CN210874149U - Concentration device for sulfuric acid process titanium white liquor - Google Patents
Concentration device for sulfuric acid process titanium white liquor Download PDFInfo
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- CN210874149U CN210874149U CN201921271292.7U CN201921271292U CN210874149U CN 210874149 U CN210874149 U CN 210874149U CN 201921271292 U CN201921271292 U CN 201921271292U CN 210874149 U CN210874149 U CN 210874149U
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- titanium
- evaporator
- preheater
- distilled water
- tube box
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- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 title claims abstract description 25
- 238000000034 method Methods 0.000 title claims abstract description 24
- 235000010215 titanium dioxide Nutrition 0.000 title claims abstract description 20
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims description 18
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims abstract description 63
- 229910052719 titanium Inorganic materials 0.000 claims abstract description 63
- 239000010936 titanium Substances 0.000 claims abstract description 63
- 239000007788 liquid Substances 0.000 claims abstract description 49
- 238000005406 washing Methods 0.000 claims abstract description 12
- 239000011552 falling film Substances 0.000 claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical group O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 50
- 239000012153 distilled water Substances 0.000 claims description 41
- 238000000926 separation method Methods 0.000 claims description 16
- DCKVFVYPWDKYDN-UHFFFAOYSA-L oxygen(2-);titanium(4+);sulfate Chemical compound [O-2].[Ti+4].[O-]S([O-])(=O)=O DCKVFVYPWDKYDN-UHFFFAOYSA-L 0.000 claims description 3
- 229910000348 titanium sulfate Inorganic materials 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims 1
- 238000001704 evaporation Methods 0.000 abstract description 30
- 230000008020 evaporation Effects 0.000 abstract description 24
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 12
- 229910002804 graphite Inorganic materials 0.000 abstract description 12
- 239000010439 graphite Substances 0.000 abstract description 12
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 33
- 239000000463 material Substances 0.000 description 16
- 238000011084 recovery Methods 0.000 description 6
- 230000006835 compression Effects 0.000 description 5
- 238000007906 compression Methods 0.000 description 5
- 239000004408 titanium dioxide Substances 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 230000007062 hydrolysis Effects 0.000 description 4
- 238000006460 hydrolysis reaction Methods 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000006378 damage Effects 0.000 description 3
- 239000010408 film Substances 0.000 description 3
- 229910000349 titanium oxysulfate Inorganic materials 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 235000003891 ferrous sulphate Nutrition 0.000 description 2
- 239000011790 ferrous sulphate Substances 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 2
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- UBAZGMLMVVQSCD-UHFFFAOYSA-N carbon dioxide;molecular oxygen Chemical compound O=O.O=C=O UBAZGMLMVVQSCD-UHFFFAOYSA-N 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- IUYOGGFTLHZHEG-UHFFFAOYSA-N copper titanium Chemical compound [Ti].[Cu] IUYOGGFTLHZHEG-UHFFFAOYSA-N 0.000 description 1
- 238000012937 correction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- YDZQQRWRVYGNER-UHFFFAOYSA-N iron;titanium;trihydrate Chemical compound O.O.O.[Ti].[Fe] YDZQQRWRVYGNER-UHFFFAOYSA-N 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000001038 titanium pigment Substances 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a concentration device of sulfate process titanium white liquid, which comprises an evaporator, wherein the evaporator is an integrated two-compartment falling film titanium evaporator, the titanium evaporator comprises an upper tube box and a lower tube box, and the upper tube box of the titanium evaporator is connected with a titanium liquid preheating device; the upper tube box and the lower tube box of the titanium evaporator are connected through a circulating pump, and a discharge hole is formed in the lower tube box of the titanium evaporator; the titanium evaporator is provided with a secondary steam outlet, the secondary steam outlet is connected with an inlet of the gas washing tower through the separator, an outlet of the gas washing tower is connected with an inlet of the compressor, and an outlet of the compressor is communicated with a shell layer of the titanium evaporator to exchange heat. The utility model can recover the heat of the system to the maximum extent, and greatly saves the steam consumption compared with the traditional titanium liquid evaporation; meanwhile, the problems of high failure rate, short service life of equipment and the like in graphite evaporation are avoided, and the device is simple in structure and stable in operation.
