CN115253735A - Titanium white waste acid concentration device and concentration process not easy to block - Google Patents
Titanium white waste acid concentration device and concentration process not easy to block Download PDFInfo
- Publication number
- CN115253735A CN115253735A CN202210650002.XA CN202210650002A CN115253735A CN 115253735 A CN115253735 A CN 115253735A CN 202210650002 A CN202210650002 A CN 202210650002A CN 115253735 A CN115253735 A CN 115253735A
- Authority
- CN
- China
- Prior art keywords
- crystallization
- chamber
- heat exchanger
- outlet
- fluidizer
- 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.)
- Pending
Links
- 239000002253 acid Substances 0.000 title claims abstract description 106
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 title claims abstract description 44
- 239000002699 waste material Substances 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims abstract description 35
- 235000010215 titanium dioxide Nutrition 0.000 title claims abstract description 31
- 238000002425 crystallisation Methods 0.000 claims abstract description 69
- 230000008025 crystallization Effects 0.000 claims abstract description 68
- 239000007788 liquid Substances 0.000 claims abstract description 50
- 238000002156 mixing Methods 0.000 claims abstract description 37
- 238000010790 dilution Methods 0.000 claims abstract description 27
- 239000012895 dilution Substances 0.000 claims abstract description 27
- 238000000605 extraction Methods 0.000 claims abstract description 15
- 239000006228 supernatant Substances 0.000 claims description 18
- 238000000926 separation method Methods 0.000 claims description 17
- 239000004408 titanium dioxide Substances 0.000 claims description 12
- 238000001704 evaporation Methods 0.000 claims description 10
- 238000007865 diluting Methods 0.000 claims description 9
- 230000008020 evaporation Effects 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 6
- 239000013589 supplement Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 2
- 125000004122 cyclic group Chemical group 0.000 claims 1
- 239000013078 crystal Substances 0.000 description 24
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 20
- 150000003839 salts Chemical class 0.000 description 9
- 239000012535 impurity Substances 0.000 description 8
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 8
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 8
- 235000003891 ferrous sulphate Nutrition 0.000 description 7
- 239000011790 ferrous sulphate Substances 0.000 description 7
- 229910052749 magnesium Inorganic materials 0.000 description 5
- 239000011777 magnesium Substances 0.000 description 5
- 239000010936 titanium Substances 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 229910052719 titanium Inorganic materials 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229910002804 graphite Inorganic materials 0.000 description 2
- 239000010439 graphite Substances 0.000 description 2
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L magnesium sulphate Substances [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000009991 scouring Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 235000001465 calcium Nutrition 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 230000003116 impacting effect Effects 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 229910000348 titanium sulfate Inorganic materials 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/40—Mixing liquids with liquids; Emulsifying
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/02—Crystallisation from solutions
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G49/00—Compounds of iron
- C01G49/14—Sulfates
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Crystallography & Structural Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a titanium white waste acid concentration device and a concentration process which are not easy to block, and the titanium white waste acid concentration device comprises a heat exchanger, wherein the liquid outlet end of the heat exchanger is connected with a flash chamber through a heat exchanger outlet circulating pipe, the upper side of the flash chamber is provided with an evaporated gas extraction port, the bottom of the flash chamber is connected with an inlet of an axial-flow pump through a central circulating pipe, and the central circulating pipe is provided with a concentrated acid liquid extraction port; the outlet of the axial flow pump is connected with a crystallization fluidizer through an outlet circulating pipe of the pump, the bottom of the crystallization fluidizer is provided with an elutriation leg, the crystallization fluidizer is provided with a liquid outlet and is connected with a dilution mixing chamber through the liquid outlet, the dilution mixing chamber is communicated with the liquid inlet end of the heat exchanger, and the dilution mixing chamber is provided with a dilute acid liquid inlet. The method has the advantages of difficult equipment blockage, simple treatment process, less increased workload, lower treatment cost and high concentration of the produced acid.
Description
Technical Field
The invention relates to a titanium white waste acid concentration device and a concentration process, in particular to a titanium white waste acid concentration device and a concentration process which are not easy to block.
Background
In the production process of titanium dioxide by a sulfuric acid method, when 1 ton of titanium dioxide is produced, about 8 tons of waste sulfuric acid with the mass concentration of about 20 percent is produced as a byproduct; this waste acid is usually concentrated before it can be reused.
The concentration process method generally utilizes the contact of the hot flue gas of a rotary kiln of titanium dioxide with 20 percent of waste sulfuric acid to concentrate the waste sulfuric acid to about 30 percent; then the concentrated sulfuric acid is concentrated to about 70% by a graphite sulfuric acid concentration evaporation heat exchange device and then is treated and utilized.
