CN116119686A - Sodium bicarbonate production process - Google Patents
Sodium bicarbonate production process Download PDFInfo
- Publication number
- CN116119686A CN116119686A CN202211667018.8A CN202211667018A CN116119686A CN 116119686 A CN116119686 A CN 116119686A CN 202211667018 A CN202211667018 A CN 202211667018A CN 116119686 A CN116119686 A CN 116119686A
- Authority
- CN
- China
- Prior art keywords
- liquid
- carbonization
- sodium bicarbonate
- caustic soda
- carbon dioxide
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 title claims abstract description 38
- 229910000030 sodium bicarbonate Inorganic materials 0.000 title claims abstract description 19
- 235000017557 sodium bicarbonate Nutrition 0.000 title claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 9
- 239000007788 liquid Substances 0.000 claims abstract description 128
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 123
- 238000003763 carbonization Methods 0.000 claims abstract description 97
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 86
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 43
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 43
- 235000011121 sodium hydroxide Nutrition 0.000 claims abstract description 41
- 238000000034 method Methods 0.000 claims abstract description 37
- 238000002425 crystallisation Methods 0.000 claims abstract description 34
- 230000008025 crystallization Effects 0.000 claims abstract description 34
- 239000000463 material Substances 0.000 claims abstract description 30
- 238000001035 drying Methods 0.000 claims abstract description 29
- 238000002360 preparation method Methods 0.000 claims abstract description 22
- 235000013373 food additive Nutrition 0.000 claims abstract description 14
- 239000002778 food additive Substances 0.000 claims abstract description 14
- 239000012452 mother liquor Substances 0.000 claims abstract description 12
- 238000009834 vaporization Methods 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 11
- 238000005406 washing Methods 0.000 claims abstract description 10
- 239000012467 final product Substances 0.000 claims abstract description 3
- 238000006243 chemical reaction Methods 0.000 claims description 16
- 238000007599 discharging Methods 0.000 claims description 15
- 239000006200 vaporizer Substances 0.000 claims description 14
- 238000005086 pumping Methods 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 8
- 239000003513 alkali Substances 0.000 claims description 7
- 239000008213 purified water Substances 0.000 claims description 4
- 238000012423 maintenance Methods 0.000 claims description 2
- 238000007689 inspection Methods 0.000 claims 1
- 239000000047 product Substances 0.000 abstract description 13
- 239000002994 raw material Substances 0.000 abstract description 7
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 abstract description 4
- 239000012535 impurity Substances 0.000 abstract description 4
- 230000015572 biosynthetic process Effects 0.000 abstract description 2
- 238000003786 synthesis reaction Methods 0.000 abstract description 2
- 239000002351 wastewater Substances 0.000 abstract 1
- 230000001276 controlling effect Effects 0.000 description 14
- 238000000926 separation method Methods 0.000 description 9
- 230000008016 vaporization Effects 0.000 description 9
- 238000004806 packaging method and process Methods 0.000 description 8
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 238000010981 drying operation Methods 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 3
- 150000003841 chloride salts Chemical class 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- 229910000272 alkali metal oxide Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000872 buffer Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
- C01D7/02—Preparation by double decomposition
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
- C01D7/22—Purification
- C01D7/24—Crystallisation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a production process of sodium bicarbonate, which comprises the following steps: preparing caustic soda preparing liquid by adopting liquid caustic soda and process water; (ii) passing the liquid carbon dioxide to a vaporiser for vaporisation; (iii) introducing caustic soda preparation liquid and vaporized carbon dioxide into a carbonization tower for carbonization synthesis to obtain carbonized liquid; (iv) transferring the carbonized liquid into a crystallizer for crystallization, centrifuging and washing the crystallized liquid to obtain a wet material, and drying the wet material to obtain a final product. The invention adopts liquid caustic soda as raw material and adopts a two-step carbonization method, the raw material is in the grade of food additive, the yield of mother liquor is small, the impurity content of the product is low, the application frequency is increased, the discharge amount of waste water is reduced, and meanwhile, the product yield is high, the production cost is effectively reduced, and the sodium bicarbonate product with high quality and uniform and stable quality is ensured to be obtained.
Description
Technical Field
The invention belongs to the technical field of sodium bicarbonate production, and particularly relates to a sodium bicarbonate production process.
