CN215516653U - Wet-process phosphoric acid ore pulp desulphurization unit - Google Patents
Wet-process phosphoric acid ore pulp desulphurization unit Download PDFInfo
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- CN215516653U CN215516653U CN202122441309.2U CN202122441309U CN215516653U CN 215516653 U CN215516653 U CN 215516653U CN 202122441309 U CN202122441309 U CN 202122441309U CN 215516653 U CN215516653 U CN 215516653U
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Abstract
The utility model provides a wet process phosphoric acid ore pulp desulphurization unit, includes pulp chest, phosphoric acid pond, flowmeter, microchannel reactor, first crystallizer, second crystallizer, feed liquor pump, whirl elevated tank, automatic back flush filter, desulfurating jar, sediment sour storage tank, extraction jar, pulp chest, phosphoric acid pond pass through the connecting pipe with microchannel reactor entry end fixed connection, microchannel reactor with the fixed flowmeter that is equipped with on pulp chest, the phosphoric acid pond connecting pipe, microchannel reactor exit end with the entry end of first crystallizer passes through the connecting tube and connects, first crystallizer and second crystallizer establish ties, the whirl elevated tank is being connected through the feed liquor pump to the exit end of second crystallizer, the clear solution exit end of whirl elevated tank pass through the connecting tube with the entry end of automatic back flush filter is connected.
Description
Technical Field
The utility model relates to the technical field of phosphoric acid desulfurization, in particular to a wet-process phosphoric acid ore pulp desulfurization device.
Background
The wet production is to decompose the powdered rock phosphate with inorganic acid, separate out the crude phosphoric acid, and then purify to obtain the phosphoric acid product. The cost of the wet-process phosphoric acid is 20-30% lower than that of the phosphoric acid by a thermal method, and the purity of the product can be comparable to that of the phosphoric acid by the thermal method after the phosphoric acid is purified by a proper method. The wet process phosphoric acid process is dominated by phosphoric acid production.
Wet phosphoric acid processes can be classified into sulfuric acid processes according to the inorganic acid used. The ore decomposition reaction formula is shown as follows, Ca5F (PO4)3+5H2SO4+ nH2O ═ 3H3PO4+5Ca SO4 nH2O + HF (1-3)
The forms of calcium salts generated by calcium in phosphate ore are different and have the characteristics. After the reaction is finished, how to separate the calcium salt out and economically produce the phosphoric acid is the key of the problem, and the ore pulp is directly added into a phosphoric acid storage tank in the existing production condition, so the reaction is insufficient, the desulfurization index is unstable, and the method is far from being insufficient for producing a phosphorus compound fertilizer product with higher taste.
Therefore, the wet-process phosphoric acid ore pulp desulfurization device is specially designed, so that the use requirement is met.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a wet-process phosphoric acid ore pulp desulfurization device to solve the problems in the background technology.
The purpose of the utility model is realized by the following technical scheme: a wet-process phosphoric acid ore pulp desulfurization device comprises an ore pulp pool, a phosphoric acid pool, a flowmeter, a microchannel reactor, a first crystallization tank, a second crystallization tank, a liquid inlet pump, a cyclone elevated tank, an automatic back-flushing filter, a desulfurization tank, a slag acid storage tank and an extraction tank, wherein the ore pulp pool and the phosphoric acid pool are fixedly connected with the inlet end of the microchannel reactor through connecting pipes;
the outlet end of the automatic back-flushing filter is connected with a desulfurating tank through a connecting pipeline;
the outlet end of the slag acid storage tank is fixedly connected with the extraction tank through a connecting pipeline.
Furthermore, PH control devices are fixedly arranged on connecting pipelines at the inlet end and the outlet end of the microchannel reactor, and the PH control devices are fixedly arranged on the connecting pipeline at the inlet end of the rotational flow head tank.
Furthermore, the automatic backwashing filters are arranged in two groups in parallel, are fixedly connected with an external pickling tank through a connecting pipeline, and are fixedly provided with pickling pumps at the outlet ends of the pickling tank.
Furthermore, the outlet end of the rotational flow elevated tank and the outlet end of the automatic back-washing filter are fixedly connected with the slag acid storage tank through a connecting pipeline.
Furthermore, the first crystallization tank and the second crystallization tank adopt a double-ribbon stirring system, and double-ribbon stirring is controlled by an external motor.
Furthermore, the microchannel reactor comprises two or more Y-shaped branch crystal pipelines which are arranged in parallel, and the end heads and the tail ends of the Y-shaped branch crystal pipelines are respectively connected with the material pipe.
Furthermore, a flowmeter is fixedly arranged at the port of the material pipe of the Y-shaped branch crystal pipeline on the micro-channel reactor;
the material pipe ports of the Y-shaped branch crystal pipelines are respectively provided with a one-way valve, and the outside of the one-way valve is connected with a regulating valve.
Furthermore, the Y-shaped branch crystal pipeline and the material pipe are connected in a flexible socket mode or in a threaded mode, and a sealing rubber ring is arranged at the joint of the Y-shaped branch crystal pipeline and the material pipe.
Furthermore, the automatic backwashing filter is of a hollow cylindrical structure, a filter liner is arranged in the hollow cavity, and filter holes are formed in the side wall and the bottom of the filter liner;
the filter liners are arranged in a circumferential manner and are arranged on a circular partition plate fixedly connected with the automatic backwashing filter, and pore channels corresponding to the filter liners are fixedly formed in the circular partition plate;
the outer surface of the filter liner is coated with a filter membrane, and the top of the filter liner is connected with a partition plate on the automatic backwashing filter through insertion or bolts.
Compared with the prior art, the utility model has the beneficial effects that:
(1) the process flow is simple, the operation can be realized by controlling the pH value, and the consumption of acid is reduced by adjusting the pH value.
(2) Calcium in the phosphorite generates different forms of calcium salts, and each has the characteristics that the precipitated particles are fine, the traditional natural sedimentation and other modes are adopted for treatment, the generated particles are not easy to settle, the treatment efficiency is low, the effect is poor, and the automatic surface filter is adopted, so that the treatment efficiency can be effectively improved and the investment cost can be saved while the treatment effect is improved.
Drawings
FIG. 1 is an overall connection diagram of the present invention;
FIG. 2 is a front view of a microchannel reactor of the present invention;
FIG. 3 is a schematic view of a microchannel reactor according to the present invention;
FIG. 4 is a schematic view of an automatic backwash filter of the present invention;
FIG. 5 is a schematic cross-sectional view of an automatic backwash filter according to the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments, and all other embodiments obtained by a person of ordinary skill in the art without creative efforts based on the embodiments of the present invention belong to the protection scope of the present invention.
As shown in figures 1-5, a wet-process phosphoric acid ore pulp desulfurization device comprises an ore pulp tank 1, a phosphoric acid tank 2, a flowmeter 3, a microchannel reactor 4, a first crystallization tank 5, a second crystallization tank 6, a liquid inlet pump 7, a rotational flow elevated tank 8, an automatic back-flushing filter 9, a desulfation tank 10, a slag acid storage tank 11 and an extraction tank 12, the slurry pool 1 and the phosphoric acid pool 2 are fixedly connected with the inlet end of the micro-channel reactor 4 through connecting pipes, a flow meter 3 is fixedly arranged on a connecting pipe of the micro-channel reactor 4, the slurry tank 1 and the phosphoric acid tank 2, the outlet end of the microchannel reactor 4 is connected with the inlet end of the first crystallization tank 5 through a connecting pipeline, the first crystallization tank 5 is connected with the second crystallization tank 6 in series, the outlet end of the second crystallization tank 6 is connected with a rotational flow elevated tank 8 through a liquid inlet pump 7, the clear liquid outlet end of the rotational flow elevated tank 8 is connected with the inlet end of the automatic back-flushing filter 9 through a connecting pipeline;
the outlet end of the automatic back-flushing filter 9 is connected with a desulfating tank 10 through a connecting pipeline;
the outlet end of the slag acid storage tank 11 is fixedly connected with the extraction tank 12 through a connecting pipeline.
In a further preferred embodiment of the present invention, PH control devices are fixedly disposed on the connecting pipes at the inlet end and the outlet end of the microchannel reactor 4, and a PH control device is fixedly disposed on the connecting pipe at the inlet end of the rotational flow elevated tank 8.
In a further preferred embodiment of the present invention, two sets of the automatic backwashing filters 9 are arranged in parallel, the automatic backwashing filters 9 are fixedly connected with an external pickling tank through a connecting pipeline, and a pickling pump is fixedly arranged at an outlet end of the pickling tank.
In a further preferred embodiment of the utility model, the outlet end of the rotational flow elevated tank 8 and the outlet end of the automatic backwashing filter 9 are fixedly connected with a slag acid storage tank (11) through a connecting pipeline.
In a further preferred embodiment of the present invention, the first crystallization tank 5 and the second crystallization tank 6 adopt a double helical ribbon stirring system, and the double helical ribbon stirring is controlled by an external motor.
In a further preferred embodiment of the present invention, the microchannel reactor 4 comprises two or more Y-shaped branched crystal pipelines arranged in parallel, and the ends and the end positions of the Y-shaped branched crystal pipelines are respectively connected with the material pipe.
In a further preferred embodiment of the present invention, a flowmeter is fixedly arranged at a port of a material pipe of the Y-shaped branch crystal pipeline on the microchannel reactor 4;
the material pipe ports of the Y-shaped branch crystal pipelines are respectively provided with a one-way valve, and the outside of the one-way valve is connected with a regulating valve.
The utility model further preferably adopts the embodiment that the Y-shaped branch crystal pipeline is connected with the material pipe in a flexible socket mode or in a threaded mode, and a sealing rubber ring is arranged at the joint of the Y-shaped branch crystal pipeline and the material pipe.
The further preferable embodiment of the utility model is that the automatic backwashing filter 9 is a hollow cylindrical structure, a filter liner is arranged in the hollow cavity, and the side wall and the bottom of the filter liner are provided with filter holes;
the filter liners are arranged in a circumferential manner and are arranged on a circular partition plate fixedly connected with the automatic backwashing filter 9, and pore channels corresponding to the filter liners are fixedly formed in the circular partition plate;
the outer surface of the filter liner is coated with a filter membrane, and the top of the filter liner is connected with a partition plate on the automatic backwashing filter 9 through insertion or bolts.
A flowmeter is fixedly arranged at the port of the material pipe of the Y-shaped branch crystal pipeline on the micro-channel reactor 4; and counting relevant information such as the flow speed, the flow rate and the like of each material through a flowmeter.
The material pipe ports of the Y-shaped branch crystal pipelines are respectively provided with a one-way valve, and the outside of the one-way valve is connected with a regulating valve. The one-way valve can control the entry of each material and prevent the mixed material from reversely flowing into a single material to pollute the material; the outside of the one-way valve is connected with an adjusting valve which controls the flow rate of the material.
The material pipe ports of the Y-shaped branch crystal pipelines on the microchannel reactor can be connected with a corresponding number of crystal pipelines, and the corresponding number of crystal pipelines are connected with a corresponding header pipe.
The microchannel reactor shown in fig. 2 comprises a reactor, a one-way valve, a regulating valve, a flowmeter and a first main pipe, a second main pipe, a third main pipe, a fourth main pipe and a fifth main pipe;
the first header pipe, the second header pipe, the third header pipe and the fourth header pipe are respectively positioned at the branch end of the microchannel reactor, and the fifth header pipe is positioned vertically below the microchannel reactor, wherein the number of the reactors is two or more, and the reactors are arranged on the first header pipe, the second header pipe, the third header pipe, the fourth header pipe and the fifth header pipe in parallel.
As shown in fig. 2, the reactor comprises a first crystal pipeline, a second crystal pipeline, a third crystal pipeline, a fourth crystal pipeline and a fifth crystal pipeline, the diameter of the crystal pipeline is 1-1000 μm, the first crystal pipeline and the second crystal pipeline are communicated with one end of the fifth crystal pipeline, the third crystal pipeline and the fourth crystal pipeline are communicated with the middle part of the fifth crystal pipeline, the other end of the first crystal pipeline is communicated with the first header pipe, the other end of the second crystal pipeline is communicated with the second header pipe, the other end of the third crystal pipeline is communicated with the third header pipe, the other end of the fourth crystal pipeline is communicated with the fourth header pipe, and the other end of the fifth crystal pipeline is communicated with the fifth header pipe.
As shown in fig. 2, the first crystal pipeline, the second crystal pipeline, the third crystal pipeline, the fourth crystal pipeline (respectively, a branch end position Y-type, the upper end of the first crystal pipeline, the upper end of the second crystal pipeline, the middle of the third crystal pipeline, and the middle of the fourth crystal pipeline) and the fifth crystal pipeline (in the vertical direction) are respectively flexibly inserted and connected to the first main pipe, the second main pipe, the third main pipe, the fourth main pipe, and the fifth main pipe in a socket manner. When the mixed reaction of corrosive materials is carried out, O-shaped rubber rings are arranged in the pipe threads of the first transistor pipeline, the second transistor pipeline, the third transistor pipeline, the fourth transistor pipeline and the fifth transistor pipeline which are connected with the first header pipe, the second header pipe, the third header pipe, the fourth header pipe and the fifth header pipe through the pipe threads.
As shown in fig. 3, the cylindrical main pipes seen in the axial direction are respectively a first main pipe, a second main pipe, a third main pipe, a fourth main pipe and a fifth main pipe, and ports at two ends of the first main pipe, the second main pipe, the third main pipe, the fourth main pipe and the fifth main pipe are respectively provided with a flow meter for counting relevant information such as flow speed, flow rate and the like of each material. The first main pipe, the second main pipe, the third main pipe, the fourth main pipe and the fifth main pipe are respectively provided with the check valve to control the entry of each material, and simultaneously prevent mixed materials from reversely flowing into a single material to pollute the material; the outside of the one-way valve is connected with an adjusting valve which controls the flow rate of the material.
When the types of the mixed materials exceed four, the crystal pipelines with the corresponding number can be connected to the fifth reactor crystal pipeline, and the crystal pipelines with the corresponding number are connected with corresponding header pipes.
The automatic backwashing filter 9 is of a cavity cylindrical barrel structure and is positioned in a cavity, a filter liner is arranged in the cavity, the automatic backwashing filter 9 is divided into an upper barrel and a lower barrel, the upper barrel and the lower barrel are connected through bolts, liquid to be filtered enters the lower barrel of the equipment through a liquid inlet valve, the filter liner is installed and fixed on a partition plate, the partition plate and the barrel body are integrated, the filtered liquid passes through a filter membrane and enters the upper barrel, and filtrate is directly filtered to be clear without backflow.
The filtering process comprises the steps of sequentially reciprocating until filter cakes are formed on the surfaces of filter membranes, improving the filtering precision, enabling the water quality to become clear, enabling qualified liquid to flow out of a clear liquid port and enter a filtering stage, enabling the filter cakes formed on the surfaces of the filter membranes to be thicker and thicker after filtering for a certain time, enabling the internal pressure of a lower barrel to be increased, closing a liquid inlet valve when a set value is reached, opening a liquid inlet backflow valve, enabling the lower barrel not to feed liquid, opening a backflushing valve at the same time, setting a certain backflushing time, enabling clear liquid of the upper barrel to fall down by utilizing the height difference between the upper barrel and the backflushing port, enabling the filter cakes on the surfaces of the filter membranes to impact and fall off, enabling the fallen filter cakes to settle at the centrum part of the lower barrel through settlement, and enabling the liquid inlet valve to continue to operate and filter at the moment. After several times of back flushing, the deposited slag on the cone part of the lower cylinder body is more and more, the water content of the slag slurry is gradually reduced, and finally the slag slurry is uniformly discharged at regular time.
The first crystallization tank 5 and the second crystallization tank 6 integrally adopt heat exchange media circularly flowing in the jacket to exchange heat with materials in the inner pot, and are assisted by stirring movement of the stirring device, so that rapid cooling and uniform crystallization are realized.
The utility model is designed aiming at the treatment of solid particles and sulfur contained in the dilute phosphoric acid, the ore pulp and phosphate radicals in the phosphoric acid are selected to be fully reflected, the phosphate radicals are finally separated out in the form of insoluble sulfate, the original solid particles in the generated refractory sulfate are removed through filtration and purification, the dilute phosphoric acid is effectively purified, the content of sulfur trioxide in the purified phosphoric acid is less than 10g/l, the solid content is less than 0.15 percent, and the dilute phosphoric acid is clear through visual observation.
It will be evident to those skilled in the art that the utility model is not limited to the details of the foregoing illustrative embodiments, and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the utility model being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.
Furthermore, it should be understood that although the present description refers to embodiments, not every embodiment may contain only a single embodiment, and such description is for clarity only, and those skilled in the art should integrate the description, and the embodiments may be combined as appropriate to form other embodiments understood by those skilled in the art.
Claims (9)
1. The wet-process phosphoric acid ore pulp desulfurization device is characterized by comprising an ore pulp pond (1), a phosphoric acid pond (2), a flowmeter (3), a microchannel reactor (4), a first crystallization tank (5), a second crystallization tank (6), a liquid inlet pump (7), a rotational flow elevated tank (8), an automatic backwashing filter (9), a desulfurating tank (10), a slag acid storage tank (11) and an extraction tank (12), wherein the ore pulp pond (1) and the phosphoric acid pond (2) are fixedly connected with the inlet end of the microchannel reactor (4) through connecting pipes, the flowmeter (3) is fixedly arranged on the connecting pipes of the microchannel reactor (4), the outlet end of the microchannel reactor (4) is connected with the inlet end of the first crystallization tank (5) through a connecting pipe, the first crystallization tank (5) is connected with the second crystallization tank (6) in series, the outlet end of the second crystallization tank (6) is connected with a rotational flow elevated tank (8) through a liquid inlet pump (7), and the clear liquid outlet end of the rotational flow elevated tank (8) is connected with the inlet end of the automatic back-flushing filter (9) through a connecting pipeline;
the outlet end of the automatic back-flushing filter (9) is connected with a desulfurating tank (10) through a connecting pipeline;
the outlet end of the slag acid storage tank (11) is fixedly connected with the extraction tank (12) through a connecting pipeline.
2. The wet-process phosphoric acid pulp desulfurization device according to claim 1, characterized in that the inlet end and outlet end connecting pipes of the microchannel reactor (4) are fixedly provided with pH control devices, and the inlet end connecting pipe of the cyclone elevated tank (8) is fixedly provided with a pH control device.
3. The wet-process phosphoric acid ore pulp desulfurization device according to claim 1, characterized in that two groups of automatic back-washing filters (9) are arranged in parallel, the automatic back-washing filters (9) are fixedly connected with an external pickling tank through connecting pipes, and a pickling pump is fixedly arranged at the outlet end of the pickling tank.
4. The wet-process phosphoric acid pulp desulfurization device according to claim 1, characterized in that the outlet end of the cyclone elevated tank (8) and the outlet end of the automatic back-flushing filter (9) are fixedly connected with the slag acid storage tank (11) through a connecting pipeline.
5. The wet-process phosphoric acid pulp desulfurization device according to claim 1, characterized in that the first crystallization tank (5) and the second crystallization tank (6) adopt a double-ribbon stirring system, and the double-ribbon stirring is controlled by an external motor.
6. The wet-process phosphoric acid pulp desulfurization device according to claim 1, wherein the microchannel reactor (4) comprises two or more Y-shaped branch crystal pipelines arranged in parallel, and the ends and the end positions of the Y-shaped branch crystal pipelines are respectively connected with a material pipe.
7. The wet-process phosphoric acid pulp desulfurization device according to claim 6, characterized in that a flowmeter is fixedly arranged at the port of the material pipe of the Y-shaped branch crystal pipeline on the microchannel reactor (4);
the material pipe ports of the Y-shaped branch crystal pipelines are respectively provided with a one-way valve, and the outside of the one-way valve is connected with a regulating valve.
8. The wet-process phosphoric acid pulp desulfurization device according to claim 7, wherein the Y-shaped branch crystal pipeline is in flexible socket joint with the material pipe or in threaded connection with the material pipe, and a sealing rubber ring is arranged at the joint of the Y-shaped branch crystal pipeline and the material pipe.
9. The wet-process phosphoric acid pulp desulfurization device according to claim 1, characterized in that the automatic back-washing filter (9) has a hollow cylindrical structure, and a filter container is arranged in the hollow cylindrical structure, and the side wall and the bottom of the filter container are provided with filter holes;
the filter liners are arranged in a circumferential manner and are arranged on a circular partition plate fixedly connected with the automatic backwashing filter (9), and pore channels corresponding to the filter liners are fixedly formed in the circular partition plate;
the outer surface of the filter liner is coated with a filter membrane, and the top of the filter liner is connected with a partition plate on the automatic backwashing filter (9) through insertion or bolts.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122441309.2U CN215516653U (en) | 2021-10-11 | 2021-10-11 | Wet-process phosphoric acid ore pulp desulphurization unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122441309.2U CN215516653U (en) | 2021-10-11 | 2021-10-11 | Wet-process phosphoric acid ore pulp desulphurization unit |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN215516653U true CN215516653U (en) | 2022-01-14 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202122441309.2U Active CN215516653U (en) | 2021-10-11 | 2021-10-11 | Wet-process phosphoric acid ore pulp desulphurization unit |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN215516653U (en) |
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2021
- 2021-10-11 CN CN202122441309.2U patent/CN215516653U/en active Active
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