CN109516478B - Production process of low-ammonia wet heavy alkali - Google Patents
Production process of low-ammonia wet heavy alkali Download PDFInfo
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- CN109516478B CN109516478B CN201811473554.8A CN201811473554A CN109516478B CN 109516478 B CN109516478 B CN 109516478B CN 201811473554 A CN201811473554 A CN 201811473554A CN 109516478 B CN109516478 B CN 109516478B
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- 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
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- 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
- C01D7/12—Preparation of carbonates from bicarbonates or bicarbonate-containing product
Abstract
The invention relates to the field of soda ash production, in particular to a low-ammonia wet heavy alkali production process. The amount of causticizing liquid required by brine refining is increased, and the OH content of refined brine is increased‑、CO3 2‑Concentration, ensuring that the turbidity index of the refined brine is less than or equal to 25ppm, and controlling the total chlorine concentration of the refined brine to be not more than 5.35mol/L to obtain low-calcium magnesium refined brine; purified brine is taken as an ammonia purification medium and is sent to a tail gas ammonia purification tower to purify and absorb ammonia from the outlet gas of the alkali filter, the outlet liquid automatically flows to a furnace gas washing tower in the light ash process, the furnace gas is purified and absorbed with ammonia again, and the light ammonia brine after ammonia absorption is sent to a light ammonia brine barrel; the heavy alkali filtering process uses low ammonia cold waste thin liquid or desalted water with ammonia concentration below 0.05mol/L as alkali filtering machine washing water to prepare wet heavy alkali with low volatile ammonia component content, and the wet heavy alkali is conveyed to downstream processes. The wet heavy alkali has the characteristic of low content of volatile ammonia components, ensures the salinity index of a terminal product, and reduces the diffusion loss of the amlodipine during wet heavy alkali filtration and downstream process production.
Description
Technical Field
The invention relates to the field of soda ash production, in particular to a low-ammonia wet heavy alkali production process.
Background
In the two processes of heavy alkali filtration and light ash furnace gas recovery in a soda production system, a single material is generally adopted to recycle cold waste weak liquor (or desalted water) with the ammonia concentration of below 1ti (0.05mol/L), and two processes of gas ammonia purification and alkali filter washing are completed. Firstly, the ammonia is used as a clean ammonia medium, the air outlet of the vacuum alkali filter and the ammonia-containing purification and recovery of light ash furnace gas are completed by gradient utilization, and then the ammonia is returned to the alkali filter for secondary utilization and is used as a washing water medium for washing and reducing the salt content of wet heavy alkali. In the original process, cold waste weak liquor (or desalted water) with ammonia concentration of less than 1ti (0.05mol/L) is reasonably recycled, but the original process has great disadvantage that after gas gradient ammonia purification is finished, the ammonia concentration of furnace gas ammonia purification liquor reaches 14ti-20t i (0.7-1 mol/L), and the cold waste weak liquor (or desalted water) is recycled as the alkali filter washing water. The wet heavy alkali separated from the alkali filter carries about 19% ammonia-containing water solution, so that the loss of ammonia gas is large in the separation, transportation and downstream production processes, the ammonia consumption in production is increased, and the ammonia odor and the air quality in related posts and device areas are poor.
Disclosure of Invention
The invention aims to solve the problems in the background art, and provides a production process of wet heavy alkali with low volatile ammonia component content, so that the ammonia consumption in production is reduced.
The invention adopts the following technical scheme:
a production process of low-ammonia wet heavy alkali comprises the following steps:
1) in the preparation process of the brine refining procedure, the amount of causticizing liquid required by brine refining is increased, and the OH content of refined brine is increased-、CO3 2-The concentration is controlled as follows: OH group-0.0075～0.0125mol/L；CO3 2-0.00375-0.00625 mol/L; stabilizing clarification operation, ensuring the turbidity index of the refined brine to be less than or equal to 25ppm, and controlling the total chlorine concentration of the refined brine to be not more than 5.35mol/L to obtain high-quality refined brine with low calcium and magnesium; the refined salt water is taken as an ammonia purification medium and sent to a tail gas ammonia purification tower in a heavy alkali filtration process to purify and absorb ammonia from the outlet gas of the alkali filter, the outlet liquid automatically flows to a furnace gas washing tower in a light ash process, the furnace gas is purified and absorbed ammonia again, and the light ammonia salt water is sent to a light ammonia salt water barrel after ammonia absorption;
2) the process is characterized in that the process of purifying and filtering tail gas is cut off from cold waste thin liquid in a high vacuum system in the heavy alkali distillation process, low-ammonia cold waste thin liquid with ammonia concentration of less than 0.05mol/L is used as alkali filter washing water to prepare wet heavy alkali with qualified salt content index and low volatile ammonia component content, and the wet heavy alkali is conveyed to a downstream process.
Compared with the prior art, the wet heavy alkali produced by the method has the characteristics of qualified salt index and low volatile ammonia component content, the salt index of a terminal product is ensured, the ammonia gas diffusion loss in wet heavy alkali filtration and downstream process production is reduced, the ammonia consumption of a soda system for producing ammonia is reduced by about 0.8kg/t alkali, and compared with a method of additionally arranging a gas collection and ammonia purification device, the method saves greater equipment investment and operation power consumption, and has more remarkable economic benefit.
The preferred scheme of the invention is as follows:
in the brine refining procedure in the step 1), crude brine is sent to a calcium-magnesium reactor, refined brine is obtained after reaction of the calcium-magnesium reactor, the refined brine is divided into branches and sent to a No. 1 brine clarifying barrel and a No. 2-4 brine clarifying barrel respectively, after causticizing liquid is supplemented in the No. 1 brine clarifying barrel, the obtained low-calcium-magnesium high-quality refined brine enters an independent storage barrel for buffering, fresh water is added, and the chlorine concentration of the refined brine is adjusted to 5.325-5.35 mol/L.
In the step 1), after the filtered ammonia purification tower effluent enters a furnace gas washing tower, the filtered ammonia purification tower effluent is in countercurrent contact with cooled ammonia-containing furnace gas in the tower, ammonia is absorbed through secondary purification, the purified ammonia effluent with ammonia concentration of 0.25-0.5 mol/L is conveyed to a fresh ammonia brine barrel through a pump, and the furnace gas generated by the furnace gas washing tower is compressed for use.
Conveying the wet heavy alkali obtained in the step 2) by a belt conveyor, performing secondary dehydration by a centrifugal machine, and then conveying the wet heavy alkali into a light ash calcining process to produce light soda ash.
Drawings
Fig. 1 is a flow chart of the prior art.
Fig. 2 is a flow chart of the present invention.
Detailed Description
The invention is described below with reference to the accompanying drawings and examples:
a low ammonia wet heavy alkali production process relates to the ammonia purification and water washing processes of heavy alkali filtration and light ash furnace gas recovery of production systems such as sodium carbonate, sodium bicarbonate and the like; in particular to a method for producing wet heavy alkali with low volatile ammonia component content.
Comprises the following steps of respectively and independently operating low-calcium magnesium refined brine and two media including cold waste weak liquor or desalted water containing 1ti (namely, 0.05mol/L) of ammonia in the production process of filtering and calcining heavy alkali in a soda ash system, and specifically comprising the following steps:
1. in the preparation process of the brine refining procedure, crude brine is sent to a calcium-magnesium reactor, refined brine is obtained after the crude brine is reacted by the calcium-magnesium reactor, the refined brine is divided into two branches and is respectively sent to a No. 1 brine clarifying barrel and a No. 2-4 brine clarifying barrel, and the flow rate of the refined brine divided into the No. 1 clarifying barrel is about 120-170 m3About/h, after adding causticizing liquid into the No. 1 brine clarifying barrel, the obtained low-calcium magnesium refined brine enters an independent storage barrel (buffer tank) for buffering, and the OH content of the refined brine is improved-、CO3 2-The concentration is controlled to 0.15-0.25 ti (i.e. OH)-0.0075～0.0125mol/L；CO3 2-0.00375-0.00625 mol/L), obtaining low-calcium-magnesium high-quality refined brine, stabilizing clarification operation, ensuring that the turbidity index of the refined brine is less than or equal to 25ppm, adding a small amount of fresh water, and ensuring that the added amount of the fresh water can adjust the refined brine to a chlorine-containing concentration of 106.5-107 ti (namely: 5.325-5.35 mol/L).
The refined salt water is used as an ammonia purification medium and is conveyed to a heavy alkali filtering ammonia purification tower through an additional independent refined salt water pump to purify and absorb ammonia from an alkali filter, the liquid outlet of the ammonia purification tower flows to a light ash process furnace gas washing tower automatically and is in countercurrent contact with cooled and cooled ammonia-containing furnace gas in the tower to purify and absorb ammonia for the second time, the purified ammonia outlet liquid with the ammonia concentration of 5-10 ti (namely, 0.25-0.5 mol/L) is conveyed to a fresh ammonia salt water barrel through the pump, and the furnace gas generated by the furnace gas washing tower is compressed and stored for further use or is directly conveyed to a downstream process for use.
2. The process is characterized in that the process of purifying and filtering tail gas is cut off from cold waste thin liquid in a high vacuum system in a heavy alkali distillation process, low-ammonia cold waste thin liquid (or desalted water from a thermoelectric water treatment process) with ammonia concentration below 1ti (namely, 0.05mol/L) is used as alkali filter washing water to prepare wet heavy alkali with qualified salt content index and low volatile ammonia component content, and the wet heavy alkali is conveyed to a downstream process: conveying the mixture by a belt conveyor, performing secondary dehydration by a centrifuge, and then conveying the mixture to a light ash calcining process to produce the light soda ash.
The process of the embodiment is characterized in that:
(1) the low-calcium magnesium refined salt water is used as a gas ammonia purification medium, the gas discharged by the absorption and purification alkali filter and the ammonia contained in the light ash furnace gas are repeatedly utilized, and the light ammonia salt water is sent to a light ammonia salt water barrel after secondary ammonia absorption.
(2) The low ammonia cold waste thin liquid (or desalted water) with the concentration of less than 1ti (namely, 0.05mol/L) is used as the washing water of an alkali filter to prepare wet heavy alkali with low content of volatile component ammonia, and the wet heavy alkali is conveyed to a downstream process.
(3) The wet heavy alkali produced by the embodiment has the characteristic of low content of volatile ammonia components, the ammonia gas diffusion loss in wet heavy alkali filtration and downstream process production is reduced on the premise of ensuring the salt content index of a terminal product, the ammonia consumption of a soda system for producing ammonia is reduced by about 0.8kg/t alkali, and compared with a mode of additionally arranging a gas collection and ammonia purification device, the method saves greater equipment investment and operation power consumption, and has more remarkable economic benefit.
The comparison of the effects before and after the implementation of the technical scheme is shown in the following table:
the comparison of the front and back process flows is as follows:
the original process comprises the following steps: the single medium multiplexing flow of the ammonia purification and water washing process (shown in figure 1).
The invention has the following processes: two media application flows of the ammonia purification and water washing process (shown in figure 2).
Claims (4)
1. A production process of low-ammonia wet heavy alkali comprises the following steps:
1) in the preparation process of the brine refining procedure, the amount of causticizing liquid required by brine refining is increased, and the OH content of refined brine is increased-、CO3 2-The concentration is controlled as follows: OH group- 0.0075～0.0125 mol/L；CO3 2-0.00375-0.00625 mol/L; stable clarifying operation, ensuring the turbidity index of the refined brine to be less than or equal to 25ppm, and controlling the total chlorine concentration of the refined brine to be not more thanAfter 5.35mol/L, high-quality refined salt water with low calcium and magnesium is obtained; the refined salt water is taken as an ammonia purification medium and sent to a tail gas ammonia purification tower in a heavy alkali filtration process to purify and absorb ammonia from the outlet gas of the alkali filter, the outlet liquid automatically flows to a furnace gas washing tower in a light ash process, the furnace gas is purified and absorbed ammonia again, and the light ammonia salt water is sent to a light ammonia salt water barrel after ammonia absorption;
2) the process is characterized in that the process of purifying and filtering tail gas is cut off from cold waste thin liquid in a high vacuum system in a heavy alkali distillation process, low-ammonia cold waste liquid with ammonia concentration of less than 0.05mol/L is used as alkali filter washing water, wet heavy alkali with qualified salt indexes and low volatile ammonia component content is prepared, and the wet heavy alkali is conveyed to a downstream process.
2. The process according to claim 1, wherein the process comprises the following steps: in the brine refining procedure in the step 1), crude brine is sent to a calcium-magnesium reactor, refined brine is obtained after reaction of the calcium-magnesium reactor, the refined brine is divided into branches and sent to a No. 1 brine clarifying barrel and a No. 2-4 brine clarifying barrel respectively, after causticizing liquid is supplemented in the No. 1 brine clarifying barrel, the obtained low-calcium-magnesium high-quality refined brine enters an independent storage barrel for buffering, fresh water is added, and the chlorine concentration of the refined brine is adjusted to 5.325-5.35 mol/L.
3. The process according to claim 1, wherein the process comprises the following steps: in the step 1), after the filtered ammonia purification tower effluent enters a furnace gas washing tower, the filtered ammonia purification tower effluent is in countercurrent contact with cooled ammonia-containing furnace gas in the tower, ammonia is absorbed through secondary purification, the purified ammonia effluent with ammonia concentration of 0.25-0.5 mol/L is conveyed to a fresh ammonia brine barrel through a pump, and the furnace gas generated by the furnace gas washing tower is compressed for use.
4. The process according to claim 1, wherein the process comprises the following steps: conveying the wet heavy alkali obtained in the step 2) by a belt conveyor, performing secondary dehydration by a centrifugal machine, and then conveying the wet heavy alkali into a light ash calcining process to produce light soda ash.
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Citations (6)
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|---|---|---|---|---|
| SU859298A1 (en) * | 1978-04-03 | 1981-08-30 | Предприятие П/Я А-3732 | Method of producing heavy soda |
| CN1063664A (en) * | 1991-04-11 | 1992-08-19 | 青岛碱厂 | A kind of method of washing heavy sodium hydrate filter cake |
| CN1544330A (en) * | 2003-11-21 | 2004-11-10 | 王禹东 | Synchronously continuous production process of low salt heavy sodium carbonate and calcinations drying oven |
| CN1605564A (en) * | 2003-10-09 | 2005-04-13 | 王禹东 | Decomposition liquid recovering technology in heavy sodium carbonate |
| CN1944291A (en) * | 2006-10-17 | 2007-04-11 | 自贡鸿鹤化工股份有限公司 | Method for teating heavy alkali filter liquid in synthesizing alkali producing method |
| CN107954454A (en) * | 2017-12-07 | 2018-04-24 | 青海盐湖工业股份有限公司 | A kind of preparation method of low-salt dense soda ash |
-
2018
- 2018-12-04 CN CN201811473554.8A patent/CN109516478B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU859298A1 (en) * | 1978-04-03 | 1981-08-30 | Предприятие П/Я А-3732 | Method of producing heavy soda |
| CN1063664A (en) * | 1991-04-11 | 1992-08-19 | 青岛碱厂 | A kind of method of washing heavy sodium hydrate filter cake |
| CN1605564A (en) * | 2003-10-09 | 2005-04-13 | 王禹东 | Decomposition liquid recovering technology in heavy sodium carbonate |
| CN1544330A (en) * | 2003-11-21 | 2004-11-10 | 王禹东 | Synchronously continuous production process of low salt heavy sodium carbonate and calcinations drying oven |
| CN1944291A (en) * | 2006-10-17 | 2007-04-11 | 自贡鸿鹤化工股份有限公司 | Method for teating heavy alkali filter liquid in synthesizing alkali producing method |
| CN107954454A (en) * | 2017-12-07 | 2018-04-24 | 青海盐湖工业股份有限公司 | A kind of preparation method of low-salt dense soda ash |
Non-Patent Citations (3)
| Title |
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| 纯碱生产中的盐耗分布;马嘉华等;《内蒙古石油化工》;20151231(第16期);第63-64页 * |
| 论氨碱法纯碱生产重碱过滤;赵普等;《纯碱工业》;20180415(第2期);第19-20页 * |
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