model relates to the field of chemical technology, specifically to a hydrogenation reaction heat recovery and utilization system. Background Technology

[0002] The core reaction of acetone gas-phase hydrogenation is a simple catalytic hydrogenation reaction: (CH3)2C=O (acetone) + H2 → (CH3)2CH-OH (isopropanol) ΔH = -55 kJ / mol, mainly used for the production of the chemical isopropanol (IPA). The reaction process includes: mixing fresh liquid acetone with recycled unreacted acetone. The mixed acetone is heated in a preheater, then mixed with excess hydrogen in a vaporizer and completely vaporized to form the reactant gas. The reactant gas is further heated to the catalyst's initial reaction temperature (typically 65-115°C). The preheated gas enters a reactor packed with nickel-based catalyst particles to react. Acetone hydrogenation is a strongly exothermic reaction, which easily leads to "hot spots" (160°C) in the bed, accelerating catalyst deactivation and side reactions. This process uses a tubular fixed-bed reactor: the catalyst is packed inside the tubes, and water is used as a cooling medium in the shell side to remove the heat of reaction and control the temperature rise (hot spots) caused by the strongly exothermic reaction. After removing the heat, the jacket water is vaporized to produce low-pressure steam, which serves as a heat source for part of the heater.

[0003] However, in the initial and middle stages of the reaction, the catalyst activity is high, and the reaction mainly occurs in the upper part of the reactor, where the hot spot temperature reaches as high as 160℃, while the lower part is only 95℃. This uneven heat distribution and localized high temperatures make the reactor prone to overheating, necessitating the use of an additional cooler to cool the jacketed cooling water. This additional cooler increases water consumption. After cooling, the jacketed water temperature is low, and the reaction heat cannot effectively vaporize the water to produce self-generated steam, thus the reaction heat cannot be effectively utilized. Furthermore, the heat exchanger, which originally used self-generated steam as a heat source, requires additional steam. As a result, the energy consumption of the unit increases significantly, and the processing efficiency decreases. Therefore, finding ways to fully utilize the heat of the high-temperature jacketed water and reduce the unit's energy consumption is of great significance. Utility Model Content

[0004] This invention provides a heat recovery and utilization system for hydrogenation reaction, which can fully utilize the heat of high-temperature condensate in the cooling jacket of the hydrogenation reactor, thereby reducing the energy consumption of the device and reducing production costs.

[0005] This utility model provides a hydrogenation reaction heat recovery and utilization system, which includes a hydrogenation reactor, a jacketed water tank, a water pump, a refining tower feed heater, and a first refining tower. The hydrogenation reactor is equipped with a cooling jacket, and the refining tower feed heater is equipped with a heat exchanger. The refining tower feed heater is used to supply heated material to the first refining tower. The outlet of the cooling jacket is connected to the jacketed water tank through a pipe, and the outlet of the jacketed water tank is connected to the water pump through a pipe. The outlet of the water pump is connected to a first pipeline and a second pipeline arranged in parallel. The first pipeline is connected to the inlet of the cooling jacket, and the second pipeline is connected to the inlet of the heat exchanger. The outlet of the heat exchanger merges into the first pipeline through a third pipeline.

[0006] During operation, the high-temperature condensate from the cooling jacket of the hydrogenation reactor passes through the jacket water tank and water pump. A portion of the condensate is diverted into the heat exchanger inside the feed heater of the refining tower to heat the material inside the feed heater. The cooled water then mixes with the portion of high-temperature condensate in the first pipeline via the third pipeline and returns to the cooling jacket to circulate and cool the hydrogenation reactor. Through this process, the reaction heat of the hydrogenation reactor is fully utilized, and the feed heater of the refining tower can heat the material without the need for steam or other heat sources, thus improving the thermal energy utilization rate. Furthermore, it eliminates the need for an additional cooler to cool the jacket water, reducing cooling water consumption and improving the economic efficiency of the unit's operation.

[0007] Furthermore, valve F1 is provided on the first pipeline and valve F2 is provided on the second pipeline. Valves F1 and F2 are used to regulate the flow rate in the first and second pipelines.

[0008] The heat generated will vary with the change in feed load of the hydrogenation reactor. In order to fully recover the heat, the amount of heat recovery can be adjusted by adjusting the water flow rate in the first and second pipelines. Therefore, valves F1 and F2 are installed. The flow rate in the first and second pipelines can be adjusted by adjusting the opening of valves F1 and F2, thereby achieving reasonable heat recovery and utilization.

[0009] Furthermore, the hydrogenation reaction heat recovery and utilization system also includes a first reboiler and a second purification tower; the first reboiler is used to supply heat to the bottom of the second purification tower; a fourth pipeline is connected to the second pipeline, the fourth pipeline is connected to the shell-side inlet of the first reboiler, and the shell-side outlet of the first reboiler is connected to the third pipeline through a pipeline.

[0010] In operation, the high-temperature condensate from the cooling jacket of the hydrogenation reactor passes through a jacket water tank and a water pump. A portion is diverted to the heat exchanger in the feed heater of the refining tower to heat the material inside the heater. The other portion is diverted to the shell side of the first reboiler to heat the second refining tower. The cooled water then mixes with the high-temperature condensate from the first pipeline via a third pipeline and returns to the cooling jacket to circulate and cool the hydrogenation reactor. This technical solution addresses situations where the hydrogenation reactor generates a large amount of reaction heat, and the feed heater of the refining tower is insufficient to fully utilize this heat; in such cases, the first reboiler recovers a portion of the heat.

[0011] Furthermore, valve F21 is installed on the second pipe near the heat exchanger inlet, and valve F22 is installed on the fourth pipe.

[0012] To fully recover heat, the amount of heat recovery can be adjusted by regulating the water flow in the second and fourth pipes. Therefore, valves F21 and F22 are installed, and the flow in the second and fourth pipes can be adjusted by regulating the opening of valves F21 and F22, thereby achieving reasonable heat recovery and utilization.

[0013] Furthermore, the hydrogenation reaction heat recovery system also includes a second reboiler for supplying heat to the bottom of the second refining tower. The second reboiler and the first reboiler are connected in parallel, and the second reboiler is provided with a steam inlet.

[0014] When the feed heater of the purification column and the first reboiler simultaneously recover the reaction heat of the hydrogenation reactor, and the heat recovered by the first reboiler is insufficient for the use of the second purification column, a portion of steam can be supplemented through the steam inlet on the second reboiler to ensure that the heat load of the second purification column is sufficient.

[0015] Furthermore, the outlet of the water pump is also connected to a fifth pipeline, which is arranged in parallel with the first and second pipelines. The fifth pipeline flows into the first pipeline after passing through the jacketed water cooler.

[0016] In the above technical solution, if the heat of reaction in the hydrogenation reactor is too great and the feed heater of the refining tower and the first reboiler are insufficient to fully utilize the heat of reaction, the jacket water cooler is used to cool the jacket water and ensure that the temperature of the water returning to the cooling jacket meets the requirements for circulating cooling of the hydrogenation reactor.

[0017] Furthermore, valve F3 is installed on the fifth pipeline.

[0018] In the above technical solution, by further configuring valve F3, the water flow rate in the first, second, and fifth pipelines can be adjusted by regulating the opening degrees of valves F1, F2, and F3, thereby adjusting the heat recovery amount and ensuring that the temperature of the water returning to the cooling jacket meets the requirements for circulating cooling of the hydrogenation reactor. It is understood that if the heat of reaction in the hydrogenation reactor is not significant, the heat from the high-temperature condensate can be recovered directly without using the jacket water cooler by closing valve F3. Furthermore, it is understood that, as needed, the portion recovering heat from the high-temperature condensate can be switched on or off as required by opening or closing valve F2.

[0019] The beneficial effects of this utility model are as follows: The hydrogenation reaction heat recovery and utilization system of this utility model, through the design of the device structure, allows the reaction heat from the hydrogenation reactor to be carried out by water in the cooling jacket. A portion of the high-temperature condensate then flows into the heat exchanger in the feed heater of the refining tower to heat the material in the refining tower heater. The cooled water mixes with another portion of the high-temperature condensate and returns to the cooling jacket to circulate and cool the hydrogenation reactor. Through this process, the temperature control in the hydrogenation reactor is more stable, and the feed heater of the refining tower can heat the material without the need for steam or other heat sources. The reaction heat of the hydrogenation reactor is fully utilized, improving the thermal energy utilization rate. Moreover, it is not necessary to use a jacket water cooler to cool the jacket water, reducing the consumption of cooling water and improving the economic efficiency of the device operation. Attached Figure Description

[0020] To more clearly illustrate the technical solutions of the embodiments of this application, the accompanying drawings used in the embodiments will be briefly introduced below. It should be understood that the following drawings only show some embodiments of this application and should not be regarded as a limitation of the scope. For those skilled in the art, other related drawings can be obtained based on these drawings without creative effort.

[0021] Figure 1 This is a schematic diagram of the hydrogenation reaction heat recovery and utilization system of this utility model.

[0022] The components include: 1. Hydrogenation reactor; 2. Jacketed water tank; 3. Water pump; 4. Refining tower feed heater; 5. First refining tower; 6. First reboiler; 7. Second refining tower; 8. Second reboiler; 9. Jacketed water cooler; 10. First pipeline; 11. Second pipeline; 12. Third pipeline; 13. Fourth pipeline; and 14. Fifth pipeline. Detailed Implementation

[0023] To facilitate understanding of this invention, a more comprehensive description will be provided below with reference to the accompanying drawings. The drawings illustrate preferred embodiments of the invention. However, this invention can be implemented in many different forms and is not limited to the embodiments described herein.

[0024] Please refer to Figure 1 The existing hydrogenation reactor 1 is equipped with a cooling jacket (not shown in the figure). The outlet of the cooling jacket is connected to the jacket water tank 2 via a pipe. The outlet of the jacket water tank 2 is connected to the water pump 3 via a pipe. The outlet of the water pump 3 is connected to two parallel pipelines. One pipeline is connected to the inlet of the cooling jacket, and the other pipeline flows into the first pipeline after passing through the jacket water cooler 9. Valves F1 and F3 are installed on the two pipelines respectively. Under ideal conditions, valve F1 on the first pipeline at the outlet of the water pump 3 is opened. The hot water removes the heat from the hydrogenation reactor 1 and then flashes in the jacket water tank 2 to generate self-produced steam. The condensate generated after the self-produced steam is used is then pumped back to the jacket water tank 2 to achieve circulation. However, during actual operation, the local temperature of hydrogenation reactor 1 is too high. When valve F1 is opened, valve F3 must be opened at the same time to divert the hot water from the outlet of water pump 3 to the jacket water cooler 9 for cooling. The condensate obtained after mixing is returned to the cooling jacket. After cooling through this process, the heat of reaction can no longer make the hot water flash evaporate to generate self-generated steam, and the heat is wasted. At the same time, the cooling water input of jacket water cooler 9 is increased.

[0025] Please continue to refer to Figure 1 This utility model discloses a hydrogenation reaction heat recovery and utilization system, which includes a hydrogenation reactor 1, a jacketed water tank 2, a water pump 3, a refining tower feed heater 4, and a first refining tower 5. The hydrogenation reactor 1 is equipped with a cooling jacket (not shown in the figure), and the refining tower feed heater 4 is equipped with a heat exchanger (not shown in the figure). The refining tower feed heater 4 is used to supply heated material to the first refining tower 5. The outlet of the cooling jacket is connected to the jacketed water tank 2 through a pipe, and the outlet of the jacketed water tank 2 is connected to the water pump 3 through a pipe. The outlet of the water pump 3 is connected to a first pipeline 10 and a second pipeline 11 arranged in parallel. The first pipeline 10 is connected to the inlet of the cooling jacket, and the second pipeline 11 is connected to the inlet of the heat exchanger. The outlet of the heat exchanger merges into the first pipeline 10 through a third pipeline 12.

[0026] During operation, the high-temperature condensate from the cooling jacket of the hydrogenation reactor 1 passes through the jacket water tank 2 and the water pump 3. A portion of the condensate is diverted into the heat exchanger inside the refining tower feed heater 4 to heat the material inside the refining tower feed heater 4. After cooling, the water mixes with the portion of high-temperature condensate in the first pipe 10 via the third pipe 12 and then returns to the cooling jacket to circulate and cool the hydrogenation reactor 1. Through this process, the reaction heat of the hydrogenation reactor 1 is fully utilized, and the refining tower feed heater 4 can heat the material without the need for steam or other heat sources, thus improving the thermal energy utilization rate. Furthermore, it eliminates the need for an additional jacket water cooler 9 to cool the jacket water, reducing cooling water consumption and improving the economic efficiency of the unit's operation.

[0027] Furthermore, valve F1 is provided on the first pipeline 10 and valve F2 is provided on the second pipeline 11. Valves F1 and F2 are used to regulate the flow rate in the first pipeline 10 and the second pipeline 11.

[0028] The heat generated varies with the feed load of the hydrogenation reactor 1. To fully recover this heat, the amount of heat recovery can be adjusted by regulating the water flow rate in the first pipeline 10 and the second pipeline 11, ensuring the normal operation of the hydrogenation reaction. Therefore, valves F1 and F2 are installed. The flow rate in the first pipeline 10 and the second pipeline 11 can be adjusted by regulating the opening of valves F1 and F2, thereby achieving reasonable heat recovery and utilization. Valve F1 and F2 can be either solenoid valves or manual valves; this is not limited.

[0029] Furthermore, the hydrogenation reaction heat recovery and utilization system also includes a first reboiler 6 and a second purification tower 7; the first reboiler 6 is used to supply heat to the bottom of the second purification tower 7; a fourth pipeline 13 is connected to the second pipeline 11, the fourth pipeline 13 is connected to the shell-side inlet of the first reboiler 6, and the shell-side outlet of the first reboiler 6 is connected to the third pipeline 12 through a pipeline.

[0030] In operation, the high-temperature condensate from the cooling jacket of the hydrogenation reactor 1 passes through the jacket water tank 2 and water pump 3. A portion is diverted into the heat exchanger within the refining tower feed heater 4 to heat the material inside the heater. The other portion is diverted into the shell side of the first reboiler 6 to heat the second refining tower 7. The cooled water then mixes with the portion of high-temperature condensate in the first pipeline 10 via the third pipeline 12, and returns to the cooling jacket to circulate and cool the hydrogenation reactor 1. This technical solution addresses the situation where the hydrogenation reactor 1 generates a large amount of reaction heat, and the refining tower feed heater 4 is insufficient to fully utilize this heat. In this case, the first reboiler 6 recovers a portion of the heat.

[0031] Furthermore, valve F21 is installed on the second pipe 11 near the heat exchanger inlet, and valve F22 is installed on the fourth pipe 13.

[0032] To ensure full heat recovery, the amount of heat recovery can be adjusted by regulating the water flow rate in the second pipeline 11 and the fourth pipeline 13, thus ensuring the normal progress of the hydrogenation reaction. Therefore, valves F21 and F22 are installed. The flow rate in the second pipeline 11 and the fourth pipeline 13 can be adjusted by regulating the opening degree of valves F21 and F22, thereby achieving reasonable heat recovery and utilization. Valves F21 and F22 can be either solenoid valves or manual valves; this is not limited.

[0033] Furthermore, the hydrogenation reaction heat recovery system also includes a second reboiler 8 for supplying heat to the bottom of the second refining tower 7. The second reboiler 8 and the first reboiler 6 are connected in parallel, and the second reboiler 8 is provided with a steam inlet.

[0034] When the feed heater 4 of the refining tower and the first reboiler 6 simultaneously recover the reaction heat of the hydrogenation reactor 1, and the heat recovered by the first reboiler 6 is insufficient for the use of the second refining tower 7, a portion of steam can be supplemented through the steam inlet on the second reboiler 8 to ensure that the heat load of the second refining tower 7 is sufficient.

[0035] Furthermore, the outlet of the water pump 3 is also connected to a fifth pipeline 14, which is arranged in parallel with the first pipeline 10 and the second pipeline 11. The fifth pipeline 14 flows into the first pipeline 10 after passing through the jacketed water cooler 9.

[0036] In the above technical solution, if the heat of reaction in the hydrogenation reactor 1 is too great and the feed heater 4 of the refining tower and the first reboiler 6 are insufficient to fully utilize the heat of reaction, the jacket water cooler 9 will cool the jacket water and ensure that the temperature of the water returning to the cooling jacket meets the requirements for circulating cooling of the hydrogenation reactor 1.

[0037] Furthermore, a valve F3 is provided on the fifth pipeline 14.

[0038] Among them, valve F3 is either a solenoid valve or a manual valve, and there is no limitation on which one.

[0039] In the above technical solution, by further configuring valve F3, the water flow rate in the first pipeline 10, the second pipeline 11, and the fifth pipeline 14 can be adjusted by regulating the opening degrees of valves F1, F2, and F3, thereby adjusting the heat recovery amount and ensuring that the temperature of the water returning to the cooling jacket meets the requirements for circulating cooling of the hydrogenation reactor 1, ensuring the normal progress of the hydrogenation reaction. It is understood that if the heat of reaction in the hydrogenation reactor 1 is low, the heat of the jacket water cooler 9 can be directly recovered from the high-temperature condensate by closing valve F3. Additionally, it is understood that, as needed, the portion recovering heat from the high-temperature condensate can be activated or deactivated at any time by opening or closing valve F2.

[0040] Before the upgrade, based on an average steam output of 4.895 t / h, an annual operating time of 8000 h, and a steam price of 224.08 yuan / t, the existing equipment resulted in a loss of 39,160 t of steam recovered annually, causing an economic loss of 8.775 million yuan. After adopting this new equipment, the heat of reaction in the initial and middle stages is fully removed and recovered, significantly improving the operational efficiency of the equipment.

[0041] Finally, it should be noted that in this document, relational terms such as "first" and "second" are used only to distinguish one entity or operation from another, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Furthermore, the terms "comprising," "including," or any other variations thereof are intended to cover non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements includes not only those elements but also other elements not expressly listed, or elements inherent to such a process, method, article, or apparatus. Without further limitations, an element defined by the phrase "comprising one..." does not exclude the presence of other identical elements in the process, method, article, or apparatus that includes said element.

[0042] Furthermore, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model according to the specific circumstances.

[0043] The various embodiments in this specification are described in a progressive manner. Each embodiment focuses on the differences from other embodiments. The various embodiments can be combined as needed, and the same or similar parts can be referred to each other.

[0044] The above description of the disclosed embodiments enables those skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the present invention. Therefore, the present invention is not to be limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A hydrogenation reaction heat recovery system characterized by comprising: The hydrogenation reaction heat recovery system includes a hydrogenation reactor, a jacketed water tank, a water pump, a refining tower feed heater, and a first refining tower. The hydrogenation reactor is equipped with a cooling jacket, and the refining tower feed heater is equipped with a heat exchanger. The refining tower feed heater is used to supply heated material to the first refining tower. The outlet of the cooling jacket is connected to the jacketed water tank through a pipe, and the outlet of the jacketed water tank is connected to the water pump through a pipe. The outlet of the water pump is connected to a first pipeline and a second pipeline arranged in parallel. The first pipeline is connected to the inlet of the cooling jacket, and the second pipeline is connected to the inlet of the heat exchanger. The outlet of the heat exchanger merges into the first pipeline through a third pipeline.

2. The hydrogenation reaction heat recycling system according to claim 1, wherein The first pipeline is equipped with valve F1, and the second pipeline is equipped with valve F2. Valves F1 and F2 are used to regulate the flow rate in the first and second pipelines.

3. The hydrogenation reaction heat recycling system according to claim 2, wherein The hydrogenation reaction heat recovery system also includes a first reboiler and a second refining tower; the first reboiler is used to supply heat to the bottom of the second refining tower; a fourth pipeline is connected to the second pipeline, the fourth pipeline is connected to the shell-side inlet of the first reboiler, and the shell-side outlet of the first reboiler is connected to the third pipeline through a pipeline.

4. The hydrogenation reaction heat recycling system according to claim 3, wherein Valve F21 is installed on the second pipe near the heat exchanger inlet, and valve F22 is installed on the fourth pipe.

5. The hydrogenation reaction heat recovery system according to claim 3 or 4, wherein The hydrogenation reaction heat recovery system also includes a second reboiler for supplying heat to the bottom of the second refining tower. The second reboiler and the first reboiler are connected in parallel, and the second reboiler is provided with a steam inlet.

6. The hydrogenation reaction heat recycling system according to claim 4, wherein The outlet of the water pump is also connected to a fifth pipeline, which is arranged in parallel with the first and second pipelines. The fifth pipeline flows into the first pipeline after passing through the jacketed water cooler.

7. The hydrogenation reaction heat recycling system according to claim 6, wherein Valve F3 is installed on the fifth pipeline.

Images