CN218740270U - Energy-saving weak liquor distillation device - Google Patents
Energy-saving weak liquor distillation device Download PDFInfo
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- CN218740270U CN218740270U CN202223197853.8U CN202223197853U CN218740270U CN 218740270 U CN218740270 U CN 218740270U CN 202223197853 U CN202223197853 U CN 202223197853U CN 218740270 U CN218740270 U CN 218740270U
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Abstract
The utility model discloses an energy-saving fresh liquid distillation device, which comprises an ammonia still, a flash evaporator, a fresh liquid tower and a heat exchanger; the liquid outlet of the ammonia still is connected with the liquid inlet of the flash tank; the gas outlet of the flash tank is connected with the gas inlet of the weak liquid tower through a gas outlet header pipe of the flash tank; the gas outlet of the fresh liquid tower is connected with the gas inlet of the heat exchanger; a liquid outlet of the heat exchanger is connected with a thin liquid barrel; a liquid outlet of the dilute liquid barrel is communicated with a liquid inlet of the dilute liquid tower; the air outlet of the ammonia still is connected with a cooling device; the air outlet of the cooling device is connected with a separator; the gas outlet of the separator is connected with an absorption tower through a gas outlet header pipe; and the air outlet of the heat exchanger is communicated with the air outlet header pipe. The device effectively reduces the resistance of the dilute liquid tower and the cooling system and the air outlet pressure of the flash evaporator, the ammonia distillation process is changed from the original positive pressure distillation into micro-negative pressure or micro-positive pressure distillation, the distillation efficiency of ammonia can reach 100 percent, namely, the content of waste dilute liquid ammonia is zero, the flash evaporation steam quantity is improved, the energy is saved, and the device is low-carbon and environment-friendly.
Description
The technical field is as follows:
the utility model relates to a soda ash manufacturing field, concretely relates to energy-conserving weak liquor distillation plant.
Background art:
in the process of producing the soda ash, a typical positive pressure distillation process is usually adopted in the traditional ammonia distillation process, as shown in figure 1, waste liquid in an ammonia distillation tower 1 enters a flash evaporator 2, steam enters a weak liquid tower 3 after natural flash evaporation, heat exchange is carried out with condensate liquid from a weak liquid barrel 5, the air outlet of the weak liquid tower 3 and the air outlet of the ammonia distillation tower 1 are cooled by a cooling device 6, then the cooled air enters a separator 7 for separation, and finally the cooled air enters an absorption tower 8. The flash evaporation steam quantity of the waste liquid is about 150kg per 1t alkali produced by the device, and is 150-200kg lower than that of a vacuum distillation process, mainly because the temperature difference between the inlet liquid and the outlet liquid of the flash evaporator is small (the temperature of the waste liquid out of the tower is 110-115 ℃, the temperature is reduced to 105-107 ℃ after flash evaporation), and the discharge temperature of the waste liquid of the flash evaporator is high. The key factor causing the high temperature of the waste liquid of the flash evaporator is that the whole resistance of a weak liquor tower system is large, in the weak liquor distillation process, the gas discharged from the weak liquor tower and the gas discharged from an ammonia still are combined and enter a cooling system, and the resistance of the cooling system is increased due to the improvement of production load; the prior dilute liquid tower has the specification of phi 1800 multiplied by 2400 multiplied by 32980 and the designed steaming amount of 25-30m 3 And h, the pipe diameter of the air outlet main pipe of the flash tank is phi 350, and the production requirements cannot be met along with the increase of the production load.
In order to improve the flash steam amount of the flash evaporator, a vacuum distillation process technology can be adopted, namely, the vacuum degree of the air outlet of the ammonia gas cooler and the thin liquid tower is improved by additionally arranging a high vacuum absorption tower so as to overcome the resistance of the existing equipment. However, the added high vacuum system has the disadvantages of large investment, complex process flow, high operation difficulty and limited popularization. Therefore, there is a need for improvements in existing equipment that have increased flash steam production and energy savings.
The utility model has the following contents:
the utility model aims to solve the technical problem of providing an energy-conserving fresh liquid distillation plant of flash steam height, fresh liquid tower resistance low, energy saving.
