CN220860685U - Device for recovering waste heat of ammonia distillation mother liquor in process of producing sodium carbonate by ammonia-soda process - Google Patents
Device for recovering waste heat of ammonia distillation mother liquor in process of producing sodium carbonate by ammonia-soda process Download PDFInfo
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- CN220860685U CN220860685U CN202322641139.1U CN202322641139U CN220860685U CN 220860685 U CN220860685 U CN 220860685U CN 202322641139 U CN202322641139 U CN 202322641139U CN 220860685 U CN220860685 U CN 220860685U
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- ammonia
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 119
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 56
- 238000004821 distillation Methods 0.000 title claims abstract description 39
- 239000012452 mother liquor Substances 0.000 title claims abstract description 33
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 title claims abstract description 26
- 229910000029 sodium carbonate Inorganic materials 0.000 title claims abstract description 13
- 238000009621 Solvay process Methods 0.000 title claims abstract description 10
- 239000002918 waste heat Substances 0.000 title claims abstract description 10
- 238000000034 method Methods 0.000 title claims description 20
- 230000008569 process Effects 0.000 title claims description 19
- 238000005406 washing Methods 0.000 claims abstract description 58
- 239000007789 gas Substances 0.000 claims abstract description 20
- 239000012071 phase Substances 0.000 claims abstract description 20
- 238000001816 cooling Methods 0.000 claims abstract description 18
- 239000007791 liquid phase Substances 0.000 claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 27
- 238000001704 evaporation Methods 0.000 abstract description 34
- 230000008020 evaporation Effects 0.000 abstract description 34
- 238000009834 vaporization Methods 0.000 abstract description 4
- 230000008016 vaporization Effects 0.000 abstract description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 10
- 235000017550 sodium carbonate Nutrition 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 8
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- 239000011780 sodium chloride Substances 0.000 description 5
- 238000003763 carbonization Methods 0.000 description 4
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 4
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 3
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 3
- 235000019738 Limestone Nutrition 0.000 description 3
- 238000001354 calcination Methods 0.000 description 3
- 239000001110 calcium chloride Substances 0.000 description 3
- 229910001628 calcium chloride Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000006028 limestone Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 235000017557 sodium bicarbonate Nutrition 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model provides a device for recovering waste heat of ammonia distillation mother liquor in an ammonia-soda process for producing sodium carbonate, which comprises a primary vacuum flash tank, a primary steam washing tower, a secondary vacuum flash tank, a secondary steam washing tower, a primary steam compressor and a secondary steam compressor, wherein the device comprises a main vacuum flash tank, a secondary steam washing tower, a primary steam compressor and a secondary steam compressor, wherein the main vacuum flash tank is connected with the main vacuum flash tank, the secondary vacuum flash tank is connected with the main vacuum flash tank, and the primary steam compressor is connected with the secondary steam compressor: the inlet of the primary vacuum flash tank is connected with the ammonia distillation tower, the liquid phase outlet is connected with the inlet of the secondary vacuum flash tank, and the gas phase outlet is connected to the secondary vapor compressor through the primary vapor washing tower; the gas phase outlet of the secondary vacuum flash tank is connected to a primary vapor compressor through a secondary vapor washing tower; the primary vapor compressor is connected with the secondary vapor compressor, and the outlet of the secondary vapor compressor is connected with the vapor inlet of the ammonia still. By adopting the serial multistage flash evaporation cooling and multistage high-energy-efficiency vapor compressor pressurization, flash evaporation steam is heated and pressurized and returned to the ammonia distillation tower for use, so that the vaporization latent heat of the flash evaporation steam is fully utilized, the energy is saved, the emission is reduced, and great economic and social benefits are realized.
Description
Technical Field
The utility model belongs to the technical field of chemical production, and particularly relates to a device for recovering waste heat of ammonia distillation mother liquor in a process for producing sodium carbonate by an ammonia-soda process.