Background
Sodium bicarbonate is produced by taking sodium carbonate as a raw material and adopting a one-step carbonization method, wherein the one-step carbonization refers to the direct reaction of sodium carbonate and carbon dioxide as raw materials to produce sodium bicarbonate, and the obtained product has high impurity concentration, large mother liquor discharge, poor quality and unstable quality.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide the production of sodium bicarbonate.
In order to achieve the above purpose, the invention adopts the following technical scheme:
a process for producing sodium bicarbonate, comprising the following steps:
preparing caustic soda preparing liquid by adopting liquid caustic soda and process water;
(ii) passing the liquid carbon dioxide to a vaporiser for vaporisation;
(iii) pumping caustic soda preparation liquid into a carbonization tower, introducing carbon dioxide, controlling the air inlet pressure and flow of the carbon dioxide, detecting the pH value of carbonized liquid discharged from the bottom of the carbonization tower when the temperature of a carbonization section of the carbonization tower begins to rise, continuously conveying the caustic soda preparation liquid and the carbon dioxide into the carbonization tower after the detection is qualified, and collecting discharged carbonized liquid to a carbonized liquid barrel;
(iv) transferring the carbonized liquid obtained in the step (iii) into a crystallizer, controlling the temperature and the circulation time of materials by adopting a circulating cooling crystallization mode, and discharging the carbonized liquid into a crystallization finished liquid barrel after the temperature of the materials is less than or equal to 60 ℃; and (3) centrifuging and washing the crystallization completion liquid to obtain a wet material, and drying the wet material to obtain a final product.
In the technical scheme, the mass concentration of the caustic soda preparation liquid is 12% -20%.
In the technical scheme, the process water is purified water, crystallization mother liquor or washing mother liquor.
In the technical scheme, the liquid alkali is food additive grade liquid alkali; the liquid carbon dioxide is a food additive grade.
In the technical scheme, the temperature in the temperature of the vaporizer is 50-90 ℃.
In the above-mentioned aspect, the carbon dioxide gas inlet pressure in the step (iii) is 0.1MPa to 0.5MPa, and the flow rate is controlled to 200Nm 3 /h～600Nm 3 /h。
In the above technical solution, the drying method is microwave drying.
In the technical scheme, the standard of the qualified pH value of the carbonized liquid is that the pH value is less than or equal to 10.
In the technical scheme, the pressure at the top of the carbonization tower is 0-0.5 MPa.
In the above technical solution, the lower part of the carbonization section in the step (iii) is a carbonization layer where carbonization occurs, and in the whole carbonization process in the step (iii), maintenance of the carbonization layer is achieved by controlling the air inlet pressure, the air inlet flow, the feed flow and the discharge flow of the carbon dioxide and caustic soda preparation liquid, and the carbonization layer is controlled to be at the highest temperature.
The beneficial effects of the invention are as follows:
the invention provides a production process for producing sodium bicarbonate by a two-step carbonization method, which adopts food additive sodium hydroxide and carbon dioxide as raw materials, prepares by liquid alkali and carbon dioxide vaporization, carbonizes and synthesizes the raw materials into carbonized liquid in a carbonization tower, and then carries out cooling crystallization, centrifugal separation and drying to produce a high-quality sodium bicarbonate product with higher stability and yield; compared with the same industry, the method adopts the raw materials with higher quality, and the impurities carried in the product are far lower than the Chinese pharmacopoeia standard; meanwhile, the enrichment period of impurity ions is prolonged, the application frequency of mother liquor (caustic soda preparation liquor) is increased, and the material loss and environmental pollution caused by mother liquor discharge are reduced; the continuous and stable reaction process in the carbonization tower is maintained by adopting a carbonization layer control method, and the carbon dioxide and the liquid alkali are fully reacted and timely conveyed to the next working procedure through flow, temperature gradient and pressure control, so that the stable technological parameters and uniform quality of the output carbonization liquid in the carbonization synthesis process are ensured; the circulating cooling crystallization mode is adopted, the solid-liquid ratio of the crystallization completion liquid is increased, the material quantity taken away by the crystallization mother liquid quantity is reduced, and the yield of batch products is increased.
Detailed Description
In order to make the technical solution of the present invention better understood by those skilled in the art, the technical solution of the present invention will be further described with reference to the following specific embodiments.
A process for producing sodium bicarbonate, comprising the following steps:
formulation (i)
Pumping the food additive grade caustic soda liquid into a caustic soda preparation liquid tank by a pump, adding process water, and preparing caustic soda preparation liquid with the mass concentration of 16% +/-4%; the process water is purified water, crystallization mother liquor or washing mother liquor.
