CN1164493C - Method for separating crystal slurry in synthetic heavy soda ash procedure - Google Patents
Method for separating crystal slurry in synthetic heavy soda ash procedure Download PDFInfo
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- CN1164493C CN1164493C CNB021126798A CN02112679A CN1164493C CN 1164493 C CN1164493 C CN 1164493C CN B021126798 A CNB021126798 A CN B021126798A CN 02112679 A CN02112679 A CN 02112679A CN 1164493 C CN1164493 C CN 1164493C
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- soda ash
- solid
- liquid
- stiff device
- alkali
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Abstract
The present invention relates to a method for separating crystal slurry in the heavy soda ash synthetic process. The present invention is characterized in that after heavy soda ash is synthesized in a carbonizer, reaction liquid which is extracted from the carbonizer flows into a thickening device at first so that crystal grains of magma continuously increase; then, a solid and liquid mixture in the thickening device is extracted to be guided into a soda ash filter to be separated; solid after separated is calcined to be made into a finished product; the liquid of an overflow mouth of the thickening device flows into a system to be recirculated after guided out; the staying time of the reaction liquid in the thickening device is 30 to 50 minutes; a stirring device is arranged in the thickening device, and agitating rotary speed is 1 to 8 circles per minute; the solid and liquid ratio of the solid and liquid mixture which is guided out from the thickening device is controlled to be 28% to 35%. The present invention has the advantages that the productivity of the soda ash filter is enhanced, and the salinity of the heavy soda ash is reduced under the condition that the water washing quantity of the soda ash filter is unchanged.
Description
Technical field
The present invention relates to a kind of preparation method of alkaline carbonate, the isolating method of magma in particularly a kind of synthetic heavy soda ash process.
Background technology
In the prior art, produce Soda Ash Danse as solvay soda process, connection alkaline process, after its traditional technology is separated for the reaction feed liquid of being taken out by carbonating tower directly enters Alkali-filter, through calcining and finished product, its weak point is: crystal grain is less in the reaction feed liquid, when entering Alkali-filter and carrying out filtering separation, crystal grain that part is tiny and the heavy alkali that is partly dissolved in the mother liquor can not be isolated, flow out with mother liquor, cause yield lower, heavy alkali salt divides under the constant situation of leaching requirement and is difficult to reduce.The size of the solid-to-liquid ratio of the reaction material liquid mixture that takes out can directly influence the production efficiency of Alkali-filter, the low then inefficiency of production of Alkali-filter of solid-to-liquid ratio; Solid-to-liquid ratio is higher can to increase the technological process of production, under the constant situation of Alkali-filter leaching requirement, is unfavorable for making the salinity of heavy alkali to reduce.
Summary of the invention
The technical problem to be solved in the present invention is at the deficiencies in the prior art, has proposed the isolating method of magma in a kind of synthetic heavy soda ash process, can improve the throughput of Alkali-filter, under the constant situation of Alkali-filter leaching requirement, the salinity of heavy alkali is reduced.
The technical problem to be solved in the present invention is achieved through the following technical solutions, the isolating method of magma in a kind of synthetic heavy soda ash process, be characterized in: after in carbonating tower, synthesizing heavy alkali, the reaction feed liquid that carbonating tower takes out is at first inserted the stiff device, the reaction feed liquid was detained in the stiff device 30～50 minutes, in the stiff device, stir simultaneously with whipping appts, the rotating speed that stirs is 1～8 rev/min, the crystal grain of magma is constantly increased, when the solid-to-liquid ratio of solidliquid mixture in the stiff device reaches 28%～35%, the solidliquid mixture importing Alkali-filter of deriving then in the stiff device separates, and the solid after separating is calcined made finished product.Its solid-to-liquid ratio of reaction feed liquid of taking out through carbonating tower is between 20～25%, the present invention draws through long-term practical experience, at carbonating tower to setting up the stiff device between the Alkali-filter, the crystal grain of magma is constantly grown up, establish a whipping appts in the stiff device simultaneously, the rotating speed of the control reaction time of feed liquid in the stiff device and control whipping appts, the solid-to-liquid ratio that then can control the solidliquid mixture of deriving in the stiff device reaches desired quantity, the solid-to-liquid ratio of the solidliquid mixture that control is derived in the stiff device reaches between 28%～35%, thereby improve the throughput of Alkali-filter, under the constant situation of Alkali-filter leaching requirement, the salinity of heavy alkali is reduced.
The technical problem to be solved in the present invention can also come by the following technical programs further to realize that the solid-to-liquid ratio of the clear liquid that control stiff device overflow port is derived is between 1%～5%, then the clear liquid of stiff device overflow port is derived to return into carbonating tower and carries out recirculation.The clear liquid that stiff device overflow port is derived is incorporated the recycle system into, and the excessive then efficient of its solid-to-liquid ratio reduces, and too smallly then can produce diluting effect to the reaction feed liquid in the carbonating tower.
The present invention compared with prior art, produce Soda Ash Danse for solvay soda process, connection alkaline process, change its traditional technology, at carbonating tower to setting up the stiff device between the Alkali-filter, the solid-to-liquid ratio of the solidliquid mixture that control is derived in the stiff device, the reaction feed liquid is detained at the stiff device, the heavy alkali of dissolved continues crystallization in the feed liquid, the crystal grain of magma is constantly increased, when feed liquid is separated, improve yield in Alkali-filter, thereby improve the throughput of Alkali-filter, under the constant situation of Alkali-filter leaching requirement, the salinity of heavy alkali is reduced.
Embodiment
Embodiment one, and the isolating method of magma in a kind of synthetic heavy soda ash process behind the synthetic heavy alkali, is taken out the reaction feed liquid in the carbonating tower in carbonating tower, and the solid-to-liquid ratio of its reaction feed liquid is 24%, and its mother liquor contains free ammonia 1.65%, fixed ammonia 6.58%, Cl
-16.4%, CO
22.35%, Na
+2.4%, the reaction feed liquid at first enters the stiff device, the time that the reaction feed liquid is detained in the stiff device is 40 minutes, in the stiff device, be provided with a whipping appts, the rotating speed that stirs is 4 rev/mins, the crystal grain of magma is constantly increased, when the solid-to-liquid ratio of the solidliquid mixture of deriving in the stiff device reaches 30%, the solidliquid mixture importing Alkali-filter that takes out then in the stiff device separates, and the main component of separating the heavy alkali in back contains NaHCO
370%, Na
2CO
37%, NaCl 0.2-0.3%, NH
4HCO
33-4%, H
2O 20%, the solid after separating calcined made finished product, incorporates system into after the clear liquid of stiff device overflow port is derived and carries out recirculation, and the solid-to-liquid ratio of the clear liquid that control stiff device overflow port is derived is between 3%.Under the constant situation of leaching requirement, the throughput of Alkali-filter has improved 10%, and the product salinity has descended 0.2% simultaneously.
Embodiment two, and the isolating method of magma in a kind of synthetic heavy soda ash process is taken out the reaction feed liquid in the carbonating tower, and the solid-to-liquid ratio of its reaction feed liquid is 20%, and its mother liquor contains free ammonia 1.6%, fixed ammonia 6.5%, Cl
-16.2%, CO
22.3%, Na
+2.3%, the reaction feed liquid at first enters the stiff device, the time that the reaction feed liquid is detained in the stiff device is 30 minutes, in the stiff device, be provided with a whipping appts, the rotating speed that stirs is 1 rev/min, the crystal grain of magma is constantly increased, when the solid-to-liquid ratio of the solidliquid mixture of deriving in the stiff device reaches 28%, the solidliquid mixture importing Alkali-filter that takes out then in the stiff device separates, solid after separating calcined make finished product, incorporate system into after the clear liquid of stiff device overflow port is derived and carry out recirculation, the solid-to-liquid ratio of the clear liquid that control stiff device overflow port is derived is between 1%.Under the constant situation of leaching requirement, the throughput of Alkali-filter has improved 93%, and the product salinity has descended 0.21% simultaneously.