Background
Soda ash is an important inorganic chemical raw material and is widely applied to the fields of light industry daily chemicals, chemical industry, food industry, metallurgy, textile, medicine and the like. The ammonia-soda process is one of the main processes for producing sodium carbonate, the production process generally takes salt and limestone as raw materials, ammonia is used as a material to be recycled in a system, and the chemical equation of the process is as follows:
NaCl+NH3+H2O+CO2→NaHCO3+NH4Cl
NaHCO3→Na2CO3+H2O+CO2
2NH4Cl+Ca(OH)2→2NH3+CaCl2+2H2O
The sodium chloride solution is made into ammonia brine after ammonia absorption, and reacts with carbon dioxide generated after limestone calcination in a carbonization tower under the condition of cooling by circulating water to generate sodium bicarbonate solid and carbonization reaction mother liquor taking ammonium chloride, sodium chloride and the like as solutes. Calcining sodium bicarbonate to obtain sodium carbonate, adding calcium hydroxide slurry prepared from calcium oxide generated after limestone calcination into carbonization reaction mother liquor in an ammonia distillation tower, directly heating and reacting by introducing steam, cooling ammonia gas generated by the reaction, absorbing the ammonia salt water with sodium chloride solution to obtain ammonia salt water, and returning the ammonia salt water to the carbonization tower to react with carbon dioxide to realize recycling of the ammonia gas; the ammonia distillation mother liquor mainly containing calcium chloride after ammonia distillation is generally directly discharged.
The ammonia distillation mother liquor after ammonia distillation can be subjected to flash evaporation operation to obtain concentrated and cooled mother liquor containing calcium chloride and the like, the concentrated and cooled mother liquor is directly discharged into a salt field or sea or is pressed into the underground of well salt for dissolving sodium chloride ore, flash evaporation steam generated by flash evaporation is generally cooled by indirect heat exchange of circulating cooling water, and heat is discharged to the atmosphere through a cooling tower. On the one hand, the heat of the flash steam is directly wasted, and on the other hand, a certain amount of circulating cooling water is consumed for cooling the flash steam. If a novel device and a novel process for recovering the residual heat of the ammonia distillation mother liquor can be provided, the device and the process have very important significance, and bring great economic and social benefits while saving energy and reducing emission.
Disclosure of utility model
The utility model aims to solve the defects in the prior art, and provides a device for recovering the waste heat of the ammonia distillation mother liquor in the process of producing sodium carbonate by an ammonia-soda process, which adopts a series multistage flash evaporation to cool and a multistage high-energy-efficiency vapor compressor to boost pressure, heats and pressurizes flash evaporation steam, returns the flash evaporation steam to an ammonia distillation tower again for use, and fully utilizes the vaporization latent heat of the flash evaporation steam; meanwhile, the circulating water quantity for cooling and heat exchanging of flash steam in the original flash evaporation cooling process is saved.
In order to achieve the above purpose, the present utility model adopts the following technical scheme:
An apparatus for recovering waste heat of ammonia distillation mother liquor in an ammonia-soda process for producing sodium carbonate, the apparatus comprises a primary vacuum flash tank, a primary steam washing tower, a secondary vacuum flash tank, a secondary steam washing tower, a primary steam compressor and a secondary steam compressor, wherein:
The inlet of the primary vacuum flash tank is connected with the mother liquor outlet of the ammonia distillation tower, the liquid phase outlet of the primary vacuum flash tank is connected with the inlet of the secondary vacuum flash tank, the gas phase outlet of the primary vacuum flash tank is connected with the gas phase inlet of the primary vapor washing tower, and the gas phase outlet of the primary vapor washing tower is connected with the inlet of the secondary vapor compressor; the gas phase outlet of the secondary vacuum flash tank is connected with the gas phase inlet of the secondary steam washing tower, and the gas phase outlet of the secondary steam washing tower is connected with the inlet of the primary steam compressor; the outlet of the primary vapor compressor is connected to the inlet of the secondary vapor compressor, and the outlet of the secondary vapor compressor is connected with the vapor inlet of the ammonia still.
The utility model is further provided that the temperature of the ammonia distillation mother liquor which is introduced into the primary vacuum flash tank is about 90 ℃, and after the temperature of the ammonia distillation mother liquor which is discharged from the secondary vacuum flash tank is about 65 ℃ after the temperature is reduced by flash evaporation twice, the ammonia distillation mother liquor is directly discharged or introduced into the subsequent process.
The utility model is further provided that the primary vacuum flash tank and the secondary vacuum flash tank are both connected with a vacuum pump to provide a vacuum environment required by vacuum flash evaporation in the tank.
The utility model is further arranged that the liquid phase inlets of the primary steam washing tower and the secondary steam washing tower are connected with a washing hot water pipeline and are used for introducing washing hot water into the steam washing tower to preheat flash steam.
The utility model is further arranged that the washing hot water is stored in the washing hot water tank and is connected with the primary steam washing tower and the secondary steam washing tower through the washing hot water pipeline.
The utility model further provides that the flash steam is compressed by the primary steam compressor and the secondary steam compressor with multi-stage high energy efficiency to obtain steam with the pressure of 0.05Mpa to 0.3Mpa, and the steam is introduced into the ammonia still for further utilization.
The present utility model is further configured such that the primary vapor compressor and the secondary vapor compressor may be one selected from a centrifugal vapor compressor, a screw vapor compressor, a roots vapor compressor, a reciprocating vapor compressor, and the like.
Compared with the prior art, the utility model has the following beneficial effects:
(1) The utility model adopts the serial multistage flash evaporation cooling and multistage high-energy-efficiency vapor compressors to boost pressure, heats and pressurizes the flash evaporation vapor twice, improves the temperature and pressure of the flash evaporation vapor, provides temperature and pressure conditions for the flash evaporation vapor to return to the ammonia still for use, fully utilizes the vaporization latent heat of the flash evaporation vapor, thereby reducing the consumption of the ammonia still from external steam supply, reducing the energy consumption of the ammonia still by 30-40 percent, and simultaneously reducing the emission of ammonia-distilling carbon dioxide by 30-40 percent.
(2) The device not only saves the circulating water quantity for cooling and heat exchanging in the original flash evaporation cooling process, but also utilizes the heat of the flash evaporation steam twice, thereby avoiding the waste of the heat discharged to the atmosphere directly through the cooling tower; the device and the process have excellent energy saving and emission reduction effects and great economic and social benefits.
Drawings
FIG. 1 is a flow chart of a device for recovering waste heat of ammonia distillation mother liquor in the process of producing sodium carbonate by an ammonia-soda process;
the reference numerals are:
1. The device comprises a primary vacuum flash tank, a primary steam washing tower, a secondary steam washing tower, a primary steam compressor, a secondary steam compressor, a primary ammonia steaming tower, a secondary steam washing tower and a washing hot water tank.
Detailed Description
The technical scheme of the utility model is further described below by the preferred embodiments with reference to the accompanying drawings.
In the present utility model, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present utility model can be understood by those of ordinary skill in the art according to the specific circumstances.
According to the utility model, as shown in fig. 1, a flow chart of a device for recovering waste heat of ammonia distillation mother liquor in an ammonia-soda process for producing sodium carbonate is provided, the device comprises a primary vacuum flash tank 1, a primary steam washing tower 2, a secondary vacuum flash tank 3, a secondary steam washing tower 4, a primary steam compressor 5 and a secondary steam compressor 6, wherein:
An inlet of the primary vacuum flash tank 1 is connected with a mother liquor outlet of the ammonia distillation tower 7, and is used for introducing ammonia distillation mother liquor at the temperature of about 90 ℃ into the primary vacuum flash tank 1, concentrating and cooling through vacuum flash evaporation, a liquid phase outlet of the primary vacuum flash tank 1 is connected with an inlet of the secondary vacuum flash tank 3, and is used for continuously introducing ammonia distillation mother liquor subjected to primary flash evaporation into the secondary vacuum flash tank 3, concentrating and cooling through vacuum flash evaporation, a gas phase outlet of the primary vacuum flash tank 1 is connected with a gas phase inlet of the primary steam washing tower 2, a gas phase outlet of the primary steam washing tower 2 is connected with an inlet of the secondary steam compressor 6, and is used for exchanging heat between primary flash evaporation steam and washing hot water in the primary steam washing tower 2, and introducing the primary flash evaporation steam into the secondary steam compressor 6 for heating and pressurizing after supersaturation; the liquid phase outlet of the secondary vacuum flash tank 3 obtains ammonia distillation mother liquor at the temperature of about 65 ℃, the ammonia distillation mother liquor is directly discharged or enters a subsequent process, the gas phase outlet of the secondary vacuum flash tank 3 is connected with the gas phase inlet of the secondary vapor washing tower 4, the gas phase outlet of the secondary vapor washing tower 4 is connected with the inlet of the primary vapor compressor 5, and the ammonia distillation mother liquor is used for exchanging heat of the secondary flash vapor with washing hot water in the secondary vapor washing tower 4, and the supersaturated ammonia distillation mother liquor is introduced into the primary vapor compressor 5 for heating and pressurizing; the outlet of the primary vapor compressor 5 is connected with the inlet of the secondary vapor compressor 6, and is used for introducing compressed vapor after primary pressurization into the secondary compressor for continuous temperature and pressure increase, the outlet of the secondary vapor compressor 6 is connected with the vapor inlet of the ammonia still 7, and the vapor compressed to 0.05Mpa to 0.3Mpa by multi-stage energy efficiency is introduced into the ammonia still 7 to supplement the heat of the ammonia still, so that the steam consumption of the ammonia still 7 is saved.
Further, the primary vacuum flash tank 1 and the secondary vacuum flash tank 3 are connected with a vacuum pump (not shown in the figure) to provide a vacuum environment in the vacuum flash tanks.
Furthermore, the liquid phase inlets of the primary steam washing tower 2 and the secondary steam washing tower 4 are connected with a washing hot water pipeline and are used for introducing washing hot water into the steam washing tower to preheat flash steam.
Further, the washing hot water is stored in a washing hot water tank 8 and is connected with the primary steam washing tower 2 and the secondary steam washing tower 4 through washing hot water pipelines.
Further, the primary vapor compressor 5 and the secondary vapor compressor 6 may be one selected from a centrifugal vapor compressor, a screw vapor compressor, a roots vapor compressor, a reciprocating vapor compressor, and the like.
The process for recovering the residual heat of the ammonia distillation mother liquor by adopting the device comprises the following steps of:
The ammonia distillation mother liquor leaving the ammonia distillation tower enters a primary vacuum flash tank to be cooled by primary vacuum flash evaporation, then enters a secondary vacuum flash tank to be cooled by secondary vacuum flash evaporation, and the ammonia distillation mother liquor at the temperature of about 65 ℃ is obtained to be directly discharged or enters the subsequent working procedure; the primary flash steam leaving the primary vacuum flash tank enters a primary steam washing tower, exchanges heat with washing hot water, heats up, and enters a secondary steam compressor; the secondary flash steam leaving the secondary vacuum flash tank enters a secondary steam washing tower, is subjected to heat exchange with washing hot water and temperature rise, enters a primary steam compressor for pressurization, enters a secondary steam compressor after the primary pressurization, is compressed and pressurized together with the primary flash steam, and is then introduced into an ammonia still for supplementing the heat of the ammonia still, so that the heat utilization of the flash steam is realized.
Compared with the prior art, the utility model has the following beneficial effects: the utility model adopts serial multistage flash evaporation cooling and multistage high-energy-efficiency steam engine compression pressurization to compress, heat and boost flash evaporation steam for two times, thereby improving the temperature and pressure of the flash evaporation steam, providing temperature and pressure conditions for the flash evaporation steam to return to the ammonia distillation tower again for utilization, fully utilizing the vaporization latent heat of the flash evaporation steam, reducing the consumption of steam supplied outside the ammonia distillation tower, and reducing the energy consumption of the ammonia distillation tower by 30 percent. Meanwhile, through the device and the process, the circulating water quantity for cooling and heat exchanging in the original flash evaporation cooling process is saved, and the heat of the flash evaporation steam is utilized for two times, so that the heat is prevented from being directly discharged to the atmosphere through the cooling tower and is wasted; the device and the process have excellent energy saving and emission reduction effects and great economic and social benefits.
The above description of the specific embodiments of the present utility model has been given by way of example only, and the present utility model is not limited to the above described specific embodiments. Accordingly, equivalent changes and modifications are intended to be included within the scope of the present utility model without departing from the spirit and scope thereof.
Claims (7)
1. The device for recovering the waste heat of the ammonia distillation mother liquor in the process of producing sodium carbonate by an ammonia-soda process is characterized by comprising a primary vacuum flash tank, a primary steam washing tower, a secondary vacuum flash tank, a secondary steam washing tower, a primary steam compressor and a secondary steam compressor, wherein:
The inlet of the primary vacuum flash tank is connected with the mother liquor outlet of the ammonia distillation tower, the liquid phase outlet is connected with the inlet of the secondary vacuum flash tank, the gas phase outlet is connected with the gas phase inlet of the primary steam washing tower, and the gas phase outlet of the primary steam washing tower is connected with the inlet of the secondary steam compressor;
The gas phase outlet of the secondary vacuum flash tank is connected with the gas phase inlet of the secondary steam washing tower, and the gas phase outlet of the secondary steam washing tower is connected with the inlet of the primary steam compressor;
The outlet of the primary vapor compressor is connected to the inlet of the secondary vapor compressor, and the outlet of the secondary vapor compressor is connected with the vapor inlet of the ammonia still.
2. The apparatus of claim 1, wherein the primary and secondary vacuum flash tanks are each connected to a vacuum pump for providing a vacuum environment within the tank required for vacuum flash.
3. The apparatus of claim 1, wherein the temperature of the ammonia distillation mother liquor introduced into the primary vacuum flash tank is about 90 ℃, and the temperature of the ammonia distillation mother liquor discharged from the secondary vacuum flash tank after two flash cooling is about 65 ℃.
4. The apparatus of claim 1, wherein the liquid phase inlets of the primary and secondary wash towers are each connected to a wash hot water line for introducing wash hot water into the wash tower to preheat flash steam.
5. The apparatus according to claim 4, wherein washing hot water is stored in a washing hot water tank, and is connected to the primary and secondary wash towers via the washing hot water pipe.
6. The apparatus of claim 1, wherein flash steam is multi-stage energy efficient compressed by said primary and secondary vapor compressors to produce 0.05Mpa to 0.3Mpa steam for waste heat utilization into said ammonia still.
7. The apparatus of claim 1, wherein the primary and secondary vapor compressors are selected from one of centrifugal vapor compressors, screw vapor compressors, roots vapor compressors, reciprocating vapor compressors.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322641139.1U CN220860685U (en) | 2023-09-27 | 2023-09-27 | Device for recovering waste heat of ammonia distillation mother liquor in process of producing sodium carbonate by ammonia-soda process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322641139.1U CN220860685U (en) | 2023-09-27 | 2023-09-27 | Device for recovering waste heat of ammonia distillation mother liquor in process of producing sodium carbonate by ammonia-soda process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220860685U true CN220860685U (en) | 2024-04-30 |
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ID=90822513
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322641139.1U Active CN220860685U (en) | 2023-09-27 | 2023-09-27 | Device for recovering waste heat of ammonia distillation mother liquor in process of producing sodium carbonate by ammonia-soda process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220860685U (en) |
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2023
- 2023-09-27 CN CN202322641139.1U patent/CN220860685U/en active Active
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