CN218359281U - Reaction device for oxidation process in iron phosphate preparation process - Google Patents
Reaction device for oxidation process in iron phosphate preparation process Download PDFInfo
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- CN218359281U CN218359281U CN202222898603.0U CN202222898603U CN218359281U CN 218359281 U CN218359281 U CN 218359281U CN 202222898603 U CN202222898603 U CN 202222898603U CN 218359281 U CN218359281 U CN 218359281U
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Abstract
The utility model relates to a reaction unit for iron phosphate preparation in-process oxidation process belongs to agitated vessel technical field, its characterized in that: the bottom at the retort is provided with the ejector, and the feed liquor pipe of ejector passes through the pipeline and is connected with heat exchanger, and the liquid outlet and the retort intercommunication of ejector still are equipped with the intake pipe on the ejector, and the intake pipe passes through pipeline and valve and the outside atmosphere intercommunication of retort. The ejector is composed of a liquid inlet pipe, an air inlet pipe, a nozzle, a throat pipe and a diffusion pipe, wherein the liquid inlet pipe is communicated with the nozzle in the ejector, the nozzle faces the inlet of the throat pipe, the outlet of the throat pipe is communicated with the diffusion pipe, and the diffusion pipe is used as a liquid outlet of the ejector and is communicated with the bottom of the reaction tank; the side wall of the ejector is provided with an air inlet pipe which is arranged beside the nozzle in the ejector. The bubble breaking device aims to effectively break bubbles, further effectively increase the contact area between gas-liquid two-phase flow, improve the mass transfer efficiency and reduce the reaction time.
Description
Technical Field
The utility model belongs to the technical field of agitated vessel, concretely relates to a reaction unit that is used for ferric phosphate preparation in-process oxidation process.
Background
A large amount of by-product ferrous sulfate is generated in the process of producing titanium dioxide every year in China, and the ferrous sulfate can be used as a raw material for producing iron phosphate in order to avoid resource waste. The specific production process of the iron phosphate comprises the following steps: firstly, removing impurities from a byproduct ferrous sulfate from a titanium dioxide manufacturer, oxidizing the ferrous sulfate into ferric sulfate by using an oxidant, adding phosphoric acid and ammonia water to generate iron phosphate precipitate, and finally filtering and drying to obtain an iron phosphate product. In order to obtain an iron phosphate product with excellent quality, excessive oxidant needs to be added in the iron phosphate oxidation process, hydrogen peroxide is expensive, and air or oxygen can be used for replacing hydrogen peroxide to oxidize ferrous sulfate so as to reduce the production cost.
The mixed reaction between gas-liquid two-phase flow is involved when air or oxygen is adopted to oxidize ferrous sulfate in the ferric phosphate oxidation procedure, the gas-liquid two-phase flow mixed reaction equipment commonly used in the market is a bubble column reactor, the gas is blown into the bottom of the reactor by adopting a blower or a compressor as a power source, the gas gradually rises from the bottom of the reactor and is mixed with liquid for mass transfer, but the bubble obtained by using the bubble column reactor has large particle size, low mass transfer efficiency and long reaction time. In order to enhance the mass transfer efficiency and improve the product quality, an efficient oxidation reaction device needs to be developed for the production of the iron phosphate.
Disclosure of Invention
To the problem that exists in the above-mentioned ferric phosphate production process, the utility model provides a reaction unit for ferric phosphate preparation in-process oxidation process, its aim at is with the effective breakage of bubble, and then effectively increases the area of contact between the gas-liquid two-phase flow, improves mass transfer efficiency, reduces reaction time.
In order to realize the purpose, the utility model adopts the technical scheme as follows:
the utility model provides a reaction unit for iron phosphate preparation in-process oxidation process, reaction unit includes the retort, outside the retort, has gas-liquid multiphase pump and heat exchanger through valve and pipe connection, is provided with draft tube, its characterized in that inside the retort: the bottom at the retort is provided with the ejector, and the feed liquor pipe of ejector passes through the pipeline and is connected with heat exchanger, and the liquid outlet and the retort intercommunication of ejector still are equipped with the intake pipe on the ejector, and the intake pipe passes through pipeline and valve and the outside atmosphere intercommunication of retort.
Preferably, the ejector consists of a liquid inlet pipe, an air inlet pipe, a nozzle, a throat pipe and a diffusion pipe, wherein the liquid inlet pipe is communicated with the nozzle in the ejector, the nozzle faces the inlet of the throat pipe, the outlet of the throat pipe is communicated with the diffusion pipe, and the diffusion pipe is used as a liquid outlet of the ejector and is communicated with the bottom of the reaction tank; the side wall of the ejector is provided with an air inlet pipe which is arranged beside the nozzle in the ejector.
Preferably, the inclination angle alpha of the air inlet pipes of the ejector and the horizontal direction is 30-90 degrees, the number of the air inlet pipes is 1~4, and the air inlet pipes are arranged at equal intervals along the direction of the central axis.
Preferably, a 1~4 stage guide shell is arranged in the reaction tank.
Preferably, a temperature sensor and a pressure sensor are arranged inside the reaction tank.