However, the waste sulfuric acid of titanium white contains FeSO4、Al(SO4)3、MgSO4And inorganic salts such as CaSO4 and TiO2And in the process of concentrating the waste sulfuric acid, soluble titanium, calcium, magnesium and ferrous sulfate crystals are easy to separate out, so that the pipe hole of the graphite heater is scaled and blocked, wherein the scales of the titanium, the calcium and the magnesium are difficult to remove. Therefore, when the concentration device generally operates for about one month, the heater needs to be integrally disassembled, assembled and cleaned, the workload is very large, and the normal operation of the waste acid concentration device is seriously influenced. Although some existing concentration processes reduce the formation of scale by pre-treating to reduce the concentration of soluble salts in the waste acid and then feeding the treated waste acid to a concentration device for concentration, the existing concentration processes increase many additional processes and workloads, and increase the cost. And, if FeSO is earlier stage4After pretreatment and removal, later soluble salts such as titanium, calcium, magnesium and the like can directly scale on the pipe wall of the heat exchanger and are more difficult to clean. Therefore, the problem of scaling of the concentration system is not solved fundamentally all the time, and is one of the bottlenecks restricting the development of the sulfuric acid method titanium dioxide industry.
Disclosure of Invention
The invention aims to provide a titanium white waste acid concentrating device and a titanium white waste acid concentrating process which are not easy to block. The method has the characteristics of difficult equipment blockage, simple treatment process, small increased workload, low treatment cost and high concentration of the produced acid.
The technical scheme of the invention is as follows: a titanium white waste acid concentration device not easy to block comprises a heat exchanger, wherein the liquid outlet end of the heat exchanger passes through the outlet of the heat exchangerThe circulating pipe is connected with a flash chamber, the upper side of the flash chamber is provided with an evaporated gas extraction outlet, the bottom of the flash chamber is connected with an inlet of the axial-flow pump through a central circulating pipe, and the central circulating pipe is provided with a concentrated acid liquid extraction outlet; the outlet of the axial flow pump is connected with a crystallization fluidizer through an outlet circulating pipe of the pump, the bottom of the crystallization fluidizer is provided with an elutriation leg, the crystallization fluidizer is provided with a liquid outlet and is connected with a dilution mixing chamber through the liquid outlet, the dilution mixing chamber is communicated with the liquid inlet end of the heat exchanger, and the dilution mixing chamber is provided with a dilute acid liquid inlet. According to the scheme, the dilute acid liquid inlet is arranged on the dilution mixing chamber above the crystallization fluidizer, and the supersaturated solution separated from the crystallization fluidizer can be diluted by adding the dilute acid, so that the supersaturation degree of the waste acid liquid entering the heat exchanger is reduced to the maximum extent, the waste acid liquid is changed into an unsaturated state, the acid concentration of the waste acid liquid in the heat exchanger is always the lowest concentration value, the crystallization driving force on the pipe wall in the heat exchanger is greatly reduced, the scaling tendency is reduced, and the equipment is not easy to block; meanwhile, through the arrangement of the crystallization fluidizer, the solution containing the crystal substances flowing out of the flash chamber can be promoted to further crystallize and grow, so that the crystal grains are continuously enlarged and then are settled and separated downwards under the action of self weight, the removal of soluble salt is realized, the amount of the soluble salt entering the heat exchanger is greatly reduced, and the blocking speed of the heat exchanger is slowed down; in addition, in the scheme, the crystal is mainly FeSO precipitated when the temperature of waste acid is more than 115 ℃ and the acid concentration is concentrated to 30-34%4The crystal nucleus is formed by adsorbing other precipitated soluble salts, so that the scheme does not need to pretreat soluble salt impurities in the waste acid liquid in advance when the waste acid is concentrated, and the practical effect of the scheme can be reduced if the pretreatment is improper in advance. Therefore, when the scheme is implemented, the blockage can be delayed, the process is simpler, the increased workload is less, and the treatment cost is lower.
In order to enable the crystallization fluidizer to better complete the crystallization separation, the titanium white waste acid concentrating device which is not easy to block comprises a straight cylinder type fluidized bed and a conical crystallization chamber which is arranged outside the straight cylinder type fluidized bed in a jacket mode, wherein the upper end of the conical crystallization chamber is connected with the outer wall of the straight cylinder type fluidized bed, and the lower end of the conical crystallization chamber exceeds the lower end of the straight cylinder type fluidized bed; the dilution and mixing chamber is connected to the top of the straight-tube type fluidized bed, and the elutriation leg is connected to the bottom of the conical crystallization chamber. The crystallization is carried out by the straight-tube fluidized bed and the downward sedimentation of the crystallisate driven by the liquid flow, thereby realizing the good separation of the crystallization.