(ii) vaporization
And (3) opening a steam valve to heat the vaporizer, raising the temperature of the vaporizer to 50-90 ℃, introducing liquid carbon dioxide of the food additive grade into the vaporizer for vaporization, regulating a pressure regulating valve until the gas is filled in a carbon dioxide buffer tank, and enabling the carbon dioxide to enter a carbonization process through a filter for use.
(iii) carbonization
The carbonization process is completed in a carbonization tower.
The carbonization tower is a sieve plate tower, the lower part of the carbonization tower is a cooling section and consists of a plurality of coolers; the middle part and the upper part of the carbonization tower are carbonization sections, and a plurality of layers of tower plates are arranged; the carbonization tower is provided with five temperature measuring points T1-T5 from bottom to top, T1 and T2 are arranged in the cooling section, T3-T5 are arranged in the carbonization section, T1 is arranged at the liquid outlet, namely, carbonized liquid or carbonized liquid is discharged, T3 is arranged at the position of the first tower plate, T4 is arranged at the position of the middle tower plate, T5 is arranged at the position of the top tower plate, and T2 is arranged between T1 and T3. The carbonization layer (carbonization reaction generation area) is arranged in the area of T3-T4, so that T3 is more than T2, T4 is more than T5, the carbonization layer T3-T4 is maintained at the highest temperature, and the pressure of the top of the tower is maintained at 0-0.5 MPa;
for example, when the height of the carbonization tower is 25m, the cooling section is 7m, the carbonization section is 18m, 15 trays are arranged in the carbonization section, T3 is arranged at the 1# tray, T4 is arranged at the 6# tray, and T5 is arranged at the 13# tray.
The flow of the carbonization tower is as follows: introducing carbon dioxide from the lower part of the carbonization tower, adding caustic soda preparation liquid from the upper part of the carbonization tower, and removing carbonized liquid and carbonized liquid from the bottom of the carbonization tower; carbon dioxide in the carbonization tower goes upwards from the bottom. The carbonization liquid is a material generated after the reaction of caustic soda preparation liquid and carbon dioxide, is discharged from the bottom of the tower, and is measured by the pH value of the carbonization liquid to determine whether the reaction is complete or not, and the carbonization liquid which is collected after the completion of the reaction is determined to be the carbonization completion liquid.
The whole carbonization process comprises a tower laying stage and a continuous stage:
(a) And (3) tower laying: zero start of process
Firstly pumping caustic soda preparation liquid into a carbonization tower, continuously introducing carbon dioxide into the carbonization tower, and then starting reaction with the caustic soda preparation liquid, wherein the temperature is raised from the bottom of the tower upwards due to heat release of the reaction. When the temperature of T1-T3 is not increased any more, the reaction is proved to be completed in the stage; the carbon dioxide inlet pressure and flow rate at this stage are controlled to be 0.1 MPa-0.5 MPa and 200Nm respectively 3 /h～600Nm 3 /h；
(b) Continuous phase
When the temperature of the temperature measuring point of the carbonization tower T4 begins to rise, the pH value of the carbonization liquid discharged from the liquid discharge port is checked, after the detection is qualified (the pH value is less than or equal to 10), the intake pressure and the flow of the carbon dioxide in the previous stage are maintained, the carbon dioxide is continuously conveyed into the carbonization tower, caustic soda configuration liquid is continuously conveyed into the carbonization tower, and meanwhile, carbonization completion liquid is discharged to a carbonization completion liquid barrel.
After T4 starts to heat up, the carbonization reaction is proved to reach the position of the middle tower plate (6 # tower plate), and the reaction is finished from the bottom of the tower to the position of the middle tower plate (6 # tower plate) or below. Synchronously feeding alkali liquor, carbon dioxide and discharging carbonized liquid, and according to the carbon dioxide: sodium hydroxide = 1:1.1, adjusting the feed and discharge flow in an equivalent ratio, and achieving dynamic reaction balance in a carbonization tower, so that the discharged materials are carbonized liquid after the reaction is finished;
with the discharge of the carbonized liquid, as long as the carbonized layer is maintained above T3 and below T4, the temperature of the area is necessarily the highest, and the area above T4 is responsible for absorbing the carbon dioxide which is not absorbed in the area of T3-T4, so as to ensure the yield. The area below T3 is carbonized liquid after reaction, heat is not released, and the temperature is reduced by carbon dioxide continuously in the downward moving process, so that the temperature is lower than that when carbonization is finished;
if the temperature gradient cannot be maintained, that is, the reaction speed and the discharge speed cannot be matched, when T5 is greater than T4, the carbonization layer is proved to move upwards, and the discharge amount is required to be increased or the feed amount is required to be reduced to be adjusted to the original area; when T2 is larger than T3, the carbonization layer moves downwards, and then the discharging colleague needs to be reduced to increase the feeding to correct the deviation (the reduction or the increase can be slowly adjusted according to the amplitude of 5%).
The invention arranges the carbonization layers at T3-T4, which is easy to cause incomplete carbonization reaction due to the too low carbonization layer; if the carbonization layer is too high, carbon dioxide overflow is easy to occur, and the yield is sacrificed.
(iv) crystallization and centrifugal separation
And transferring the carbonized liquid into a crystallizer through a carbonized liquid pump, controlling the temperature and the circulation time of the materials by adopting a circulation cooling crystallization mode, and discharging the carbonized liquid into a crystallization completion liquid barrel after the temperature of the materials is less than or equal to 60 ℃. Transferring the crystallization completion liquid into a centrifuge through a crystallization completion liquid pump, and transferring wet materials into a dryer for drying after separation and washing. The crystallization is carried out by adopting a forced external circulation type crystallizer, the crystallizer comprises a crystallization chamber, a forced circulation pump, a heat exchanger and salt collecting legs, the crystallization chamber is communicated with the heat exchanger through a circulation pipeline, the forced circulation pump is arranged on the circulation pipeline, and the salt collecting legs are used for collecting salt after crystallization in the crystallizer;
(v) drying and packaging
The drying operation is performed using a microwave drying technique. And (3) turning on a belt conveyor and a switch of a magnetron box, controlling the belt conveying speed to be 2-6 m/min, transferring wet materials into a dryer for drying, and packaging after the drying is finished to obtain the product.
Example 1
(1) Preparing
Pumping the food additive grade caustic soda liquid into a caustic soda preparation liquid tank by a pump, adding purified water, and preparing the caustic soda preparation liquid with the concentration of 16%.
(2) Vaporization
The vaporizer is heated by opening the steam valve, the temperature of the vaporizer is increased to 80 ℃, and the liquid carbon dioxide of the food additive grade is introduced into the vaporizer for vaporization.
(3) Carbonization
Pumping 13m3 caustic soda configuration liquid into a carbonization tower, and controlling the air inlet pressure and flow of carbon dioxide at 0.3MPa and 500Nm3/h respectively. When the temperature of the temperature measuring point of the carbonization tower T4 begins to rise, the pH value (pH is less than or equal to 10) of the carbonized liquid is checked. And after the test is qualified, continuously conveying caustic soda preparation liquid and carbon dioxide into the carbonization tower, and discharging carbonization liquid to a carbonization completion liquid barrel. By adjusting the air inlet pressure, the air inlet flow, the feeding flow and the discharging flow, the carbonization layer is kept in the area of T3-T4, so that T3 is more than T2, T4 is more than T5, and the pressure of the top of the tower is kept at 0MPa.
(4) Crystallization and centrifugal separation
And transferring the carbonized liquid into a crystallizer through a carbonized liquid pump, controlling the temperature and the circulation time of the materials, and discharging the carbonized liquid into a crystallized liquid barrel when the temperature of the materials is less than or equal to 50 ℃. Transferring the crystallization completion liquid into a centrifuge through a crystallization completion liquid pump, and transferring wet materials into a dryer for drying after separation and washing.
(5) Drying and packaging
The drying operation is performed using a microwave drying technique. And (3) turning on a belt conveyor and a magnetron box switch, controlling the belt conveying speed to be 4m/min, transferring wet materials into a dryer for drying, and packaging after the drying is finished to obtain the product.
Example 2
(1) Preparing
Pumping the food additive grade caustic soda liquid into a caustic soda preparation liquid tank by a pump, adding crystallization mother liquor, and preparing the caustic soda preparation liquid with the concentration of 16%.
(2) Vaporization
The vaporizer is heated by opening the steam valve, the temperature of the vaporizer is increased to 80 ℃, and the liquid carbon dioxide of the food additive grade is introduced into the vaporizer for vaporization.
(3) Carbonization
Pumping 13m3 caustic soda configuration liquid into a carbonization tower, and controlling the air inlet pressure and flow of carbon dioxide at 0.3MPa and 500Nm respectively 3 And/h. CarbonizationWhen the temperature of the tower T4 begins to rise, the pH value (pH is less than or equal to 10) of the carbonized liquid is checked. And after the test is qualified, continuously conveying caustic soda preparation liquid and carbon dioxide into the carbonization tower, and discharging carbonization liquid to a carbonization completion liquid barrel. By adjusting the air inlet pressure, the air inlet flow, the feeding flow and the discharging flow, the carbonization layer is kept in the area of T3-T4, so that T3 is more than T2, T4 is more than T5, and the pressure of the top of the tower is kept at 0MPa.
(4) Crystallization and centrifugal separation
And transferring the carbonized liquid into a crystallizer through a carbonized liquid pump, controlling the temperature and the circulation time of the materials, and discharging the carbonized liquid into a crystallized liquid barrel when the temperature of the materials is less than or equal to 50 ℃. Transferring the crystallization completion liquid into a centrifuge through a crystallization completion liquid pump, and transferring wet materials into a dryer for drying after separation and washing.
(5) Drying and packaging
The drying operation is performed using a microwave drying technique. And (3) turning on a belt conveyor and a magnetron box switch, controlling the belt conveying speed to be 4m/min, transferring wet materials into a dryer for drying, and packaging after the drying is finished to obtain the product.
Example 3
(1) Preparing
Pumping the food additive grade caustic soda liquid into a caustic soda preparation liquid tank by a pump, adding crystallization mother liquor, and preparing the caustic soda preparation liquid with the concentration of 16%.
(2) Vaporization
The vaporizer is heated by opening the steam valve, the temperature of the vaporizer is increased to 80 ℃, and the liquid carbon dioxide of the food additive grade is introduced into the vaporizer for vaporization.
(3) Carbonization
Will be 13m 3 Pumping caustic soda configuration liquid into a carbonization tower, and controlling the air inlet pressure and flow of carbon dioxide to be 0.35MPa and 550Nm respectively 3 And/h. When the temperature of the temperature measuring point of the carbonization tower T4 begins to rise, the pH value (pH is less than or equal to 10) of the carbonized liquid is checked. And after the test is qualified, continuously conveying caustic soda preparation liquid and carbon dioxide into the carbonization tower, and discharging carbonization liquid to a carbonization completion liquid barrel. The carbonization layer is kept in the region of T3-T4 by adjusting the air inlet pressure, the air inlet flow, the feeding flow and the discharging flow, so that T3 is more than T2, T4 is more than T5, and the pressure of the top of the tower is kept at 0.5MPa。
(4) Crystallization and centrifugal separation
And transferring the carbonized liquid into a crystallizer through a carbonized liquid pump, controlling the temperature and the circulation time of the materials, and discharging the carbonized liquid into a crystallized liquid barrel when the temperature of the materials is less than or equal to 50 ℃. Transferring the crystallization completion liquid into a centrifuge through a crystallization completion liquid pump, and transferring wet materials into a dryer for drying after separation and washing.
(5) Drying and packaging
The drying operation is performed using a microwave drying technique. And (3) turning on a belt conveyor and a magnetron box switch, controlling the belt conveying speed to be 4m/min, transferring wet materials into a dryer for drying, and packaging after the drying is finished to obtain the product.
The products obtained in examples 1 to 3 are compared with the standard as follows:
| project | Content/% | Loss on drying/% | Alkalinity (basicity) | Chlorides (CPS) | Clarity of the product | Batch yield |
| Standard of | 99.6～100.5％ | ＜0.25％ | pH＜8.6 | ＜0.002％ | Should be clarified | 80～90％ |
| Example 1 | 100.2 | 0.013 | 8.43 | Much less than 0.002% | Clarifying | 82.1％ |
| Example 2 | 100.1 | 0.007 | 8.51 | Much less than 0.002% | Clarifying | 81.5％ |
| Example 3 | 100.0 | 0.006 | 8.37 | Much less than 0.002% | Clarifying | 83.3％ |
It should be noted that, without conflict, the embodiments of the present invention and features of the embodiments may be combined with each other.
The applicant declares that the above is only a specific embodiment of the present invention, but the scope of the present invention is not limited thereto, and it should be apparent to those skilled in the art that any changes or substitutions that are easily conceivable within the technical scope of the present invention disclosed by the present invention fall within the scope of the present invention and the disclosure.
Claims (10)
1. A production process of sodium bicarbonate is characterized in that: the method comprises the following steps:
preparing caustic soda preparing liquid by adopting liquid caustic soda and process water;
(ii) passing the liquid carbon dioxide to a vaporiser for vaporisation;
(iii) pumping caustic soda configuration liquid into a carbonization tower, introducing carbon dioxide, controlling the air inlet pressure and flow of the carbon dioxide, detecting the pH value of carbonized liquid discharged from the bottom of the carbonization tower when the temperature of a carbonization section of the carbonization tower begins to rise, and collecting discharged carbonized liquid to a carbonized liquid barrel after the carbonized liquid is qualified by inspection;
(iv) transferring the carbonized liquid obtained in the step (iii) into a crystallizer, controlling the temperature and the circulation time of materials by adopting a circulating cooling crystallization mode, and discharging the carbonized liquid into a crystallization finished liquid barrel after the temperature of the materials is less than or equal to 60 ℃; and (3) centrifuging and washing the crystallization completion liquid to obtain a wet material, and drying the wet material to obtain a final product.
2. The process for producing sodium bicarbonate according to claim 1, wherein: the mass concentration of the caustic soda preparation liquid is 12% -20%.
3. The process for producing sodium bicarbonate according to claim 1, wherein: the process water is purified water, crystallization mother liquor or washing mother liquor.
4. The process for producing sodium bicarbonate according to claim 1, wherein: the liquid alkali is food additive grade liquid alkali; the liquid carbon dioxide is a food additive grade.
5. The process for producing sodium bicarbonate according to claim 1, wherein: the temperature in the vaporizer is 50-90 ℃.
6. The process for producing sodium bicarbonate according to claim 1, wherein: the carbon dioxide inlet pressure in the step (iii) is 0.1-0.5 MPa, and the flow rate is controlled to be 200-600 Nm3/h 3 /h。
7. The process for producing sodium bicarbonate according to claim 1, wherein: the drying method is microwave drying.
8. The process for producing sodium bicarbonate according to claim 1, wherein: the standard of the qualified pH value of the carbonized liquid is that the pH value is less than or equal to 10.
9. The process for producing sodium bicarbonate according to claim 1, wherein: the pressure at the top of the carbonization tower is 0-0.5 MPa.
10. The process for producing sodium bicarbonate according to claim 1, wherein: the lower part of the carbonization section in the step (iii) is a carbonization layer in which carbonization reaction occurs, and in the whole carbonization process of the step (iii), the maintenance of the carbonization layer is realized by controlling the air inlet pressure, the air inlet flow, the feeding flow and the discharging flow of the carbon dioxide and caustic soda configuration liquid, and the carbonization layer is controlled to be at the highest temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211667018.8A CN116119686A (en) | 2022-12-22 | 2022-12-22 | Sodium bicarbonate production process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211667018.8A CN116119686A (en) | 2022-12-22 | 2022-12-22 | Sodium bicarbonate production process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116119686A true CN116119686A (en) | 2023-05-16 |
Family
ID=86303739
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211667018.8A Pending CN116119686A (en) | 2022-12-22 | 2022-12-22 | Sodium bicarbonate production process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116119686A (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5288472A (en) * | 1993-02-08 | 1994-02-22 | Ruiz Raymundo L | Process for the recovery of the sodium hydroxide and sodium chloride from the effluent of a diaphragm cell as solid sodium bicarbonate |
| CN1091395A (en) * | 1994-01-19 | 1994-08-31 | 李兴德 | The method of soda production from sodium sulfate |
| CN102134084A (en) * | 2011-01-22 | 2011-07-27 | 内蒙古博源工程有限责任公司 | System and method for producing calcined soda or producing calcined soda and baking soda |
| CN201914926U (en) * | 2011-01-22 | 2011-08-03 | 内蒙古博源工程有限责任公司 | System for realizing co-production of sodium carbonate and baking soda |
| CN108147435A (en) * | 2018-02-05 | 2018-06-12 | 重庆宜化化工有限公司 | A kind of carbonization technique for soda manufacture |
| CN110937612A (en) * | 2019-12-30 | 2020-03-31 | 中国天辰工程有限公司 | Process for preparing high-quality heavy soda ash by using crude sodium bicarbonate |
| CN112758959A (en) * | 2021-03-12 | 2021-05-07 | 自贡鸿鹤制药有限责任公司 | Preparation method of sodium bicarbonate |
-
2022
- 2022-12-22 CN CN202211667018.8A patent/CN116119686A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5288472A (en) * | 1993-02-08 | 1994-02-22 | Ruiz Raymundo L | Process for the recovery of the sodium hydroxide and sodium chloride from the effluent of a diaphragm cell as solid sodium bicarbonate |
| CN1091395A (en) * | 1994-01-19 | 1994-08-31 | 李兴德 | The method of soda production from sodium sulfate |
| CN102134084A (en) * | 2011-01-22 | 2011-07-27 | 内蒙古博源工程有限责任公司 | System and method for producing calcined soda or producing calcined soda and baking soda |
| CN201914926U (en) * | 2011-01-22 | 2011-08-03 | 内蒙古博源工程有限责任公司 | System for realizing co-production of sodium carbonate and baking soda |
| CN108147435A (en) * | 2018-02-05 | 2018-06-12 | 重庆宜化化工有限公司 | A kind of carbonization technique for soda manufacture |
| CN110937612A (en) * | 2019-12-30 | 2020-03-31 | 中国天辰工程有限公司 | Process for preparing high-quality heavy soda ash by using crude sodium bicarbonate |
| CN112758959A (en) * | 2021-03-12 | 2021-05-07 | 自贡鸿鹤制药有限责任公司 | Preparation method of sodium bicarbonate |
Non-Patent Citations (2)
| Title |
|---|
| 赵师琦: "《无机物工艺》", 31 August 1985, 化学工业出版社, pages: 296 * |
| 齐皓琰;: "颗粒状药用碳酸氢钠的探索与展望", 天津化工, no. 01, 30 January 2018 (2018-01-30) * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108439434B (en) | Method and device for producing baking soda | |
| CN103159194B (en) | Continuous crystallization process for monopotassium phosphate | |
| CN104787823B (en) | Yeast wastewater Zero discharge treatment method | |
| CN105771304B (en) | Monosodium glutamate two imitates countercurrent evaporation crystal system and its course of work | |
| CN105056565B (en) | Device and method for evaporation and crystallization of sodium gluconate solution | |
| CN108358220B (en) | Method and device for producing baking soda | |
| CN106904639A (en) | The new technology of sodium chloride and sodium sulphate is obtained in a kind of sodium chloride, sodium sulphate mixed solution respectively | |
| CN101928016B (en) | Process for producing ammonium sulfate by adopting negative pressure double-countercurrent evaporation and crystallization mode | |
| CN206508573U (en) | A kind of function of mechanical steam recompression evaporation and crystallization system of high-salt wastewater | |
| CN104211018B (en) | A kind of method and apparatus that high-purity sulphur is reclaimed in the foam from sulphur | |
| CN116119686A (en) | Sodium bicarbonate production process | |
| CN112573504B (en) | Continuous production process of mesophase carbon microsphere | |
| CN102515202A (en) | Method for producing ionic membrane flake caustic by using fire coal falling film method | |
| CN112758959A (en) | Preparation method of sodium bicarbonate | |
| CN103373747A (en) | Evaporation concentration method of yeast wastewater | |
| CN216236063U (en) | Sodium bromide apparatus for producing | |
| CN208413873U (en) | A kind of device producing sodium bicarbonate | |
| CN209872398U (en) | Ferrous sulfate crystallization device for sulfate process titanium dioxide | |
| CN211946275U (en) | Process device for passivating and modifying continuous crystal form of hydrotalcite product | |
| CN110339585B (en) | Maleic anhydride device solvent dehydration drying treatment process and equipment | |
| CN115959696B (en) | Method for preparing calcium carbonate and ammonium sulfate based on direct steam heating | |
| CN111204778A (en) | Production process of anhydrous sodium sulfite | |
| CN106745093B (en) | Mirabilite hydrate is dehydrated the method and related molten nitre equipment of anhydrous sodium sulphate processed in a kind of chlor-alkali production | |
| CN114456075B (en) | Industrial dimethyl diallyl ammonium chloride synthesis method | |
| CN220779078U (en) | Crystallization device is used in dipotassium hydrogen phosphate production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |