CN212272328U - Spray drying tower waste gas recovery device - Google Patents
Spray drying tower waste gas recovery device Download PDFInfo
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- CN212272328U CN212272328U CN202020718605.5U CN202020718605U CN212272328U CN 212272328 U CN212272328 U CN 212272328U CN 202020718605 U CN202020718605 U CN 202020718605U CN 212272328 U CN212272328 U CN 212272328U
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Abstract
The utility model discloses a spray drying tower waste gas recovery device, which comprises a cyclone separator, a first heat exchanger, a turbine, a generator, a second heat exchanger, a working medium pump, a waste gas pipeline, a working medium pipeline and a cooling water pipeline; the cyclone separator is provided with a waste gas inlet and is connected with the first heat exchanger through a waste gas pipeline, the first heat exchanger is provided with a waste gas discharge pipeline and is connected with the turbine through the working medium pipeline, the turbine is connected with the second heat exchanger through the working medium pipeline, the output shaft of the turbine is further connected with the generator, the second heat exchanger is connected with the working medium pump through the working medium pipeline, the two cooling water pipelines are connected with the second heat exchanger, the working medium pump is connected with the first heat exchanger through the working medium pipeline, and working medium fluid with the boiling point of 20-30 ℃ under standard conditions is arranged in the working medium pipeline. The waste heat recovery device has the advantages that powder materials can be recycled, and waste heat of low-temperature waste gas can be recovered.
Description
Technical Field
The utility model relates to a chemical industry field, concretely relates to spray drying tower waste gas recovery device.
Background
In the chemical field, a spray drying tower is commonly used for quickly crystallizing materials, firstly, hot air is introduced into the top of the drying tower, the materials are pumped to the top of the tower by a pump and sprayed into vaporous droplets through an atomizer, and the droplets are small in diameter and large in surface area, so that moisture is quickly evaporated after the droplets are contacted with the high-temperature hot air, and the droplets can be dried within a few seconds. However, the waste gas after drying brings out partial powder, which causes material waste, and the hot air temperature is still high, which causes a great deal of heat loss. For waste heat recovery, high-temperature gas is mainly recovered at the present stage, the temperature of a gas outlet of a spray drying tower is about 100 ℃, and the effect of using water as a working medium for waste heat recovery is not ideal.
SUMMERY OF THE UTILITY MODEL
To the not enough of above-mentioned prior art existence, the utility model provides a spray drying tower waste gas recovery device, it has can recycle powder material, and can carry out the advantage of retrieving to the waste heat of low temperature waste gas.
The utility model adopts the technical proposal that:
a spray drying tower waste gas recovery device comprises a cyclone separator, a first heat exchanger, a turbine, a generator, a second heat exchanger, a working medium pump, a waste gas pipeline, a working medium pipeline and a cooling water pipeline; the top of the side curved surface of the cyclone separator is provided with a waste gas inlet, the top surface of the cyclone separator is connected with a waste gas inlet of the first heat exchanger through a waste gas pipeline, a waste gas outlet of the first heat exchanger is provided with a waste gas discharge pipeline, a working medium outlet of the first heat exchanger is connected with a working medium inlet of the turbine through the working medium pipeline, a working medium outlet of the turbine is connected with a working medium inlet of the second heat exchanger through the working medium pipeline, an output shaft of the turbine is also connected with the generator, a working medium outlet of the second heat exchanger is connected with an input end of the working medium pump through the working medium pipeline, two cooling water pipelines are respectively connected with a cooling water inlet and a cooling water outlet of the second heat exchanger, and an output end of the working medium pump is connected with the working medium inlet of the first heat exchanger through the working medium pipeline, the working medium pipeline is internally provided with working medium fluid with the boiling point of 20-30 ℃ under the standard condition.
After the waste gas passes through the cyclone separator, dust in the waste gas flows out from an outlet at the lower end of the cyclone separator, residual heat gas flows out from a gas outlet at the top end of the cyclone separator and enters the first heat exchanger along a waste gas pipeline, the residual heat gas exchanges heat with working fluid in the first heat exchanger and evaporates the working fluid from a liquid phase to a gas phase, the working fluid flows through a turbine along a working fluid pipeline, the working fluid expands and works in the turbine to convert energy into mechanical energy, the mechanical energy is converted into electric energy again through a generator to be stored, the pressure of the working fluid after working is reduced, the working fluid is condensed into a liquid phase in the second heat exchanger, and the liquid phase is pumped into the first heat exchanger through a.
