Chemical crystallization granulation fluidized bed

Abstract

The embodiment of the invention provides a chemical crystallization granulation fluidized bed. The chemical crystallization granulation fluidized bed comprises an outer cylinder body, a first inner cylinder body, a second inner cylinder body and a separation device. The upper end and the lower end of each of the first inner cylinder body and the second inner cylinder body are opened to form a flocculation reaction channel, and the first inner cylinder body and the second inner cylinder body are arranged in the outer cylinder body in a spaced mode in the height direction of the outer cylinder body to form a flocculation sedimentation reaction channel; a gap is formed between the first inner barrel and the sludge collecting area in the height direction of the outer barrel, a liquid inlet and a medicament adding port are formed below the first inner barrel, and the fluid resistance in the flocculation reaction channel is smaller than that in the coagulation sedimentation reaction channel so as to form a flow velocity difference; and the separating device is arranged on an opening at the upper end of the outer barrel. Therefore, the chemical crystallization granulation fluidized bed provided by the embodiment of the invention has the advantage of enhancing the sewage softening capability of the fluidized bed.

Description

Technical Field

[0001] The invention relates to the technical field of environmental protection equipment, and in particular to a chemical crystallization granulation fluidized bed. Background Art

[0002] In the related art, the crystallization fluidized bed device is a technology for producing granular solid products, which combines fluidized bed technology and crystallization process. It includes an outer cylinder, and chemicals and crystal seeds are added into the outer cylinder. The surface of the crystal seeds continues to gather. When the crystals grow to a certain size, they will break the fluidization balance and automatically settle back to the mud collection area at the bottom. The sludge in the mud collection area is subjected to a mud-water separation process by a filter press, and finally forms a mud cake. Under the premise of ensuring the sedimentation effect of tiny particles (ensuring the turbidity upper limit of overflow water), the overall flow rate in the crystallization fluidized bed is also limited. Exceeding the flow upper limit will cause a large number of tiny particles to no longer be effectively settled in the large-diameter sedimentation device and be discharged with the overflow water, resulting in an increase in the turbidity of the external drainage. Summary of the invention

[0003] The present invention aims to solve one of the technical problems in the related art at least to a certain extent. To this end, an embodiment of the present invention provides a chemical crystallization granulation fluidized bed. The chemical crystallization granulation fluidized bed has the advantage of enhancing the ability of the fluidized bed to soften sewage.

[0004] The chemical crystallization granulation fluidized bed of the embodiment of the present invention comprises an outer cylinder, a first inner cylinder, a second inner cylinder and a separation device.

[0005] The outer cylinder has a liquid inlet, a reagent addition port, a seed addition port, an opening at the upper end and a mud collecting area at the lower end; the upper and lower ends of each of the first inner cylinder and the second inner cylinder are open to form a flocculation reaction channel, the first inner cylinder and the second inner cylinder are arranged in the outer cylinder at intervals along the height direction of the outer cylinder to form a flocculation sedimentation reaction channel between the outer cylinder and the first inner cylinder and the second inner cylinder, and the second inner cylinder is arranged above the first inner cylinder and the mud collecting area, the first inner cylinder and the mud collecting area are spaced in the height direction of the outer cylinder, the liquid inlet and the reagent addition port are arranged below the first inner cylinder, the fluid resistance in the flocculation reaction channel is smaller than the fluid resistance in the coagulation sedimentation reaction channel so as to form a flow rate difference; the separation device is arranged on the opening at the upper end of the outer cylinder.