In order to further promote the crystallization separation effect of the crystallization fluidizer, a supernatant separation chamber is arranged between the crystallization fluidizer and the dilution mixing chamber. The sedimentation of the crystal is further promoted by the arrangement of the supernatant separation chamber, so as to achieve the aim of crystal separation.
In order to further promote the crystallization separation effect of the crystallization fluidizer, the titanium white waste acid concentrating device which is not easy to block is characterized in that the supernatant liquid separating chamber is a chamber with a smaller caliber than those of the crystallization fluidizer and the dilution mixing chamber, and the crystallization fluidizer, the supernatant liquid separating chamber and the dilution mixing chamber form an hourglass-shaped structure. Through the arrangement of the hourglass-shaped structure, the acid liquor naturally collides with the inner wall of the cavity to sink in the upward flowing process, and the purpose of separating crystals is achieved.
In the titanium dioxide waste acid concentrating device not easy to block, the heat exchanger is a tubular heat exchanger.
In order to further reduce the cost and the energy consumption, the titanium white waste acid concentration device which is not easy to block is characterized in that a heat exchange jacket is arranged outside the pipe wall of the heat exchanger, a cold dilute acid supplement inlet and a preheated dilute acid discharge outlet are arranged on the heat exchange jacket, and the preheated dilute acid discharge outlet is communicated with a dilute acid inlet. The dilute acid is preheated by recovering the heat emitted to the air by the heat exchanger, so that the energy conservation and emission reduction are realized, and the cost is reduced.
In order to further avoid the blockage caused by scaling, the outlet circulating pipe of the heat exchanger of the titanium white waste acid concentrating device which is not easy to block is tangentially connected with the inner cavity of the flash evaporation chamber. By forming a circular flow of liquid and scouring the inner walls of the chamber by the tangential connection, the formation of scale is reduced.
In order to further avoid the blockage caused by scaling, the outlet circulating pipe of the pump of the titanium white waste acid concentrating device which is not easy to block is tangentially connected with the inner chamber of the crystallization fluidizer. By forming a circular flow of liquid and scouring the inner walls of the chamber by the tangential connection, the formation of scale is reduced.
A titanium white waste acid concentration process not easy to block is characterized in that dilute waste acid is fed into a dilution mixing chamber from a dilute acid liquid inlet, then flows through a heat exchanger and a flash evaporation chamber in sequence from the dilution mixing chamber to be heated, evaporated and exhausted, concentrated solution after being exhausted is fed into a crystallization fluidizer to be crystallized and separated under the action of an axial flow pump, and supernate is continuously fed into the heat exchanger through the dilution mixing chamber to be circularly concentrated until the supernate is concentrated to the required concentration and then is discharged through a concentrated acid liquid extraction port.
The invention has the advantages of
1. According to the invention, by utilizing the continuous increase of the temperature and the concentration of the acid liquor in the concentration process, when the temperature is higher than 115 ℃ and the concentration is concentrated to 30-34%, a large amount of soluble Fe, ti, ca and Mg impurities are separated out, and the researchers of the invention prove that when ferrous sulfate crystals exist in the system, the soluble Ti, ca and Mg impurities can be preferentially adsorbed on the ferrous sulfate crystals, the ferrous sulfate crystals are relatively easy to remove substances which are difficult to scale from the system, and when the Ti, ca and Mg impurities which are easy to scale are attached on the ferrous sulfate crystals and are discharged out of the system through a crystallization fluidizer, the possibility of scale generation in the system is greatly reduced, and the scale formation is reduced, so that the system is less prone to be blocked, especially for the blockage of a heat exchanger. Therefore, the system realizes effective separation of impurities by utilizing the characteristics of the impurities in the waste acid and the process characteristics of the concentration system under the condition of not pre-treating the impurities in the waste acid in advance, reduces the phenomenon of scaling blockage, and also saves the process and the cost of waste acid pretreatment.
2. The system of the invention adopts a process of continuously extracting ferrous sulfate crystals along with the process of concentration and evaporation, which is different from the traditional process of extracting ferrous sulfate crystals in advance by adopting cooling crystallization at a low-concentration section.
3. The system can realize the balance of the extraction of the crystal and the concentrated acid in the concentration process, and can ensure that the equipment is not easy to block on the premise of not pre-treating soluble salt impurities in the crystal.
4. The concentrated acid liquid extraction port of the device is arranged at the front end where the raw material dilute acid enters and at the rear end where the concentrated acid is evaporated, so that the concentration of the outlet acid is extracted at the highest point of the acid concentration of the system, and the concentration of the extracted acid is about 5% higher than that of the acid extracted at the rear end of the feeding and mixing process in the traditional method.
5. The heat exchanger of the device is externally provided with a heat exchange jacket, dilute acid serving as a raw material passes through the heat exchange jacket and then is injected into the evaporation device, and the heat loss (generally about 15 percent) caused by the high temperature in the heat exchanger directly facing the atmosphere is avoided while the material is preheated; the structure of the device can reduce the heat loss of the system to below 5 percent, save energy, reduce consumption and save cost.
6. The dilute acid liquid inlet is arranged on the diluting and mixing chamber above the crystallization fluidizer, and the supersaturated solution separated from the crystallization fluidizer can be diluted by adding the dilute acid, so that the supersaturation degree of the waste acid liquid entering the heat exchanger is reduced to the maximum extent, the waste acid liquid is changed into an unsaturated state, the acid concentration of the waste acid liquid in the heat exchanger is always the lowest concentration value, the crystallization driving force on the pipe wall in the heat exchanger is greatly reduced, the scaling tendency is reduced, and the equipment is not easy to block.
In conclusion, the invention has the advantages of difficult equipment blockage, simple treatment process, less increased workload, lower treatment cost and high concentration of the produced acid.
Drawings
FIG. 1 is a schematic diagram of the structure of the apparatus of the present invention;
FIG. 2 is a cross-sectional view of a crystallization fluidizer of the present invention;
FIG. 3 isbase:Sub>A view A-A of FIG. 2 shown in the non-cut-away position;
FIG. 4 is a schematic diagram of the supernatant separation chamber of the present invention;
FIG. 5 is a bottom view of the crystallization fluidizer of the present invention;
FIG. 6 is a schematic view of the heat exchanger of the present invention;
FIG. 7 is a view B-B of FIG. 1;
description of reference numerals: 1-heat exchanger, 2-heat exchanger outlet circulating pipe, 3-flash chamber, 4-evaporation gas extraction port, 5-central circulating pipe, 6-concentrated acid liquid extraction port, 7-axial flow pump, 8-pump outlet circulating pipe, 9-crystallization fluidizer, 10-elutriation leg, 11-supernatant separation chamber, 12-dilution mixing chamber, 13-dilute acid liquid inlet, 14-conical crystallization chamber, 15-straight cylinder type fluidized bed, 16-heat exchange jacket, 17-cold dilute acid supplement inlet and 18-preheated dilute acid discharge port.
Detailed Description
The present invention is further illustrated by the following examples, which are not to be construed as limiting the invention.
Examples of the invention
A titanium white waste acid concentration device which is not easy to block is shown in attached figures 1-7 and comprises a heat exchanger 1, wherein the liquid outlet end of the heat exchanger 1 is connected with a flash chamber 3 through a heat exchanger outlet circulating pipe 2, the upper side of the flash chamber 3 is provided with an evaporated gas extraction port 4, the bottom of the flash chamber is connected with the inlet of an axial flow pump 7 through a central circulating pipe 5, and the central circulating pipe 5 is provided with a concentrated acid liquid extraction port 6; the outlet of the axial-flow pump 7 is connected with a crystallization fluidizer 9 through an outlet circulating pipe 8, the bottom of the crystallization fluidizer 9 is provided with an elutriation leg 10, the crystallization fluidizer 9 is provided with a liquid outlet and is connected with a dilution mixing chamber 12 through the liquid outlet, the dilution mixing chamber 12 is communicated with the liquid inlet end of the heat exchanger 1, and the dilution mixing chamber 12 is provided with a dilute acid liquid inlet 13.
The concentration method comprises the following steps: sending dilute waste acid with the concentration of about 20% into a diluting and mixing chamber 12 from a dilute acid liquid inlet 13, then sequentially flowing through a heat exchanger 1 and a flash evaporation chamber 3 from the diluting and mixing chamber 12 for heating evaporation and steam exhaust, sending the concentrated solution after steam exhaust into a crystallization fluidizer 9 for crystallization separation under the action of an axial flow pump 7, continuously sending the supernatant into the heat exchanger 1 through the diluting and mixing chamber 12 for circulating concentration until the supernatant is concentrated to the required concentration, and then discharging the supernatant through a concentrated acid liquid outlet 6; in the concentration process, new dilute waste acid is continuously fed from the dilute acid liquid inlet 13, and continuous slag discharge is carried out through the elutriation leg 10, so that the effects of continuous concentration and extraction are realized. When the concentrated sulfuric acid is concentrated to the required concentration, the concentrated sulfuric acid is extracted from a concentrated sulfuric acid liquid extraction port 6.
In another embodiment, as shown in FIGS. 1 to 7, the crystallization fluidizer 9 comprises a cylindrical fluidized bed 15 and a conical crystallization chamber 14 arranged outside the cylindrical fluidized bed 15 in a jacket manner, wherein the upper end of the conical crystallization chamber 14 is connected with the outer wall of the cylindrical fluidized bed 15, and the lower end of the conical crystallization chamber exceeds the lower end of the cylindrical fluidized bed 15; the dilution and mixing chamber 12 is connected to the top of a straight cylindrical fluidized bed 15 and the elutriation legs 10 are connected to the bottom of a conical crystallization chamber 14. When acid liquor is fed into the crystallization fluidizer 9 from the pump outlet circulating pipe 8, the acid liquor is positioned between the outer wall of the straight-tube-shaped fluidized bed 15 and the inner wall of the conical crystallization chamber 14, then flows downwards firstly and then enters the straight-tube-shaped fluidized bed 15, larger crystals directly settle downwards in the flowing process and enter the bottom of the conical crystallization chamber 14, smaller crystals continue to grow in the straight-tube-shaped fluidized bed 15, and naturally fall after growing to a certain weight, so that the crystallization separation of soluble salt is completed, and after a certain amount of crystals are settled, a switch below the elutriation leg 10 is opened to remove the crystals.
In another embodiment, as shown in FIGS. 1-7, a supernatant separator 11 is provided between the crystallization fluidizer 9 and the dilution mixing chamber 12. The acid liquor with the smaller crystals continues to grow and separate as it flows up into the supernatant separator chamber 11, and the larger crystals settle into the conical crystallization chamber 14.
In another embodiment, as shown in FIGS. 1-7, the supernatant separator 11 is a smaller diameter chamber than the crystallization fluidizer 9 and the diluting and mixing chamber 12, and the crystallization fluidizer 9, the supernatant separator 11 and the diluting and mixing chamber 12 form an hourglass-shaped structure. The hourglass-shaped structure enables the flow channel in the middle to have higher speed, and a circular flow is formed around the flow channel, so that suspended crystal particles quickly sink under the action of the circular flow after impacting the cavity wall at the top, and the separation of crystals can be further promoted.
In another embodiment, as shown in fig. 1-7, the heat exchanger 1 is a tubular heat exchanger.
In another embodiment, as shown in fig. 1-7, a heat exchange jacket 16 is provided outside the tube wall of the heat exchanger 1, a cold dilute acid supply port 17 and a preheated dilute acid discharge port 18 are provided on the heat exchange jacket 16, and the preheated dilute acid discharge port 18 is communicated with the dilute acid inlet 13. The newly supplemented cold dilute acid (about 25 ℃) enters the heat exchange jacket 16 from the cold dilute acid supplement port 17 to absorb the heat emitted by the heat exchanger 1 so as to increase the temperature, and when the cold dilute acid is discharged from the preheated dilute acid discharge port 18, the temperature can be increased to about 70 ℃.
In another embodiment, as shown in FIGS. 1-7, the heat exchanger outlet recycle tube 2 is tangentially connected to the inner portion of the flash chamber 3. The tangential connection is that the outermost side of the flowing direction of the water in the heat exchanger outlet circulating pipe 2 is tangent with the circumferential surface of the inner cavity of the flash chamber 3, so that the liquid can enter tangentially along the inner cavity of the flash chamber 3 to form high-speed circulation in the flash chamber 3, and the inner cavity wall of the flash chamber 3 is flushed.
In another embodiment, as shown in FIGS. 1-7, the pump outlet circulation pipe 8 is connected tangentially to the inner chamber of the crystallization fluidizer 9. The specific structure and principle in this embodiment are the same as above.
Although the invention has been described with reference to specific embodiments, it will be understood by those skilled in the art that various changes in form and details may be made without departing from the spirit and scope of the invention.
Claims (9)
1. The utility model provides a titanium white spent acid enrichment facility that is difficult for blockking up which characterized in that: the device comprises a heat exchanger (1), wherein the liquid outlet end of the heat exchanger (1) is connected with a flash chamber (3) through a heat exchanger outlet circulating pipe (2), the upper side of the flash chamber (3) is provided with an evaporated gas extraction outlet (4), the bottom of the flash chamber is connected with an inlet of an axial flow pump (7) through a central circulating pipe (5), and the central circulating pipe (5) is provided with a concentrated acid liquid extraction outlet (6); the outlet of the axial-flow pump (7) is connected with a crystallization fluidizer (9) through a pump outlet circulating pipe (8), the bottom of the crystallization fluidizer (9) is provided with an elutriation leg (10), a liquid outlet is arranged on the crystallization fluidizer (9) and is connected with a dilution mixing chamber (12) through the liquid outlet, the dilution mixing chamber (12) is communicated with the liquid inlet end of the heat exchanger (1), and a dilute acid liquid inlet (13) is arranged on the dilution mixing chamber (12).
2. The titanium dioxide spent acid concentrating device not prone to blockage according to claim 1, wherein: the crystallization fluidizer (9) consists of a straight cylindrical fluidized bed (15) and a conical crystallization chamber (14) which is arranged outside the straight cylindrical fluidized bed (15) in a jacket mode, wherein the upper end of the conical crystallization chamber (14) is connected with the outer wall of the straight cylindrical fluidized bed (15), and the lower end of the conical crystallization chamber exceeds the lower end of the straight cylindrical fluidized bed (15); the dilution and mixing chamber (12) is connected to the top of a straight cylindrical fluidized bed (15) and the elutriation legs (10) are connected to the bottom of a conical crystallization chamber (14).
3. The titanium dioxide spent acid concentrating apparatus not prone to clogging of claim 1 or 2, wherein: a supernatant separation chamber (11) is arranged between the crystallization fluidizer (9) and the dilution mixing chamber (12).
4. The titanium dioxide spent acid concentrating device not prone to blockage according to claim 3, wherein: the supernatant separation chamber (11) is a chamber with the caliber smaller than the calibers of the crystallization fluidizer (9) and the dilution mixing chamber (12), and the crystallization fluidizer (9), the supernatant separation chamber (11) and the dilution mixing chamber (12) form an hourglass-shaped structure.
5. The titanium dioxide spent acid concentrating device not prone to blockage according to claim 1, wherein: the heat exchanger (1) is a tubular heat exchanger.
6. The titanium dioxide spent acid concentrating device not prone to blockage according to claim 5, wherein: the pipe wall of the heat exchanger (1) is externally provided with a heat exchange jacket (16), the heat exchange jacket (16) is provided with a cold dilute acid supplement inlet (17) and a preheated dilute acid outlet (18), and the preheated dilute acid outlet (18) is communicated with the dilute acid inlet (13).
7. The titanium dioxide spent acid concentrating device which is not easy to block according to claim 1, wherein: the heat exchanger outlet circulating pipe (2) is tangentially connected with the inner cavity of the flash chamber (3).
8. The titanium dioxide spent acid concentrating device not prone to blockage according to claim 1, wherein: the pump outlet circulating pipe (8) is tangentially connected with the inner chamber of the crystallization fluidizer (9).
9. A titanium white waste acid concentration process not easy to block is characterized in that: dilute waste acid is sent into a diluting and mixing chamber (12) from a dilute acid liquid inlet (13), then flows through a heat exchanger (1) and a flash evaporation chamber (3) in sequence from the diluting and mixing chamber (12) for heating evaporation and steam exhaust, concentrated solution after steam exhaust is sent into a crystallization fluidizer (9) for crystallization separation under the action of an axial flow pump (7), and supernatant is continuously sent into the heat exchanger (1) through the diluting and mixing chamber (12) for cyclic concentration until the supernatant is concentrated to the required concentration and then is discharged through a concentrated acid liquid outlet (6).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210650002.XA CN115253735A (en) | 2022-06-10 | 2022-06-10 | Titanium white waste acid concentration device and concentration process not easy to block |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210650002.XA CN115253735A (en) | 2022-06-10 | 2022-06-10 | Titanium white waste acid concentration device and concentration process not easy to block |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN115253735A true CN115253735A (en) | 2022-11-01 |
Family
ID=83760322
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210650002.XA Pending CN115253735A (en) | 2022-06-10 | 2022-06-10 | Titanium white waste acid concentration device and concentration process not easy to block |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115253735A (en) |
Citations (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1590317A (en) * | 2003-09-05 | 2005-03-09 | 哈尔滨工业大学 | Speed changing ascending flow anaerobic treatment method |
| CN101081357A (en) * | 2006-05-31 | 2007-12-05 | 中国石油化工股份有限公司 | Slurry bed circulatory flow reactor and uses thereof |
| CN201154904Y (en) * | 2008-07-11 | 2008-11-26 | 中国轻工业长沙工程有限公司 | External heating type vaporizing saltpeter-separating-out tank |
| CN103432756A (en) * | 2013-08-16 | 2013-12-11 | 江苏嘉泰蒸发结晶设备有限公司 | All-in-one evaporation and crystallization device |
| WO2016001445A1 (en) * | 2014-07-04 | 2016-01-07 | Centre National De La Recherche Scientifique (C.N.R.S) | Method for producing cocrystals by means of flash evaporation |
| CN205145655U (en) * | 2015-10-29 | 2016-04-13 | 中石化南京工程有限公司 | Tower crystallizer |
| CN106185842A (en) * | 2016-07-13 | 2016-12-07 | 钮德明 | A kind of titanium white waste acid enrichment facility |
| CN206518915U (en) * | 2017-01-04 | 2017-09-26 | 吉林维达机械设备有限公司 | Force interior circulation crystallizer |
| CN206980155U (en) * | 2016-11-13 | 2018-02-09 | 兰州交通大学 | Sewerage nitrogen and phosphor reclaims circulating integrated fluid bed |
| CN108079607A (en) * | 2017-12-25 | 2018-05-29 | 合肥恒力装备有限公司 | A kind of evaporative crystallization anti-block apparatus |
| CN108704420A (en) * | 2018-07-03 | 2018-10-26 | 深圳市高德威技术有限公司 | A kind of Venturi tube washer |
| CN108970166A (en) * | 2018-07-09 | 2018-12-11 | 周惠荣 | One kind being used for chemical products crystallization apparatus |
| CN211097622U (en) * | 2019-10-09 | 2020-07-28 | 浙江工业大学 | Circulation continuous crystallizer |
| CN111632409A (en) * | 2020-05-12 | 2020-09-08 | 尚铁军 | Venturi inner member for sedimentation tank |
| CN211798905U (en) * | 2019-12-31 | 2020-10-30 | 河北云瑞化工设备有限公司 | High-efficient evaporation crystallization device of lithium chloride |
| CN212282904U (en) * | 2020-06-02 | 2021-01-05 | 浙江环诺环保科技股份有限公司 | Crystallization evaporator anti-blocking pipe |
| CN113149043A (en) * | 2021-03-23 | 2021-07-23 | 格尔木藏格锂业有限公司 | Crystallization prevention device for salt lake old brine conveying system |
| CN213834613U (en) * | 2020-11-14 | 2021-07-30 | 温州市金榜轻工机械有限公司 | High-efficient environmental protection high salt waste water concentration crystallization equipment |
| CN215327362U (en) * | 2021-04-06 | 2021-12-28 | 山东久泰环保科技有限公司 | Microcrystal softened water treatment equipment |
| CN217828885U (en) * | 2022-06-10 | 2022-11-18 | 贵州兰鑫石墨机电设备制造有限公司 | Titanium white waste acid concentration device not easy to block |
-
2022
- 2022-06-10 CN CN202210650002.XA patent/CN115253735A/en active Pending
Patent Citations (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1590317A (en) * | 2003-09-05 | 2005-03-09 | 哈尔滨工业大学 | Speed changing ascending flow anaerobic treatment method |
| CN101081357A (en) * | 2006-05-31 | 2007-12-05 | 中国石油化工股份有限公司 | Slurry bed circulatory flow reactor and uses thereof |
| CN201154904Y (en) * | 2008-07-11 | 2008-11-26 | 中国轻工业长沙工程有限公司 | External heating type vaporizing saltpeter-separating-out tank |
| CN103432756A (en) * | 2013-08-16 | 2013-12-11 | 江苏嘉泰蒸发结晶设备有限公司 | All-in-one evaporation and crystallization device |
| WO2016001445A1 (en) * | 2014-07-04 | 2016-01-07 | Centre National De La Recherche Scientifique (C.N.R.S) | Method for producing cocrystals by means of flash evaporation |
| CN205145655U (en) * | 2015-10-29 | 2016-04-13 | 中石化南京工程有限公司 | Tower crystallizer |
| CN106185842A (en) * | 2016-07-13 | 2016-12-07 | 钮德明 | A kind of titanium white waste acid enrichment facility |