The whole process is based on Rankine cycle, and waste heat is recovered through four processes of isobaric heating to adiabatic expansion to isobaric heat release and then to adiabatic compression.
Preferably, the working fluid is isopentane.
The gas temperature at the outlet of the cyclone separator is only about 100 ℃, water with the boiling point of 100 ℃ is not easy to vaporize, isopentane with the boiling point of 28 ℃ and the like can be easily evaporated into a gas phase, and therefore the working medium is an excellent working medium which is easy to work.
Preferably, the first heat exchanger is a tubular heat exchanger and comprises more than two rows of serpentine tubes arranged in parallel and an outer wall, one end of each serpentine tube is connected with the exhaust gas pipeline, the other end of each serpentine tube is connected with the exhaust gas discharge pipeline, the working fluid is arranged between each serpentine tube and the outer wall, an opening for the working fluid to flow in is formed in the position, close to the bottom, of the outer wall, and an opening for the working fluid to flow out is formed in the position, close to the top, of the outer wall.
The heat exchange area can be greatly increased by taking a large number of side-by-side snakelike tube type heat exchangers as a heat exchange mode, the tube side is walked by the waste gas, the shell side is walked by the working medium fluid because a bottom which is a heating area is formed inside the first heat exchanger, the middle part is a boiling area, the top is a state of a gas phase area, and the high-temperature gas and the low-temperature working medium fluid enter from the bottom of the first heat exchanger and can enhance the heat exchange efficiency.
Preferably, the turbine is an impulse turbine, and comprises a transmission shaft, an impeller and a turbine casing, wherein the transmission shaft is connected with the generator.
The impulse turbine is selected instead of the screw expander because the low-boiling point working medium has large expansion ratio, small enthalpy difference and small volume flow, so the low-boiling point working medium turbine mostly adopts the impulse turbine with simple structure to achieve better conversion efficiency of internal energy and mechanical energy.
Preferably, the second heat exchanger is a straight-line tube type heat exchanger, and cooling water with the temperature of less than 20 ℃ is introduced into one of the two cooling water pipelines.
The boiling point of the working medium fluid is 20-30 ℃, so that the working medium can be converted into a liquid phase from a gas phase again by selecting cooling water with the temperature of less than 20 ℃.
The beneficial effects of the utility model include:
1. after the waste gas passes through the cyclone separator, dust in the waste gas flows out from an outlet at the lower end of the cyclone separator, residual heat gas flows out from a gas outlet at the top end of the cyclone separator and enters a first heat exchanger along a waste gas pipeline, the residual heat gas exchanges heat with working fluid in the first heat exchanger and evaporates the working fluid from a liquid phase to a gas phase, the working fluid flows through a turbine along a working fluid pipeline, the working fluid expands and works in the turbine to convert energy into mechanical energy, the mechanical energy is converted into electric energy again through a generator to be stored, the pressure of the working fluid after working is reduced, the working fluid is condensed into a liquid phase in a second heat exchanger, and the liquid phase is pumped into the first heat exchanger through a;
according to Rankine cycle, the whole process is respectively subjected to four processes of isobaric heating, adiabatic expansion, isobaric heat release and adiabatic compression to recover waste heat;
2. the gas temperature at the outlet of the cyclone separator is only about 100 ℃, water with the boiling point of 100 ℃ is not easy to vaporize, isopentane with the boiling point of 28 ℃ and the like can be easily evaporated into gas phase, and therefore the working medium becomes an excellent working medium which is easy to work;
3. the heat exchange area can be greatly increased by taking a large number of side-by-side serpentine tube type heat exchangers as a heat exchange mode, the waste gas flows away from the tube side, and the working medium fluid flows away from the shell side because a state that the bottom is a heating area, the middle is a boiling area and the top is a gas phase area is formed in the first heat exchanger, so that high-temperature gas and low-temperature working medium fluid enter from the bottom of the first heat exchanger to enhance the heat exchange efficiency;
4. the impulse turbine is selected instead of the screw expander because the low-boiling point working medium has large expansion ratio, small enthalpy difference and small volume flow, so the low-boiling point working medium turbine mostly adopts the impulse turbine with simple structure to achieve better conversion efficiency of internal energy and mechanical energy;
5. the boiling point of the working medium fluid is 20-30 ℃, so that the working medium can be converted into a liquid phase from a gas phase again by selecting cooling water with the temperature of less than 20 ℃.