[0006] The chemical crystallization granulation fluidized bed of the embodiment of the present invention is provided with a first inner cylinder and a second inner cylinder in an outer cylinder, and the liquid inlet and the reagent addition port are provided below the first inner cylinder. The fluid resistance in the flocculation reaction channel is less than the fluid resistance in the coagulation and sedimentation reaction channel so as to form a flow rate difference. The sewage and the added reagent entering the outer cylinder through the liquid inlet at the bottom will preferentially enter the first inner cylinder, so that the reagent will circulate and crystallize. The fine crystal particles will continue to circulate upward into the second inner cylinder, so that the calcium carbonate crystal particles will further condense. The larger particles will preferentially pass through the flocculation and sedimentation reaction channel. Since the relative flow rate of the fluid in the flocculation and sedimentation reaction channel is low, the particle sedimentation is convenient and it is beneficial to reduce the threshold of particle sedimentation. Finally, the clean water will be discharged from the opening at the top of the outer cylinder through the separation device, which greatly improves the crystallization efficiency and strengthens the ability of the fluidized bed to soften sewage.

[0007] Therefore, the chemical crystallization granulation fluidized bed of the embodiment of the present invention has the advantage of enhancing the ability of the fluidized bed to soften sewage.

[0008] In some embodiments, the outer cylinder includes a sewage inlet section located in the lower section and a granulation section connected to the top of the mud collecting section, the sewage inlet section is provided with the liquid inlet and the agent addition port, the bottom of the sewage inlet section forms the mud collecting area, the granulation section is provided with the seed addition port, the cross-section of the granulation section is larger than the cross-sectional area of ​​the sewage inlet section, and the first inner cylinder and the second inner cylinder are arranged in the granulation section.

[0009] In some embodiments, the granulation section includes a first section and a second section, the first section is provided with a first flared section at the connection with the pollution inlet section, and the second section is provided with a second flared section at the connection with the first section.

[0010] In some embodiments, the inclination angle of each of the first flared section and the second section is 40°-50°.

[0011] In some embodiments, the difference between the diameter of the first segment and the diameter of the second segment is 200 mm-300 mm.

[0012] In some embodiments, the diameter of the sewage inlet section is 2200mm-3200mm; the height of the outer cylinder is 6700mm-7700mm.

[0013] In some embodiments, the lower end of the second inner cylinder has a bell mouth, and the bell mouth and the second expansion section are correspondingly arranged in the height direction of the outer cylinder.

[0014] In some embodiments, the inclination angle at the bell mouth is 40°-50°.

[0015] In some embodiments, the ratio of the diameter of the bell mouth of the second inner cylinder to the diameter of the first inner cylinder is 1.05-1.15:1.

[0016] In some embodiments, the roughness of the inner wall surface of the outer cylinder is greater than the roughness of the inner wall surface of the first inner cylinder and the roughness of the inner wall surface of the second inner cylinder to make the flow rate difference.

[0017] In some embodiments, central axes of the first inner cylinder and the second inner cylinder are collinearly arranged.

[0018] In some embodiments, the distance between the upper end surface of the second inner cylinder and the lower end surface of the separation device is 500 mm-700 mm.

[0019] In some embodiments, a distance between the first inner cylinder and the second inner cylinder in a height direction of the outer cylinder is 600 mm-800 mm.

[0020] In some embodiments, the diameter of the first inner cylinder is 1900 mm-2900 mm, and the height of the first inner cylinder is 2000 mm-2400 mm.

[0021] In some embodiments, the diameter of the second inner cylinder is 1900 mm-2900 mm, and the height of the second inner cylinder is 2000 mm-2400 mm.

[0022] In some embodiments, the separation device includes a ring plate, the ring plate covers the opening of the outer cylinder, and the ring plate is provided with a plurality of inclined holes.

[0023] In some embodiments, the separation device includes a plurality of connected and obliquely arranged tubes, each of which has an inclined hole.

[0024] In some embodiments, the diameter of the tube is 30 mm to 50 mm; the length of the tube is 200 mm to 300 mm;

[0025] The inclination angle of the tube body is 40°-50°. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 It is a schematic structural diagram of a chemical crystallization granulation fluidized bed according to an embodiment of the present invention.

