Reactor for preparing inorganic polymeric flocculant from fly ash
By designing a multi-channel reactor and an internal grinding chamber, the problem of difficult aluminum leaching from fly ash was solved, achieving efficient aluminum leaching and improved product quality. This also improved the particle size and reactivity of fly ash and enhanced the mass transfer process.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- SHAANXI QINLONG ELECTRIC POWER CO LTD
- Filing Date
- 2025-05-14
- Publication Date
- 2026-04-17
AI Technical Summary
In existing processes for producing inorganic flocculants from fly ash, aluminum has low reaction efficiency and is difficult to dissolve, resulting in low aluminum chloride content in the product and poor economic efficiency. Furthermore, aluminum in fly ash mainly exists in crystalline and glassy forms, making it difficult to dissolve efficiently.
A multi-channel reactor is designed, including a first channel, a second channel, a third channel, and a fourth channel. An inner grinding chamber and an outer grinding chamber are set up. Fly ash, inorganic acid, and co-solvent are injected into the inner grinding chamber through a nozzle assembly using an ultra-high pressure air pump. Combined with multi-layer baffles, the materials are mixed and ground to achieve multi-level material input and mixing, thereby promoting chemical reactions.
It improves the leaching rate of aluminum in fly ash, enhances product quality, improves the particle size and surface reactivity of fly ash particles, strengthens the mass transfer process, and increases the leaching rate of valuable elements such as aluminum and iron.
Smart Images
Figure CN224127306U_ABST
Abstract
Description
Technical Field
[0001] This utility model belongs to the field of fly ash resource utilization technology, specifically relating to a reactor for producing inorganic polymer flocculants from fly ash. Background Technology
[0002] Fly ash is a solid waste discharged from the hydraulic ash removal system of thermal power plants. Since approximately 90% of the alumina in fly ash is in a glassy state with low reactivity, it is difficult to dissolve directly with acid. Previously, the soda lime method was commonly used, but this method involves large equipment investment, high corrosiveness to equipment, high energy consumption, and requires large amounts of soda ash, making it impractical for production. Some researchers have used KF and NH4F as co-solvents to open the silicon-aluminum bonds before acid dissolution to increase the alumina dissolution rate, yielding aluminum chloride, which is then adjusted for basicity using pyrolysis or sodium hydroxide. Lu Sheng et al. used fly ash as raw material and NH4F as a co-solvent to produce polyaluminum chloride, but the utilization rate of aluminum remained low. Given that Al2O3 in fly ash exists in the form of inactive alumina-rich glassy andalusite (3AL2O3·SiO2), it is difficult to dissolve directly with acid.
[0003] Existing technologies for producing inorganic flocculants from fly ash mainly suffer from low aluminum reaction efficiency, difficulty in dissolution, low aluminum chloride content in the product, and poor economic efficiency. Aluminum in fly ash primarily exists in crystalline muganite and glassy aluminosilicate forms, which are very stable and require harsh conditions such as high temperature, high acidity, and high alkaliness for dissolution, and the dissolution rate is generally low.
[0004] Based on the above problems, this utility model proposes a reactor for producing inorganic polymer flocculants from fly ash. Utility Model Content
[0005] The purpose of this invention is to provide a reactor for producing inorganic polymeric flocculants from fly ash. To achieve the above objective, the technical solution adopted by this invention is as follows:
[0006] A reactor for producing inorganic polymeric flocculants from fly ash, comprising:
[0007] First passage;
[0008] The second channel is arranged around the outer periphery of the first channel;
[0009] The third channel is arranged around the outer periphery of the second channel;
[0010] The fourth channel is arranged around the outer perimeter of the third channel;
[0011] The inner grinding chamber is located below the first channel, the second channel, the third channel, and the fourth channel, and is connected to the first channel, the second channel, and the third channel;
[0012] The outer grinding chamber is located below the inner grinding chamber and is connected to the inner grinding chamber. An outlet is provided at the bottom of the outer grinding chamber.
