CN113247925A - Process for reducing hydrolysis loss of alumina - Google Patents
Process for reducing hydrolysis loss of alumina Download PDFInfo
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- CN113247925A CN113247925A CN202110392350.7A CN202110392350A CN113247925A CN 113247925 A CN113247925 A CN 113247925A CN 202110392350 A CN202110392350 A CN 202110392350A CN 113247925 A CN113247925 A CN 113247925A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
- C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
Abstract
The invention discloses a process for reducing the hydrolysis loss of alumina, belonging to the technical field of alumina production. The invention relates to liquid separation treatment in a decomposition evaporation process and a dissolution and sedimentation process for producing alumina by a Bayer process, which comprises the following steps: (1) sending the bottom flow washing liquid of the first washing and settling tank to the second washing and settling tank, sending part of overflow washing liquid of the first washing and settling tank to a decomposition area for crystal seed decomposition, and sending the rest overflow washing liquid to a dissolution dilution tank for dilution; (2) after the slurry is decomposed by the seed crystal, part of the separated decomposed mother liquor is sent to a dissolving slurry flash evaporator, and the rest decomposed mother liquor is sent to an evaporation station. The invention can effectively reduce the hydrolysis loss of the alumina, reduce the production cost and realize the continuous and stable yield of the alumina by reducing the delta Rp value of the dissolution liquid and the refined liquid and improving the solution stability of the dilution tank.
Description
Technical Field
The invention relates to the technical field of alumina production, in particular to a process for reducing alumina hydrolysis loss.
Background
In recent years, along with the continuous reduction of ore grade, a large amount of alumina hydrolysis loss is caused in the processes of dilution, deep desiliconization and sedimentation washing of dissolving ore pulp. The loss increase of hydrolysising not only causes alumina loss increase, ore consumption to increase and alumina manufacturing cost risees, increases the clearance degree of difficulty of subsider moreover, shortens the clearance cycle, is unfavorable for the steady operation of subsider, causes the decline of seminal fluid Rp simultaneously, and decomposition power reduces, has restricted the improvement of decomposition rate for alumina output reduces. If the net dissolution rate cannot be effectively improved without solving the problem of large hydrolysis loss of the sodium aluminate solution, the alumina loss caused by hydrolysis alone is very large.
In order to improve the yield of the alumina and the utilization rate of equipment, the solid content of the feed of the diaphragm pump can be improved. However, the solid content of the feed of the diaphragm pump is improved, the supersaturation degree of sodium aluminate of the dissolution liquid Rp is increased along with the increase of the dissolution liquid Rp, the stability of the solution is lowered, the difference value between the dissolution liquid Rp and the semen Rp is increased, and the problem of the increase of the hydrolysis loss of the solution can occur. Therefore, under the condition of unchanged dissolving and feeding flow and solid content, in order to ensure the completion of the yield and cost target, how to reduce the delta Rp values of the dissolving liquid and the semen and reduce the hydrolysis loss is the main research direction of production enterprises.
Disclosure of Invention
The invention aims to solve the problems in the prior art and provides a process for reducing the hydrolysis loss of alumina.
In order to achieve the purpose, the technical scheme of the invention is as follows:
a process for reducing alumina hydrolysis loss, which carries out liquid separation treatment in a decomposition evaporation process and a dissolution and sedimentation process for producing alumina by a Bayer process, comprises the following steps: (1) part of overflow washing liquid of the first washing and settling tank is sent to a decomposition area for crystal seed decomposition, and the rest of overflow washing liquid is sent to a dissolution dilution tank for dilution; (2) after the slurry is decomposed by the seed crystal, part of the separated decomposed mother liquor is sent to a dissolving slurry flash evaporator, and the rest decomposed mother liquor is sent to an evaporation station.
Further, the process of the step (1) is specifically as follows: a shunt pipe is additionally arranged at the bottom of an overflow groove of a first washing and settling tank, the shunt pipe is connected with a first washing liquid flash tank, and the first washing liquid flash tank is connected with a first decomposition tank; the shunt pipe is provided with an adjusting valve and a flowmeter to adjust the flow; when the process is normally put into use, the overflow washing liquid of the first washing sedimentation tank flows out from the overflow groove in two ways, wherein one way of overflow washing liquid is sent to the dissolution dilution tank through the original pipeline, the other way of overflow washing liquid enters the first washing liquid flash tank through the newly added shunt pipe, is cooled and depressurized and then is sent to the decomposition tank in the decomposition area, and the secondary gas of the first washing liquid flash tank is sent to the five-effect separation chamber.
Furthermore, a shunt branch pipe is additionally arranged on a shunt pipe between an overflow groove of a washing and settling tank and a primary washing liquid flash tank, the shunt branch pipe is respectively connected with a decomposed concentrate tank and a decomposed crude liquid tank, the decomposed concentrate tank and the decomposed crude liquid tank are arranged in parallel, and the shunt branch pipe connected with the decomposed concentrate tank and the decomposed crude liquid tank is provided with an adjusting valve; when the overflow washing liquid of a washing and settling tank flows to the decomposition tank abnormally or stops using, the overflow washing liquid is changed to a decomposition concentrate tank or a decomposition crude liquid tank.
Further, the process of the step (2) is specifically as follows: a mother liquor flow dividing pipe is newly added to the dissolving-out slurry flash evaporator at the outlet of a mother liquor decomposing device, the mother liquor flow dividing pipe and a water injection flow collision port of the dissolving-out slurry flash evaporator share one flow, wherein the mother liquor injecting and decomposing flow of the dissolving-out slurry flash evaporator is separated from the water injection flow by using a solid blind plate so as to be used in a switching flow; the mother liquor shunt pipe is provided with an adjusting valve, a check valve and a flowmeter; when the process is normally put into use, the decomposed mother liquor is divided into two paths to flow out, wherein one path is sent to an evaporation station through an original pipeline, and the other path is sent to a dissolved slurry flash evaporator through a newly-added mother liquor shunt pipe.
Further, the dissolving slurry flash evaporator is a dissolving final-stage flash evaporator and/or a dissolving sub-final-stage flash evaporator.
Further, the dissolving slurry flash evaporator comprises a dissolving final-stage flash evaporator and a dissolving sub-final-stage flash evaporator; the mother liquor shunt tubes comprise a mother liquor shunt main tube and two mother liquor shunt branch tubes connected with the mother liquor shunt main tube, wherein one mother liquor shunt branch tube is connected with the dissolution final-stage flash evaporator, the other mother liquor shunt branch tube is connected with the dissolution sub-final-stage flash evaporator, the two mother liquor shunt branch tubes are respectively provided with a regulating valve, the mother liquor shunt main tube receives the decomposed mother liquor from an equipment outlet of the decomposed mother liquor and then transfers to one of the mother liquor shunt branch tubes, and the other mother liquor shunt branch tube is reserved through a closing valve.
Further, in the step (1), 10% -30% of overflow washing liquor in the first washing and settling tank is sent to a decomposition area for seed crystal decomposition, and the rest overflow washing liquor is sent to a dissolution dilution tank for dilution.
Further, in the step (2), the separated decomposition mother liquor with the flow rate of 5-10% is sent to a dissolving-out slurry flash evaporator, and the rest decomposition mother liquor is sent to an evaporation station.
Has the advantages that:
according to the invention, through multi-direction research, the settled primary washing liquid belongs to an unstable solution with lower caustic alkali concentration, hydrolysis is easy to generate after the temperature is reduced, and meanwhile, the caustic alkali concentration of the solution is reduced after the primary washing liquid is added into a dissolution dilution tank, so that the solution stability is poor, and the hydrolysis loss is increased.
The method improves the caustic alkali concentration of the diluted tank solution by improving the adding mode of the primary washing liquid: in the traditional process, a primary washing liquid is completely added into a dilution tank, so that the concentration of the diluted solution in the tank is low, the stability of the solution is low, and the hydrolysis loss is large. According to the invention, a secondary dilution technology is adopted after improvement, a part of primary washing liquor is added into a dilution tank, and the rest of washing liquor is added into a decomposition first tank, so that the caustic soda concentration of the diluted tank solution is improved, the solution stability is improved, the alumina hydrolysis loss is reduced, meanwhile, the retention time of ore pulp in the diluted tank is shortened, the refined liquor silicon content index is controlled to be in a proper range (180-200), and the silicon content in the product alumina is still qualified.
In addition, after the process improvement, the problem of how to reduce the temperature of the primary washing liquid before adding the primary washing liquid into the first decomposition tank needs to be considered. In consideration of the characteristic of easily hydrolyzed materials after the temperature of the primary washing liquid is reduced, the invention adopts a vacuum flash evaporation temperature reduction mode, namely, the six-effect vacuum degree of the evaporation station is utilized, the primary washing liquid which is settled and pressed by self is sent to the decomposition first tank after being subjected to flash evaporation temperature reduction through the self-evaporator, the reasonable control of the temperature of the decomposition tank is ensured, and the heat of the primary washing liquid is also recovered to the evaporation station for use. And meanwhile, in order to ensure that the process can be stably put into use and ensure the caustic alkali concentration of the diluted tank solution, the primary washing liquid is introduced into the fine liquid tank (or the crude liquid tank) again, and when the process of the primary decomposition tank is abnormal, the primary washing liquid is changed into the fine liquid tank (or the crude liquid tank).
The invention divides the decomposed mother liquor into the dissolving slurry flash evaporator, and reduces the Rp value of the high-Rp dissolving liquid after the high-Rp dissolving liquid is obtained by pipeline dissolving under the condition of unchanged dissolving feeding flow and solid content and before hydrolysis reaction, so as to obtain the relatively stable sodium aluminate dissolving liquid. Finally, the difference between the solution Rp and the semen Rp is reduced, the hydrolysis loss is reduced, and the productivity of the system is improved. Meanwhile, a part of decomposition mother liquor is recycled, so that the caustic alkali concentration of the solution in the red mud separation and sedimentation process is improved, the sodium aluminate solution has sufficient stability during the separation and washing of the red mud, and the hydrolysis loss is reduced.
Drawings
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a flow diagram of an overflow wash liquor diversion system for a wash settler;
FIG. 3 is a flow diagram of a decomposition mother liquor diversion system;
reference in figures 2 and 3: 1-washing an overflow groove of a settling tank; 2-a primary washing liquid flash tank; 3-a first washing liquor booster pump; 4-a flow meter; 5-adjusting the valve; 6-check valve; 7-manual valve; 101-a final digestion flash vessel; 102-dissolution penultimate flash vessel.
Detailed Description
The invention is further described with reference to the following figures and specific examples.
Examples
A process for reducing alumina hydrolysis loss is to carry out liquid separation treatment in a decomposition evaporation process and a dissolution and sedimentation process for producing alumina by a Bayer process, and comprises the following steps: (1) sending the bottom flow washing liquid of the first washing and settling tank to the second washing and settling tank, sending a part of overflow washing liquid of the first washing and settling tank to a decomposition area for crystal seed decomposition, and sending the rest overflow washing liquid to a dissolution dilution tank for dilution; (2) after the seed crystal decomposition is carried out on the slurry, a part of decomposed mother liquor separated out is sent to a dissolving slurry flash evaporator, and the rest decomposed mother liquor is sent to an evaporation station.
As shown in fig. 1, a general process flow diagram of this embodiment is shown, and the specific process is as follows: dissolving slurry enters a dilution tank after being flashed from a final stage, the slurry in the dilution tank is sent to a dilution rear tank, is subjected to deep desiliconization and then is sent to a separation settling tank, the slurry in the separation settling tank overflows and is sent to a decomposition area (comprising a decomposition concentrate tank, a decomposition crude liquid tank, a decomposition tank and the like) for seed crystal decomposition, and a decomposed mother liquid is separated and sent to an evaporation station; after modification, this example sent 8% of the decomposition mother liquor in the decomposition zone to the last flash evaporator of the digestion stage, and the remaining decomposition mother liquor to the evaporation station. In other embodiments, the flow of the decomposition mother liquor to the last stage flash vessel of the digestion may take any value from 5% to 10%. Meanwhile, the bottom flow of the separation settling tank is sent to a first washing settling tank, the bottom flow of the first washing settling tank is sent to a second washing settling tank, all the devices and the connection mode are the prior art, and the details are not repeated herein; after modification, in this embodiment, the 20% flow of the overflow washing liquid in the first washing and settling tank is sent to the decomposition area for seed crystal decomposition, and the rest of the overflow washing liquid is sent to the dissolution dilution tank for dilution. In other embodiments, the overflow wash liquor flow to a first wash settler of the decomposition zone may take any value from 10% to 30%.
In this embodiment, step (1) is performed in an overflow wash liquid diversion system of a wash settler, as shown in fig. 2: the overflow washing liquid shunting system of the first washing and settling tank comprises an overflow tank 1 of the first washing and settling tank, a primary washing liquid flash tank 2, a primary washing liquid booster pump 3, a flow meter 4 and an adjusting valve 5; specifically, the method comprises the following steps: adding a shunt pipe at the bottom of an overflow tank 1 of a first washing and settling tank, wherein the shunt pipe, a primary washing liquid flash tank 2 and a first decomposition tank are sequentially connected, specifically, a liquid inlet of the primary washing liquid flash tank 2 is connected with the bottom of the overflow tank 1 of the first washing and settling tank through the shunt pipe, a liquid outlet of the primary washing liquid flash tank 2 is connected with a primary washing liquid booster pump 3 through a pipeline, and the primary washing liquid booster pump 3 is connected with the first decomposition tank; the shunt pipe is provided with an adjusting valve 5 and a flowmeter 4, so that the flow can be adjusted and the index can be controlled in time; when the process is normally put into use, the overflow washing liquid of a first washing and settling tank flows out from an overflow groove 1 of the first washing and settling tank in two ways, wherein one way of overflow washing liquid is sent to a dissolution and dilution tank through an original pipeline, and the original pipeline is also provided with a regulating valve 5 and a flowmeter 4 to regulate the flow; and the other path of overflow washing liquor enters a primary washing liquor flash tank 2 through a newly-added flow dividing pipe, is cooled and depressurized, and is pumped to a first decomposition tank in a decomposition area through a primary washing liquor booster pump 3, wherein secondary gas in the primary washing liquor flash tank 2 escapes from the top of the tank and is sent to a five-effect separation chamber to recover heat.
In this embodiment, in order to make the process stably put into use and ensure the caustic concentration of the diluted tank solution, a branch pipe is added on the branch pipe between the overflow tank 1 of a washing and settling tank and the primary washing liquid flash tank 2, the branch pipe is respectively connected with the fine decomposition liquid tank and the coarse decomposition liquid tank, the fine decomposition liquid tank and the coarse decomposition liquid tank are arranged in parallel, and the branch pipes connected with the fine decomposition liquid tank and the coarse decomposition liquid tank are provided with regulating valves 5; when the overflow washing liquid of a washing and settling tank flows to the first decomposition tank abnormally or stops using, the overflow washing liquid is changed to a fine decomposition liquid tank or a coarse decomposition liquid tank.
In this embodiment, the process of step (2) is as follows: a mother liquor shunt pipe is additionally arranged at the outlet (a decomposition flat disc outlet) of a mother liquor decomposition device to the dissolution slurry flash evaporator, the mother liquor shunt pipe and a water injection flow collision port of the dissolution slurry flash evaporator share one flow, wherein the mother liquor injection and decomposition flow of the dissolution slurry flash evaporator is separated from the water injection flow by using a solid blind plate so as to be used in a switching flow; when the process is normally put into use, the decomposed mother liquor is divided into two paths to flow out, wherein one path is sent to an evaporation station through an original pipeline, and the other path is sent to a dissolved slurry flash evaporator through a newly-added mother liquor shunt pipe. Specifically, the step (2) of distributing the decomposed mother liquor to the digested slurry flash evaporator is performed in a decomposed mother liquor distribution system, as shown in fig. 3, the decomposed mother liquor distribution system includes a digested slurry flash evaporator, the digested slurry flash evaporator includes a digested penultimate flash evaporator 101 and a digested penultimate flash evaporator 102, the mother liquor distribution pipe includes a mother liquor distribution main pipe and two mother liquor distribution branch pipes connected to the mother liquor distribution main pipe, one mother liquor distribution branch pipe is connected to the digested penultimate flash evaporator 101, the other mother liquor distribution branch pipe is connected to the digested penultimate flash evaporator 102, the two mother liquor distribution branch pipes are both provided with a manual valve 7, the mother liquor distribution main pipe is provided with a regulating valve 5, a flow meter 4 (for regulating flow rate), and a check valve 6 (the check valve is provided to prevent backflow due to higher pressure ratio of the flash evaporators); the mother liquor diversion header pipe receives the decomposed mother liquor from an outlet of the mother liquor decomposition device and transfers the decomposed mother liquor into one of the mother liquor diversion branch pipes, the decomposed mother liquor is injected into the dissolution final-stage flash evaporator (or the dissolution secondary final-stage flash evaporator) and then goes to the dilution tank, and the other mother liquor diversion branch pipe closes the manual valve 7 so as to enable the dissolution secondary final-stage flash evaporator (or the dissolution final-stage flash evaporator) to be in a standby state. In the process, the slurry enters a secondary digestion stage flash evaporator 102 according to the original flow, then is transferred to a final digestion stage flash evaporator 101, and finally is transferred to a dilution tank after being mixed with split decomposition mother liquor; the stripping exhaust steam on the top of the stripping last-stage flash evaporator 101 goes to a stripping desilication tank to heat slurry and evaporate and heat mother liquor, and the stripping exhaust steam on the top of the stripping penultimate-stage flash evaporator 102 goes to a first-stage preheating sleeve.
In the present example, the above modified and added process flows are carried out, and the slurry feeding amount is 850m3When the daily production of alumina is 2500t, after part of primary washing liquid is sent to a concentrate tank or a decomposition tank, the primary washing liquid amount of a dilution tank is reduced, the caustic soda concentration of the diluted tank is increased from 162.54g/L to 179.05g/L, the concentration of the diluted solution is increased, the stability of the solution is increased, after mother liquid is injected in a flash evaporation mode, the control range of Rp of dissolved ore pulp is 1.185-1.195, and the amount of the mother liquid injected in the flash evaporation mode is 40-50m3The amount of the semen is increased by 58.6m compared with that before the mother liquor is not injected3The semen yield ratio is reduced by 1.26% due to the reduction of the semen Rp; the difference value between the dissolved ore and the semen Rp before the injection of the mother liquor is 0.0474, and the difference value after the injection of the mother liquor is 0.0448, which is subtracted from the difference value after the injection of the mother liquorThe grain size is 0.0026, which is equivalent to improving the semen Rp0.0026, and the alumina hydrolysis loss can be reduced by about 10 tons every day.
Although the present invention has been described with respect to the preferred embodiments, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (8)
1. A process for reducing the hydrolysis loss of alumina is characterized in that: the liquid separation treatment is carried out in the decomposition and evaporation process and the dissolution and sedimentation process of producing alumina by the Bayer process, and comprises the following steps: (1) part of overflow washing liquid of the first washing and settling tank is sent to a decomposition area for crystal seed decomposition, and the rest of overflow washing liquid is sent to a dissolution dilution tank for dilution; (2) after the slurry is decomposed by the seed crystal, part of the separated decomposed mother liquor is sent to a dissolving slurry flash evaporator, and the rest decomposed mother liquor is sent to an evaporation station.
2. The process for reducing the alumina hydrolysis loss according to claim 1, wherein the process in the step (1) is specifically as follows: a shunt pipe is additionally arranged at the bottom of an overflow groove of a first washing and settling tank, the shunt pipe is connected with a first washing liquid flash tank, and the first washing liquid flash tank is connected with a first decomposition tank; the shunt pipe is provided with an adjusting valve and a flowmeter to adjust the flow; when the process is normally put into use, the overflow washing liquid of the first washing and settling tank flows out from the overflow tank in two ways, wherein one way of overflow washing liquid is sent to the dissolution dilution tank through the original pipeline, the other way of overflow washing liquid enters the first washing liquid flash tank through the newly added shunt pipe, is cooled and depressurized and then is sent to the first decomposition tank in the decomposition area, and the secondary gas of the first washing liquid flash tank is sent to the five-effect separation chamber.
3. The process for reducing the hydrolysis loss of alumina according to claim 2, wherein: a shunt branch pipe is additionally arranged on a shunt pipe between an overflow groove of a washing and settling tank and a primary washing liquid flash tank, the shunt branch pipe is respectively connected with a fine decomposition liquid tank and a coarse decomposition liquid tank, the fine decomposition liquid tank and the coarse decomposition liquid tank are arranged in parallel, and the shunt branch pipe connected with the fine decomposition liquid tank and the coarse decomposition liquid tank is provided with an adjusting valve; when the overflow washing liquid of a washing and settling tank flows to the first decomposition tank abnormally or stops using, the overflow washing liquid is changed to a fine decomposition liquid tank or a coarse decomposition liquid tank.
4. The process for reducing the alumina hydrolysis loss according to claim 1, wherein the process in the step (2) is specifically as follows: a mother liquor flow dividing pipe is newly added to the dissolving-out slurry flash evaporator at the outlet of a mother liquor decomposing device, the mother liquor flow dividing pipe and a water injection flow collision port of the dissolving-out slurry flash evaporator share one flow, wherein the mother liquor injecting and decomposing flow of the dissolving-out slurry flash evaporator is separated from the water injection flow by using a solid blind plate so as to be used in a switching flow; the mother liquor shunt pipe is provided with an adjusting valve, a check valve and a flowmeter; when the process is normally put into use, the decomposed mother liquor is divided into two paths to flow out, wherein one path is sent to an evaporation station through an original pipeline, and the other path is sent to a dissolved slurry flash evaporator through a newly-added mother liquor shunt pipe.
5. The process of claim 4, wherein the alumina hydrolysis loss is reduced by: the digestion slurry flash evaporator comprises a digestion last-stage flash evaporator and/or a digestion penultimate-stage flash evaporator.
6. The process of claim 5, wherein the alumina hydrolysis loss is reduced by: the digestion slurry flash evaporator comprises a digestion final-stage flash evaporator and a digestion sub-final-stage flash evaporator; the mother liquor shunt tubes include mother liquor shunt header and two mother liquor shunt branch pipes connected with the mother liquor shunt header, wherein one mother liquor shunt branch pipe is connected with the dissolution last stage flash evaporator, and another mother liquor shunt branch pipe is connected with the dissolution penult stage flash evaporator, all be equipped with the governing valve on two mother liquor shunt branch pipes, the mother liquor shunt header receives from the equipment export of decomposition mother liquor and shifts over to one of them mother liquor shunt branch pipe after decomposing the mother liquor, and another mother liquor shunt branch pipe is through closing the governing valve reserve.
7. The process of claim 1, wherein the alumina hydrolysis loss is reduced by: in the step (1), 10-30% of overflow washing liquor in the first washing and settling tank is sent to a decomposition area for crystal seed decomposition, and the rest overflow washing liquor is sent to a dissolution dilution tank for dilution.
8. The process of claim 1, wherein the alumina hydrolysis loss is reduced by: in the step (2), 5% -10% of the separated decomposition mother liquor is sent to a dissolving slurry flash evaporator, and the rest decomposition mother liquor is sent to an evaporation station.
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