Embodiment three, and the isolating method of magma in a kind of synthetic heavy soda ash process is taken out the reaction feed liquid in the carbonating tower, and the solid-to-liquid ratio of its reaction feed liquid is 25%, and its mother liquor contains free ammonia 1.7%, fixed ammonia 7.0%, Cl
-16.8%, CO
22.4%, Na
+2.5%, the reaction feed liquid at first enters the stiff device, the time that the reaction feed liquid is detained in the stiff device is 50 minutes, in the stiff device, be provided with a whipping appts, the rotating speed that stirs is 8 rev/mins, the crystal grain of magma is constantly increased, when the solid-to-liquid ratio of the solidliquid mixture of deriving in the stiff device reaches 35%, the solidliquid mixture importing Alkali-filter that takes out then in the stiff device separates, solid after separating calcined make finished product, incorporate system into after the clear liquid of stiff device overflow port is derived and carry out recirculation, the solid-to-liquid ratio of the clear liquid that control stiff device overflow port is derived is between 5%.Under the constant situation of leaching requirement, the throughput of Alkali-filter has improved 11%, and the product salinity has descended 0.19% simultaneously.
Claims (2)
1. the isolating method of magma in the synthetic heavy soda ash process, it is characterized in that: after in carbonating tower, synthesizing heavy alkali, the reaction feed liquid that carbonating tower takes out is at first inserted the stiff device, the reaction feed liquid was detained in the stiff device 30～50 minutes, in the stiff device, stir simultaneously with whipping appts, the rotating speed that stirs is 1～8 rev/min, the crystal grain of magma is constantly increased, when the solid-to-liquid ratio of solidliquid mixture in the stiff device reaches 28%～35%, the solidliquid mixture importing Alkali-filter of deriving in the stiff device separates, and the solid after separating is calcined made finished product.
2. the isolating method of magma in the synthetic heavy soda ash process according to claim 1, it is characterized in that: the solid-to-liquid ratio of the clear liquid that control stiff device overflow port is derived is between 1%～5%, then the clear liquid of stiff device overflow port is derived to return into carbonating tower and carries out recirculation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021126798A CN1164493C (en) | 2002-02-10 | 2002-02-10 | Method for separating crystal slurry in synthetic heavy soda ash procedure |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021126798A CN1164493C (en) | 2002-02-10 | 2002-02-10 | Method for separating crystal slurry in synthetic heavy soda ash procedure |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1413909A CN1413909A (en) | 2003-04-30 |
| CN1164493C true CN1164493C (en) | 2004-09-01 |
Family
ID=4742178
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB021126798A Expired - Lifetime CN1164493C (en) | 2002-02-10 | 2002-02-10 | Method for separating crystal slurry in synthetic heavy soda ash procedure |
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| CN (1) | CN1164493C (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108298568B (en) * | 2018-01-26 | 2020-02-18 | 安徽德邦化工有限公司 | Process for thickening heavy alkali filtrate |
| CN109850924B (en) * | 2019-01-09 | 2021-10-22 | 生命之友(宁夏)生物科技有限公司 | Environment-friendly heavy alkali apparatus for producing |
| CN115417432B (en) * | 2022-10-14 | 2023-07-28 | 天津渤化工程有限公司 | Heavy ash production process system and production process thereof |
| CN117756140A (en) * | 2024-02-22 | 2024-03-26 | 南京新筛分科技实业有限公司 | process in sodium carbonate production |
-
2002
- 2002-02-10 CN CNB021126798A patent/CN1164493C/en not_active Expired - Lifetime
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|---|---|
| CN1413909A (en) | 2003-04-30 |
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Owner name: ZHAO XIANGHAI Free format text: FORMER OWNER: DEBANG CHEMICAL INDUSTRY GROUP CO. LTD., JIANGSU Effective date: 20050812 |
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Effective date of registration: 20050812 Address after: Room 2, unit 21, building 6, 401, neat Road, Sinpo District, Jiangsu, Lianyungang, 222001 Patentee after: Zhao Xianghai Address before: 222023 Jiangsu city of Lianyungang province Haizhou Jiang Hua Lu No. 51 Patentee before: Debang Chemical Industry Group Co., Ltd., Jiangsu |
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Owner name: DEBANG CHEMICAL INDUSTRY GROUP CO. LTD., JIANGSU Free format text: FORMER OWNER: ZHAO XIANGHAI Effective date: 20140930 |
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