[0013] Furthermore, the first channel has an axial inward reduction of 2-5 mm relative to the second channel.
[0014] Furthermore, nozzle assemblies are installed at the outlets of the first, second, and third channels.
[0015] Furthermore, the nozzle assembly includes a first nozzle, a second nozzle, and a third nozzle. The first nozzle is located at the channel outlet of the first channel, the second nozzle is located at the channel outlet of the second channel, and the third nozzle is located at the channel outlet of the third channel.
[0016] Furthermore, the first nozzle has an axial inward retraction of 10-30 mm relative to the second nozzle.
[0017] Furthermore, an ultra-high pressure air pump is installed at the inlet of the first channel.
[0018] Furthermore, the inner grinding cavity is equipped with multiple layers of baffles.
[0019] Furthermore, the baffles are horizontally positioned within the inner grinding chamber.
[0020] Furthermore, the baffle plate is inclinedly arranged inside the inner grinding chamber.
[0021] Furthermore, the baffles are arranged in a labyrinthine manner within the inner grinding chamber.
[0022] This utility model has the following advantages due to the adoption of the above technical solution:
[0023] This invention discloses a reactor for producing inorganic polymeric flocculants from fly ash. By incorporating a first, second, third, and fourth channel, it achieves multi-stage material input and mixing. This improves the mixing uniformity between materials and promotes the full conduct of chemical reactions. The internal grinding chamber provides ample grinding space for the reacted materials, helping to refine material particles and improve product quality. The reactor designed in this application can improve the particle size of fly ash particles, enhance surface reactivity, and strengthen mass transfer. Attached Figure Description
[0024] Figure 1 This is a schematic diagram of the reactor used in the production of inorganic polymer flocculants from fly ash according to this invention.
[0025] Figure 2 This is a bottom view of the nozzle assembly of the reactor used in the production of inorganic polymer flocculants from fly ash according to this utility model.
[0026] The attached diagram is labeled as follows: 1-First channel, 2-Second channel, 3-Third channel, 4-Fourth channel, 5-Inner grinding chamber, 6-Outer grinding chamber, 7-Baffle plate, 8-First nozzle, 9-Second nozzle, 10-Third nozzle. Detailed Implementation
[0027] The preferred embodiments of the present invention will be described in detail below with reference to the accompanying drawings, so as to better understand the purpose, features and advantages of the present invention. It should be understood that the embodiments shown in the drawings are not intended to limit the scope of the present invention, but are only for illustrating the essential spirit of the technical solution of the present invention.
[0028] This utility model provides a reactor for producing inorganic polymeric flocculants from fly ash, specifically as follows: Figure 1 , Figure 2 As shown, the reactor includes a first channel 1, a second channel 2, a third channel 3, a fourth channel 4, an inner grinding chamber 5, and an outer grinding chamber 6. The first channel 1 is a fly ash channel, primarily used for fly ash to enter the inner grinding chamber 5. The second channel 2 is arranged around the outer periphery of the first channel 1 and is an inorganic acid channel, primarily used for inorganic acids to enter the inner grinding chamber 5. The third channel 3 is arranged around the outer periphery of the second channel 2 and is a co-solvent channel, primarily used for co-solvents to enter the inner grinding chamber 5. The co-solvent in the third channel 3 is a mixture of epoxy nonionic surfactant and fluorinated polyacrylamide. The fourth channel 4 is arranged around the outer periphery of the third channel 3 and is a cooling water jacket. The cooling water jacket circulates cooling water to absorb and remove the heat generated by the fly ash, inorganic acid, and co-solvent, thereby maintaining a stable internal temperature of the reactor. The internal grinding chamber 5 is located below the first channel 1, the second channel 2, the third channel 3, and the fourth channel 4. The inlet of the internal grinding chamber 5 is streamlined, which reduces fluid resistance, improves flow efficiency, and helps reduce wear. The outlets of the first channel 1, the second channel 2, and the third channel 3 are connected to the inlet of the internal grinding chamber 5. It is understandable that the outlets of the first channel 1, the second channel 2, and the third channel 3 can also be streamlined. Figure 1 , Figure 2 The example shown is that the outlets of the first channel 1, the second channel 2, and the third channel 3 are designed to be streamlined.