The utility model discloses implement by following technical scheme:
the energy-saving fresh liquid distillation device comprises an ammonia still, a flash evaporator, a fresh liquid tower and a heat exchanger; the liquid outlet of the ammonia still is connected with the liquid inlet of the flash tank; the gas outlet of the flash tank is connected with the gas inlet of the weak liquid tower through a gas outlet main pipe of the flash tank; the gas outlet of the fresh liquid tower is connected with the gas inlet of the heat exchanger; a liquid outlet of the heat exchanger is connected with a dilute liquid barrel through a first condensate pipeline; a liquid outlet of the dilute liquid barrel is communicated with a liquid inlet of the dilute liquid tower; the air outlet of the ammonia still is connected with a cooling device; the air outlet of the cooling device is connected with a separator; the gas outlet of the separator is connected with an absorption tower through a gas outlet main pipe; and the air outlet of the heat exchanger is communicated with the air outlet header pipe. The waste liquid from the ammonia still enters the flash evaporator, enters the weak liquid tower after flash evaporation, exchanges heat with the condensate from the weak liquid barrel, and the formed gas enters the heat exchanger from a gas outlet at the upper end of the weak liquid tower for cooling; the condensate in the heat exchanger enters the thin liquid barrel; and the ammonia gas discharged from the ammonia still enters a separator for separation after being cooled by the cooling device, and the gas discharged from the separator and the gas discharged from the heat exchanger are converged into the gas outlet header pipe and are conveyed to the absorption tower. The gas discharged from the weak liquor tower is independently cooled by the heat exchanger, and the gas discharged from the ammonia still is cooled by the cooling device, so that compared with the cooling device shared by the weak liquor tower gas outlet and the ammonia still gas outlet in the original design, the gas outlet resistance of the ammonia still can be effectively reduced.
Further, the cooling device comprises an ammonia gas condenser and an ammonia gas cooler; and the air outlet of the ammonia condenser is connected with the air inlet of the ammonia cooler. And the ammonia gas discharged from the ammonia still enters the ammonia gas condenser for condensation, the cooled gas enters the ammonia gas cooler for cooling, and the cooled gas enters the separator.
Further, the liquid outlet of the ammonia condenser is communicated with the weak liquid barrel through a second condensate pipeline. And the condensate discharged by the ammonia condenser flows into the dilute liquid barrel through the second condensate pipeline.
Further, the liquid outlet of the separator is communicated with the second condensate pipeline. The separator separates the materials conveyed by the ammonia gas cooler, the separated gas enters the absorption tower, and the liquid enters the weak liquor barrel through the second condensate pipeline.
Further, one end, close to the light liquid barrel, of the first condensate pipe is provided with a U-shaped liquid seal; the U-shaped liquid seal comprises a positive U-shaped pipe and a reverse U-shaped pipe, and a liquid outlet of the positive U-shaped pipe is connected with a liquid inlet of the reverse U-shaped pipe; the height difference between the bottom of the regular U-shaped pipe and the top of the inverted U-shaped pipe is not less than 2000mm.
Further, one end, close to the light liquid barrel, of the second condensate pipe is provided with a U-shaped liquid seal; the U-shaped liquid seal comprises a positive U-shaped pipe and a reverse U-shaped pipe, and the liquid outlet of the positive U-shaped pipe is connected with the liquid inlet of the reverse U-shaped pipe; the height difference between the bottom of the regular U-shaped pipe and the top of the inverted U-shaped pipe is not less than 2000mm. The U-shaped liquid seal gas seal has good effect, and can prevent ammonia gas from the ammonia gas condenser, the separator or the heat exchanger from entering the dilute liquid barrel in a driving or abnormal process state.
Further, the pipe diameter of the main gas outlet pipe of the flash tank is phi 600. The pipe diameter of the air outlet main pipe of the flash generator is thickened, so that the resistance of a pipeline can be reduced.
Further, the heat exchanger is a corrugated pipe heat exchanger. The corrugated pipe heat exchanger has large pipe diameter and reduced resistance, and can achieve the function of reducing the resistance of the heat exchanger while meeting the cooling function.
