CN214360287U - Be used for aluminium oxide production to dissolve out evaporation integration process units - Google Patents
Be used for aluminium oxide production to dissolve out evaporation integration process units Download PDFInfo
- Publication number
- CN214360287U CN214360287U CN202023344579.3U CN202023344579U CN214360287U CN 214360287 U CN214360287 U CN 214360287U CN 202023344579 U CN202023344579 U CN 202023344579U CN 214360287 U CN214360287 U CN 214360287U
- Authority
- CN
- China
- Prior art keywords
- falling
- film evaporator
- evaporation
- steam
- heat exchanger
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Manufacture And Refinement Of Metals (AREA)
Abstract
The utility model discloses a dissolving-out and evaporation integrated process device for alumina production, which comprises a pressure decanter, a dissolving-out heat preservation tank, a new steam heater, a new steam condensate water preheater, a secondary steam preheater, a red mud heat exchanger discharged after dissolving-out, a falling film evaporator, an evaporation circulating pump, an evaporation material passing pump, a solution flash evaporator, an indirect heat exchanger, a water cooler and a water seal tank, wherein the condensate water tank of the condensate water tank comprises a new steam condensate water tank and an evaporation condensate water tank; the components are correspondingly connected to form an ore pulp channel, a red mud discharging channel after digestion, a digestion liquid channel, an evaporation stock solution channel, a new steam channel, a secondary steam channel, a new steam condensate channel and a secondary steam condensate channel. The device is suitable for a Bayer process alumina production process system, and is particularly suitable for newly-built Bayer process alumina plants. The process device can mutually utilize the dissolving energy and the evaporation energy, reduce a flash evaporation system, improve the heat efficiency, reduce the investment cost and reduce the operation cost.
Description
Technical Field
The utility model belongs to the technical field of alumina production, and relates to an integrated process unit for dissolution and evaporation in alumina production.
Background
The Bayer process is used in alumina producing plant in China and includes the reaction between bauxite and caustic alkali solution at certain temperature in leaching workshop to produce leached slurry, diluting the leached slurry with one washing liquid, depositing and separating the diluted solution to obtain refined solution, adding aluminum hydroxide seed, crystallizing while stirring, roasting the produced aluminum hydroxide to burn out the attached water and crystal water to obtain alumina product, evaporating the decomposed mother solution to obtain evaporated mother solution, washing and depositing the evaporated mother solution to dilute the leached slurry, and forming the digestion-dilution-decomposition-evaporation circulation. At present, in alumina factories in China, a dissolution process device and an evaporation process device are two independent systems, each system is provided with a flash evaporation cooling system, and the problems of low thermal efficiency and the like caused by multiple energy conversion due to the multiple flash evaporation systems exist.
SUMMERY OF THE UTILITY MODEL
The utility model provides a dissolve out evaporation integration process units for alumina production, which aims at solving the problems of the existing dissolution device and evaporation device in the alumina plant. The device is suitable for a Bayer process alumina production process system, and is particularly suitable for newly-built Bayer process alumina plants. The process device can mutually utilize the dissolving energy and the evaporation energy, reduce a flash evaporation system, improve the heat efficiency, reduce the investment cost and reduce the operation cost.
The utility model adopts the following technical scheme:
the utility model provides a be used for aluminium oxide production to dissolve out evaporation integration process units, includes pressure decanter, dissolves out heat preservation jar, new steam heater, new steam condensate water pre-heater, secondary steam pre-heater, discharges red mud heat exchanger outside after dissolving out, falling film evaporator, evaporation circulating pump, evaporation material passing pump, solution flash vessel, indirect heat exchanger, water cooler and water seal tank, the condensate water jar include new steam condensate water jar and evaporation condensate water jar, wherein:
the secondary steam preheater, the new steam condensate water preheater, the new steam heater, the dissolution heat-preservation tank and the pressure decanter 1 are sequentially connected, and the secondary steam preheater is connected into the raw ore pulp to form an ore pulp channel;
the indirect heat exchangers are provided with a plurality of heat exchangers, and specifically comprise a first indirect heat exchanger, a second indirect heat exchanger, … and an nth indirect heat exchanger; wherein the second indirect heat exchanger to the nth indirect heat exchanger are connected in series;
the pressure decanter comprises a bottom outlet and a top overflow port, and the bottom outlet is connected with an outward red mud heat exchanger to form an outward red mud channel after dissolution; the top overflow port is connected with the second indirect heat exchanger to form a dissolving liquid channel;
n-1 secondary steam preheaters are arranged in series;
the falling film evaporator entry connect new steam for evaporation, the falling film evaporator includes anterior segment falling film evaporator and back end falling film evaporator, anterior segment falling film evaporator be used for realizing that the raw ore pulp preheats, wherein:
the front section falling-film evaporator and the indirect heat exchanger are both provided with n, the front section falling-film evaporator and the indirect heat exchanger are sequentially connected in series, specifically, the nth falling-film evaporator is connected with the nth-1 falling-film evaporator through the nth indirect heat exchanger, the nth-1 falling-film evaporator is connected with the nth-2 falling-film evaporator through the nth-1 indirect heat exchanger, … … the second falling-film evaporator is connected with the first falling-film evaporator through the second indirect heat exchanger, the first falling-film evaporator is connected with the first indirect heat exchanger, and the outlet of the first indirect heat exchanger is connected with the dissolution heat-preservation tank;
the falling-film evaporators are provided with upper steam outlets and bottom mother liquor outlets, and the steam outlets of the falling-film evaporators are connected with the next falling-film evaporator, wherein the steam outlet of the front falling-film evaporator is sequentially connected with the secondary steam preheater in series, specifically, the steam outlet of the first falling-film evaporator is connected with the second falling-film evaporator through the (n-1) th secondary steam preheater, the steam outlet of the second falling-film evaporator is connected with the third falling-film evaporator through the (n-2) th secondary steam preheater, and the steam outlet of the (n-1) th falling-film evaporator is connected with the nth falling-film evaporator through the first secondary steam preheater;
the rear-stage falling-film evaporator is provided with n + x falling-film evaporators, including the (n + 1) th falling-film evaporator, … and the (n + x) th falling-film evaporator, namely the last-effect falling-film evaporator;
the nth indirect heat exchanger is connected with the (n + 1) th falling film evaporator through solution flash steam;
the red mud outward-discharging heat exchanger is communicated with an evaporation stock solution, the red mud outward-discharging heat exchanger is respectively connected with the front section falling-film evaporator and the rear section falling-film evaporator, each falling-film evaporator is provided with a liquid inlet and a mother liquid outlet, all the falling-film evaporators are sequentially connected through liquid pipelines to realize step evaporation and concentration, and particularly, the mother liquid outlet of the rear-stage falling-film evaporator is connected with the liquid inlet of the front-stage falling-film evaporator.
And a new steam condensate water collecting tank is connected between the new steam heater and the new steam condensate water preheater.
The last effect falling film evaporator is sequentially connected with a water cooler and a water seal tank, the water cooler introduces circulating upper water, and the water seal tank discharges circulating lower water.
The falling-film evaporators are all provided with condensate water tanks, wherein the first falling-film evaporator is provided with a new steam condensate water tank, the rest falling-film evaporators are connected with evaporation condensate water tanks, and the evaporation condensate water tanks are sequentially connected through pipelines.
The bottom of the falling film evaporator is connected with an evaporation circulating pump and an evaporation material passing pump.
The device forms an ore pulp channel, a red mud discharging channel after digestion, a digestion liquid channel, an evaporation stock solution channel, a new steam channel, a secondary steam channel, a new steam condensate channel and a secondary steam condensate channel. The process trend of each channel is as follows:
a pulp channel:
raw ore pulp from a raw material grinding workshop sequentially enters a secondary steam preheater, a new steam condensate water preheater, a new steam heater, a dissolution heat-preservation tank and a pressure decanter.
The secondary steam preheater preheats the ore pulp by adopting high-temperature secondary steam from evaporation, the fresh steam condensate preheater preheats the ore pulp by dissolving fresh steam condensate at high temperature, the fresh steam heater heats the preheated ore pulp by adopting medium-high pressure fresh steam, the ore pulp is heated to the dissolving temperature and then is connected into a dissolving-out heat-preserving tank by a pipeline, and the ore pulp enters a pressure decanter after being kept for 10-30 min.
Discharging the red mud out of the red mud channel after dissolution:
and after dissolution, the ore pulp is subjected to solid-liquid separation by a pressure decanter, and the underflow is connected into a red mud heat exchanger after dissolution.
A dissolution liquid channel:
after digestion, the ore pulp is subjected to solid-liquid separation by a pressure decanter, overflow is dissolved liquid, the dissolved liquid is connected to an indirect heat exchanger, the indirect heat exchanger is used for cooling the dissolved liquid and raising the temperature of evaporation stock solution, the number of the indirect heat exchangers is determined according to the effect number of evaporators, and generally 3 evaporators with 6 effects and 4 evaporators with 7 effects are proposed.
Evaporating the stock solution channel:
the evaporation stock solution is divided into two strands, wherein one strand is sequentially connected with a digestion and discharge red mud heat exchanger, a falling film evaporator, an indirect heat exchanger, a new steam heater and a digestion heat-preservation tank.
The other strand is connected to a rear-stage falling-film evaporator.
The falling-film evaporator adopts 6-effect or 7-effect two-stage process, wherein one stage of stock solution is discharged through 6-effect and 5-effect, the other stage of stock solution is discharged through 4-effect, 3-effect, 2-effect and 1-effect, indirect heat exchangers are arranged between 4-1-effect, heat exchange is carried out between the indirect heat exchangers and the dissolution liquid, the high-temperature evaporation stock solution from 1-effect is connected to a first indirect heat exchanger and is heated to a certain temperature, and then the high-temperature evaporation stock solution enters a dissolution heat-preservation tank;
a new steam channel:
introducing new steam for dissolution into a new steam heater; and new steam for evaporation is connected into the first indirect heat exchanger and the falling film evaporator.
The new steam for dissolving out is connected with a new steam heater; the new steam for evaporation is respectively connected with a new steam heater and a falling film evaporator
A secondary steam passage:
the secondary steam which is evaporated is connected to a secondary steam preheater, the secondary steam which is flashed from the dissolved liquid is connected to the falling film evaporator, the last secondary steam which is evaporated is connected to the water cooler, and the secondary steam which is flashed from the condensation water tank is connected to the falling film evaporator.
Wherein, the secondary steam which is evaporated is connected into a secondary steam preheater for preheating the primary ore pulp, and the cooling water of a water cooler is evaporation circulating water which is generally about 35 ℃;
fresh steam condensate passage:
the new steam condensate water in the digestion section is connected into a new steam condensate water tank and a new steam condensate water preheater;
the new steam condensate water at the evaporation section is connected into a new steam condensate water tank;
secondary steam condensate water channel:
secondary steam condensate water from the falling film evaporator and the secondary steam preheater is connected into a secondary steam condensate water tank;
the channel connections are all pipeline connections;
the pressure decanter is a dissolving ore pulp pressure solid-liquid separator, the overflow is high-temperature dissolving liquid, and the underflow is discharged red mud after dissolving;
the dissolution heat-preservation tank determines whether stirring is added or not according to the diameter, and stirring is required to be added for enhancing dissolution effect when the diameter of the heat-preservation tank is larger than 4.5 m.
The new steam heater is a sleeve heater, the shell side of the sleeve is connected with new steam, and the tube side is connected with ore pulp or evaporation mother liquor.
The new steam condensate water preheater is a sleeve heater, the shell side of the sleeve is connected with new steam condensate water, and the tube side is connected with ore pulp.
The secondary steam preheater is a sleeve heater, the shell side of the sleeve is connected with the secondary steam for evaporation, and the tube side is connected with the ore pulp.
The heat exchanger for discharging red mud after digestion is a casing heater, the casing side of the casing is connected with evaporation stock solution, and the ore pulp after digestion is underflow of a pressure decanter.
The falling film evaporator is a 6-7-effect evaporator.
In the device, 1 condensation water tank is respectively arranged on each falling-film evaporator, wherein the first falling-film evaporator is connected with a new steam condensation water tank, the other falling-film evaporators are connected with an evaporation condensation water tank, and a circulating pump and a material passing pump are also required to be arranged on the falling-film evaporators.
The device can realize the full utilization of the dissolving-out evaporation heat energy; and the secondary temperature flashed by the one-effect falling-film evaporator is higher than the secondary steam flashed by the primary flash evaporator of the existing digestion device, so that the high-temperature evaporation secondary steam is introduced into the digestion secondary steam preheating section, the preheating temperature of the digestion pulp can be increased, the temperature difference is increased, and the area of a digestion preheater can be reduced.
The process adopting the device can adjust the feeding proportion of the evaporation stock solution at the high-temperature section of the evaporator according to the dissolved liquid Rp, and particularly, when the dissolved liquid Rp is increased, the feeding quantity of the evaporation stock solution at the high-temperature section is reduced; when the Rp of the dissolution liquid is reduced, the feeding amount of the evaporation stock solution at the high-temperature evaporation section is increased.
By adopting the process of the device, the evaporated mother liquor which is removed from dissolution does not need to be cooled, and is directly fed into the dissolution heat-preservation tank after being concentrated, so that the heat efficiency can be improved, the heat energy conversion times can be reduced, and the dissolution rate can be improved.
The device for dissolving and evaporating in the production of alumina comprises the following steps:
step 1, primary pulp preheating
Preheating the primary ore pulp by using secondary steam for evaporation, preheating the primary ore pulp from 70 ℃ to about 85-120 ℃, and then entering the step 2;
step 2, preheating ore pulp by using fresh steam condensate water
Indirectly preheating the preheated ore pulp from the step 1 by using high-temperature live steam condensate through a live steam condensate preheater;
in the step 2, the high-temperature condensed water is 180-210 ℃, and the temperature is reduced to 100-125 ℃. The raw ore pulp can be increased by about 10 ℃ through the indirect preheating of the new steam condensate water;
step 3, heating the ore pulp by new steam
The preheated ore pulp entering the new steam heater is indirectly heated to 145 +/-10 ℃ by new steam;
in the step 3, the new steam is one of the grades of 1.4MPa and 1.0MPa, the grades are different, the temperature of the condensate water obtained after the new steam is heated by the low-temperature new steam heater is different, and the preheating temperature of the preheated ore pulp is determined according to the temperature of the condensate water obtained by the low-temperature new steam heater in the low-temperature condensate water preheater.
Step 4, dissolution heat preservation reaction
The 145 +/-10 ℃ ore pulp coming out of the ore pulp channel of the warm fresh steam heater and part of the evaporation mother liquor from the step (8) are subjected to heat preservation and stay for 10-30 min, and qualified dissolved ore pulp is obtained;
in the step 4, the heat preservation can be performed by a pipeline or a heat preservation tank, and the dissolution temperature is 145 +/-10 ℃.
Step 5, solid-liquid separation
The qualified leached ore pulp from the step 4 enters a pressure decanter for solid-liquid separation to obtain overflow and leached red mud; the overflow is high-temperature dissolution liquid at about 145 ℃, the high-temperature dissolution liquid is pumped to the indirect heat exchanger in the step 8,
in the step 5, the content of suspended matters in the overflow obtained by the pressure decanter is less than or equal to 15mg/L, and the mass percentage concentration of the separated dissolved red mud is 40-45%.
Step 6, cooling the ore pulp after dissolution
Preheating the evaporation stock solution by the leached ore pulp from the step 5, discharging the leached ore pulp out of a red mud heat exchanger by a preheater, cooling the leached red mud to about 105 ℃, and then sending the leached red mud to a red mud washing process.
In the step 6, the heat exchange medium for dissolving out the red mud at high temperature adopts evaporation stock solution, the dissolving-out red mud is connected with a tube side, and the shell side is connected with the evaporation stock solution.
Step 7, evaporating the stock solution for preheating
And (3) carrying out heat exchange on the digested evaporation stock solution from the outside through the discharged red mud in the step (6) and the high-temperature digested red mud, and sending the heat-exchanged evaporation stock solution to the step (8).
Step 8, evaporating the evaporation stock solution
Flow path of evaporating stock solution
And (3) feeding the evaporation stock solution from the step (7) in 2 strands, wherein one strand of the evaporation stock solution sequentially enters a 6-effect falling-film evaporator and a 5-effect falling-film evaporator, is sent to other workshops of an alumina plant after being evaporated and concentrated to 180-200 g/l, and the other strand of the evaporation stock solution sequentially enters a 4-effect falling-film evaporator, a 3-effect indirect preheater, a 3-effect falling-film evaporator, a 2-effect indirect preheater, a 2-effect falling-film evaporator, a 1-effect indirect preheater and a 1-effect falling-film evaporator, and is sent to a dissolution heat-preserving tank by a pump after being concentrated.
Flow path of evaporation steam
The method comprises the following steps that 1 effect is heated by using new steam, one part of secondary steam evaporated by the 1 effect falling-film evaporator is sent to the step 1, the other part of the secondary steam evaporated by the 2 effect falling-film evaporator is sent to the step 1, the other part of the secondary steam evaporated by the 3 effect falling-film evaporator is sent to the step 1, the other part of the secondary steam is sent to the 4 effect falling-film evaporator for heating, the secondary steam evaporated by the 4 effect falling-film evaporator and the secondary steam from the step 9 are sent to the 5 effect falling-film evaporator for heating, the secondary steam evaporated by the 5 effect falling-film evaporator is sent to the 6 effect falling-film evaporator for heating, and the secondary steam evaporated by the 6 effect falling-film evaporator is connected to a water cooler.
Flow path for evaporating water
Each effect of evaporator is provided with a condensed water tank, the condensed water tank is connected by a pipeline, high-temperature condensed water is flashed step by step, flash secondary steam is connected into a heating chamber of the effect of falling film evaporator, and the process of pumping hot water station is used after the flash secondary steam condensed water enters the final effect of condensed water tank.
In the step 7, the other workshops are alumina plant raw material grinding workshops for grinding bauxite. The evaporation stock solution is connected with the tube pass of the falling film evaporator, and the new steam and the secondary steam are connected with the shell pass of the falling film evaporator. The water cooler cools and recovers the 6-effect secondary steam by adopting circulating water at about 35 ℃, and the outlet water temperature of the final-effect condensation water tank is about 68 ℃.