[0027] Reference numerals:

[0028] Outer cylinder 1; sewage inlet section 11; first expansion section 12; first subsection 13; second expansion section 14; second subsection 15;

[0029] Liquid inlet 101; reagent addition port 102; seed addition port 103; opening 104; mud collection area 105;

[0030] The first inner cylinder 2;

[0031] The second inner cylinder 3; the bell mouth 31;

[0032] Separating device 4; inclined hole 41. DETAILED DESCRIPTION

[0033] Embodiments of the present invention are described in detail below, and examples of the embodiments are shown in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are exemplary and intended to be used to explain the present invention, but should not be understood as limiting the present invention.

[0034] Reference below Figure 1 The chemical crystallization granulation fluidized bed according to an embodiment of the present invention is described.

[0035] The chemical crystallization granulation fluidized bed of the embodiment of the present invention comprises an outer cylinder 1 , a first inner cylinder 2 , a second inner cylinder 3 and a separation device 4 .

[0036] The outer cylinder 1 has a liquid inlet 101, a reagent addition port 102, a seed addition port 103, an opening 104 at the upper end and a mud collecting area 105 at the lower end; the upper and lower ends of each of the first inner cylinder 2 and the second inner cylinder 3 are open to form a flocculation reaction channel, the first inner cylinder 2 and the second inner cylinder 3 are arranged in the outer cylinder 1 at intervals along the height direction of the outer cylinder 1 to form a flocculation sedimentation reaction channel between the outer cylinder 1 and the first inner cylinder 2 and the second inner cylinder 3, and the second inner cylinder 3 is arranged above the first inner cylinder 2 and the mud collecting area 105, the first inner cylinder 2 and the mud collecting area 105 are spaced in the height direction of the outer cylinder 1, the liquid inlet 101 and the reagent addition port 102 are arranged below the first inner cylinder 2, the fluid resistance in the flocculation reaction channel is smaller than the fluid resistance in the coagulation sedimentation reaction channel so as to form a flow rate difference; the separation device 4 is arranged on the opening 104 at the upper end of the outer cylinder 1.

[0037] The chemical crystallization granulation fluidized bed of the embodiment of the present invention is provided with a first inner cylinder 2 and a second inner cylinder 3 in an outer cylinder 1, and a liquid inlet 101 and a reagent addition port 102 are provided below the first inner cylinder 2. The fluid resistance in the flocculation reaction channel is less than the fluid resistance in the coagulation and sedimentation reaction channel so as to form a flow rate difference. The sewage and the added reagent entering the outer cylinder 1 through the liquid inlet 101 at the bottom will preferentially enter the first inner cylinder 2, so that the reagent (calcium carbonate particles) will be circulated and crystallized. The fine crystal particles will continue to circulate upward into the second inner cylinder 3, so that the calcium carbonate crystal particles will further condense. The larger particles will preferentially pass through the flocculation and sedimentation reaction channel. Since the relative flow rate of the fluid in the flocculation and sedimentation reaction channel is low, the particle sedimentation is convenient and the threshold value of particle sedimentation is reduced. Finally, the clean water will be discharged from the opening 104 at the top of the outer cylinder 1 through the separation device 4, which greatly improves the crystallization efficiency of calcium carbonate and strengthens the ability of the fluidized bed to soften sewage.

[0038] Therefore, the chemical crystallization granulation fluidized bed of the embodiment of the present invention has the advantage of enhancing the ability of the fluidized bed to soften sewage.

[0039] like Figure 1 As shown, the outer cylinder 1 includes a sewage inlet section 11 located at the lower section and a granulation section connected to the top of the mud collecting section, the sewage inlet section 11 is provided with a liquid inlet 101 and a reagent addition port 102, the bottom of the sewage inlet section 11 forms a mud collecting area 105, the granulation section is provided with a seed addition port 103, the cross-section of the granulation section is larger than the cross-sectional area of ​​the sewage inlet section 11, and the first inner cylinder 2 and the second inner cylinder 3 are arranged in the granulation section.

[0040] The chemical crystallization granulation fluidized bed of the embodiment of the present invention includes a sewage inlet section 11 located at the lower section and a granulation section connected to the upper part of the mud collection section through the outer cylinder 1, and the cross section of the granulation section is larger than the cross section of the sewage inlet section 11. In actual use, because the flow velocity of the same volume of fluid in the flow channel with a larger cross section is lower than the flow velocity in the flow channel with a smaller cross section, there will be a greater resistance when the sewage enters the flocculation sedimentation reaction channel, so that most of the sewage flows into the flocculation reaction channel as much as possible to participate in the flocculation reaction. This promotes the softening efficiency of the chemical crystallization granulation fluidized bed for sewage.

[0041] like Figure 1 As shown, the granulation section includes a first section 13 and a second section 15 . The first section 13 is provided with a first expansion section 12 at the connection with the sewage inlet section 11 , and the second section 15 is provided with a second expansion section 14 at the connection with the first section 13 .

[0042] The chemical crystallization granulation fluidized bed of the embodiment of the present invention is characterized in that the granulation section is divided into a first section 13 and a second section 15. The first section 13 is provided with a first flared section 12 at the connection with the sewage inlet section 11, and the second section 15 is provided with a second flared section 14 at the connection with the first section 13. Since the flow velocity of the same volume of fluid in a flow channel with a larger cross-section is smaller than that in a flow channel with a smaller cross-section, the water flow velocity can be gradually reduced along the flow direction of the fluid, which is beneficial to prolonging the coagulation time, thereby further improving the crystallization efficiency of calcium carbonate.

[0043] Specifically, Figure 1 As shown, the sewage inlet section 11, the first expansion section 12, the first subsection 13, the second expansion section 14 and the second subsection 15 are arranged in sequence from bottom to top.

[0044] The inclination angle of each of the first flared section 12 and the second segment 15 (the angle between the first flared section 12 and the second segment 15 and the vertical direction) is 40°-50°. On the one hand, it avoids the problem that the inclination angle is too large, which makes the condensation and sedimentation reaction channel too narrow, resulting in the water flow rate therein being too large and not conducive to sedimentation. On the other hand, it also avoids the problem that the inclination angle is too small, the fluid velocity in the condensation and sedimentation reaction channel is not significantly reduced, the reaction time of the reactants in the condensation and sedimentation reaction channel is too short, and the particles therein are slowly settled and aggregated. Furthermore, the chemical crystallization granulation fluidized bed of the embodiment of the present invention has the advantage of further reducing the turbidity of the external drainage.

[0045] Alternatively, the inclination angle of each of the first expansion section 12 and the second section 15 may be 40°, 41°, 42°, 43°, 44°, 45°, 46°, 47°, 48°, 49° and 50°.

[0046] The difference between the diameter of the first section 13 and the diameter of the second section 15 is 200 mm to 300 mm.

[0047] Optionally, the difference between the diameter of the first segment 13 and the diameter of the second segment 15 is 200 mm, 210 mm, 220 mm, 230 mm, 240 mm, 250 mm, 260 mm, 270 mm, 280 mm, 290 mm and 300 mm.

[0048] The distance between the first inner cylinder 2 and the second inner cylinder 3 in the height direction of the outer cylinder 1 is 600 mm-800 mm.

[0049] The chemical crystallization granulation fluidized bed of the embodiment of the present invention can accurately control the temperature, pH value and other physical and chemical conditions of crystal growth by limiting the spacing between the first inner cylinder 2 and the second inner cylinder 3 in the height direction of the outer cylinder 1, which helps to obtain the ideal crystal morphology and particle size distribution, and the relative speed between the liquid and the solid enhances the material exchange rate, especially for substances with low solubility such as calcium carbonate, which helps to accelerate their precipitation from the solution.

[0050] Furthermore, the spacing between the first inner cylinder 2 and the second inner cylinder 3 in the height direction of the outer cylinder 1 may be 600 mm, 620 mm, 650 mm, 680 mm, 700 mm, 720 mm, 750 mm, 780 mm and 800 mm.

[0051] The diameter of the first inner cylinder 2 is 1900 mm-2900 mm, and the height of the first inner cylinder 2 is 2000 mm-2400 mm.

[0052] Optionally, the diameter of the first inner cylinder 2 is 1900 mm, 2000 mm, 2100 mm, 2200 mm, 2300 mm, 2400 mm, 2500 mm, 2600 mm, 2700 mm, 2800 mm and 2900 mm.

[0053] Optionally, the height of the first inner cylinder 2 is 2000 mm, 2050 mm, 2100 mm, 2150 mm, 2200 mm, 2250 mm, 2300 mm, 2350 mm and 2400 mm.

[0054] The diameter of the second inner cylinder 3 is 1900 mm-2900 mm. The height of the second inner cylinder 3 is 2000 mm-2400 mm.

[0055] Optionally, the diameter of the second inner cylinder 3 is 1900 mm, 2000 mm, 2100 mm, 2200 mm, 2300 mm, 2400 mm, 2500 mm, 2600 mm, 2700 mm, 2800 mm and 2900 mm.

[0056] Optionally, the height of the second inner cylinder 3 is 2000 mm, 2050 mm, 2100 mm, 2150 mm, 2200 mm, 2250 mm, 2300 mm, 2350 mm and 2400 mm.

[0057] The lower end of the second inner cylinder 3 has a bell mouth 31, and the bell mouth 31 and the second expanded section 14 are arranged correspondingly in the height direction of the outer cylinder 1. In this way, the smaller particles flowing out of the second expanded section 14 in the flocculation and sedimentation reaction channel can flow back into the flocculation reaction channel, and the larger particles will continue to sink due to their heavy weight. Therefore, the second expanded section 14 has a certain separation effect.

[0058] The lower end of the second inner cylinder 3 has a bell mouth 31 , and the inclination angle of the bell mouth 31 is 40°-50°.

[0059] The chemical crystallization granulation fluidized bed of the embodiment of the present invention has a bell mouth 31 at the lower end of the second inner cylinder 3, so that when the fluid in the first inner cylinder 2 flows from bottom to top, the fluid will diverge after passing through the first inner cylinder 2, and the bell mouth 31 at the lower end of the second inner cylinder 3 smoothly flows into the second inner cylinder 3, so that the calcium carbonate crystal particles are circulated for the second time. And the circulation process can make the fine particles that are not completely crystallized return to the reaction zone again to continue to participate in the reaction.

[0060] The roughness of the inner wall of the outer cylinder 1 is greater than that of the inner wall of the first inner cylinder 2 and the inner wall of the second inner cylinder 3 to make the flow rate difference. Therefore, the chemical crystallization granulation fluidized bed of the embodiment of the present invention has the advantage of simple structure.

[0061] Optionally, the ratio of the diameter of the bell mouth 31 of the second inner cylinder 3 to the diameter of the first inner cylinder 2 is 1.05-1.15:1.

[0062] The distance between the upper end surface of the second inner cylinder 3 and the lower end surface of the separation device 4 is 500mm-700mm.

[0063] The chemical crystallization granulation fluidized bed of the embodiment of the present invention limits the distance between the upper end surface of the second inner cylinder 3 and the lower end surface of the separation device 4, thereby preventing the water with sludge particles at the lower end of the second inner cylinder 3 from disturbing the flow direction of the fluid coagulation and sedimentation reaction channel in the separation device 4. Therefore, the chemical crystallization granulation fluidized bed has the advantage of increasing the sedimentation rate.

[0064] Optionally, the distance between the upper end surface of the second inner cylinder 3 and the lower end surface of the separation device 4 may be 500 mm, 550 mm, 600 mm, 650 mm and 700 mm.

[0065] The central axes of the first inner cylinder 2 and the second inner cylinder 3 are arranged on the same line.

[0066] The separation device 4 comprises a ring plate, which covers the opening 104 of the outer cylinder 1 and is provided with a plurality of inclined holes 41 .

[0067] The chemical crystallization granulation fluidized bed of the embodiment of the present invention can prevent the overflow of sludge particles by setting a ring plate with inclined holes 41, because the overflowing sludge particles can collide with the hole wall of the inclined hole 41, and then the particles sink to achieve the separation of water and sludge particles, further reducing the turbidity of the external drainage.

[0068] The embodiments of the present invention are not limited thereto. For example, in other embodiments, the separation device 4 includes a plurality of tubes that are connected and inclined, and each tube has an inclined hole 41 .

[0069] The chemical crystallization granulation fluidized bed of the embodiment of the present invention has a specific working principle as follows: sewage enters from the bottom of the inner cylinder 3 and is stirred by the blades, the suspended matter begins to flocculate, the sewage flows upward to the top of the middle cylinder 2 and begins to flow back from the outside, and then returns to the bottom to start circulation. The tiny flocculated particles accumulate and become larger with the circulation, and eventually settle to the sludge collecting area 105 to become sludge. The inclined holes 41 in the separation device 4 further prevent the sludge particles from overflowing, and the clean water is discharged from the sump above the fluidized bed, and finally the turbidity removal of the sewage is completed.

[0070] The diameter of the tube body is 30mm-50mm. Optionally, the diameter of the tube body is 30mm, 32mm, 35mm, 38mm, 40mm, 42mm, 45mm, 48mm and 50mm.

[0071] The length of the tube body is 200mm-300mm; optionally, the length of the tube body can be 200mm, 210mm, 220mm, 230mm, 240mm, 250mm, 260mm, 270mm, 280mm, 290mm and 300mm.

[0072] The inclination angle of the pipe body is 40°-50°. The inclination angle of the pipe body can be 40°, 41°, 42°, 43°, 44°, 45°, 46°, 47°, 48°, 49° and 50°.

[0073] In the description of the present invention, it is to be understood that the terms “center”, “longitudinal”, “lateral”, “length”, “width”, “thickness”, “up”, “down”, “front”, “back”, “left”, “right”, “vertical”, “horizontal”, “top”, “bottom”, “inside”, “outside”, “clockwise”, “counterclockwise”, “axial”, “radial”, “circumferential”, etc., indicating orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as limiting the present invention.

[0074] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. In the description of the present invention, the meaning of "plurality" is at least two, such as two, three, etc., unless otherwise clearly and specifically defined.

[0075] In the present invention, unless otherwise clearly specified and limited, the terms "installed", "connected", "connected", "fixed" and the like should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral one; it can be a mechanical connection, an electrical connection, or communication with each other; it can be a direct connection, or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements, unless otherwise clearly defined. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0076] In the present invention, unless otherwise clearly specified and limited, a first feature being "above" or "below" a second feature may mean that the first and second features are in direct contact, or the first and second features are in indirect contact through an intermediate medium. Moreover, a first feature being "above", "above" or "above" a second feature may mean that the first feature is directly above or obliquely above the second feature, or simply means that the first feature is higher in level than the second feature. A first feature being "below", "below" or "below" a second feature may mean that the first feature is directly below or obliquely below the second feature, or simply means that the first feature is lower in level than the second feature.

[0077] In the present invention, the terms "one embodiment", "some embodiments", "examples", "specific examples", or "some examples" etc. mean that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the described specific features, structures, materials or characteristics may be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art may combine and combine the different embodiments or examples described in this specification and the features of the different embodiments or examples, without contradiction.

[0078] Although the embodiments of the present invention have been shown and described above, it is to be understood that the above embodiments are exemplary and are not to be construed as limitations of the present invention. A person skilled in the art may change, modify, replace and vary the above embodiments within the scope of the present invention.

Claims

1. A chemical crystallization granulation fluidized bed, characterized in that: include: An outer cylinder, the outer cylinder having a liquid inlet, a reagent addition port, a seed addition port, an opening at the upper end and a mud collection area at the lower end; A first inner cylinder and a second inner cylinder, each of which has upper and lower ends open to form a flocculation reaction channel, the first inner cylinder and the second inner cylinder are arranged in the outer cylinder at intervals along the height direction of the outer cylinder to form a flocculation sedimentation reaction channel between the outer cylinder and the first inner cylinder and the second inner cylinder, the second inner cylinder is arranged above the first inner cylinder and the mud collecting area, and the first inner cylinder and the mud collecting area are spaced apart in the height direction of the outer cylinder, the liquid inlet and the reagent addition port are arranged below the first inner cylinder, and the fluid resistance in the flocculation reaction channel is smaller than the fluid resistance in the flocculation sedimentation reaction channel so as to form a flow rate difference; A separation device is arranged on the opening of the upper end of the outer cylinder.

2. The chemical crystallization granulation fluidized bed according to claim 1, characterized in that: The outer cylinder includes a sewage inlet section located at the lower section and a granulation section connected to the top of the mud collecting section, the sewage inlet section is provided with the liquid inlet and the reagent addition port, the bottom of the sewage inlet section forms the mud collecting area, the granulation section is provided with the seed addition port, the cross-section of the granulation section is larger than the cross-sectional area of ​​the sewage inlet section, and the first inner cylinder and the second inner cylinder are arranged in the granulation section.

3. The chemical crystallization granulation fluidized bed according to claim 2, characterized in that: The granulation section comprises a first section and a second section. The first section is provided with a first flaring section at a connection with the sewage inlet section, and the second section is provided with a second flaring section at a connection with the first section.

4. The chemical crystallization granulation fluidized bed according to claim 3, characterized in that: The inclination angle of each of the first flared section and the second section is 40°-50°; The difference between the diameter of the first segment and the diameter of the second segment is 200 mm to 300 mm; The diameter of the sewage inlet section is 2200mm-3200mm, and the height of the outer cylinder is 6700mm-7700mm.

5. The chemical crystallization granulation fluidized bed according to claim 3, characterized in that: The lower end of the second inner cylinder has a bell mouth, and the bell mouth and the second expanding section are correspondingly arranged in the height direction of the outer cylinder.

6. The chemical crystallization granulation fluidized bed according to claim 5, characterized in that: The inclination angle at the bell mouth is 40°-50°; The ratio of the diameter of the bell mouth of the second inner cylinder to the diameter of the first inner cylinder is 1.05-1.15:

1.

7. The chemical crystallization granulation fluidized bed according to claim 1, characterized in that: The roughness of the inner wall surface of the outer cylinder is greater than the roughness of the inner wall surface of the first inner cylinder and the roughness of the inner wall surface of the second inner cylinder to make the flow velocity difference; The central axes of the first inner cylinder and the second inner cylinder are arranged collinearly; And / or, the distance between the upper end surface of the second inner cylinder and the lower end surface of the separation device is 500mm-700mm.

8. The chemical crystallization granulation fluidized bed according to claim 4, characterized in that: The distance between the first inner cylinder and the second inner cylinder in the height direction of the outer cylinder is 600mm-800mm; The diameter of the first inner cylinder is 1900mm-2900mm, and the height of the first inner cylinder is 2000mm-2400mm; The diameter of the second inner cylinder is 1900mm-2900mm, and the height of the second inner cylinder is 2000mm-2400mm.

9. The chemical crystallization granulation fluidized bed according to claim 1, characterized in that: The separation device comprises a ring plate, the ring plate covers the opening of the outer cylinder, and the ring plate is provided with a plurality of inclined holes; Alternatively, the separation device comprises a plurality of connected and obliquely arranged tubes, each of which has an inclined hole.

10. The chemical crystallization granulation fluidized bed according to claim 9, characterized in that: The diameter of the tube body is 30mm-50mm; the length of the tube body is 200mm-300mm; The inclination angle of the tube body is 40°-50°.

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