[0029] Furthermore, the first channel 1 has an axial inward reduction of 2-5 mm relative to the second channel 2.
[0030] Furthermore, nozzle assemblies are installed at the outlets of the first channel 1, the second channel 2, and the third channel 3.
[0031] Specifically, refer to Figure 2The nozzle assembly includes a first nozzle 8, a second nozzle 9, and a third nozzle 10. The first nozzle 8 is located at the channel outlet of the first channel 1, the second nozzle 9 is located at the channel outlet of the second channel 2, and the third nozzle 10 is located at the channel outlet of the third channel 3.
[0032] Optionally, the nozzle assembly includes a first nozzle ring tube, a second nozzle ring tube, and a third nozzle ring tube. The second nozzle ring tube is nested within the first nozzle ring tube, and the third nozzle ring tube is nested within the second nozzle ring tube. The first nozzle ring tube is located at the outlet of the third channel 3, the second nozzle ring tube is located at the outlet of the second channel 2, and the third nozzle ring tube is located at the outlet of the first channel 1. The structure of the first, second, and third nozzle ring tubes, by arranging multiple nozzles on a single annular pipe, increases the spray area and improves spray efficiency.
[0033] Alternatively, a venturi nozzle can be used.
[0034] Alternatively, the third nozzle ring tube may have an axial inward reduction of 10-30 mm relative to the second nozzle ring tube.
[0035] Furthermore, an ultra-high pressure air pump is installed at the inlet of the first channel 1. As a pneumatic conveying device, the ultra-high pressure air pump can spray fly ash into the inner grinding chamber 5 through a venturi-shaped nozzle under the condition of nitrogen or air as the carrier gas. When exiting the nozzle, the initial velocity of the fly ash particles exceeds 3-10 times the speed of sound.
[0036] Furthermore, the inner grinding chamber 5 is equipped with multiple layers of baffles 7. While the inner grinding chamber 5 does not contain a mechanical grinding device, it does have multiple layers of impact baffles 7. The high-speed airflow fly ash particles undergo multiple impacts and crushing within the inner grinding chamber. Under the action of inorganic acids and co-solvents, the particles, initially 50-100 micrometers in size, gradually react, disperse, and dissolve into solutions of aluminum salts, iron salts, and silica nanoparticles. This enhances the reaction process and improves the reactivity and leaching rate of valuable metals such as aluminum and iron in the fly ash with inorganic acids.
[0037] Alternatively, the baffle plate 7 may be made of a high-strength metal with a wear-resistant ceramic-based coating.
[0038] Alternatively, the multi-layer baffle 7 can be horizontally arranged inside the inner grinding chamber 5.
[0039] Alternatively, the multi-layer baffles 7 can be inclined within the inner grinding chamber 5. The inclined baffles allow the material to slide down the inclined baffles, thereby accelerating the movement of the material and the grinding process.
[0040] Alternatively, the multi-layer baffles 7 can be arranged in a labyrinthine pattern within the inner grinding chamber 5. The labyrinthine arrangement of the baffles allows the material to achieve a more thorough grinding effect through multiple reversals and collisions.
[0041] Furthermore, by setting the outer grinding chamber 6, the material coming out of the inner grinding chamber can be naturally depressurized.
[0042] Example 1
[0043] In this embodiment, fly ash produced by a pulverized coal boiler in a power plant is used as raw material. Its alumina content is 35%, silicon oxide is 50%, iron oxide is 10%, and the remainder is metal oxides such as calcium oxide, sodium oxide, and potassium oxide.