Further, the weak liquor tower is a filler weak liquor tower; the specification of the packing dilute solution tower is phi 3000 × 38895. Compared with a bubble column and a sieve plate column, the filler weak liquid column has small resistance; the large-size filler dilute liquid tower can enhance the production capacity and increase the carrying area of the tower so that the resistance of the dilute liquid tower is lower.
Furthermore, the upper part of the filler weak liquor tower is provided with a distribution plate, the middle part is provided with three filler sections, and the lower part is provided with three filler sectionsIs provided with a storage barrel section. The dilute liquid of the dilute liquid barrel enters the dilute liquid tower, is uniformly sprayed on the filler section through a distribution plate in the filler dilute liquid tower, and evaporates NH in tower liquid in a way of countercurrent with the steam entering from the air inlet 3 And CO 2 The distilled liquid is used as waste thin liquid to enter a storage barrel section, and the waste thin liquid is conveyed to each working procedure for use through a pump.
The utility model has the advantages that:
the utility model provides an energy-saving weak liquor distillation device, which effectively reduces the resistance of a weak liquor tower and a cooling system and the air outlet pressure of a flash evaporator, the ammonia distillation process is changed from the original positive pressure distillation into micro negative pressure or micro positive pressure distillation, the distillation efficiency of ammonia can reach 100 percent, namely the waste weak liquor ammonia content is zero, and the flash evaporation steam volume is improved; the device has simple structure, does not need to be additionally provided with a vacuum absorption tower, simplifies the process flow and reduces the investment; after the device is used, the water consumption and the coal consumption are greatly reduced, the energy is saved, and the device is low-carbon and environment-friendly.
Description of the drawings:
in order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic diagram of a light liquid distillation apparatus according to the background art;
fig. 2 is a schematic structural diagram of an energy-saving weak liquor distillation device provided by the utility model.
The drawings illustrate the following: 1. an ammonia still; 2. a flash tank; 21. a main gas outlet pipe of the flash tank; 3. a weak liquor tower; 31. a distribution plate; 32. a filler section; 33. a barrel storage section; 4. a heat exchanger; 5. a dilute solution barrel; 51. a first condensate conduit; 52. a second condensate conduit; 53. u-shaped liquid seal; 6. a cooling device; 61. an ammonia gas condenser; 62. an ammonia gas cooler; 7. a separator; 8. an absorption tower; 9. and a gas outlet header pipe.
The specific implementation mode is as follows:
the technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by a person skilled in the art without making creative efforts belong to the protection scope of the present invention.
Example 1
An energy-saving weak liquor distillation device comprises an ammonia still 1, a flash evaporator 2, a weak liquor tower 3 and a heat exchanger 4. The liquid outlet of the ammonia still 1 is connected with the liquid inlet of the flash tank 2; the gas outlet of the flash tank 2 is connected with the gas inlet of the weak liquor tower 3 through a flash tank gas outlet main pipe 21, and the diameter of the flash tank gas outlet main pipe 21 is phi 600; the gas outlet of the weak liquor tower 3 is connected with the gas inlet of the heat exchanger 4; a liquid outlet of the heat exchanger 4 is connected with a thin liquid barrel 5 through a first condensate pipeline 51; the liquid outlet of the dilute liquid barrel 5 is communicated with the liquid inlet of the dilute liquid tower 3.
The air outlet of the ammonia still 1 is connected with a cooling device 6; the cooling device 6 comprises an ammonia gas condenser 61 and an ammonia gas cooler 62, wherein the air outlet of the ammonia gas condenser 61 is connected with the air inlet of the ammonia gas cooler 62; the gas outlet of the ammonia gas cooler 62 is connected with a separator 7; the gas outlet of the separator 7 is connected with an absorption tower 8 through a gas outlet header pipe 9. The air outlet of the heat exchanger 4 is communicated with an air outlet header pipe 9.