The utility model has the advantages as follows:
(1) The jet device is adopted to crush the gas into micron-sized small bubbles, so that the contact area during the mixing reaction of the gas-liquid two-phase flow is increased, the reaction efficiency is improved, and the problems of large bubble particle size and long reaction time of the traditional bubble column reactor are solved.
(2) By changing the number of the air inlet pipes of the jet device and the inclination angle between the air inlet pipes and the horizontal direction, the uniformity of the air content at the outlet of the throat pipe is effectively improved, and the quality of products is improved.
(3) The multistage guide shell is arranged in the reaction tank, so that the retention time of gas in the reaction tank is prolonged, the circulating liquid velocity and the gas content outside the guide shell are improved, and the mixing effect of gas-liquid two-phase flow inside the reaction tank is improved.
(4) The gas which is not completely reacted in the reaction tank can enter the ejector through a pipeline to participate in the reaction again, so that the influence of the gas discharge on the environment is avoided.
Description of the drawings:
FIG. 1 is a schematic structural view of a reaction apparatus for an oxidation process in an iron phosphate preparation process of the present invention:
fig. 2 is the structure schematic diagram of the ejector of the utility model:
fig. 3 is the utility model discloses the ejector structure sketch map of different intake pipe quantity:
in the figure: 1-reaction tank, 2-first pipeline, 3-gas-liquid mixed transportation pump, 4-second pipeline, 5-heat exchanger, 6-third pipeline, 7-ejector, 8-fourth pipeline, 9-gas flow control valve, 10-fifth pipeline, 11-discharge valve, 12-guide cylinder, 13-temperature sensor, 14-pressure sensor, 15-retaining wall, 16-liquid inlet, 17-gas outlet, 18-sixth pipeline, 21-liquid inlet, 22-gas inlet pipe, 23-nozzle, 24-throat, 25-diffusion pipe and alpha-inclination angle.
The specific implementation mode is as follows:
the present invention will be described in further detail with reference to the accompanying drawings.
Example 1
A reaction device for an oxidation process in the preparation process of iron phosphate is shown in a schematic structural diagram in figure 1, and comprises a reaction tank 1, a gas-liquid mixed transportation pump 3, a heat exchanger 5, an ejector 7, a guide shell 12, a pipeline, a valve and a sensor; the gas-liquid mixed transportation pump 3, the heat exchanger 5 and the ejector 7 are arranged outside the reaction tank, and the guide cylinder 12 is arranged inside the reaction tank.
The inlet of the gas-liquid mixed transmission pump 3 is communicated with the reaction tank 1 through a first pipeline 2, and the outlet of the gas-liquid mixed transmission pump is communicated with a heat exchanger 5 through a second pipeline 4. The ejector 7 is composed of a liquid inlet pipe 21, an air inlet pipe 22, a nozzle 23, a throat pipe 24 and a diffusion pipe 25. The ejector 7 is arranged at the bottom of the reaction tank 1, and the liquid inlet 21 is communicated with the heat exchanger 5 through a third pipeline 6. The inclination angle of the air inlet pipes 22 of the jet device 7 to the horizontal direction is 30-90 degrees, the number of the air inlet pipes 22 is 1~4, the air inlet pipes are arranged at equal intervals along the central axis direction, the inclination angle is 30-90 degrees, the number of the air inlet pipes 22 is limited, and the air bubbles in the jet device 7 can be well crushed along the central axis direction.
One end of a sixth pipeline 18 is communicated with the air outlet 17 of the reaction tank 1, and the other end is communicated with the fourth pipeline 8. The guide shell 12 is disposed inside the reaction tank 1 and divided into 2 stages. The reaction tank 1 is a pressure vessel, and the pressure is 0.4MPa to 0.5MPa. A temperature sensor 13 and a pressure sensor 14 are provided inside the reaction tank 1. A gas flow control valve 9 is provided on the fourth line 8 to regulate the flow of intake gas by a PID controller based on signal feedback from a temperature sensor 13 and a pressure sensor 14. The temperature in the reaction tank 1 is regulated by a PID controller to be stabilized at 80-90 ℃. A discharge valve 11 is arranged on the fifth line 10. The reaction tank 1, the ejector 7, the guide shell 12 and the pipeline in the reaction device are all made of 316L materials.
The working principle of the embodiment 1 is as follows:
firstly, a proper amount of mixed solution of ferrous sulfate and sulfuric acid is added through a liquid inlet 16 at the top of a reaction tank 1, then the mixed solution is conveyed to a gas-liquid mixed conveying pump 3 through a first pipeline 2, the mixed solution discharged from the gas-liquid mixed conveying pump 3 enters a heat exchanger 5 through a second pipeline 4 to be heated, and the heated mixed solution is conveyed to a liquid inlet pipe 21 of an ejector 7 through a third pipeline 6.
The gas flow control valve 9 is opened and oxygen enters the inlet pipe 22 of the ejector 7 through the fourth line 8. At the moment, the mixed solution and the oxygen are mixed in the ejector 7, because the diameter of the nozzle 23 of the ejector 7 is smaller than that of the liquid inlet pipe 21, the speed of the mixed solution is increased, the turbulence intensity is increased, the mixed solution and the oxygen violently collide at the throat pipe 24, the oxygen is crushed into micron-sized small bubbles, the contact area of the mixed solution and the oxygen is increased, the mass transfer efficiency is improved, and then the completely mixed gas-liquid two-phase flow enters the reaction tank 1 through the diffusion pipe 25.
The mixed solution and oxygen enter the reaction tank 1 and then move upwards from the bottom of the reaction tank 1 along the inside of the guide shell 12, and when the mixed solution and the oxygen reach the middle gap and the top of the guide shell 12, the mixed solution and the oxygen can move downwards to the bottom of the reaction tank 1 along the outside of the guide shell 12 to form circulation, and the flow circulation formed inside the reaction tank 1 can improve the oxygen content outside the guide shell 12 and prolong the retention time of the oxygen.
The temperature and pressure change conditions are monitored in real time through a temperature sensor 13 and a pressure sensor 14 in the reaction tank 1, the pressure is kept between 0.4MPa and 0.5MPa through a PID controller, and the temperature is kept between 80 ℃ and 90 ℃.
Unreacted oxygen in the reaction tank 1 is gathered at the top of the reaction tank 1 under the action of buoyancy, and the oxygen participates in the reaction again through a sixth pipeline 18 from an air outlet 17.
And opening a discharge valve 11, and discharging a product obtained through full oxidation reaction in the reaction tank 1 from a fifth pipeline 10.
Example 2
As shown in fig. 3, the structural schematic diagram of the present embodiment 2 is similar to that of fig. 2, except that the number of the air inlet pipes 22 of the ejector 7 and the inclination angle of the air inlet pipes 22 with respect to the horizontal direction are different, in the present embodiment 2, four air inlet pipes 22 are adopted, and the inclination angle of the air inlet pipes 22 with respect to the horizontal direction is 70 ° and the air inlet pipes are arranged at equal intervals along the central axis.
The above, only be the more typical embodiment in the utility model, it is not right the utility model discloses a design and protection scope are injectd, do not deviate from the utility model discloses a design under the prerequisite of design, according to the utility model discloses various deformation and improvement that technical scheme made all should be covered within the protection scope of the utility model, the specific protection scope of the utility model uses the claim as the standard.
Claims (5)
1. The utility model provides a reaction unit for iron phosphate preparation in-process oxidation process, reaction unit includes retort (1), outside retort (1), has gas-liquid multiphase pump (3) and heat exchanger (5) through valve and pipe connection, is provided with draft tube (12), its characterized in that inside retort (1): the bottom of the reaction tank (1) is provided with an ejector (7), a liquid inlet pipe (21) of the ejector (7) is connected with the heat exchanger (5) through a pipeline, a liquid outlet of the ejector (7) is communicated with the reaction tank (1), the ejector (7) is further provided with an air inlet pipe (22), and the air inlet pipe (22) is communicated with the atmosphere outside the reaction tank (1) through a pipeline and a valve.
2. The reaction device for the oxidation process in the preparation process of iron phosphate according to claim 1, wherein: the ejector (7) is composed of a liquid inlet pipe (21), an air inlet pipe (22), a nozzle (23), a throat pipe (24) and a diffusion pipe (25), the liquid inlet pipe (21) is communicated with the nozzle (23) in the ejector (7), the nozzle (23) is right opposite to the inlet of the throat pipe (24), the outlet of the throat pipe (24) is communicated with the diffusion pipe (25), and the diffusion pipe (25) is used as a liquid outlet of the ejector (7) and is communicated with the bottom of the reaction tank (1); an air inlet pipe (22) is arranged on the side wall of the ejector (7) and is arranged beside a nozzle (23) in the ejector (7).
3. The reaction device for the oxidation process in the preparation process of iron phosphate according to claim 2, wherein: the inclination angle alpha of the air inlet pipes (22) of the ejector (7) to the horizontal direction is 30-90 degrees, the number of the air inlet pipes (22) is 1~4, and the air inlet pipes are arranged at equal intervals along the direction of the central axis.
4. The reaction device for the oxidation process in the preparation process of iron phosphate according to claim 1, wherein: the reaction tank (1) is internally provided with a 1~4 stage guide shell (12).
5. The reaction device for the oxidation process in the preparation process of iron phosphate according to claim 1, wherein: and a temperature sensor (13) and a pressure sensor (14) are arranged in the reaction tank (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222898603.0U CN218359281U (en) | 2022-11-01 | 2022-11-01 | Reaction device for oxidation process in iron phosphate preparation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222898603.0U CN218359281U (en) | 2022-11-01 | 2022-11-01 | Reaction device for oxidation process in iron phosphate preparation process |
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| Publication Number | Publication Date |
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| CN218359281U true CN218359281U (en) | 2023-01-24 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
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| CN202222898603.0U Active CN218359281U (en) | 2022-11-01 | 2022-11-01 | Reaction device for oxidation process in iron phosphate preparation process |
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| Country | Link |
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| CN (1) | CN218359281U (en) |
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2022
- 2022-11-01 CN CN202222898603.0U patent/CN218359281U/en active Active
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