[0044] Using the reactor designed in this invention, fly ash and nitrogen are pressurized to 20 MPa at the inlet of the first channel by an ultra-high pressure gas pump under a volume ratio of 1:20. The mixture is then conveyed into the first channel (i.e., the high-pressure fly ash channel). After being sprayed by the nozzle assembly at the outlet of the first channel, the fly ash outlet velocity is three times the speed of sound. Simultaneously, 20% hydrochloric acid at three times the mass flow rate of the fly ash is sprayed into the inner grinding chamber 5 through the second channel (i.e., the inorganic acid channel). The co-solvent in the third channel is prepared as a 3% mass-dispersed aqueous solution using an op-10:dodecyl polyacrylamide mass ratio of 10:1, and is then sprayed into the inner grinding chamber through the third channel. Cooling water is then circulated through the fourth channel (i.e., the cooling water channel). The residence time of the material in the inner grinding chamber is controlled to be 2 seconds before entering the outer grinding chamber for depressurization. The aluminum dissolution rate before and after the reaction is 95%.
[0045] Comparative Example 1
[0046] Using the same raw materials and process as in Example 1, under the conditions of a conventional stirred tank reactor, the aluminum dissolution rate before and after the reaction was 32%.
[0047] Example 2
[0048] In this embodiment, fly ash produced by a pulverized coal boiler in a power plant is used as raw material. Its alumina content is 40%, silicon oxide content is 40%, iron oxide content is 8%, and the remainder is metal oxides such as calcium oxide, sodium oxide, and potassium oxide.
[0049] Using the reactor designed in this invention, fly ash and nitrogen are pressurized to 25 MPa at the inlet of the first channel by an ultra-high pressure gas pump under a volume ratio of 1:25, and then transported into the first channel (i.e., the high-pressure fly ash channel). After being sprayed by the nozzle assembly at the outlet of the first channel 1, the fly ash outlet velocity is 3.8 times the speed of sound. Simultaneously, 25% hydrochloric acid at 2.5 times the mass flow rate of fly ash is sprayed into the inner grinding chamber 5 through the second channel (i.e., the inorganic acid channel). The co-solvent in the third channel is prepared as a 1% mass-dispersed aqueous solution of op-10:dodecyl polyacrylamide = 10:1, and then sprayed into the inner grinding chamber through the third channel. Then, cooling water is circulated through the fourth channel (i.e., the cooling water channel). The residence time of the material in the inner grinding chamber is controlled to be 2 seconds before entering the outer grinding chamber for depressurization. The dissolution rate of aluminum element before and after the reaction is 91%.
[0050] Comparative Example 2
[0051] Using the same raw materials and process as in Example 1, under the conditions of a conventional stirred tank reactor, the aluminum dissolution rate before and after the reaction was 45%.
[0052] Example 3
[0053] In this embodiment, fly ash produced by a circulating fluidized bed boiler in a power plant is used as raw material. Its alumina content is 25%, silicon oxide is 52%, iron oxide is 11%, and the remainder is metal oxides such as calcium oxide, sodium oxide, and potassium oxide.
[0054] Using the reactor designed in this invention, fly ash and nitrogen are pressurized to 35 MPa by an ultra-high pressure gas pump at the inlet of the first channel at a volume ratio of 1:35, and then transported into the first channel (i.e., the high-pressure fly ash channel). After being sprayed by the nozzle assembly at the outlet of the first channel 1, the fly ash outlet velocity is 6 times the speed of sound. Simultaneously, 18% hydrochloric acid at 4 times the mass flow rate of fly ash is sprayed into the inner grinding chamber 5 through the second channel (i.e., the inorganic acid channel). The co-solvent in the third channel is prepared as a 3% mass-dispersed aqueous solution of op-10:dodecyl polyacrylamide = 10:1, and then sprayed into the inner grinding chamber through the third channel. Cooling water is then circulated through the fourth channel (i.e., the cooling water channel). The residence time of the material in the inner grinding chamber is controlled to be 2 seconds before entering the outer grinding chamber for depressurization. The dissolution rate of aluminum element before and after the reaction is 98%.
[0055] Comparative Example 3
[0056] Using the same raw materials and process as in Example 1, under the conditions of a conventional stirred tank reactor, the aluminum dissolution rate before and after the reaction was 32%.
[0057] This application uses high-pressure nitrogen or air as the carrier gas. An ultra-high-pressure air pump at the inlet of the first channel transports fly ash to the nozzle assembly at the outlet of the first channel. The fly ash is then injected into the inner grinding chamber at hypersonic speeds under high-speed airflow. The fly ash particles collide violently with the baffles within the inner grinding chamber. Then, inorganic acid from the second channel and co-solvent from the third channel enter the inner grinding chamber and mix with the fly ash. During the mixing process, the fly ash gradually disperses into nanoparticles and reacts with the inorganic acid. The alumina in the fly ash dissolves with the acid to form salts. The reactor designed in this application improves the particle size of the fly ash particles, enhances surface reactivity, strengthens mass transfer, and improves the inorganic acid wetting contact content between the inorganic acid and the inner pores of the mullite camera glass phase in the fly ash, thereby increasing the dissolution rate of valuable elements such as aluminum and iron in the fly ash.
Claims
1. A reactor for the production of inorganic polymer flocculants from fly ash, characterized in that, include; First channel (1); The second channel (2) is arranged around the outer periphery of the first channel (1); The third channel (3) is arranged around the outer periphery of the second channel (2); A fourth channel (4) is arranged around the outer periphery of the third channel (3); The inner grinding chamber (5) is located below the first channel (1), the second channel (2), the third channel (3) and the fourth channel (4), and is connected to the first channel (1), the second channel (2) and the third channel (3); An outer grinding chamber (6) is located below the inner grinding chamber (5) and communicates with the inner grinding chamber (5). An outlet is provided at the bottom of the outer grinding chamber (6).
2. The reactor for producing inorganic polymer flocculants from fly ash according to claim 1, wherein The first channel (1) has an axial inward amount of 2-5 mm relative to the second channel (2).
3. The reactor for producing inorganic polymer flocculants from fly ash according to claim 2, wherein Nozzle assemblies are provided at the outlets of the first channel (1), the second channel (2) and the third channel (3).
4. The reactor for producing inorganic polymer flocculants from fly ash according to claim 3, wherein The nozzle assembly includes a first nozzle (8), a second nozzle (9) and a third nozzle (10). The first nozzle (8) is located at the channel outlet of the first channel (1), the second nozzle (9) is located at the channel outlet of the second channel (2), and the third nozzle (10) is located at the channel outlet of the third channel (3).
5. The reactor for producing inorganic polymeric flocculants from fly ash according to claim 4, characterized in that, The first nozzle (8) has an axial inward amount of 10-30 mm relative to the second nozzle (9).
6. The reactor for producing inorganic polymer flocculants from fly ash according to any one of claims 1 to 5, characterized in that, An ultra-high pressure air pump is installed at the inlet of the first channel (1).
7. A reactor for producing inorganic polymer flocculants from fly ash according to claim 6, characterized in that, The inner grinding cavity (5) is provided with multiple layers of baffles (7).
8. The reactor for producing inorganic polymer flocculants from fly ash according to claim 7, wherein The baffle plate (7) is horizontally arranged inside the inner grinding cavity (5).
9. The reactor for producing inorganic polymer flocculants from fly ash according to claim 7, wherein The baffle plate (7) is inclinedly disposed inside the inner grinding cavity (5).
10. The reactor for producing inorganic polymer flocculants from fly ash according to claim 7, wherein The baffle plate (7) is arranged in a labyrinthine manner inside the inner grinding cavity (5).