The liquid outlet of the ammonia condenser 61 is communicated with the weak liquid barrel 5 through a second condensate pipeline 52; the liquid outlet of the separator 7 communicates with a second condensate line 52. The first condensate pipe 51 is provided with a U-shaped liquid seal 53 at one end close to the dilute liquid barrel 5; one end of the second condensate pipe 52 close to the dilute liquid barrel 2 is provided with a U-shaped liquid seal 53; the U-shaped liquid seal 53 comprises a regular U-shaped pipe and an inverted U-shaped pipe, and the liquid outlet of the regular U-shaped pipe is connected with the liquid inlet of the inverted U-shaped pipe; the height difference between the bottom of the regular U-shaped pipe and the top of the inverted U-shaped pipe is not less than 2000mm. The heat exchanger 4 is a corrugated pipe heat exchanger, the diameter of the corrugated pipe heat exchanger is phi 1800, and the resistance drop is less than 2kPa. The dilute solution tower 3 is a filler dilute solution tower, and the specification of the dilute solution tower is phi 3000X 38895; the upper part is provided with a distribution plate 31, the middle part is provided with three sections of filling sections 32, and the lower part is provided with a storage barrel section 33.
When the device operates, the dilute liquid in the dilute liquid barrel 5 enters the dilute liquid tower 3 and is uniformly sprayed on the filler section 32 through the distribution plate 31 in the dilute liquid tower 3; the waste liquid from the ammonia still 1 enters a flash evaporator 2, enters a weak liquid tower 3 after flash evaporation, and NH in the weak liquid is evaporated in a countercurrent way 3 And CO 2 The distilled liquid is taken as waste weak liquid to enter a storage barrel section 33, the ammonia content of the waste weak liquid is zero, and the waste weak liquid is conveyed to each working procedure for use through a pump; the formed gas components comprise ammonia gas, carbon dioxide gas and water vapor, the gas enters the heat exchanger 4 from the gas outlet at the upper end of the dilute liquid tower 3 for cooling, the ammonia gas, the carbon dioxide gas and other gases are dissolved into condensed water extremely along with the condensation of the water vapor, the gas volume is reduced rapidly, the pressure in the heat exchanger 4 is reduced, and the resistance is reduced accordingly. The gas remaining in the heat exchanger 4 enters the absorption column 8 and the condensate enters the thin liquor drum 5 through a first condensate line 51. The ammonia gas discharged from the ammonia still 1 is cooled by an ammonia gas condenser 61 and an ammonia gas cooler 62 in sequence and then enters a separator 7 for gas-liquid separation, and the separator 7 conveys the gas with the temperature of 60-65 ℃ cooled by the cooling device 6 to the absorption tower 8 through a gas outlet header pipe 9. The ammonia gas discharged from the ammonia still 1 is condensed by the ammonia gas condenser 61 to obtain condensate, and the condensate obtained by the separation of the separator 7 enters the weak liquor barrel 5 through the second condensate pipeline 52. The first condensate pipe 51 and the second condensate pipe 52 are respectively provided with a U-shaped liquid seal 53 at one end close to the thin liquid barrel 5, the gas seal effect is good, and ammonia gas from the heat exchanger 4, the ammonia gas condenser 61 or the separator 7 can be prevented from entering the thin liquid barrel 5 in a driving or process abnormal state.
Example 2: a thin liquid distillation apparatus of the background art was modified according to example 1, and the specific data before and after modification are shown in the following table:
TABLE 1 relevant parameters before and after modification of the thin liquid distillation apparatus
As can be seen from Table 1, the present inventionThe pressure of the flash evaporator of the energy-saving weak liquid distillation device is reduced by 13.62kPa, and the flash steam amount of the waste liquid flash evaporator is increased. The temperature of the waste liquid discharged by the flash tank is reduced from 106.7 ℃ to 99.8 ℃, the temperature is reduced by 6.9 ℃, the steam consumption per ton of alkali can be saved by 87.71kg, 36 ten thousand tons of soda ash can be produced all year round, and the steam consumption is saved by 31575.6t. The device effectively reduces the resistance drop of a dilute liquid tower system, the pressure difference between the air outlet pressure and the bottom pressure is only 1.78kPa, and the dilute liquid distillation tower is converted into micro-negative pressure or micro-positive pressure distillation from the original positive pressure distillation, so that the resistance drop of the corrugated pipe heat exchanger is less than 2kPa, the distillation efficiency of ammonia in normal operation can reach 100 percent, namely the content of waste dilute liquid ammonia is zero. After improvement, the device reduces the consumption of circulating water and the amount of cooling water by 72m 3 The water utilization rate is improved; the energy consumption of unit products is reduced, 7.09kg of standard coal can be saved per ton of alkali produced, 2550.4t of standard coal is saved according to 36 ten thousand tons of soda produced all year round, and the method has the advantages of energy conservation and environmental protection.
The above description is only for the preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. An energy-saving weak liquor distillation device is characterized by comprising an ammonia still, a flash evaporator, a weak liquor tower and a heat exchanger; the liquid outlet of the ammonia still is connected with the liquid inlet of the flash evaporator; the gas outlet of the flash tank is connected with the gas inlet of the weak liquid tower through a gas outlet main pipe of the flash tank; the gas outlet of the dilute liquid tower is connected with the gas inlet of the heat exchanger;
a liquid outlet of the heat exchanger is connected with a thin liquid barrel through a first condensate pipeline; a liquid outlet of the dilute liquid barrel is communicated with a liquid inlet of the dilute liquid tower;
the air outlet of the ammonia still is connected with a cooling device; the air outlet of the cooling device is connected with a separator; the gas outlet of the separator is connected with an absorption tower through a gas outlet main pipe; and the air outlet of the heat exchanger is communicated with the air outlet header pipe.
2. An energy-saving weak liquor distillation device according to claim 1, wherein the cooling device comprises an ammonia gas condenser and an ammonia gas cooler; and the air outlet of the ammonia condenser is connected with the air inlet of the ammonia cooler.
3. An energy-saving weak solution distillation apparatus according to claim 2, wherein the liquid outlet of the ammonia gas condenser is communicated with the weak solution barrel through a second condensate pipeline.
4. An energy efficient weak liquid distillation apparatus according to claim 3 wherein the liquid outlet of said separator is in communication with said second condensate conduit.
5. An energy-saving weak liquid distillation device according to claim 3 or 4, wherein one end of the second condensate pipe close to the weak liquid barrel is provided with a U-shaped liquid seal; the U-shaped liquid seal comprises a positive U-shaped pipe and a reverse U-shaped pipe, and the liquid outlet of the positive U-shaped pipe is connected with the liquid inlet of the reverse U-shaped pipe; the height difference between the bottom of the regular U-shaped pipe and the top of the inverted U-shaped pipe is not less than 2000mm.
6. The energy-saving weak liquor distillation device according to claim 1, wherein one end of the first condensate pipeline close to the weak liquor barrel is provided with a U-shaped liquid seal; the U-shaped liquid seal comprises a positive U-shaped pipe and a reverse U-shaped pipe, and a liquid outlet of the positive U-shaped pipe is connected with a liquid inlet of the reverse U-shaped pipe; the height difference between the bottom of the regular U-shaped pipe and the top of the inverted U-shaped pipe is not less than 2000mm.
7. The energy-saving weak liquor distillation device according to claim 1, wherein the diameter of the outlet main pipe of the flash evaporator is phi 600.
8. An energy-saving weak liquid distillation apparatus according to claim 1, wherein the heat exchanger is a vertical bellows heat exchanger.
9. An energy-saving weak liquor distillation device according to claim 1, wherein the weak liquor tower is a packed weak liquor tower; the specification of the filler dilute liquid tower is phi 3000 × 38895.
10. An energy-saving fresh water distilling device according to claim 9, wherein the upper part of the packed fresh water tower is provided with a distribution plate, the middle part is provided with three sections of packing sections, and the lower part is provided with a storage barrel section.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202223197853.8U CN218740270U (en) | 2022-11-30 | 2022-11-30 | Energy-saving weak liquor distillation device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202223197853.8U CN218740270U (en) | 2022-11-30 | 2022-11-30 | Energy-saving weak liquor distillation device |
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| CN218740270U true CN218740270U (en) | 2023-03-28 |
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| CN202223197853.8U Active CN218740270U (en) | 2022-11-30 | 2022-11-30 | Energy-saving weak liquor distillation device |
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