Description
Technical Field
The utility model relates to a enrichment facility of titanium white liquid especially relates to a enrichment facility of sulfuric acid process titanium white liquid.
Background
In the production process of titanium dioxide by a sulfuric acid method, ilmenite reacts with sulfuric acid, water is used for dissolving and settling, ferrous sulfate is separated, and then filtration is carried out to obtain a clear titanium liquid. The dilute titanium solution can enter the next hydrolysis process after being concentrated to reach a certain concentration so as to ensure the pigment index.
The dilute titanium solution mainly contains solutes such as titanyl sulfate, titanium sulfate, ferrous sulfate and the like, but the titanyl sulfate and the titanium sulfate belong to heat-sensitive substances and can be hydrolyzed when the temperature is higher than 75 ℃; if the titanium pigment is directly heated and evaporated under the normal pressure state, the titanium liquid is subjected to uncontrollable hydrolysis to generate irregular hydrated titanium dioxide particles when the boiling point (104-114 ℃) is not reached, and finally the pigment-grade titanium dioxide cannot be obtained. To avoid premature hydrolysis, the titanium solution must be cryoconcentrated under vacuum.
At present, the traditional single-effect film evaporation concentration titanium liquid is adopted in the titanium white industry in China. The evaporator is generally made of a titanium tube heat exchanger or a copper-titanium heat exchanger. On average, 1.2-2.0 tons of fresh steam are consumed for producing one ton of titanium dioxide. Another evaporation method is an evaporator made of graphite and adopts a mechanical vapor compressor for evaporation, and the graphite evaporator has the defects of influence of graphite properties, high failure rate, low heat exchange efficiency, large occupied area and no contribution to stable operation of a system; and in severe cases even damage to the compressor wheel operating at high speed.
The existing titanium liquid concentration process technology has the following defects:
1. the steam consumption is large, and if single-effect or multi-effect evaporation is adopted, 0.8-1.5 tons of steam is consumed for evaporating one ton of water.
2. Due to the fact that fresh steam with the temperature of more than 120 ℃ needs to be adopted in the evaporation process, the phenomenon of local overheating can be generated during evaporation, firstly, the property of the concentrated titanium liquid is unstable, and the quality of the product is influenced finally; secondly, the tube is blocked due to hydrolysis and scaling of titanyl sulfate, so that the heat exchange efficiency is reduced, and the steam consumption is increased; thirdly, the heat exchange tube after scaling can only depend on mechanical cleaning, and the damage to equipment is large.
3. The graphite evaporator has high failure rate, and frequent failures can influence the productivity and even lead the operation stability of the compressor.
4. The heat exchange coefficient of the graphite evaporator heat exchanger is low, and the heat exchange volume of the graphite evaporator heat exchanger with the same evaporation area is 1-2 times larger than that of the titanium material; is not beneficial to the large-scale production requirement of the titanium dioxide device.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem that a enrichment facility of sulfuric acid process titanium white liquid is provided, can the concentrated energy consumption of greatly reduced titanium liquid, steady operation.
The utility model provides a technical scheme for solving the technical problems and providing a titanium white liquor concentration device by sulfuric acid process, which comprises an evaporator, wherein the evaporator is an integrated two-compartment falling film titanium evaporator, the titanium evaporator comprises an upper tube box and a lower tube box, and the upper tube box of the titanium evaporator is connected with a titanium liquor preheating device; the upper tube box and the lower tube box of the titanium evaporator are connected through a circulating pump, and a discharge hole is formed in the lower tube box of the titanium evaporator; the titanium evaporator is provided with a secondary steam outlet, the secondary steam outlet is connected with an inlet of the gas washing tower through the separator, an outlet of the gas washing tower is connected with an inlet of the compressor, and an outlet of the compressor is communicated with a shell layer of the titanium evaporator to exchange heat.
Furthermore, the titanium liquid preheating device comprises a primary non-condensable gas preheater, a secondary distilled water preheater and a tertiary steam generation preheater which are sequentially connected, one path of input of the primary non-condensable gas preheater is connected with the titanium liquid, the other path of input of the primary non-condensable gas preheater is connected with the non-condensable gas, one path of output of the primary non-condensable gas preheater is connected with the secondary distilled water preheater, and the other path of output of the primary non-condensable gas preheater is connected with the gas-liquid separation device; the other input of the secondary distilled water preheater is connected with a distilled water tank through a distilled water pump, and the output of the primary distilled water preheater is connected with a secondary raw steam preheater; and the other path of input of the three-level raw steam preheater is connected with primary steam, one path of output of the three-level raw steam preheater is connected with an upper pipe box of the titanium evaporator, and the other path of output of the three-level raw steam preheater is connected with a distilled water tank.
Further, the gas-liquid separation device is connected with the distilled water tank through a U-shaped pipeline, and the primary non-condensable gas preheater is arranged 4-9 m above the distilled water tank.
Furthermore, the upper end and the lower end of the shell layer of the evaporator are respectively provided with a vacuumizing port connected with a vacuum pump.
Further, a hollow ball filler is arranged at the outlet of the gas washing tower
The utility model discloses contrast prior art has following beneficial effect: the utility model provides a sulfate process titanium white liquor concentration device, which can recover the heat of the system to the maximum extent and greatly save the steam consumption compared with the traditional titanium liquor evaporation; meanwhile, the problems of high failure rate, short service life of equipment and the like in graphite evaporation are avoided, and the device is simple in structure and stable in operation.
Drawings
FIG. 1 is a schematic structural view of a titanium liquid preheating device in a concentration device of the present invention;
fig. 2 is a schematic structural diagram of an evaporation device in the concentration device of the present invention.
In the figure:
1 first-stage noncondensable gas preheater, 2 second-stage distilled water preheater and 3 third-stage raw steam preheater
4 gas-liquid separation device, 5 vacuum pump and 6U-shaped pipeline
7 compressor 8 scrubber 9 separator
10 evaporator 11 discharge pump 12 circulating pump
13 distilled water tank 14 distilled water pump 15 washing pump
16 heat recovery line 17 non-condensable gas line
Detailed Description
The invention is further described with reference to the following figures and examples.
FIG. 1 is a schematic structural view of a titanium liquid preheating device in a concentration device of the present invention; fig. 2 is a schematic structural diagram of an evaporation device in the concentration device of the present invention.
Please refer to fig. 1 and fig. 2, the utility model provides a enrichment facility of sulfate process titanium white liquid, including titanium liquid preheating device and evaporimeter 10, the titanium material evaporimeter of evaporimeter 10 railway carriage or compartment as an organic whole, titanium liquid preheating device includes one-level noncondensable gas preheater 1, second grade distilled water preheater 2 and tertiary steam pre-heater 3, the upper hose box distributor of titanium material evaporimeter is directly got into to the titanium liquid after preheating, get into the lower hose box after primary concentration, return the last hose box that gets into the evaporimeter through circulating pump 12, it is connected to the pipeline that the lower hose box sent to next process through discharge pump 11 once more to concentrate.
The utility model discloses the secondary steam that the evaporator 10 lower tube box produced gets into separator 9, gets into scrubbing tower 8 after carrying out the preliminary separation, through the liquid caustic soda circulation washing in washing pump 15, and the secondary steam after the washing gets into compressor 7 and carries out mechanical type compression and intensifies, and the secondary steam after the intensification gets into the shell heat transfer of evaporator 10.
The utility model discloses the comdenstion water that the secondary steam produced in evaporimeter 10 gets into distilled water jar 13, and distilled water of distilled water jar 13 gets into second grade distilled water pre-heater 2 through distilled water pump 14, and the distilled water after the heat recovery carries out the retrieval and utilization through heat recovery pipeline 16.
The utility model discloses the residual noncondensable gas of secondary steam at 10 condensations of evaporimeter gets into one-level noncondensable gas pre-heater 1 through noncondensable gas pipeline 17, and the gas-water mixture after the condensation carries out gas-liquid separation through gas-liquid separation device 4, and the liquid phase of separation gets into distilled water tank 13 retrieval and utilization through U type pipeline 6, and the gaseous phase after the separation gets into 5 suction atmospheres of vacuum pump.
The utility model also provides a sulfuric acid process titanium white liquor's concentration method, wherein: and (3) boosting and heating secondary steam generated in the evaporation and concentration process of the clear titanium liquid by using a mechanical steam compressor, and returning the secondary steam to the evaporation and concentration system, wherein the evaporation system is kept to operate under-0.08 MPa.
The clear titanium liquid is preheated to 68 ℃ by a pump through a first-stage non-condensable gas preheater 1, a second-stage distilled water preheater 2 and a third-stage raw steam preheater 3 in sequence, and directly enters a falling-film titanium evaporator for evaporation primary concentration, enters another titanium box through a circulating pump 12, is subjected to falling-film concentration again, and the concentrated liquid enters the next procedure. The generated secondary steam is subjected to mist and foam separation, enters an alkaline washing tower and then enters a steam compressor, the temperature and the pressure are increased by the compressor and then are used as heat sources to return to the system, the heat sources are only sent to the falling film evaporator, and condensed water generated by a heating chamber of the evaporator is used for secondary preheating of the dilute titanium liquid and then is recycled. The initial temperature of the secondary steam is 60 ℃ and the initial pressure is 20 KPa; after compression by the compressor 7, the temperature was 78 ℃, the pressure was 43.7KPa, and the compression ratio was 2.
The utility model discloses a enrichment facility, the titanium liquid material that gets into the system at first preheats with noncondensable gas foreheat. The evaporation system can ensure the stable property of the titanium liquid under-0.08 MPa, and the preferred property is-0.08 MPa to 0.093 MPa. Because the material contains non-condensable gas and the gas tightness of the system in the actual production process cannot reach 100 percent. Therefore, the utility model discloses a enrichment facility adopts vacuum pump 5 to continuously take out the negative pressure to the system, and the negative pressure air extraction volume is about 5% of evaporation capacity, and this wherein inevitable contains about 80% flash steam, directly gets into vacuum pump system and can cause the heat loss of vacuum pump 5 operation burden and this part like crossing flash steam, so the utility model discloses a titanium liquid heat transfer about one-level noncondensable gas preheater 1 and the about 20 ℃ of entering system has both alleviateed the heat burden of vacuum pump 5 operation in-process, has retrieved the heat simultaneously again.
In the noncondensable gas heat recovery, the first-stage noncondensable gas preheater 1 is preferably arranged at a position of 4-9 m above the distilled water tank 13, and a gas-liquid separation device 4 is adopted after condensation, so that the separation of condensed water and the noncondensable gas is fully ensured. The fully separated condensed water adopts a U-shaped pipeline 6 falling water design, so that the condensed water can smoothly enter the distilled water tank 13, and meanwhile, the formed liquid seal can prevent heat in the distilled water from entering a vacuum pump system.
The utility model discloses a heat of heat transfer, further among the recovery system is carried out with second grade distilled water pre-heater 2 to enrichment facility behind the 1 heat transfer of one-level noncondensable gas pre-heater. And then enters a three-stage raw steam preheater 3, the temperature of the material is preferably controlled by a steam regulating valve to be about 68 ℃, and the temperature is the titanium liquid bubble point temperature under the pressure after the data of the measured amount experiment and the correction of the engineering case and is the optimal feeding temperature. The three-stage raw steam preheater 3 adopts raw steam for preheating (the temperature of the raw steam is 120 ℃), and the reasons why secondary steam cannot be adopted for preheating are as follows: the quality of the secondary steam is equal to the quality of the evaporation in the evaporator, the temperature of the secondary steam is improved after mechanical compression, if a part of the secondary steam is used for preheating cold materials to the temperature of a bubble point, the secondary steam used for evaporating the materials is inevitably reduced, the evaporation amount is further reduced, the secondary steam used for compressing is reduced, and the circulating system cannot operate.
The material that preheats to the bubble point through tertiary live steam gets into the falling film separator that titanium material is given first place, the utility model discloses a falling film evaporator structure that the enrichment facility adopted is the falling film evaporator of two-effect as an organic whole formula, and the material is at first through the double-deck cloth liquid dish of an effect, forms even film on falling film pipe, because the effect of gravity flow to one-effect evaporating chamber, carries out the heat transfer once with the secondary steam of shell at this in-process, carries out the preliminary evaporation, and this in-process material boiling point risees lower. The material after the first evaporation enters the evaporation chamber, enters the double-layer liquid distribution disc with the second effect through the circulating pump, continues to exchange heat with secondary steam after forming a uniform film, and enters the next procedure through the discharge pump after reaching the preset concentration. The titanium material integrated two-effect type is characterized in that: good heat exchange effect, stable performance, long service life, lower evaporation temperature, convenient processing and maintenance and the like. The graphite evaporator is generally adopted in the prior art, but the graphite evaporator cannot achieve 'integrative two-effect' due to structural limitation, and then the failure rate is higher, and the influence on the compressor running at high speed due to the failure of the graphite evaporator is not paid, so the utility model discloses a titanium evaporator, but not the graphite evaporator.
The secondary steam that the material evaporating chamber produced smugglies a small amount of liquid drops secretly, and the pH value is lower, if directly get into the compressor, can cause unrepairable harm to the compressor impeller, the utility model discloses a enrichment facility adopts the secondary treatment to secondary steam, fully guarantees the steady operation of compressor. The utility model discloses a secondary steam that enrichment facility produced at first gets into gas-liquid separation device 4, and gas-liquid separation device 4's principle utilizes the increase gas flow way, reduces the gas flow rate, and the liquid drop that gravity is greater than gaseous lift can enrich in vapour and liquid separator's bottom, returns the evaporating chamber through the bottom collecting pipe. The gas can pass through the two baffle plates in the rising process, the gas flow rate is slower, and the gas-liquid separation is more sufficient.
The secondary steam primarily separated by the gas-liquid separation device 4 enters the scrubber 8 to fully contact with liquid alkali from top to bottom, acid mist in the secondary steam is fully eliminated, the secondary steam enters the compressor 7 after fog drops are eliminated by hollow ball fillers, the temperature is raised by mechanical compression, and the secondary steam after temperature rise enters the shell layer of the titanium material integrated dual-effect evaporator.
Distilled water produced after the condensation of the secondary steam enters the distilled water tank 13. And the distilled water is recycled after exchanging heat with the materials through the distilled water pump 14 and the secondary distilled water preheater 2.
The secondary steam contains non-condensable gases such as oxygen, carbon dioxide and nitrogen, and the existence of the gases can affect the vacuum degree of the system and the heat exchange efficiency of the evaporator, so that the system needs to be continuously vacuumized by a vacuum pump. The utility model discloses a vacuum pumping position for being located each department in both ends about the evaporimeter shell layer, can guarantee the vacuum of system, can take out the noncondensable gas in the evaporimeter shell layer as far as again, does not influence the heat exchange efficiency of evaporimeter. If the position of adopting the evacuation is located the distilled water jar, this is unfavorable for the extraction of evaporimeter middle part condensable gas, and secondly preheating in the distilled water jar can be taken out to the vacuum system, is unfavorable for the recovery of preheating and increases vacuum system's heat burden.
Although the present invention has been described with reference to the preferred embodiments, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (5)
1. The concentration device of the sulfuric acid process titanium white liquid comprises an evaporator (10), and is characterized in that the evaporator (10) is an integrated two-compartment falling film titanium evaporator, the titanium evaporator comprises an upper tube box and a lower tube box, and the upper tube box of the titanium evaporator is connected with a titanium liquid preheating device;
the upper tube box and the lower tube box of the titanium evaporator are connected through a circulating pump (12), and a discharge hole is formed in the lower tube box of the titanium evaporator;
the titanium evaporator is provided with a secondary steam outlet, the secondary steam outlet is connected with an inlet of the gas washing tower (8) through a separator (9), an outlet of the gas washing tower (8) is connected with an inlet of the compressor (7), and an outlet of the compressor (7) is communicated with a shell layer of the titanium evaporator to exchange heat.
2. The titanium white liquor concentration device according to claim 1, wherein the titanium liquor preheating device comprises a primary noncondensable gas preheater (1), a secondary distilled water preheater (2) and a tertiary steam generation preheater (3) which are connected in sequence, one input of the primary noncondensable gas preheater (1) is connected with the titanium liquor, the other input of the primary noncondensable gas preheater (1) is connected with the noncondensable gas, one output of the primary noncondensable gas preheater (1) is connected with the secondary distilled water preheater (2), and the other output of the primary noncondensable gas preheater (1) is connected with the gas-liquid separation device (4); the other path of input of the secondary distilled water preheater (2) is connected with a distilled water tank (13) through a distilled water pump (14), and one path of output of the secondary distilled water preheater (2) is connected with a third-level raw steam preheater (3); the device is characterized in that the other path of the three-level raw steam preheater (3) is connected with primary steam in an input mode, one path of output of the three-level raw steam preheater (3) is connected with an upper pipe box of the titanium evaporator, and the other path of output of the three-level raw steam preheater is connected with a distilled water tank (13).
3. A titanium white liquor concentrating apparatus according to claim 2, wherein said gas-liquid separating means (4) is connected to a distilled water tank (13) through a U-shaped pipe (6), and said primary noncondensable gas preheater is placed 4-9 m above the distilled water tank (13).
4. The apparatus for concentrating titanium white liquor according to claim 1, wherein the evaporator has vacuum ports connected to vacuum pumps (5) at the upper and lower ends of the shell.
5. A device for concentrating white titanium sulfate process according to claim 1, wherein a hollow ball packing is provided at the outlet of the scrubber (8).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921271292.7U CN210874149U (en) | 2019-08-07 | 2019-08-07 | Concentration device for sulfuric acid process titanium white liquor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921271292.7U CN210874149U (en) | 2019-08-07 | 2019-08-07 | Concentration device for sulfuric acid process titanium white liquor |
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| CN210874149U true CN210874149U (en) | 2020-06-30 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110465107A (en) * | 2019-08-07 | 2019-11-19 | 浙江宣达环境科技股份有限公司 | A kind of enrichment facility and method of sulfate process titanium dioxide liquid |
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2019
- 2019-08-07 CN CN201921271292.7U patent/CN210874149U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110465107A (en) * | 2019-08-07 | 2019-11-19 | 浙江宣达环境科技股份有限公司 | A kind of enrichment facility and method of sulfate process titanium dioxide liquid |
| CN110465107B (en) * | 2019-08-07 | 2023-12-22 | 浙江宣达环境科技股份有限公司 | Concentrating device and method for sulfuric acid process titanium white liquid |
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