Step 9, flash evaporation of the dissolution liquid
And (4) carrying out heat exchange on the dissolved liquid from the step (5) by the indirect heat exchanger for evaporating the stock solution in the step (8) to a certain temperature, then cooling the dissolved liquid in a dissolved liquid flash evaporator, sending the cooled dissolved liquid to the next working section, and introducing the flash-evaporated secondary steam into the heating chamber of the 5-effect falling-film evaporator in the step (8).
In the step 9, the solution flash evaporator is adopted for flash evaporation of the dissolution liquid, an ore pulp flash evaporator is not adopted, and the flash evaporation temperature is about 105 ℃.
Has the advantages that:
1. the utility model discloses a be used for aluminium oxide production to dissolve out evaporation integration process units can reduce evaporation high temperature section stoste feed volume to reduce evaporation station and use vapour volume, reduce high temperature section evaporimeter heat transfer area, reduce the equipment investment and reduce, and the high temperature secondary vapour that evaporates out preheats for former ore pulp, can be higher with dissolving out the ore pulp preheating temperature, reduce and dissolve out the vapour volume.
2. The utility model directly pumps the evaporated high-temperature discharge to the dissolution heat-preservation tank for adjusting the dissolution liquid Rp and reducing the energy conversion times, thereby improving the heat efficiency; meanwhile, a separation settling tank for separating and washing red mud and a leaf filter for controlling filtration can be omitted, the process is simplified, and the operation cost and the investment cost are reduced.
3. The utility model discloses device make full use of high temperature dissolves liquid and preheats for high temperature section evaporation stock solution, dissolves liquid and carries out the flash distillation cooling through the flash vessel after the heat transfer, and the flash vessel connects to evaporation negative pressure section, realizes dissolving liquid ejection of compact temperature and further reduces, guarantees evaporation back end evaporation capacity simultaneously, but make full use of dissolves liquid heat.
4. Compared with the conventional device, the utility model discloses device flash vessel quantity reduces, only sets up 1 total and dissolves out liquid flash vessel, and adopts the device to evaporate thick back high temperature section evaporation mother liquor and directly send into the holding vessel, and high temperature mother liquor Rp value is lower, and solution alumina is great in the saturation degree not, directly gets into the holding vessel, can shorten the digestion time, dual reduction investment cost.
Drawings
FIG. 1 is a schematic structural diagram of a digestion and evaporation integrated process unit for alumina production according to embodiment 1 of the present invention;
fig. 2 is a flow chart of the dissolution and evaporation integrated process for alumina production of embodiment 1 of the present invention, wherein:
1-pressure decanter, 2-stripping heat-preserving tank, 3-new steam heater, 4-new steam condensate water preheater, 5-third secondary steam preheater, 6-second secondary steam preheater, 7-first secondary steam preheater, 8-new steam condensate water collecting tank, 9-stripping after-discharge red mud heat exchanger, 10-first indirect heat exchanger, 11-first falling film evaporator, 12-second falling film evaporator, 13-third falling film evaporator, 14-fourth falling film evaporator, 15-fifth falling film evaporator, 16-sixth falling film evaporator, 17-water cooler, 18-water seal tank, 19-new steam condensate water tank, 20-second evaporation condensate water tank, 21-third evaporation condensate water tank, 22-fourth evaporation condensate water tank, 23-a fifth evaporation condensate water tank, 24-a sixth evaporation condensate water tank, 25-an evaporation circulating pump, 26-an evaporation material passing pump, 27-a second indirect heat exchanger, 28-a third indirect heat exchanger, 29-a fourth indirect heat exchanger, 30-a solution flash evaporator, 31-circulating water feeding, 32-new steam, 33-evaporation stock solution, 34-raw ore pulp, 35-new steam, 36-dissolved new steam condensate water, 37-dissolved red mud, 38-circulating water discharging, 39-secondary steam condensate water, 40-evaporated new steam condensate water, 41-evaporation mother liquor and 42-dissolved liquor.
Detailed Description
The present invention will be described in further detail with reference to examples.
The utility model provides a be used for aluminium oxide production to dissolve out evaporation integration process units, includes pressure decanter, dissolves out heat preservation jar, new steam heater, new steam condensate water pre-heater, secondary steam pre-heater, new steam condensate water jar, discharge red mud heat exchanger after dissolving out, falling film evaporator, evaporation circulating pump, evaporation material passing pump, evaporation condensate water jar, solution flash vessel, indirect heat exchanger, water cooler and water seal tank, wherein:
the secondary steam preheater, the new steam condensate water preheater, the new steam heater, the dissolution heat-preservation tank and the pressure decanter are sequentially connected, and the secondary steam preheater is connected into the raw ore pulp to form an ore pulp channel;
the indirect heat exchangers are provided with a plurality of heat exchangers, and specifically comprise a first indirect heat exchanger, a second indirect heat exchanger, … and an nth indirect heat exchanger; the second indirect heat exchanger and the nth indirect heat exchanger are connected in series;
the pressure decanter comprises a bottom outlet and a top overflow port, and the bottom outlet is connected with an outward red mud heat exchanger to form an outward red mud channel after dissolution; the top overflow port is connected with the second indirect heat exchanger to form a dissolving liquid channel;
n-1 secondary steam preheaters are arranged in series;
the falling film evaporator entry connect new steam for evaporation, the falling film evaporator includes anterior segment falling film evaporator and back end falling film evaporator, anterior segment falling film evaporator be used for realizing that the raw ore pulp preheats, wherein:
the front section falling-film evaporator and the indirect heat exchanger are both provided with n, the front section falling-film evaporator and the indirect heat exchanger are sequentially connected in series, specifically, the nth falling-film evaporator is connected with the nth-1 falling-film evaporator through the nth indirect heat exchanger, the nth-1 falling-film evaporator is connected with the nth-2 falling-film evaporator through the nth-1 indirect heat exchanger, … … the second falling-film evaporator is connected with the first falling-film evaporator through the second indirect heat exchanger, the first falling-film evaporator is connected with the first indirect heat exchanger, and the outlet of the first indirect heat exchanger is connected with the dissolution heat-preservation tank;
the falling-film evaporators are provided with upper steam outlets and bottom mother liquor outlets, and the steam outlets of the falling-film evaporators are connected with the next falling-film evaporator, wherein the steam outlet of the front falling-film evaporator is sequentially connected with the secondary steam preheater in series, specifically, the steam outlet of the first falling-film evaporator is connected with the second falling-film evaporator through the (n-1) th secondary steam preheater, the steam outlet of the second falling-film evaporator is connected with the third falling-film evaporator through the (n-2) th secondary steam preheater, and the steam outlet of the (n-1) th falling-film evaporator is connected with the nth falling-film evaporator through the first secondary steam preheater;
the rear-stage falling-film evaporator is provided with n + x falling-film evaporators, including the (n + 1) th falling-film evaporator, … and the (n + x) th falling-film evaporator, namely the last-effect falling-film evaporator;
the nth indirect heat exchanger is connected with the (n + 1) th falling film evaporator through solution flash steam;
the red mud outward-discharging heat exchanger is communicated with an evaporation stock solution, the red mud outward-discharging heat exchanger is respectively connected with the front section falling-film evaporator and the rear section falling-film evaporator, each falling-film evaporator is provided with a liquid inlet and a mother liquid outlet, all the falling-film evaporators are sequentially connected through liquid pipelines to realize step evaporation and concentration, and particularly, the mother liquid outlet of the rear-stage falling-film evaporator is connected with the liquid inlet of the front-stage falling-film evaporator.
And a new steam condensate water collecting tank is connected between the new steam heater and the new steam condensate water preheater.
The last effect falling film evaporator is sequentially connected with a water cooler and a water seal tank, the water cooler introduces circulating upper water, and the water seal tank discharges circulating lower water.
The falling-film evaporators are all provided with condensate water tanks, wherein the first falling-film evaporator is provided with a new steam condensate water tank, the rest falling-film evaporators are connected with evaporation condensate water tanks, and the evaporation condensate water tanks are sequentially connected through pipelines.
The bottom of the falling film evaporator is connected with an evaporation circulating pump and an evaporation material passing pump.
Example 1
A dissolving-out and evaporating integrated process device for alumina production is shown in a schematic structural diagram in figure 1, and comprises all devices in the figure, wherein the devices are connected through pipelines. The connection mode is as follows:
the bottom flow of a pressure decanter 1 is connected with a tube pass of a red mud heat exchanger 9 which is discharged after digestion, the overflow is connected with a tube pass of a second indirect heat exchanger 27, new steam 32 is connected with a shell pass of a new steam heater 3, raw ore pulp 34 is connected with a tube pass of the first secondary steam preheater 7, the second secondary steam preheater 6 and a third secondary steam preheater 5, the tube pass of the new steam condensate water preheaters 4 is connected through a pipeline, a new steam condensate water collecting tank 8 is connected between the new steam heater 3 and the new steam condensate water preheater 4, the new steam condensate water preheater 4 obtains the digestion new steam condensate water 36, the secondary steam which is evaporated is connected with the third secondary steam preheater 5, the second secondary steam preheater 6, the shell pass of the first secondary steam preheater 7, the outlet of the tube pass of the new steam heater 3 is connected with a digestion heat-preserving tank 2, the digestion heat-preserving tank 2 is connected with the pressure decanter 1, the evaporation stock solution 33 is connected with the shell pass of a digestion-finished discharged red mud heat exchanger 9 to obtain digestion-finished red mud 37, the shell pass outlet of the digestion-finished discharged red mud heat exchanger is connected with a sixth falling film evaporator 16, a fourth falling film evaporator 14 is connected with a tube pass, the sixth falling film evaporator 16 is connected with a fifth falling film evaporator 15, each falling film evaporator is connected with an evaporation circulating pump 25 and an evaporation material pump 26, the fifth falling film evaporator 15 is connected with evaporation mother solution 41, the 4-effect falling film tube pass outlet is connected with a fourth indirect heat exchanger 29, the shell pass outlet of the fourth indirect heat exchanger 29 is connected with a 4-effect falling film tube pass, the 3-effect falling film tube pass outlet is connected with a third indirect heat exchanger 28, the shell pass outlet of the third indirect heat exchanger 28 is connected with a 2-effect falling film tube pass, the shell pass outlet of the 2-effect falling film tube pass is connected with a second indirect heat exchanger 27, the shell pass outlet of the second indirect heat exchanger 27 is connected with a 1-effect falling film tube pass outlet, the 1-effect falling film tube pass outlet is connected with a first indirect heat exchanger 10, the tube pass outlet of the first indirect heat exchanger 10 is connected with the digestion heat-preservation tank 2, the tube pass outlet of the second indirect heat exchanger 27 is connected with the tube pass inlet of the third indirect heat exchanger 28, the tube pass outlet of the third indirect heat exchanger 28 is connected with the tube pass inlet of the fourth indirect heat exchanger 29, the tube pass outlet of the fourth indirect heat exchanger 29 is connected with the inlet of the solution flash evaporator 30, the steam outlet of the solution flash evaporator 30 is connected with the shell pass of the falling-film evaporator 15, the solution outlet of the solution flash evaporator 30 is connected with the digestion liquid 42, the steam outlet of the first falling-film evaporator 11 is connected with the shell pass of the second falling-film evaporator 12 and the shell pass of the secondary steam preheater 5, the steam outlet of the second falling-film evaporator 12 is connected with the shell pass of the third falling-film evaporator 13 and the shell pass of the secondary steam preheater 6, the steam outlet of the third falling-film evaporator 13 is connected with the shell pass of the fourth falling-film evaporator 14 and the shell pass of the secondary steam preheater 7, the steam outlet of the fourth falling-film evaporator 14 is connected with the shell pass of the fifth falling-film evaporator 15, the shell pass of the fifth falling-film evaporator 15 is connected with the shell pass of the sixth falling film evaporator 16, a steam outlet of the sixth falling-film evaporator 16 is connected with a water cooler 17, the water cooler 17 is connected with circulating water supply 31, a water outlet of the water cooler 17 is connected with a water seal tank 18, an outlet of the water seal tank 18 is connected with circulating water supply 38, new steam 35 is connected with an indirect heat exchanger shell side and a falling-film evaporator 11 shell side, a new steam condensate water tank 19, a second steam condensate water tank 20, a third steam condensate water tank 21, a fourth steam condensate water tank 22, a fifth steam condensate water tank 23, a sixth steam condensate water tank 24 steam ports are respectively connected with the first falling-film evaporator 11, the second falling-film evaporator 12, the third falling-film evaporator 13, the fourth falling-film evaporator 14, the fifth falling-film evaporator 15, the sixth falling-film evaporator 16 shell side condensate water, outlets of the first falling-film evaporator 11-16 shell side are correspondingly connected with the new steam condensate water tank 19, inlets of the second falling-film evaporator 20-24, and a new steam condensate water tank 19 discharges new steam condensate water 40, the sixth steam condensate tank 24 discharges secondary steam condensate 39.
A dissolution and evaporation integrated process method for alumina production is carried out by adopting the device, the process flow chart is shown in figure 2, and the process method comprises the following steps:
step 1, primary pulp preheating
70.86 ℃, preheating raw ore pulp by using secondary steam for evaporation at 300g/l, Rp0.652 and Nk182g/l of raw ore pulp to about 89.43 ℃, and then entering the step 2;
step 2, preheating ore pulp by using fresh steam condensate water
Preheating ore pulp at 89.43 ℃ from the step 1, indirectly preheating by utilizing high-temperature live steam condensate water through a live steam condensate water preheater to 98.40 ℃, and cooling the high-temperature condensate water from 180 ℃ to 105.65 ℃;
step 3, heating the ore pulp by new steam
Heating 105.65 deg.C with 180 deg.C saturated fresh steam to 148.93 deg.C;
step 4, dissolution heat preservation reaction
Carrying out heat preservation and retention on 148.93 ℃, 168.29g/l of solid content, Rp1.236 and Nk159g/l of ore pulp from the step 3 and 144.76 ℃, Rp0.57 and Nk206.86g/l of evaporation mother liquor from the step 8 for 10min to obtain 108.90g/l, Rp1.19 and Nk165.5g/l of qualified digestion ore pulp;
step 5, solid-liquid separation
Enabling the qualified digestion ore pulp with solid content of 108.90g/l, Rp1.19 and Nk165.5g/l from the step 4 to enter a pressure decanter for solid-liquid separation to obtain overflow digestion liquid with solid content of 0.015g/l, Rp1.19 and Nk165.5g/l and digestion red mud with solid content of 739 g/l; the overflow is high temperature dissolution liquid at about 145 ℃, the overflow is pumped to the indirect heat exchanger in the step 8, and the underflow is sent to the step 6.
Step 6, cooling the ore pulp after dissolution
Preheating the 145 ℃ solid content 739g/l digested ore pulp from the step 5 to 89.17 ℃ for 84.47 ℃, Rp0.57 and Nk144.98g/l evaporation stock solution, cooling the digested red mud from 145 ℃ to 105 ℃, and sending the cooled digested red mud to a red mud washing process.
Step 7, evaporating the stock solution for preheating
84.47 ℃, Rp0.57 and Nk144.98g/l of evaporation stock solution from the outside is subjected to heat exchange and preheating of discharged red mud after digestion in the step 6 to 89.17 ℃, and then the red mud is sent to the step 8.
Step 8, evaporating the evaporation stock solution
Flow path of evaporating stock solution
And (3) feeding 89.17 ℃, Rp0.57 and Nk144.98g/l of evaporation stock solution from the step 7 by 2 strands, sequentially feeding 76.5 percent of evaporation stock solution into a 6-effect falling-film evaporator and a 5-effect falling-film evaporator, evaporating and concentrating to 185g/l, then feeding the evaporation stock solution into other workshops of an alumina plant, and sequentially feeding the rest of the evaporation stock solution, 23.5 percent, 89.17 ℃, Rp0.57 and Nk144.98g/l of evaporation stock solution into a 4-effect falling-film evaporator, a 3-effect indirect preheater, a 3-effect falling-film evaporator, a 2-effect indirect preheater, a 2-effect falling-film evaporator, a 1-effect indirect preheater and a 1-effect falling-film evaporator, concentrating to 206g/l, and then pumping to a dissolution heat-preservation tank.
Flow path of evaporation steam
The 1-effect evaporator is heated by using 158 ℃ saturated new steam, 60% of 132 ℃ secondary steam evaporated by the 1-effect falling-film evaporator is sent to the step 1, the other 40% of the 132 ℃ secondary steam is sent to the 2-effect falling-film evaporator for heating, 60% of 117 ℃ secondary steam evaporated by the 2-effect falling-film evaporator is sent to the step 1, the other 40% of the 3-effect falling-film evaporator is sent to the step 1 for heating, the other 40% of the 105 ℃ secondary steam evaporated by the 3-effect falling-film evaporator is sent to the step 1 for heating, the 94 ℃ secondary steam evaporated by the 4-effect falling-film evaporator and the 94 ℃ secondary steam from the step 9 are sent to the 5-effect falling-film evaporator for heating together, the 68 ℃ secondary steam evaporated by the 5-effect falling-film evaporator is sent to the 6-effect falling-film evaporator for heating, and the 50 ℃ secondary steam evaporated by the 6-effect falling-film evaporator is sent to the water cooler.
Flow path for evaporating water
Each effect evaporator is provided with a condensed water tank, the condensed water tank is connected by a pipeline, high-temperature condensed water is flashed step by step, flash secondary steam is connected into a heating chamber of the effect falling film evaporator, and 68 ℃ secondary steam condensed water 39 is evaporated and enters the final effect condensed water tank and then is pumped into a hot water station.
Step 9, flash evaporation of the dissolution liquid
And (3) evaporating the dissolved liquid at 145 ℃ from the step (5) by using an indirect stock solution heat exchanger in the step (8), after heat exchange is carried out to 124 ℃, entering a dissolved liquid flash evaporator for cooling, sending to the next section after cooling to 102.8 ℃, and introducing the flash-evaporated secondary steam at 94 ℃ into the heating chamber of the 5-effect falling-film evaporator in the step (8).
Example 2
The structure of the integrated dissolving and evaporating process device for producing alumina is the same as that of the embodiment 1, and the integrated dissolving and evaporating process device is particularly used for dissolving the mixed bauxite of gibbsite and boehmite.
A gibbsite and boehmite mixed bauxite dissolving-out process method adopts the device and comprises the following steps:
step 1, primary pulp preheating
70.86 ℃, preheating raw ore pulp by using secondary steam for evaporation at 300g/l, Rp0.652 and Nk182g/l of raw ore pulp, preheating to about 86.78 ℃, and then entering the step 2;
step 2, preheating ore pulp by using fresh steam condensate water
Preheating ore pulp at 86.78 ℃ from the step 1, indirectly preheating the ore pulp by using high-temperature live steam condensate water through a live steam condensate water preheater to 96.23 ℃, and cooling the high-temperature condensate water from 180 ℃ to 104.64 ℃;
step 3, heating the ore pulp by new steam
Heating 104.64 deg.C with 180 deg.C saturated fresh steam to 149.08 deg.C;
step 4, dissolution heat preservation reaction
Keeping the 149.08 ℃, 168.29g/l, Rp1.236 and Nk159g/l of ore pulp from the step 3 and 144.28 ℃, Rp0.57 and Nk201g/l of evaporation mother liquor from the step 8 at the same time for 15min to obtain 105.85g/l, Rp1.17 and Nk165.62g/l of qualified digestion ore pulp;
step 5, solid-liquid separation
Enabling the qualified digestion ore pulp with solid content of 105.85g/l, Rp1.17 and Nk165.62g/l from the step 4 to enter a pressure decanter for solid-liquid separation to obtain overflow digestion liquid with solid content of 0.015g/l, Rp1.17 and Nk165.62g/l and digestion red mud with solid content of 739 g/l; the overflow is high temperature dissolution liquid at about 145 ℃, the overflow is pumped to the indirect heat exchanger in the step 8, and the underflow is sent to the step 6.
Step 6, cooling the ore pulp after dissolution
Preheating the 145 ℃ solid content 739g/l digested ore pulp from the step 5 to 89.17 ℃ for 84.47 ℃, Rp0.57 and Nk144.98g/l evaporation stock solution, cooling the digested red mud from 145 ℃ to 105 ℃, and sending the cooled digested red mud to a red mud washing process.
Step 7, evaporating the stock solution for preheating
84.47 ℃, Rp0.57 and Nk144.98g/l of evaporation stock solution from the outside is subjected to heat exchange and preheating of discharged red mud after digestion in the step 6 to 89.17 ℃, and then the red mud is sent to the step 8.
Step 8, evaporating the evaporation stock solution
Flow path of evaporating stock solution
And (3) feeding 89.17 ℃, Rp0.57 and Nk144.98g/l of evaporation stock solution from the step 7 by 2 strands, sequentially feeding 73.5 percent of evaporation stock solution into a 6-effect falling-film evaporator and a 5-effect falling-film evaporator, evaporating and concentrating to 186g/l, then feeding the evaporation stock solution into other workshops of an alumina plant, and sequentially feeding the rest 26.5 percent, 89.17 ℃, Rp0.57 and Nk144.98g/l of evaporation stock solution into a 4-effect falling-film evaporator, a 3-effect indirect preheater, a 3-effect falling-film evaporator, a 2-effect indirect preheater, a 2-effect falling-film evaporator, a 1-effect indirect preheater and a 1-effect falling-film evaporator, concentrating to 201g/l, and then pumping to a dissolution heat-preserving tank.
Flow path of evaporation steam
The 1-effect evaporator is heated by using 158 ℃ saturated new steam, 50% of 132 ℃ secondary steam evaporated by the 1-effect falling-film evaporator is sent to the step 1, 50% of the other steam is sent to the 2-effect falling-film evaporator for heating, 50% of 117 ℃ secondary steam evaporated by the 2-effect falling-film evaporator is sent to the step 1, 50% of the other steam is sent to the 3-effect falling-film evaporator for heating, 50% of 105 ℃ secondary steam evaporated by the 3-effect falling-film evaporator is sent to the step 1, 50% of the other steam is sent to the 4-effect falling-film evaporator for heating, 94 ℃ secondary steam evaporated by the 4-effect falling-film evaporator and 94 ℃ secondary steam from the step 9 are sent to the 5-effect falling-film evaporator for heating, 68 ℃ secondary steam evaporated by the 5-effect falling-film evaporator is sent to the 6-effect falling-film evaporator for heating, and 50 ℃ secondary steam evaporated by the 6-effect falling-film evaporator is sent to the water cooler.
Flow path for evaporating water
Each effect of evaporator is provided with a condensed water tank, the condensed water tank is connected by a pipeline, the high-temperature condensed water is flashed step by step, flash secondary steam is connected into a heating chamber of the effect of falling film evaporator, and the secondary steam condensed water at 68 ℃ is evaporated and enters the final effect of condensed water tank and then is pumped into a hot water station.
Step 9, flash evaporation of the dissolution liquid
And (3) evaporating the dissolved liquid at 145 ℃ from the step (5) by using an indirect stock solution heat exchanger in the step (8), after heat exchange is carried out to 122 ℃, entering a dissolved liquid flash evaporator for cooling, sending to the next section after cooling to 102.8 ℃, and introducing the flash-evaporated secondary steam at 94 ℃ into the heating chamber of the 5-effect falling-film evaporator in the step (8).
Claims (4)
1. The utility model provides a be used for aluminium oxide production to dissolve out evaporation integration process units, its characterized in that, includes pressure decanter, dissolves out heat preservation jar, new steam heater, new steam condensate water pre-heater, secondary steam pre-heater, discharges red mud heat exchanger, falling film evaporator, evaporation circulating pump, evaporation material passing pump, solution flash vessel, indirect heat exchanger, water cooler and water seal tank after dissolving out, the condensate water jar include new steam condensate water jar and evaporation condensate water jar, wherein:
the secondary steam preheater, the new steam condensate water preheater, the new steam heater, the dissolution heat-preservation tank and the pressure decanter are sequentially connected, and the secondary steam preheater is connected to the raw ore pulp;
the indirect heat exchangers are provided with a plurality of heat exchangers, and specifically comprise a first indirect heat exchanger, a second indirect heat exchanger, … and an nth indirect heat exchanger; the second indirect heat exchanger … to the nth indirect heat exchanger are connected in series;
the pressure decanter comprises a bottom outlet and a top overflow port, and the bottom outlet is connected with an outward red mud heat exchanger to form an outward red mud channel after dissolution; the top overflow port is connected with the second indirect heat exchanger to form a dissolving liquid channel;
n-1 secondary steam preheaters are arranged in series;
the falling film evaporator entry connect new steam for evaporation, the falling film evaporator includes anterior segment falling film evaporator and back end falling film evaporator, anterior segment falling film evaporator be used for realizing that the raw ore pulp preheats, wherein:
the front section falling-film evaporator and the indirect heat exchanger are both provided with n, the front section falling-film evaporator and the indirect heat exchanger are sequentially connected in series, specifically, the nth falling-film evaporator is connected with the nth-1 falling-film evaporator through the nth indirect heat exchanger, the nth-1 falling-film evaporator is connected with the nth-2 falling-film evaporator through the nth-1 indirect heat exchanger, … … the second falling-film evaporator is connected with the first falling-film evaporator through the second indirect heat exchanger, the first falling-film evaporator is connected with the first indirect heat exchanger, and the outlet of the first indirect heat exchanger is connected with the dissolution heat-preservation tank;
the falling-film evaporators are provided with upper steam outlets and bottom mother liquor outlets, and the steam outlets of the falling-film evaporators are connected with the next falling-film evaporator, wherein the steam outlet of the front falling-film evaporator is sequentially connected with the secondary steam preheater in series, specifically, the steam outlet of the first falling-film evaporator is connected with the second falling-film evaporator through the (n-1) th secondary steam preheater, the steam outlet of the second falling-film evaporator is connected with the third falling-film evaporator through the (n-2) th secondary steam preheater, and the steam outlet of the (n-1) th falling-film evaporator is connected with the nth falling-film evaporator through the first secondary steam preheater;
the rear-stage falling-film evaporator is provided with n + x falling-film evaporators, including the (n + 1) th falling-film evaporator, … and the (n + x) th falling-film evaporator, namely the last-effect falling-film evaporator;
the nth indirect heat exchanger is connected with the (n + 1) th falling film evaporator through solution flash steam;
the red mud outward-discharging heat exchanger is communicated with an evaporation stock solution, the red mud outward-discharging heat exchanger is respectively connected with the front section falling-film evaporator and the rear section falling-film evaporator, each falling-film evaporator is provided with a liquid inlet and a mother liquid outlet, all the falling-film evaporators are sequentially connected through liquid pipelines to realize step evaporation and concentration, and particularly, the mother liquid outlet of the rear-stage falling-film evaporator is connected with the liquid inlet of the front-stage falling-film evaporator.
2. The integrated digestion and evaporation process unit for alumina production according to claim 1, wherein the last-effect falling-film evaporator is connected with a water cooler and a water seal tank in sequence, the water cooler introduces circulating upper water, and the water seal tank discharges circulating lower water.
3. The integrated digestion and evaporation process unit for alumina production according to claim 1, wherein the condensate tank is connected with each falling-film evaporator in a matching manner, wherein the first falling-film evaporator is connected with the new steam condensate tank, and the remaining falling-film evaporators are connected with the evaporation condensate water tank.
4. The integrated dissolving and evaporating process unit for aluminum oxide production according to claim 1, wherein the evaporating circulating pump and the evaporating material passing pump are connected to the bottom of each falling-film evaporator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023344579.3U CN214360287U (en) | 2020-12-31 | 2020-12-31 | Be used for aluminium oxide production to dissolve out evaporation integration process units |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023344579.3U CN214360287U (en) | 2020-12-31 | 2020-12-31 | Be used for aluminium oxide production to dissolve out evaporation integration process units |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214360287U true CN214360287U (en) | 2021-10-08 |
Family
ID=77952353
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202023344579.3U Active CN214360287U (en) | 2020-12-31 | 2020-12-31 | Be used for aluminium oxide production to dissolve out evaporation integration process units |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214360287U (en) |
-
2020
- 2020-12-31 CN CN202023344579.3U patent/CN214360287U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108715456B (en) | Method for recycling electrode foil corrosion waste nitric acid | |
| CN109650413B (en) | Method and system for enriching lithium from sodium aluminate solution in alumina plant | |
| CN110613951A (en) | Evaporation concentration flash evaporation cooling crystallization equipment and process thereof | |
| CN110028087B (en) | Method for reducing carbon-alkali concentration of system in alumina production process | |
| CN115650256A (en) | Industrial potassium chloride purification process and production system | |
| CN214360287U (en) | Be used for aluminium oxide production to dissolve out evaporation integration process units | |
| CN211971803U (en) | Novel materialized wastewater triple-effect evaporation system | |
| CN113307433A (en) | Four-effect cross-flow pharmaceutical wastewater evaporative crystallization system with external heat exchanger | |
| CN112807721A (en) | Process method for extracting concentrated and light brine by adopting five-effect concurrent evaporation process | |
| CN114949893B (en) | Evaporation crystallization process and device for producing lithium chloride from salt lake brine | |
| CN218130003U (en) | Evaporation crystallization device for producing borax from salt lake lithium extraction discharge liquid | |
| CN1915827B (en) | Method and equipment for vaporizing full flash distillation of sodium aluminate liquor in technique for producing alumina | |
| CN215781585U (en) | Multiple-effect evaporation crystallizer suitable for viscose fiber acid bath concentration crystallization | |
| CN211896157U (en) | Nitric acid wastewater treatment system containing aluminum nitrate | |
| CN212954328U (en) | Evaporation and dissolution integrated process equipment | |
| CN209809543U (en) | Seven-effect tube type falling film evaporator set | |
| CN211920887U (en) | Device for dissolving out gibbsite and boehmite mixed bauxite | |
| US6555076B1 (en) | Bauxite ore digestion in the bayer process | |
| CN220989729U (en) | Clear solution crystallization system of sodium chloride | |
| CN111661859A (en) | Evaporation and dissolution integrated process equipment and process flow thereof | |
| CN219823691U (en) | System for solving scab of forced effect heating device | |
| CN215439695U (en) | Concentrated crystallization device for preparing high-purity ammonium sulfate | |
| CN220300448U (en) | Evaporation crystallization system for treating ferric phosphate wastewater | |
| CN219972413U (en) | Movable waste water lithium extraction equipment | |
| CN218058514U (en) | Precursor mother liquor processing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |