CN212954328U - Evaporation and dissolution integrated process equipment - Google Patents
Evaporation and dissolution integrated process equipment Download PDFInfo
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- CN212954328U CN212954328U CN202021349552.0U CN202021349552U CN212954328U CN 212954328 U CN212954328 U CN 212954328U CN 202021349552 U CN202021349552 U CN 202021349552U CN 212954328 U CN212954328 U CN 212954328U
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Abstract
The utility model belongs to the technical field of meticulous alumina production, concretely relates to evaporation is dissolved out integration process equipment. The utility model discloses under the circumstances that does not change the reinforced mode of aluminium hydroxide, unify two processes of evaporation in the aluminium hydroxide production and dissolving out into a whole, simplified the flow, reduced equipment quantity, promoted the thermal efficiency that whole evaporation dissolved out the system, practiced thrift equipment investment cost and area, improve the total thermal efficiency of system, reduce the consumption of steam in the production, do benefit to the simplification of whole factory's production, control system, more high-efficient, energy-conservation than prior art.
Description
Technical Field
The utility model belongs to the technical field of meticulous alumina production, concretely relates to evaporation is dissolved out integration process equipment.
Background
At present, the Bayer process for producing and purifying alumina at home and abroad generally adopts a method that seed precipitation mother liquor is evaporated and then the evaporated mother liquor is subjected to dissolution reaction with bauxite (aluminum hydroxide). The number of heat exchange equipment is large, and the equipment investment cost is high. The main characteristics of the prior art are as follows: firstly, the dissolution and the evaporation are two process units, the evaporation process realizes the concentration of the evaporation stock solution, and the dissolution process adopts the batching of the evaporation mother solution to complete the dissolution of the aluminum hydroxide (gibbsite ore). And secondly, the high-temperature dissolved-out slurry adopts a flash evaporation process, flash evaporation exhaust steam is returned to the waste heat cold slurry, and flash evaporation moisture is less.
At present, the main processes of domestic and foreign production lines are as follows:
first, an evaporation process
For 6-effect countercurrent evaporation, the evaporation stock solution and new steam are in countercurrent contact. The steam generated after the flash evaporation of the new steam condensate and the dead steam condensate returns to the evaporator for reuse.
The material flow is as follows, and the detailed flow is shown in the attached figure 2.
The evaporation stock solution → 6-effect evaporator and separation chamber → 5-effect evaporator and separation chamber → 4-effect evaporator and separation chamber → 3-effect evaporator and separation chamber → 2-effect evaporator and separation chamber → 1-effect evaporator and separation chamber → concentrated mother liquor (high pressure, high temperature) → mother liquor 1-stage flash tank → mother liquor 2-stage flash tank → mother liquor 3-stage flash tank → mother liquor 4-stage flash tank → concentrated mother liquor (normal pressure, low temperature).
② dissolving out process
The concentrated mother liquor and aluminum hydroxide under normal pressure are sent into a three-stage preheater and a new steam heater after being pulped, and then enter the subsequent procedures after being subjected to heat preservation and dissolution and being cooled to 107-plus 110 ℃ through three-stage flash evaporation. The steam generated after the flash evaporation of the new steam condensate and the dead steam condensate is returned to the preheater for reuse.
Concentrated mother liquor (normal pressure, low temperature) + aluminum hydroxide → first-stage preheater → second-stage preheater → third-stage preheater → new steam preheater → heat preservation tank → first-stage flash tank of dissolution liquid → second-stage flash tank of dissolution liquid → third-stage flash tank of dissolution liquid → dissolution liquid (107-.
Problems or disadvantages with the above procedure:
(1) heating the evaporation stock solution, heating to about 143 ℃, then carrying out flash evaporation and cooling to about 90 ℃, mixing with aluminum hydroxide and pulping, and then heating to about 143 ℃. The process requires the use of an evaporant flash tank to lower the temperature of the concentrate to mix with the aluminum hydroxide for slurry preparation. Although the evaporation liquid flash tank can reduce the temperature of the concentrated liquid and recover secondary steam, the total thermal efficiency of the system can be reduced due to the influence of heat exchange efficiency, temperature difference loss and heat dissipation loss.
(2) The evaporation process is countercurrent evaporation, each effect is provided with a material passing pump, and the power consumption is high.
(3) The dissolving-out process has no water cooler system, the secondary steam pressure can only be reduced to normal pressure (absolute pressure) at the lowest after the dissolving-out liquid is subjected to flash evaporation, and the discharging temperature of the dissolving-out liquid is 107-110 ℃ due to the rising of the boiling point, so that the temperature is very close to the normal-pressure boiling point, and some secondary steam is lost in the air of the dissolving-out liquid storage tank.
(4) The number of heat exchange equipment is more, and two processes all have concentrated mother liquor (or solution) flash tanks, new steam condensate flash tanks, exhaust steam condensate flash tanks and the like, and too much heat exchange equipment reduces the total thermal efficiency of the system and increases the equipment investment at the same time.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects of the prior art, the utility model provides an evaporation and dissolution integrated process device, which shortens and integrates the evaporation process and the dissolution process of the fine alumina industry, and completes the evaporation of water and the feeding and dissolution of aluminum hydroxide in one system; therefore, the number of equipment can be reduced, the equipment investment cost and the occupied area are reduced, the total heat efficiency of the system is improved, and the consumption of steam in production is reduced.
The evaporation and dissolution integrated process equipment of the utility model combines the evaporation of water and the dissolution of aluminum hydroxide into a heat balance system; the equipment comprises a stock solution III-effect evaporator and separation chamber, a stock solution II-effect evaporator and separation chamber, a stock solution I-effect evaporator and separation chamber, a beating tank, a new steam heater, a heat preservation tank, a dissolution liquid I-effect evaporator and separation chamber, a dissolution liquid II-effect evaporator and separation chamber, a dissolution liquid III-effect evaporator and separation chamber, a dissolution liquid flash tank, a new steam water seal tank, a new steam condensate I-stage flash tank, a new steam condensate II-stage flash tank, a new steam condensate III-stage flash tank, a new steam condensate IV-stage flash tank, a new steam condensate V-stage flash tank, an exhaust steam seal tank, an exhaust steam condensate I-stage flash tank, an exhaust steam condensate II-stage flash tank, an exhaust steam condensate III-stage flash tank, an exhaust steam condensate IV-stage flash tank and a water cooler.
Wherein:
the stock solution III-effect evaporator and the separation chamber are connected with a stock solution II-effect evaporator and a separation chamber, the stock solution II-effect evaporator and the separation chamber are connected with a stock solution I-effect evaporator and the separation chamber, the stock solution I-effect evaporator and the separation chamber are connected with a beating tank, the beating tank is connected with a new steam heater, the new steam heater is connected with a heat preservation tank, the heat preservation tank is connected with a dissolution liquid I-effect evaporator and the separation chamber, the dissolution liquid I-effect evaporator and the separation chamber are connected with a dissolution liquid II-effect evaporator and the separation chamber, the dissolution liquid II-effect evaporator and the separation chamber are connected with a dissolution liquid III-effect evaporator and the separation chamber, and the dissolution liquid III-effect evaporator and the separation chamber are connected;
the new steam heater, the first-effect evaporator of the dissolved liquid and the separation chamber are respectively connected with a new steam water seal tank, the new steam water seal tank is connected with a first-stage flash tank of new steam condensate, the first-stage flash tank of new steam condensate is connected with a second-stage flash tank of new steam condensate, the second-stage flash tank of new steam condensate is connected with a third-stage flash tank of new steam condensate, the third-stage flash tank of new steam condensate is connected with a fourth-stage flash tank of new steam condensate, and the fourth-stage flash tank of new steam condensate is connected with a fifth-stage flash tank of new steam condensate;
the dissolved liquid II-effect evaporator and the separation chamber are connected with a steam exhaust water seal tank, the steam exhaust water seal tank is connected with a steam exhaust condensate I-stage flash tank, the steam exhaust condensate I-stage flash tank is connected with a steam exhaust condensate II-stage flash tank, the steam exhaust condensate II-stage flash tank is connected with a steam exhaust condensate III-stage flash tank, and the steam exhaust condensate III-stage flash tank is connected with a steam exhaust condensate IV-stage flash tank; the stock solution III-effect evaporator and the separation chamber are connected with a water cooler.
Preferably, the number of the stock solution multi-effect evaporators, the number of the dissolution solution multi-effect evaporators, the number of the new steam condensate flash tanks and the number of the dead steam condensate flash tanks are increased or decreased according to the Nk concentration of the concentrated solution and the Nk concentration of the dissolution solution. The concentrated solution is the liquid from the original solution I-effect evaporator and the separation chamber.
Preferably, the equipment also comprises an MVR evaporation system, and the MVR evaporation system is connected with the stock solution III-effect evaporator and the separation chamber.
The evaporation and dissolution integrated process flow adopting the equipment is used for evaporation of water and dissolution of aluminum hydroxide in the fine alumina industry; the process divides the distilled water into two parts, wherein one part of the distilled water is distilled before dissolution, the other part of the distilled water is distilled after dissolution, and the dissolution equipment is arranged between the two sections of the distilled water to jointly form an evaporation and dissolution integrated process flow; the method mainly comprises the following steps:
the evaporation stock solution flows through an MVR evaporator, a stock solution III-effect evaporator and a separation chamber, a stock solution II-effect evaporator and a separation chamber, a stock solution I-effect evaporator and a separation chamber are evaporated and concentrated, the concentrated stock solution is mixed with aluminum hydroxide in a beating tank for pulp preparation and then enters a new steam heater, the new steam heater stays in a heat preservation tank for dissolution, the dissolution liquid flows through a dissolution liquid I-effect evaporator and a separation chamber, the dissolution liquid II-effect evaporator and a separation chamber, the dissolution liquid III-effect evaporator and a separation chamber, and the dissolution liquid enters a subsequent process after passing through a dissolution liquid flash tank.
Preferably, the water is evaporated before dissolution by adopting a countercurrent evaporation mode; the water is evaporated after dissolution and the concurrent evaporation mode is adopted.
Preferably, the temperature of the solution is 90-108 ℃, and is generally about 98 ℃. The effluent temperature refers to the effluent temperature of the dissolved liquid flash tank, namely the temperature of entering the subsequent processes, wherein the subsequent processes can be a decoloring process, a leaf filtering process, a decomposition process and the like.
Preferably, the waste steam generated by the dissolution liquid III-effect evaporator and the separation chamber is used as a heat source of the raw liquid I-effect evaporator and the separation chamber.
In the process, a two-stage water evaporation system is adopted for evaporation of water, part of water is evaporated before dissolution, an evaporation stock solution is heated and concentrated by adopting a countercurrent mode and using dead steam evaporated in a concurrent flow manner as a heat source, the temperature of a concentrated solution is controlled below a normal-pressure boiling point, and the concentrated solution is directly mixed with aluminum hydroxide to prepare slurry; and evaporating out the other part of water after dissolution, adopting a concurrent flow mode, supplementing heat energy by using the heat energy of the dissolved high-temperature slurry and adding part of new steam, and using the generated dead steam as a heat source for countercurrent evaporation. The dissolving-out equipment is embedded between the two sections of water evaporating systems, and only new steam is used as a heat source to heat the slurry. The two-stage water evaporating system and the dissolving-out equipment are fused into an evaporation and dissolving-out integrated system, and evaporation of water and dissolution of aluminum hydroxide are completed in the system.
In the prior art, the Nk concentration of the concentrated solution is relatively high (such as 160-. The dissolved liquid after heat preservation flows through a multi-effect concurrent flow evaporator, the temperature is reduced step by step, heat energy generated by temperature reduction is completely used for heating in the evaporation process, and the temperature reduction of materials and the evaporation of water are synchronously carried out. By adopting the concurrent evaporation, on one hand, a multi-effect evaporator can be used for replacing a flash tank in the prior art, and on the other hand, the evaporation water quantity is also improved.
The evaporation stock solution is heated and concentrated by using a dissolution liquid III-effect evaporator and secondary steam in a separation chamber, and the evaporation process adopts a counter-current multi-effect evaporator. The temperature of the concentrated solution is about 97 ℃, the temperature is lower, and the concentrated solution with the low temperature is used for pulping and mixing with the aluminum hydroxide.
The concentrated solution and the slurry after the aluminum hydroxide pulping are heated to about 143 ℃ by a new steam heater, enter a heat preservation tank, stay for a certain time, and the dissolved solution flows into a group of downstream multi-effect evaporators to evaporate the residual water. Only introducing new steam into the first effect evaporator of the dissolution liquid. The dissolved liquid after water evaporation passes through a flash tank, is cooled to a boiling point lower than the normal pressure, and is pumped into the subsequent working procedures by a pump.
The new steam condensate and the exhausted steam condensate are subjected to flash evaporation step by step to recover the generated secondary steam. The generated secondary steam is used as a supplementary heat source of the stock solution multi-effect evaporator or the dissolution liquid multi-effect evaporator.
The process is still applicable to the condition that the concentration of the evaporated stock solution Nk is less than 80g/L, and only an MVR evaporator is added before entering the stock solution evaporator to evaporate the stock solution to about 80g/L of Nk concentration.
Because the Nk concentration of evaporation stock solution and solution is different, or the required volume of evaporating water is different, more or less processes of effect number may be adopted to following current multi-effect evaporator or adverse current multi-effect evaporator, but the same with this technology principle, should be contained within the utility model discloses.
Compared with the prior art, the beneficial effects of the utility model are that:
1. the utility model discloses can directly add aluminium hydroxide mixture and join in marriage the thick liquid in the concentrate that the temperature is lower (about 97 ℃), the lower (80-150g/L) of Nk concentration, and needn't join in marriage the thick liquid with aluminium hydroxide after cooling to 97 ℃ with 143 ℃ concentrate flash distillation in the former technology. Therefore, the concentrated mother liquor flash tank can be omitted, the reduction of the number of the devices is beneficial to reducing heat dissipation loss, the total heat exchange efficiency is improved, and the number of the devices is reduced.
2. The dissolving liquid evaporator adopts a downstream multi-effect evaporator, and a material passing pump is not needed, so that the number of the material passing pumps is reduced, and the power consumption is saved. The adoption of a concurrent evaporation mode can also omit a dissolution liquid flash tank in the prior art.
3. As the evaporation and dissolution integrated process equipment is adopted, the process can recover the secondary steam of the dissolution liquid flash tank by utilizing the vacuum degree of the water cooler, so that the temperature of the dissolution liquid is lower than the boiling point under normal pressure, and the loss of the secondary steam generated when the dissolution liquid flows into a subsequent normal-pressure storage tank is reduced.
4. The process is only provided with 1 set of new steam condensate flash evaporation system and 1 set of exhaust steam condensate flash evaporation system. The specifications of each equipment are slightly increased, but the total equipment quantity and the equipment investment are reduced.
5. In a word, the evaporation and dissolution integrated process can reduce the number of heat exchange equipment, the total heat loss of a system, the equipment investment cost and the occupied area.
Take the evaporation stock solution Nk 90g/L, the concentration mother solution Nk 110g/L, and the dissolution liquid Nk 130g/L as examples. Through heat balance calculation, the consumption of steam (saturated steam at 160 ℃) in the prior art is 2.58t/t-AO, and the heat loss of the system accounts for 4.5 percent; the steam consumption of the process is 2.26t/t-AO, and the heat loss of the system accounts for 1.0 percent. The main reason of lower steam consumption in the process is that the effluent temperature of the digestion solution is reduced to 97 ℃ from 108 ℃ in the prior art, so that the heat of the generated secondary steam is recovered; the main reason for the heat loss of the system is to reduce the number of heat exchange devices. In the prior art, the number of the material passing pumps is 6, the number of the material passing pumps is 3, and 3 pumps are saved; in the prior art, 7 material flash tanks are adopted, and only one dissolved liquid flash tank is needed in the process; the prior art needs 14 new steam condensate flash tanks and exhausted steam condensate flash tanks, and only 9 new steam condensate flash tanks and exhausted steam condensate flash tanks are needed in the process.
Drawings
FIG. 1 is a schematic view of the process equipment of the present invention;
FIG. 2 is a prior art evaporation and dissolution flow diagram;
in the figure: 1-MVR evaporation system, 2-stock solution III effect evaporator and separation chamber, 3-stock solution II effect evaporator and separation chamber, 4-stock solution I effect evaporator and separation chamber, 5-beating tank, 6-new steam heater, 7-heat preservation tank, 8-dissolution liquid I effect evaporator and separation chamber, 9-dissolution liquid II effect evaporator and separation chamber, 10-dissolution liquid III effect evaporator and separation chamber, 11-dissolution liquid flash tank, 12-new steam water seal tank, 13-new steam condensate I level flash tank, 14-new steam condensate II level flash tank, 15-new steam condensate III level flash tank, 16-new steam condensate IV level flash tank, 17-new steam condensate V level flash tank, 18-steam exhaust water seal tank, 19-steam exhaust condensate I level flash tank, 20-a waste steam condensate II-level flash tank, 21-a waste steam condensate III-level flash tank, 22-a waste steam condensate IV-level flash tank and 23-a water cooler.
Detailed Description
The invention is further described with reference to the following figures and examples.
Example 1
As shown in fig. 1, the evaporation and dissolution integrated process equipment combines the evaporation of water and the dissolution of aluminum hydroxide into a heat balance system; the equipment comprises an MVR evaporation system 1, a stock solution III-effect evaporator and separation chamber 2, a stock solution II-effect evaporator and separation chamber 3, a stock solution I-effect evaporator and separation chamber 4, a beating tank 5, a new steam heater 6, a heat preservation tank 7, a dissolution liquid I-effect evaporator and separation chamber 8, a dissolution liquid II-effect evaporator and separation chamber 9, a dissolution liquid III-effect evaporator and separation chamber 10, a dissolution liquid flash tank 11, a new steam water seal tank 12, a new steam condensate I-stage flash tank 13, a new steam condensate II-stage flash tank 14, a new steam condensate III-stage flash tank 15, a new steam condensate IV-stage flash tank 16, a new steam condensate V-stage flash tank 17, an exhaust steam water seal tank 18, an exhaust steam condensate I-stage flash tank 19, an exhaust steam condensate II-stage flash tank 20, an exhaust steam condensate III-stage flash tank 21, an exhaust steam condensate IV-stage flash tank 22 and a water cooler 23.
The MVR evaporation system 1 is connected with a stock solution III-effect evaporator and separation chamber 2, the stock solution III-effect evaporator and separation chamber 2 is connected with a stock solution II-effect evaporator and separation chamber 3, the stock solution II-effect evaporator and separation chamber 3 is connected with a stock solution I-effect evaporator and separation chamber 4, the stock solution I-effect evaporator and separation chamber 4 is connected with a beating tank 5, the beating tank 5 is connected with a new steam heater 6, the new steam heater 6 is connected with a heat preservation tank 7, the heat preservation tank 7 is connected with a dissolution liquid I-effect evaporator and separation chamber 8, the dissolution liquid I-effect evaporator and separation chamber 8 is connected with a dissolution liquid II-effect evaporator and separation chamber 9, the dissolution liquid II-effect evaporator and separation chamber 9 is connected with a dissolution liquid III-effect evaporator and separation chamber 10, and the dissolution liquid III-effect evaporator and separation chamber 10 is connected with a dissolution liquid flash tank 11;
the new steam heater 6 and the first-effect evaporator of the dissolved liquid and the separation chamber 8 are respectively connected with a new steam water seal tank 12, the new steam water seal tank 12 is connected with a first-stage flash tank 13 of new steam condensate, the first-stage flash tank 13 of new steam condensate is connected with a second-stage flash tank 14 of new steam condensate, the second-stage flash tank 14 of new steam condensate is connected with a third-stage flash tank 15 of new steam condensate, the third-stage flash tank 15 of new steam condensate is connected with a fourth-stage flash tank 16 of new steam condensate, and the fourth-stage flash tank 16 of new steam condensate is connected with a fifth-stage flash tank 17 of new steam condensate;
the dissolution liquid II-effect evaporator and separation chamber 9 is connected with a steam exhaust water seal tank 18, the steam exhaust water seal tank 18 is connected with a steam exhaust condensate I-stage flash tank 19, the steam exhaust condensate I-stage flash tank 19 is connected with a steam exhaust condensate II-stage flash tank 20, the steam exhaust condensate II-stage flash tank 20 is connected with a steam exhaust condensate III-stage flash tank 21, and the steam exhaust condensate III-stage flash tank 21 is connected with a steam exhaust condensate IV-stage flash tank 22; the stock solution III effect evaporator and the separation chamber 2 are connected with a water cooler 23.
Take the saturated steam at 160 deg.C as the new steam, evaporate stock solution Nk 90g/L, concentrate mother liquor Nk 110g/L, dissolve out liquid Nk 130g/L as the example.
If the concentration of the evaporation stock solution Nk is lower than 80-90g/L, the evaporation concentration can be increased to 80-90g/L by using an MVR evaporation system 1.
Nk 90g/L of evaporation stock solution enters a countercurrent multi-effect evaporator, flows through a stock solution III-effect evaporator and separation chamber 2, a stock solution II-effect evaporator and separation chamber 3 and a stock solution I-effect evaporator and separation chamber 4, and is gradually evaporated to Nk 110g/L to obtain a 97 ℃ concentrated solution. The secondary steam with the temperature of 101 ℃ in the separation chamber 10 of the III-effect evaporator of the autolysis liquid enters the I-effect evaporator of the stock solution and the separation chamber 4, and is in countercurrent contact with the evaporation liquid for heat exchange, and the exhaust steam after heat exchange flows into a water cooler 23. The concentrated mother liquor with the boiling point lower than the normal pressure flows into a pulping tank 5 to be mixed with aluminum hydroxide for pulp preparation. The slurry flows into a new steam heater 6, is heated to 143 ℃, flows into a heat preservation tank 7, stays for 1-1.5 hours, flows into a downstream multi-effect evaporator, flows through a dissolution liquid I-effect evaporator and separation chamber 8, a dissolution liquid II-effect evaporator and separation chamber 9, a dissolution liquid III-effect evaporator and separation chamber 10, simultaneously, new steam is introduced into the dissolution liquid I-effect evaporator 8, the dissolution liquid is heated by the steam to evaporate water while flashing, and the temperature of the dissolution liquid flowing out of the dissolution liquid III-effect evaporator and separation chamber 10 is about 109 ℃. The dissolved liquid flows into a dissolved liquid flash tank 11, the flash evaporation temperature is reduced to 98 ℃, and the generated secondary steam is merged into the heating steam of the stock solution II-effect evaporator 3.
And after the new steam condensate flows into a new steam water seal tank 12, the new steam condensate flows into a new steam condensate I-level flash tank 13, a new steam condensate II-level flash tank 14, a new steam condensate III-level flash tank 15, a new steam condensate IV-level flash tank 16 and a new steam condensate V-level flash tank 17 step by step, and the new steam condensate is cooled to 80 ℃ and then flows into an aluminum hydroxide washing process as washing liquid. And the secondary steam generated by each stage of new steam condensate flash tank is merged into each evaporator to be used as heating steam.
And after the exhaust steam condensate flows into an exhaust steam water seal tank 18, the exhaust steam condensate flows into an exhaust steam condensate I-stage flash tank 19, an exhaust steam condensate II-stage flash tank 20, an exhaust steam condensate III-stage flash tank 21 and an exhaust steam condensate IV-stage flash tank 22 step by step, and the temperature of the exhaust steam condensate III-stage flash tank is reduced by 80 ℃ to be used as washing liquid to flow into an aluminum hydroxide washing process. And the secondary steam generated by each stage of the dead steam condensate flash tank is merged into each evaporator to be used as heating steam.
Through heat balance calculation, the consumption of steam (saturated steam at 160 ℃) in the prior art is 2.58t/t-AO, and the heat loss of the system accounts for 4.5 percent; the steam consumption of the process is 2.26t/t-AO, and the heat loss of the system accounts for 1.0 percent. The main reason of lower steam consumption in the process is that the effluent temperature of the digestion solution is reduced to 97 ℃ from 108 ℃ in the prior art, so that the heat of the generated secondary steam is recovered; the main reason for the heat loss of the system is to reduce the number of heat exchange devices. In the prior art, the number of the material passing pumps is 6, the number of the material passing pumps is 3, and 3 pumps are saved; in the prior art, 7 material flash tanks are adopted, and only one dissolved liquid flash tank is needed in the process; the prior art needs 14 new steam condensate flash tanks and exhausted steam condensate flash tanks, and only 9 new steam condensate flash tanks and exhausted steam condensate flash tanks are needed in the process.
Claims (2)
1. An evaporation and dissolution integrated process device is characterized in that: the evaporation of water and the dissolution of aluminum hydroxide are combined into a heat balance system; the equipment comprises a stock solution III-effect evaporator and separation chamber (2), a stock solution II-effect evaporator and separation chamber (3), a stock solution I-effect evaporator and separation chamber (4), a beating tank (5), a new steam heater (6), a heat preservation tank (7), a dissolution liquid I-effect evaporator and separation chamber (8), a dissolution liquid II-effect evaporator and separation chamber (9), a dissolution liquid III-effect evaporator and separation chamber (10), a dissolution liquid flash tank (11), a new steam water seal tank (12), a new steam condensate I-stage flash tank (13), a new steam condensate II-stage flash tank (14), a new steam condensate III-stage flash tank (15), a new steam condensate IV-stage flash tank (16), a new steam condensate V-stage flash tank (17), an exhaust steam water seal tank (18), an exhaust steam condensate I-stage flash tank (19), an exhaust steam condensate II-stage flash tank (20), an exhaust steam condensate III-stage flash tank (21), An IV-level flash tank (22) of dead steam condensate and a water cooler (23);
the original liquid III-effect evaporator and separation chamber (2) is connected with an original liquid II-effect evaporator and separation chamber (3), the original liquid II-effect evaporator and separation chamber (3) is connected with an original liquid I-effect evaporator and separation chamber (4), the original liquid I-effect evaporator and separation chamber (4) is connected with a beating tank (5), the beating tank (5) is connected with a new steam heater (6), the new steam heater (6) is connected with a heat insulation tank (7), the heat insulation tank (7) is connected with a dissolving liquid I-effect evaporator and separation chamber (8), the dissolving liquid I-effect evaporator and separation chamber (8) is connected with a dissolving liquid II-effect evaporator and separation chamber (9), the dissolving liquid II-effect evaporator and separation chamber (9) is connected with a dissolving liquid III-effect evaporator and separation chamber (10), and the dissolving liquid III-effect evaporator and separation chamber (10) is connected with a dissolving liquid flash tank (11);
the new steam heater (6), the first-effect evaporator of the dissolved liquid and the separation chamber (8) are respectively connected with a new steam water seal tank (12), the new steam water seal tank (12) is connected with a first-stage flash tank (13) of new steam condensate, the first-stage flash tank (13) of new steam condensate is connected with a second-stage flash tank (14) of new steam condensate, the second-stage flash tank (14) of new steam condensate is connected with a third-stage flash tank (15) of new steam condensate, the third-stage flash tank (15) of new steam condensate is connected with a fourth-stage flash tank (16), and the fourth-stage flash tank (16) of new steam condensate is connected with a fourth-stage flash tank (17) of new steam condensate;
the II-effect dissolved liquid evaporator and separation chamber (9) is connected with a dead steam water seal tank (18), the dead steam water seal tank (18) is connected with a dead steam condensate I-level flash tank (19), the dead steam condensate I-level flash tank (19) is connected with a dead steam condensate II-level flash tank (20), the dead steam condensate II-level flash tank (20) is connected with a dead steam condensate III-level flash tank (21), and the dead steam condensate III-level flash tank (21) is connected with a dead steam condensate IV-level flash tank (22); the stock solution III-effect evaporator and the separation chamber (2) are connected with a water cooler (23);
the number of the stock solution multi-effect evaporators, the number of the dissolution solution multi-effect evaporators, the number of the new steam condensate flash tanks and the number of the dead steam condensate flash tanks are increased or decreased according to the Nk concentration of the concentrated solution and the Nk concentration of the dissolution solution.
2. The integrated evaporative dissolution process apparatus according to claim 1, wherein: the equipment also comprises an MVR evaporation system (1), wherein the MVR evaporation system (1) is connected with the stock solution III-effect evaporator and the separation chamber (2).
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| CN202021349552.0U CN212954328U (en) | 2020-07-10 | 2020-07-10 | Evaporation and dissolution integrated process equipment |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111661859A (en) * | 2020-07-10 | 2020-09-15 | 中铝山东工程技术有限公司 | Evaporation and dissolution integrated process equipment and process flow thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111661859A (en) * | 2020-07-10 | 2020-09-15 | 中铝山东工程技术有限公司 | Evaporation and dissolution integrated process equipment and process flow thereof |
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