CN218654450U - Acetic acid propionic acid device reactor biphase heat recovery system - Google Patents
Acetic acid propionic acid device reactor biphase heat recovery system Download PDFInfo
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- CN218654450U CN218654450U CN202222766620.9U CN202222766620U CN218654450U CN 218654450 U CN218654450 U CN 218654450U CN 202222766620 U CN202222766620 U CN 202222766620U CN 218654450 U CN218654450 U CN 218654450U
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Abstract
The utility model discloses a sour propionic acid device reactor biphase heat recovery system relates to chemical industry preparation equipment technical field. The utility model discloses a fluid stirring reactor, steam generator and circulative cooling ware, fluid stirring reactor is provided with first gaseous phase export and reaction liquid export, steam generator's tube side with first gaseous phase exit linkage, circulative cooling ware's tube side with reaction liquid exit linkage, steam generator's shell side with circulative cooling ware's shell side all is connected with the boiler water pipe. The utility model discloses the reaction heat that produces gas phase and liquid phase in the preparation process to acetic acid or propionic acid has been retrieved, has increased the utilization ratio to the energy, has reduced the waste to the reaction waste heat.
Description
Technical Field
The utility model belongs to the technical field of chemical industry preparation equipment, especially, relate to a sour propionic acid device reactor biphase heat recovery system.
Background
Energy conservation and emission reduction are a basic national policy in China, are inevitable choices for realizing the sustainable development of the economy in China, and are taken as the chemical production industry of households with large energy consumption, so that the problem is more emphasized. Energy conservation and consumption reduction are measures which are feasible technically and reasonable economically, so that the utilization efficiency of energy is improved, and the energy consumption is reduced to the maximum extent.
The acetic acid or propionic acid device generates a lot of energy in the production process, and also has more waste heat resources, such as reaction heat of acetic acid or propionic acid, however, the waste heat resources cannot be well recycled in the existing acetic acid or propionic acid plant, and part of plants reform a liquid phase circulation cooler of a reactor into a steam generator, but a gas phase still adopts a water cooler, and with the increase of the production scale of the acetic acid or propionic acid device, the waste heat carried in the gas phase is inevitably increased, so that the water consumption is increased, and the energy saving and consumption reduction are not facilitated. In conclusion, the prior art has the problem of waste of reaction heat in the preparation process of acetic acid or propionic acid.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a sour propionic acid device reactor biphase heat recovery system for solve the extravagant problem of reaction heat in acetic acid or the propionic acid preparation process.
In order to solve the technical problem, the utility model discloses a following technical scheme realizes:
a two-phase heat recovery system of a acetic acid propionic acid device reactor comprises a fluid stirring reactor, wherein the fluid stirring reactor is a reaction site in the preparation process of acetic acid or propionic acid, and is provided with a gas inlet and a liquid inlet, and the gas inlet and the liquid inlet are respectively used for adding gas-phase and liquid-phase raw materials into the fluid stirring reactor. When the reaction occurs in the fluid agitation reactor, a large amount of heat is generated, and thus a part of the liquid is evaporated into a gas phase during the reaction. The heat recovery system further comprises a gas-phase waste heat recovery device, the fluid stirring reactor is provided with a first gas-phase outlet and a reaction liquid outlet, and the gas-phase waste heat recovery device is connected with the first gas-phase outlet of the fluid stirring reactor and used for performing heat recovery on gas exhausted from the fluid stirring reactor. The gas phase waste heat recovery device can adopt a steam generator, and the gas waste heat is utilized to heat boiler water to prepare steam, so that steam can be generated as a byproduct during the preparation of the acetic acid propionic acid. The steam generator comprises a tube side and a shell side, wherein the tube side is a pipeline through which high-temperature gas flows, the shell side of the steam generator is connected with a boiler water pipe, and the tube side passes through the inside of the shell side, so that the high-temperature gas in the tube side heats the boiler water in the shell side. The gas in the gas phase in the fluid stirring reactor is discharged from the first gas phase outlet and then enters the tube side of the steam generator, and the tube side and the shell side of the steam generator exchange heat. The gas temperature in the high-temperature gas phase in the tube pass is transferred to the shell pass to heat boiler water in the shell pass, so that the gas waste heat in the tube pass is utilized. Therefore, after the first gas phase outlet of the fluid stirring reactor is connected with the steam generator, the problem of large waste of reaction heat of acetic acid or propionic acid is solved.
The fluid stirring reactor adopts a liquid phase waste heat recovery device to recover heat of reaction liquid, and the liquid phase waste heat recovery device can adopt a circulating cooler. The circulation cooler also comprises a tube side and a shell side, wherein the tube side is a flow passage of the reaction liquid, and the shell side is connected with a boiler water pipe. The tube side passes through the inside of the shell side, so that the boiler water in the shell side can be heated by the reaction liquid. And the tube pass of the circulating cooler is connected with the reaction liquid outlet, so that the circulating cooler is used for carrying out heat recovery on the liquid phase discharged from the fluid stirring reactor. The reaction liquid enters the tube side of the circulating cooler, the high-temperature reaction liquid exchanges heat with boiler water in the shell side through the tube side, so that the heat of the reaction liquid is transferred to the boiler water, namely, the boiler water is heated by the reaction liquid, and the waste heat of the reaction liquid is recycled.
Preferably, the heat recovery system further comprises a water cooler and a gas-liquid separator, the water cooler is connected with the gas-liquid separator and the tube pass of the steam generator, the gas-liquid separator is provided with a second gas-phase outlet and a liquid-phase outlet, the fluid stirrer is provided with a liquid-phase return port, and the liquid-phase outlet is connected with the liquid-phase return port. After the heat exchange of the gas discharged from the first gas phase outlet occurs in the steam generator, the temperature will drop, but the temperature of the gas will not drop to the normal temperature, so that a water cooler is arranged at the rear end of the steam generator to cool the gas discharged from the steam generator again. In the water cooler, part of the gas will change to the liquid phase due to the temperature decrease. To avoid waste, part of the liquid phase can be re-fed to the fluid stirrer for stirring, while part of the gaseous phase can be fed to another working unit. Therefore, a gas-liquid separator is arranged at the rear end of the water cooler and is used for separating a gas phase from a liquid phase in a gas-liquid mixture output by the water cooler.
Since the gas-liquid separator needs to separate the gas phase and the liquid phase, the gas-liquid separator is further provided with a gas phase outlet for discharging the gas separated by the gas-liquid separator after the gas phase and the liquid phase in the water cooler are separated.
The fluid stirring reactor is provided with a reaction liquid return port, and two ends of the tube pass of the circulating cooler are respectively connected with the reaction liquid outlet and the reaction liquid return port. And the heat diffusion temperature of the reaction liquid is reduced when the reaction liquid passes through the circulating cooler, and the reaction liquid with the reduced temperature returns to the fluid stirring reactor through the reaction liquid return port. Therefore, the effect of controlling the temperature in the fluid agitation reactor is achieved by the circulating cooling effect of the circulating cooler on the reaction liquid.
Therefore, the arrangement of the circulating cooler not only can achieve the effect of waste heat recovery, but also has the technical effects of recycling the reaction liquid and reducing the production cost, and meanwhile, the technical effect of controlling the internal temperature of the fluid stirring reactor is achieved.
The utility model discloses following beneficial effect has:
the utility model discloses the reaction heat to producing in the preparation of acetic acid or propionic acid process has been retrieved, has increased the utilization ratio to the energy, has reduced the waste to the reaction waste heat.
Drawings
In order to more clearly illustrate the technical solution of the present invention, the drawings used in the description of the embodiments will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to these drawings without creative efforts.
Fig. 1 is a schematic view of the internal structure of the present invention.
In the drawings, the components represented by the respective reference numerals are listed below:
1. a fluid agitation reactor; 11. a gas inlet; 12. a liquid inlet; 13. a reaction liquid outlet; 14. returning the reaction liquid; 15. a first gas phase outlet; 16. a liquid phase return port; 2. a circulation cooler; 21. a cooling pump; 22. a cooling circulation pipe; 23. a second boiler water inlet; 24. a second steam outlet; 3. a steam generator; 31. a first boiler water inlet; 32. a first steam outlet; 4. a water cooler; 41. a circulating water inlet; 42. a circulating water outlet; 5. a gas-liquid separator; 51. a liquid phase outlet; 52. a second gas phase outlet.
Detailed Description
The technical solution of the present invention is clearly and completely explained below with reference to the accompanying drawings through the concrete implementation of the embodiments of the present invention.
Example one
Please refer to fig. 1, the utility model relates to a propionic acid acetate device reactor biphase heat recovery system, including fluid stirring reactor 1, steam generator 3 and circulative cooler 2, fluid stirring reactor 1 is provided with first gaseous phase export 15 and reaction liquid export 13, steam generator 3's tube side with first gaseous phase export 15 is connected, circulative cooler 2's tube side with reaction liquid export 13 is connected, steam generator 3's shell side with circulative cooler 2's shell side all is connected with the boiler water pipe.
The steam generator 3 is used for recovering the waste heat of the gas discharged from the fluid stirring reactor 1, and the circulation cooler 2 is used for recovering the waste heat of the liquid discharged from the fluid stirring reactor 1. The steam generator 3 and the circulation cooler 2 are both provided with tube sides and shell sides, the tube sides are both communicated with the fluid stirring reactor 1, and the shell sides are both communicated with boiler water pipes. So that the high-temperature liquid or high-temperature gas in the tube side heats the boiler water in the shell side. Boiler water is heated to generate steam, and the steam is input into a steam pipe network to be used in other procedures, so that waste heat recovery and energy recycling are realized.
For the sake of easy illustration of the boiler water tubes connecting the steam generator 3 and the recooler 2, the boiler water tubes connected to the steam generator 3 are therefore first boiler water tubes, which are connected to a first boiler water inlet 31 provided in the steam generator 3 for conveying boiler water from the first boiler water inlet 31 into the shell side of the steam generator 3. The boiler water pipe connected with the circulation cooler 2 is a second boiler water pipe, and the second boiler water pipe is connected with a second boiler water inlet 23 arranged on the circulation cooler and is also used for conveying boiler water from the second boiler water inlet 23 to the shell side of the circulation cooler 2.
It should be noted here that, since the reaction in the production method of producing acetic acid or propionic acid is an exothermic reaction, the reaction temperature of the reaction is too high to be advantageous for the reaction itself. Therefore, the reaction temperature needs to be controlled during the reaction, so that the temperature of the reaction solution is reduced by using the circulation cooler 2. In order to avoid waste of heat of the reaction liquid, the circulation cooler 2 is connected with a boiler water pipe, steam is prepared by utilizing the characteristic of high temperature of the reaction liquid, the aim of controlling the temperature of the reaction liquid is achieved, the heat of the reaction liquid is recycled, a byproduct steam is prepared by the heat, and extra economic benefit is generated.
After the gas is input into the steam generator 3 from the first gas phase outlet 15, the high-temperature gas is subjected to heat exchange in the steam generator 3, so that the temperature of the high-temperature gas is reduced, and the gas with the reduced temperature still has a certain temperature, and therefore the gas needs to be treated again. The heat recovery system further comprises a water cooler 4 and a gas-liquid separator 5, wherein the water cooler 4 is connected with the gas-liquid separator 5, the gas-liquid separator 5 is provided with a second gas-phase outlet 52 and a liquid-phase outlet 51, the fluid stirrer is provided with a liquid-phase return port 16, and the liquid-phase outlet 51 is connected with the liquid-phase return port 16.
The water cooler 4 is used to cool the gas discharged from the steam generator 3, and during the cooling process, part of the gas is liquefied into liquid, i.e. reaction liquid is condensed again. The liquefied part of the liquid, that is, the reaction solution in the fluid agitation reactor 1, is provided with a liquid phase return port 16 in order to reduce the waste of the reaction solution and to enable the reaction solution to be reused. The liquid phase return port 16 is used for re-conveying the reaction liquid condensed out from the water cooler 4 to the reflux body stirring reactor 1. In order to feed the condensed reaction solution into the fluid agitation reactor 1 again through the liquid phase return port 16, it is necessary to first perform gas-liquid separation on the gas-liquid mixture discharged from the water cooler 4. Therefore, a gas-liquid separator 5 is connected to the rear end of the water cooler 4 to separate the gas-liquid mixture discharged from the water cooler 4 into gas and liquid. The separated liquid phase portion is transported to the liquid phase return port 16 through the liquid phase outlet port 51, and then enters the fluid agitation reactor 1 from the liquid phase return port 16. The liquid phase outlet 51 is connected to the liquid phase return port 16 by a pipe. And the liquid phase part is conveyed into the reflux stirring reactor 1 again, so that the part of reaction liquid is reused, and the technical effect of reducing the production cost is achieved.
The water cooler 4 cools the gas channel inside by using circulating water, and is similar to the boiler water and tube pass heat exchange inside the steam generator 3 in nature. Since the temperature of the gas entering the water cooler 4 has already decreased to some extent, it is difficult to efficiently recycle the heat in the gas, and therefore, the gas is cooled. The water cooler 4 is provided with a circulating water inlet 41 and a circulating water outlet 42 which are used as interfaces of a circulating water pipe, so that circulating water can circularly enter the water cooler 4, and gas flowing through the water cooler 4 is cooled.
The gas-liquid separator 5 is provided with a second gas phase outlet 52 for discharging the separated gas. The gas phase portion separated from the gas-liquid mixture is discharged from the second gas phase outlet 52 to other working units for use.
The fluid stirring reactor 1 is provided with a reaction liquid return port 14, and two ends of the tube pass of the circulating cooler 2 are respectively connected with the reaction liquid outlet 13 and the reaction liquid return port 14. That is, after the reaction solution enters the circulation cooler 2, the reaction solution heats the boiler water, and the temperature of the reaction solution itself decreases. The reaction liquid is returned to the fluid agitation reactor 1 through the reaction liquid return port 14 after the temperature of the reaction liquid is lowered. The reaction liquid is circulated between the fluid agitation reactor 1 and the circulation cooler 2, and a temperature decrease of the reaction liquid occurs during the circulation flow of the reaction liquid. The provision of the circulation cooler 2 also has the effect of controlling the temperature of the reaction liquid in the fluid agitation reactor 1.
After the boiler water in the shell side of the steam generator 3 and the shell side of the circulating cooler 2 is heated, steam is formed, and the steam is used as a byproduct in the preparation process of the acetic acid propionic acid. The steam formed needs to be treated in order to avoid wasting energy. Therefore, the shell side of the steam generator 3 is provided with a first steam outlet 32, the shell side of the circulating cooler 2 is provided with a second steam outlet 24, and the first steam outlet 32 and the second steam outlet 24 are both connected to a steam pipe network. The steam is conveyed to the steam pipe network, so that the steam can be applied to other working units, and the purpose of recycling the recovered energy is achieved.
The steam generator 3 and the circulation cooler 2 are equivalent to a hollow shell structure provided with pipelines, a shell of the hollow shell structure is used for containing boiler water and is connected with the boiler water pipe, and the pipelines in the hollow shell structure are channels of high-temperature gas or high-temperature liquid. The heat of the high-temperature gas or the high-temperature liquid is transferred to the boiler water from the pipe wall of the pipeline in a heat transfer mode, so that the boiler water is heated. The shape of the hollow shell structure can refer to the shape of a cylindrical tank body.
After the operation of the fluid agitation reactor 1 is completed, the reaction liquid after the completion of the reaction needs to be transferred to other downstream operation units. Therefore, two pipes are connected to the reaction liquid outlet 13 of the fluid agitation reactor 1, one of the pipes is connected to the tube side of the circulation cooler 2, and the other pipe guides the reaction liquid to other operation units downstream. When the reaction is carried out, the reaction liquid only enters the pipeline connected with the circulating cooler 2 and does not enter the pipelines leading to other working units; after the reaction is completed, the reaction liquid is introduced not into the pipe connected to the circulation cooler 2 but into the pipe leading to other working units. The control of the flow direction of the reactant liquid can be achieved by providing shut-off valves on both of the conduits. When the two stop valves are opened and closed one by one, the reaction liquid can only enter the pipeline with the opened stop valves but can not enter the pipeline with the closed stop valves.
A cooling pump 21 is arranged between the reaction liquid outlet 13 of the fluid stirring reactor 1 and the tube side of the circulating cooler 2. Compared with the gas flowing under the action of gas pressure and temperature, the gas flowing does not need additional power, but the flowing of the reaction liquid needs to be provided with separate power to realize circulating flow. The cooling pump 21 is thus used to power the flow of the reaction liquid. Note that the cooling pump 21 is a name in the present embodiment, and the pump itself does not have a cooling function. The reaction liquid is made to circulate between the fluid agitator and the circulation cooler 2 by the pumping action of the cooling pump 21.
Preferably, after the reaction is finished, the reaction solution may be pumped to the circulation cooler 2 by the cooling pump 21, so as to recycle the residual heat of the reaction solution. After the temperature of the reaction liquid in the fluid agitation reactor 1 is lowered to a suitable temperature, another pipe connected to the reaction liquid outlet 13 is opened to discharge the reaction liquid.
After using the system of the present invention, the actual production conditions are as follows:
the reaction temperature in the fluid stirred reactor 1 was set at 185 ℃, the reaction pressure was set at 3.0MPa, and the methanol feed rate was set at 20 tons/hour. In this production state, the by-product steam 0.7MPa was 1.4 ton/hr.
Example two
This example provides another set of production data:
the reaction temperature in the fluid agitation reactor 1 was set at 195 ℃, the reaction pressure was set at 3.2MPa, and the ethanol feed amount was set at 1.25 ton/hour. In this production state, the by-product steam was 1.5 ton/hr at 0.5 MPa.
EXAMPLE III
This embodiment provides a new set of data:
the reaction temperature in the fluid agitation reactor 1 was set at 190 ℃, the reaction pressure was 3.0MPa, the methanol feed rate was 10 tons/hour, and the ethanol feed rate was 30 tons/hour. In this production state, the by-product steam 0.8MPa was 3 tons/hr.
It can be seen from the production data of the first, second and third embodiments that the system of the present invention uses steam as a byproduct, and whether methanol is used to prepare acetic acid or ethanol is used to prepare propionic acid, the quality of the raw material is used as a reference, and the yield of the byproduct is very high in the preparation process, i.e. the byproduct can generate obvious economic benefits. The system of the utility model has the technical effects of large recovery of waste heat and high utilization rate of energy.
In the present invention, the vapor generator 3 and the circulation cooler 2 are respectively used to recover the waste heat of the gas generated by the reaction and the reaction liquid. In other embodiments, devices such as a dividing wall type heat exchanger or a regenerative heat exchanger can be used to recover the waste heat, so as to achieve the purpose of energy conservation.
Claims (8)
1. The utility model provides a propionic acid acetate plant reactor biphase heat recovery system, includes fluid stirring reactor (1), its characterized in that: the device is characterized by further comprising a gas phase waste heat recovery device and a liquid phase waste heat recovery device, wherein the fluid stirring reactor (1) is provided with a first gas phase outlet (15) and a reaction liquid outlet (13), the gas phase waste heat recovery device is connected with the first gas phase outlet (15), and the liquid phase waste heat recovery device is connected with the reaction liquid outlet (13).
2. The acetic acid propionic acid plant reactor biphasic heat recovery system of claim 1, wherein: the gas phase waste heat recovery device is a steam generator (3), the liquid phase waste heat recovery device is a circulating cooler (2), the steam generator (3) and the circulating cooler (2) comprise a tube pass and a shell pass, the tube pass of the steam generator (3) is connected with the first gas phase outlet (15), the tube pass of the circulating cooler (2) is connected with the reaction liquid outlet (13), and the shell pass of the steam generator (3) and the shell pass of the circulating cooler (2) are connected with boiler water pipes.
3. The acetic acid propionic acid plant reactor biphasic heat recovery system of claim 2, wherein: still include water cooler (4) and vapour and liquid separator (5), water cooler (4) with vapour and liquid separator (5) with the tube side of steam generator (3) is connected, vapour and liquid separator (5) are provided with liquid phase export (51), fluid stirring reactor (1) is provided with liquid phase and returns mouth (16), liquid phase export (51) with liquid phase returns mouth (16) and is connected.
4. The acetic acid propionic acid plant reactor biphase heat recovery system of claim 3, characterized in that: the gas-liquid separator (5) is further provided with a second gas-phase outlet (52) for discharging the gas separated by the gas-liquid separator (5).
5. The acetic acid propionic acid plant reactor biphasic heat recovery system of claim 2, wherein: the fluid stirring reactor (1) is provided with a reaction liquid return opening (14), and two ends of the tube pass of the circulating cooler (2) are respectively connected with the reaction liquid outlet (13) and the reaction liquid return opening (14).
6. The acetic acid propionic acid plant reactor biphasic heat recovery system of claim 5, wherein: the shell side of the steam generator (3) is provided with a first steam outlet (32), the shell side of the circulating cooler (2) is provided with a second steam outlet (24), and the first steam outlet (32) and the second steam outlet (24) are connected to a steam pipe network.
7. The acetic acid propionic acid plant reactor biphase heat recovery system of claim 5, characterized in that: and a reaction liquid outlet (13) of the fluid stirring reactor (1) is connected with two pipelines, one pipeline is connected with the tube side of the circulating cooler (2), and the other pipeline guides the reaction liquid to other downstream operation units.
8. The acetic acid propionic acid plant reactor biphasic heat recovery system of claim 2, wherein: and a cooling pump (21) is arranged between the reaction liquid outlet (13) of the fluid stirring reactor (1) and the tube pass of the circulating cooler (2).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222711672 | 2022-10-14 | ||
| CN2022227116726 | 2022-10-14 |
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| Publication Number | Publication Date |
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| CN218654450U true CN218654450U (en) | 2023-03-21 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202222766620.9U Active CN218654450U (en) | 2022-10-14 | 2022-10-20 | Acetic acid propionic acid device reactor biphase heat recovery system |
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