Drawings
Fig. 1 is a schematic view of a spray drying tower waste gas recovery device according to an embodiment of the present invention;
fig. 2 is a top view of a spray drying tower waste gas recovery device according to an embodiment of the present invention;
FIG. 3 is a cross-sectional view of section A-A of FIG. 2;
fig. 4 is a sectional view of section B-B in fig. 3.
Reference numerals:
the system comprises a cyclone separator 1, a waste gas inlet 11, a first heat exchanger 2, a waste gas discharge pipeline 21, an outer wall 22, a serpentine tube array 23, a turbine 3, a transmission shaft 31, an impeller 32, a turbine shell 33, a second heat exchanger 4, a working medium pump 5, a generator 6, a waste gas pipeline 7, a working medium pipeline 8 and a cooling water pipeline 9.
Detailed Description
The embodiments of the present invention will be further explained with reference to the drawings.
Example 1:
as shown in fig. 1 and fig. 2, a spray drying tower waste gas recovery device comprises a cyclone separator 1, a first heat exchanger 2, a turbine 3, a generator 6, a second heat exchanger 4, a working medium pump 5, a waste gas pipeline 7, a working medium pipeline 8 and a cooling water pipeline 9; the top of the side curved surface of the cyclone separator 1 is provided with a waste gas inlet 11, the top surface of the cyclone separator 1 is connected with a waste gas inlet of the first heat exchanger 2 through a waste gas pipeline 7, a waste gas discharge port of the first heat exchanger 2 is provided with a waste gas discharge pipeline 21, a working medium outlet of the first heat exchanger 2 is connected with a working medium inlet of the turbine 3 through a working medium pipeline 8, a working medium outlet of the turbine 3 is connected with a working medium inlet of the second heat exchanger 4 through the working medium pipeline 8, an output shaft of the turbine 3 is further connected with a generator 6, a working medium outlet of the second heat exchanger 4 is connected with an input end of the working medium pump 5 through the working medium pipeline 8, two cooling water pipelines 9 are respectively connected with a cooling water inlet and a cooling water outlet of the second heat exchanger 4, an output end of the working medium pump 5 is connected with the working medium inlet of the first heat exchanger 2 through the working medium pipeline.
After the waste gas passes through the cyclone separator 1, dust in the waste gas flows out from an outlet at the lower end of the cyclone separator 1, residual heat gas flows out from a gas outlet at the top end of the cyclone separator 1 and enters the first heat exchanger 2 along the waste gas pipeline 7, the residual heat gas exchanges heat with working fluid in the first heat exchanger 2 and evaporates the working fluid from a liquid phase to a gas phase, the working fluid flows through the turbine 3 along the working fluid pipeline 8, the energy is converted into mechanical energy by expansion acting in the turbine 3, the mechanical energy is converted into electric energy again by the generator 6 and stored, the pressure of the working fluid after acting is reduced, the working fluid is condensed into a liquid phase in the second heat exchanger 4 and then is pumped into the first heat exchanger 2 again through the working fluid pump 5.
The whole process is based on Rankine cycle, and waste heat is recovered through four processes of isobaric heating, adiabatic expansion, isobaric heat release and adiabatic compression.
Example 2:
on the basis of example 1, the working fluid was isopentane.
The gas temperature at the outlet of the cyclone separator 1 is only about 100 ℃, water with the boiling point of 100 ℃ is not easy to vaporize, isopentane with the boiling point of 28 ℃ and the like can be easily evaporated into gas phase, and therefore the working medium is an excellent working medium which can easily do work.
Example 3:
as shown in fig. 1 and fig. 3, on the basis of embodiment 1, the first heat exchanger 2 is a tube type heat exchanger, and includes more than two rows of serpentine tubes 23 and outer walls 22 arranged side by side, one end of the serpentine tube 23 is connected to the exhaust gas pipeline 7, the other end is connected to the exhaust gas discharge pipeline 21, the working fluid is disposed between the serpentine tube 23 and the outer wall 22, an opening for the working fluid to flow in is disposed near the bottom of the outer wall 22, and an opening for the working fluid to flow out is disposed near the top of the outer wall 22.
The heat exchange area can be greatly increased by taking a large number of parallel snakelike tube array 23-type heat exchangers as a heat exchange mode, the tube pass is walked by waste gas, the shell pass is walked by working medium fluid because a bottom which is a heating area is formed inside the first heat exchanger 2, the middle part is a boiling area, the top is a state of a gas phase area, and high-temperature gas and low-temperature working medium fluid enter from the bottom of the first heat exchanger 2 and can enhance the heat exchange efficiency.
Example 4:
as shown in fig. 1 and 4, in embodiment 1, the turbine 3 is an impulse turbine, and includes a drive shaft 31, an impeller 32, and a turbine casing 33, and the drive shaft 31 is connected to the generator 6.
The impulse turbine is selected instead of the screw expander because the low-boiling point working medium has large expansion ratio, small enthalpy difference and small volume flow, so the low-boiling point working medium turbine mostly adopts the impulse turbine with simple structure to achieve better conversion efficiency of internal energy and mechanical energy.
Example 5:
on the basis of the embodiment 1, the second heat exchanger 4 is a straight-line tubular heat exchanger, and cooling water with the temperature of less than 20 ℃ is introduced into one of the two cooling water pipelines 9.
The boiling point of the working medium fluid is 20-30 ℃, so that the working medium can be converted into a liquid phase from a gas phase again by selecting cooling water with the temperature of less than 20 ℃.
The above-mentioned embodiments only express the specific embodiments of the present invention, and the description thereof is specific and detailed, but not construed as limiting the scope of the present invention. It should be noted that, for those skilled in the art, without departing from the spirit of the present invention, several variations and modifications can be made, which are within the scope of the present invention.
Claims (5)
1. A spray drying tower waste gas recovery device is characterized by comprising a cyclone separator, a first heat exchanger, a turbine, a generator, a second heat exchanger, a working medium pump, a waste gas pipeline, a working medium pipeline and a cooling water pipeline; the top of the side curved surface of the cyclone separator is provided with a waste gas inlet, the top surface of the cyclone separator is connected with a waste gas inlet of the first heat exchanger through a waste gas pipeline, a waste gas outlet of the first heat exchanger is provided with a waste gas discharge pipeline, a working medium outlet of the first heat exchanger is connected with a working medium inlet of the turbine through the working medium pipeline, a working medium outlet of the turbine is connected with a working medium inlet of the second heat exchanger through the working medium pipeline, an output shaft of the turbine is also connected with the generator, a working medium outlet of the second heat exchanger is connected with an input end of the working medium pump through the working medium pipeline, two cooling water pipelines are respectively connected with a cooling water inlet and a cooling water outlet of the second heat exchanger, and an output end of the working medium pump is connected with the working medium inlet of the first heat exchanger through the working medium pipeline, the working medium pipeline is internally provided with working medium fluid with the boiling point of 20-30 ℃ under the standard condition.
2. The spray drying tower waste gas recovery device of claim 1, wherein the working fluid is isopentane.
3. The waste gas recovery device of claim 2, wherein the first heat exchanger is a tubular heat exchanger, and comprises more than two rows of serpentine tubes and an outer wall, the serpentine tubes are arranged in parallel, one end of each serpentine tube is connected with the waste gas pipeline, the other end of each serpentine tube is connected with the waste gas discharge pipeline, the working fluid is arranged between the serpentine tubes and the outer wall, an opening for the working fluid to flow in is formed in a position, close to the bottom, of the outer wall, and an opening for the working fluid to flow out is formed in a position, close to the top, of the outer wall.
4. The spray drying tower exhaust gas recovery device of claim 1, wherein the turbine is an impulse turbine.
5. The spray drying tower waste gas recovery device of claim 1, wherein the second heat exchanger is an inline tube heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020718605.5U CN212272328U (en) | 2020-04-30 | 2020-04-30 | Spray drying tower waste gas recovery device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020718605.5U CN212272328U (en) | 2020-04-30 | 2020-04-30 | Spray drying tower waste gas recovery device |
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| Publication Number | Publication Date |
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| CN212272328U true CN212272328U (en) | 2021-01-01 |
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| CN202020718605.5U Active CN212272328U (en) | 2020-04-30 | 2020-04-30 | Spray drying tower waste gas recovery device |
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| CN (1) | CN212272328U (en) |
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