| CN206980155U (en) * | 2016-11-13 | 2018-02-09 | 兰州交通大学 | Sewerage nitrogen and phosphor reclaims circulating integrated fluid bed |
| CN206518915U (en) * | 2017-01-04 | 2017-09-26 | 吉林维达机械设备有限公司 | Force interior circulation crystallizer |
| CN108079607A (en) * | 2017-12-25 | 2018-05-29 | 合肥恒力装备有限公司 | A kind of evaporative crystallization anti-block apparatus |
| CN108704420A (en) * | 2018-07-03 | 2018-10-26 | 深圳市高德威技术有限公司 | A kind of Venturi tube washer |
| CN108970166A (en) * | 2018-07-09 | 2018-12-11 | 周惠荣 | One kind being used for chemical products crystallization apparatus |
| CN211097622U (en) * | 2019-10-09 | 2020-07-28 | 浙江工业大学 | Circulation continuous crystallizer |
| CN211798905U (en) * | 2019-12-31 | 2020-10-30 | 河北云瑞化工设备有限公司 | High-efficient evaporation crystallization device of lithium chloride |
| CN111632409A (en) * | 2020-05-12 | 2020-09-08 | 尚铁军 | Venturi inner member for sedimentation tank |
| CN212282904U (en) * | 2020-06-02 | 2021-01-05 | 浙江环诺环保科技股份有限公司 | Crystallization evaporator anti-blocking pipe |
| CN213834613U (en) * | 2020-11-14 | 2021-07-30 | 温州市金榜轻工机械有限公司 | High-efficient environmental protection high salt waste water concentration crystallization equipment |
| CN113149043A (en) * | 2021-03-23 | 2021-07-23 | 格尔木藏格锂业有限公司 | Crystallization prevention device for salt lake old brine conveying system |
| CN215327362U (en) * | 2021-04-06 | 2021-12-28 | 山东久泰环保科技有限公司 | Microcrystal softened water treatment equipment |
| CN217828885U (en) * | 2022-06-10 | 2022-11-18 | 贵州兰鑫石墨机电设备制造有限公司 | Titanium white waste acid concentration device not easy to block |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105036222B (en) | A kind of recovery and treatment method of high-salt wastewater | |
| CN106007133B (en) | A kind of desulfurization wastewater concentration and evaporation, crystallization, salt separating technology | |
| CN104973726A (en) | Recovery processing method of high salinity wastewater containing sodium chloride and sodium sulfate | |
| CN107902823A (en) | The recovery and treatment method of the high-salt wastewater of sodium chloride-containing and sodium sulphate | |
| CN110615456B (en) | Device and process for continuously producing aluminum sulfate octadecahydrate | |
| CN102850092A (en) | Technology for producing ammonium sulfate fertilizer through desulfurizing smoke by ammonia process, and apparatus thereof | |
| CN217828885U (en) | Titanium white waste acid concentration device not easy to block | |
| CN111977733A (en) | Complete device and process for recycling salt or nitrate from high-salinity wastewater through fractional crystallization | |
| CN105771304A (en) | Double-effect countercurrent evaporation crystallization system for monosodium glutamate and working process thereof | |
| CN115253735A (en) | Titanium white waste acid concentration device and concentration process not easy to block | |
| CN103043841B (en) | ADCA (Azodicarbonamide) foaming agent liquid waste disposal process | |
| CN103432756A (en) | All-in-one evaporation and crystallization device | |
| CN207845410U (en) | A kind of zinc borate production wastewater treatment equipment | |
| CN216426800U (en) | System for chloride ion content in slurry at bottom of ammonia process desulfurizing tower | |
| CN216513307U (en) | Ferric phosphate effluent disposal system | |
| CN216584204U (en) | System for recycling and preparing electronic-grade sulfuric acid from sulfuric acid waste liquid | |
| CN105152186A (en) | Technique for simple substance salt separation with co-production of sodium sulfide from high-salinity wastewater | |
| CN202263416U (en) | Monosodium glutamate normal-pressure crystallizing equipment | |
| CN210795831U (en) | Double-effect falling film and single-effect forced circulation double-row double-steam-inlet MVR evaporation crystallization system | |
| CN209828630U (en) | Dewatering device for benzoic acid waste gas | |
| CN209778705U (en) | calcium gluconate continuous crystallization system | |
| CN85103681A (en) | The method of prevention evaporimeter heating tube fouling in the alumina producing | |
| CN209809543U (en) | Seven-effect tube type falling film evaporator set | |
| CN210993085U (en) | Sodium sulfate freezing continuous crystallization device | |
| CN104772033B (en) | Flue gas dry wet purification recovery processing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |