A high concentration organic liquid treatment device

Abstract

The invention provides a high-concentration organic liquid treatment device, belonging to the technical field of biomass combustion boilers and equipment thereof, comprising an evaporation reactor, wherein a first feed port of the evaporation reactor is connected to waste liquid, a discharge port of the evaporation reactor is connected to a centrifuge, a water outlet of the centrifuge is connected to a second feed port of the evaporation reactor through a reflux pipe; the evaporation reactor is connected to an incinerator through an organic waste gas pipe, the incinerator is connected to a waste heat boiler through a high-temperature flue gas pipe, the waste heat boiler is connected to a steam inlet of the evaporation reactor through a steam pipe, a condensate outlet of the evaporation reactor is connected to a soft water tank through a water pipe, and the soft water tank is connected to the waste heat boiler; a combined burner is provided on the incinerator, a waste gas nozzle connected to the organic waste gas pipe and a plurality of natural gas nozzles surrounding the waste gas nozzle are provided in the burner, the natural gas nozzle is connected to a natural gas pipe, and a regulating valve is provided on the natural gas pipe.

Description

Technical Field

[0001] This invention relates to the field of biomass combustion boilers and related equipment, and particularly to a high-concentration organic liquid treatment device. Background Technology

[0002] Wastewater containing low-melting-point sodium and potassium salts and with high organic matter content requires treatment. Currently, the main treatment method for high-salt organic liquids on the market is direct incineration. A typical example is the horizontal wastewater incinerator.

[0003] Although the high temperature of the incinerator can destroy toxic and harmful substances in the waste liquid, the waste liquid is directly injected through a two-fluid spray gun. When the low-melting-point salts enter the furnace, they melt at the high temperature of 1100°C. This leads to coking, corrosion of refractory materials, and consequently, a series of problems such as poor system stability, short operating cycle, and high operating and maintenance costs.

[0004] To address this issue, patent application number 2015103402881 discloses a process for treating high-salt, high-concentration organic waste liquid. The process involves continuously evaporating the waste liquid to form a concentrated solution containing toxic and harmful substances. After continuous evaporation, the concentration of the concentrated solution to be incinerated increases, meaning that water is being evaporated. The crystalline salts are then separated using a centrifuge, and a portion of the concentrated solution is sent to an incineration plant for combustion.

[0005] Furthermore, patent application number 2022101415694 discloses a method and apparatus for treating organic waste liquid by incineration. Compared to traditional direct incineration, this method does indeed avoid salt coking. However, it requires continuous evaporation, resulting in low treatment efficiency. Secondly, allowing the concentrated liquid to enter the incineration workshop inevitably leads to incomplete combustion, resulting in poor waste liquid treatment. Summary of the Invention

[0006] The present invention aims to solve the above-mentioned technical problems by providing a high-concentration organic liquid treatment device.

[0007] The technical solution of this invention is a high-concentration organic liquid treatment device, comprising an evaporation reactor. The first inlet of the evaporation reactor is connected to waste liquid, and the outlet of the evaporation reactor is connected to a centrifuge. The outlet of the centrifuge is connected to the second inlet of the evaporation reactor via a return pipe. The evaporation reactor is connected to an incinerator via an organic waste gas pipe. The incinerator is connected to a waste heat boiler via a high-temperature flue gas pipe. The waste heat boiler is connected to the steam inlet of the evaporation reactor via a steam pipe. The condensate outlet of the evaporation reactor is connected to a soft water tank via a water pipe. The soft water tank is connected to the waste heat boiler. The incinerator is equipped with a combined burner. The burner contains a waste gas nozzle connected to the organic waste gas pipe and several natural gas nozzles surrounding the waste gas nozzles. The incinerator is connected to a natural gas pipeline with a regulating valve. Several combustion-supporting pipes are inserted into the furnace from its periphery, and each combustion-supporting pipe is connected to an air inlet pipe with a blower. An organic waste gas pipe is equipped with a flow meter, which has upper and lower limits for comparison. When the flow meter measures a flow rate greater than the upper limit, the regulating valve opens less; when the flow meter measures a flow rate less than the lower limit, the regulating valve opens more. When the regulating valve is at its minimum opening, the natural gas flow rate in the natural gas pipeline is not less than the waste gas flow rate in the organic waste gas pipeline when the flow meter measures a flow rate less than the upper limit. The waste heat boiler is connected to an induced draft fan, and the soft water tank is connected to industrial water.

[0008] In one embodiment, the evaporation reactor is an enamel-lined evaporation reactor.

[0009] In one implementation, the waste heat boiler is a shell-and-tube boiler.

[0010] In one embodiment, the evaporation reactor is equipped with a stirrer.

[0011] In one implementation, a circulation pump is provided on the return pipe.

[0012] In one embodiment, the soft water tank is connected to the waste heat boiler via a gas scrubbing device. The gas scrubbing device includes a detachably connected pipe section. A first filter plate and a second filter plate are provided inside the pipe section. The first filter plate is located near the upper end of the pipe section, and the second filter plate is located near the lower end of the pipe section. A gas scrubbing space is formed between the first filter plate and the second filter plate. A heat-resistant layer is provided in the gas scrubbing space and attached to the inner wall of the pipe section. An inlet branch pipe and an outlet branch pipe are provided on the outer side of the pipe section. Both the inlet branch pipe and the outlet branch pipe are connected to the gas scrubbing space. The inlet branch pipe is also connected to the induced draft fan, and the outlet branch pipe is also connected to a gas collecting tank.

[0013] In one embodiment, the upper end of the pipe section is provided with an upper threaded connection end.

[0014] In one embodiment, the lower end of the pipe section is provided with a threaded connection end.

[0015] In one embodiment, the gas collecting tank is a long cylindrical tank.

[0016] The advantages of this invention compared to existing technologies are that it changes the original method of forming a concentrated liquid through multi-effect evaporation. Instead, it uses positive pressure evaporation in the evaporation reactor, generating an organic mixed gas that enters the incinerator through an organic waste gas pipe. After the waste liquid enters the evaporation reactor, steam generated by a subsequent waste heat boiler is introduced to evaporate the waste liquid, causing the water and organic components in the waste liquid to evaporate and pyrolyze, forming an organic mixed gas. During this process, the waste liquid concentration in the evaporation reactor reaches a certain value, after which it is discharged. After being cooled by a centrifuge, salt crystallization occurs, and under centrifugal force, the wastewater is discharged back into the evaporation reactor through the outlet and return pipe, thus forming the first cycle.

[0017] After combustion in the incinerator, high-temperature flue gas of 750–850°C is generated. This high-temperature flue gas enters the waste heat boiler, where it generates steam. As described above, this steam enters the evaporation reactor to evaporate the waste liquid. Simultaneously, the condensate generated by the heat exchange in the evaporation reactor is recovered through a soft water tank and then fed back to the waste heat boiler, thus forming a second cycle.

[0018] The flow rate of the organic mixed gas through the organic waste gas pipe is detected by a flow meter. As the amount of organic mixed gas increases, the opening of the regulating valve is adjusted to reduce the natural gas supply, thus decreasing the future amount of organic mixed gas. Conversely, as the amount of organic mixed gas decreases, the opening of the regulating valve is adjusted to increase the natural gas supply, thus increasing the future amount of organic mixed gas. Unlike traditional methods that aim to match the amount of organic mixed gas entering the incinerator for complete combustion, this adjustment of the natural gas supply aims to adjust the calorific value of the high-temperature flue gas exiting the high-temperature flue gas pipe. For example, if a large amount of organic mixed gas enters the incinerator, and the calorific value of the high-temperature flue gas produced after complete combustion is sufficient to generate steam for the waste heat boiler, then the natural gas supply is appropriately reduced. Conversely, if a small amount of organic mixed gas enters the incinerator, and the calorific value of the high-temperature flue gas produced is insufficient, then the natural gas supply is appropriately increased, because the temperature generated by the combustion of natural gas is higher than that generated by the combustion of the organic mixed gas. This forms the third cycle.

[0019] This high-concentration organic liquid treatment device forms the above three cycles, enabling the entire system to achieve dynamic balance. This is reflected in the continuous inflow of waste liquid, industrial water, natural gas, and air, and the continuous outflow of crystalline salt and high-temperature flue gas, making it a completely new organic liquid treatment system. Attached Figure Description

[0020] Figure 1 A process system diagram of a high-concentration organic liquid treatment device provided for embodiments of the present invention;

[0021] Figure 2 A partial enlarged view of the burner provided for an embodiment of the present invention;

[0022] Figure 3 A schematic diagram of the air scrubbing device provided in an embodiment of the present invention.

[0023] In the diagram: 1. Evaporation reactor; 2. Centrifuge; 3. Return pipe; 4. Organic waste gas pipe; 5. Incinerator; 6. High-temperature flue gas pipe; 7. Waste heat boiler; 8. Steam pipe; 9. Water pipe; 10. Soft water tank; 11. Burner; 111. Waste gas nozzle; 112. Natural gas nozzle; 12. Regulating valve; 13. Flow meter; 14. Exhaust fan; 15. Natural gas pipe; 16. Combustion aid pipe; 17. Inlet pipe; 18. Blower; 19. Agitator; 20. Circulating pump; 21. Gas scrubbing device; 211. Pipe section; 212. First filter plate; 213. Second filter plate; 214. Gas scrubbing space; 215. Heat-resistant layer; 216. Inlet branch pipe; 217. Outlet branch pipe; 218. Gas collection tank; 219. Upper threaded connection end; 2110. Lower threaded connection end. Detailed Implementation

[0024] The above and other embodiments and advantages of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments.

[0025] In one implementation, such as Figure 1 and Figure 2 As shown.

[0026] The high-concentration organic liquid treatment device provided in this embodiment includes an evaporation reactor 1. The first inlet of the evaporation reactor 1 is connected to waste liquid. The outlet of the evaporation reactor 1 is connected to a centrifuge 2. The outlet of the centrifuge 2 is connected to the second inlet of the evaporation reactor 1 via a return pipe 3. The evaporation reactor 1 is connected to an incinerator 5 via an organic waste gas pipe 4. The incinerator 5 is connected to a waste heat boiler 7 via a high-temperature flue gas pipe 6. The waste heat boiler 7 is connected to the steam inlet of the evaporation reactor 1 via a steam pipe 8. The condensate outlet of the evaporation reactor 1 is connected to a soft water tank 10 via a water pipe 9. The soft water tank 10 is connected to the waste heat boiler 7. The incinerator 5 is equipped with a combined burner 11. The burner 11 contains a waste gas nozzle 111 connected to the organic waste gas pipe 4 and several natural gas nozzles 112 surrounding the waste gas nozzle 111. A natural gas pipe 15 is connected to the incinerator 5, and a regulating valve 12 is installed on the natural gas pipe 15. Several combustion-supporting pipes 16 are inserted into the furnace around the incinerator 5. The combustion-supporting pipes 16 are connected to an air inlet pipe 17, and a blower 18 is installed on the air inlet pipe 17. An organic waste gas pipe 4 is equipped with a flow meter 13, which is configured with an upper limit and a lower limit for comparison. When the flow meter 13 measures that the flow rate in the organic waste gas pipe 4 is greater than the upper limit, the opening of the regulating valve 12 decreases. When the flow meter 13 measures that the flow rate in the organic waste gas pipe 4 is less than the lower limit, the opening of the regulating valve 12 increases. When the regulating valve 12 is at its minimum opening, the natural gas flow rate in the natural gas pipe is not less than the waste gas flow rate in the organic waste gas pipe 4 when the flow meter 13 measures that the flow rate in the organic waste gas pipe 4 reaches the upper limit. A waste heat boiler 7 is connected to an induced draft fan 14, and a soft water tank 10 is connected to industrial water.

[0027] In this embodiment, the high-concentration organic liquid treatment device differs from the original method of forming a concentrated liquid through three evaporations. Instead, the evaporation reactor 1 uses positive pressure evaporation, generating an organic mixed gas that enters the incinerator 5 through the organic waste gas pipe 4. After the waste liquid enters the evaporation reactor 1, steam generated by the subsequent waste heat boiler 7 is introduced to evaporate the waste liquid, causing the water and organic components in the waste liquid to evaporate and pyrolyze, forming an organic mixed gas, i.e., the waste gas. During this process, the concentration of the waste liquid in the evaporation reactor 1 reaches a certain value, and then it is discharged. After being cooled by the centrifuge 2, the salt crystallizes, and under centrifugal force, the wastewater is discharged back into the evaporation reactor 1 through the outlet and the return pipe 3, thus forming the first cycle. Under this cycle, crystallized salt can be continuously generated, and the organic mixed gas can be continuously sent to the incinerator 5 for combustion.

[0028] After combustion in incinerator 5, high-temperature flue gas of 750-850°C is generated. This high-temperature flue gas enters waste heat boiler 7, where it generates steam. This steam, as described above, enters evaporation reactor 1 to evaporate the waste liquid. Simultaneously, the condensate generated by heat exchange in evaporation reactor 1 is recovered through soft water tank 10 and then replenishes waste heat boiler 7, thus forming a second cycle. In this cycle, the high-temperature flue gas after combustion and incineration can be cooled to approximately 200°C before being discharged by induced draft fan 14, providing heat energy to evaporation reactor 1 before cooling. The organic mixture is more easily combusted than the concentrated liquid.

[0029] The flow rate of the organic gas mixture through the organic waste gas pipe 4 is detected by the flow meter 13. As the amount of organic gas mixture increases, the opening of the regulating valve 12 is adjusted to reduce the natural gas supply, thus decreasing the future amount of organic gas mixture. Conversely, as the amount of organic gas mixture decreases, the opening of the regulating valve 12 is adjusted to increase the natural gas supply, thus increasing the future amount of organic gas mixture. It is important to note that a specific limit is placed on the minimum adjustment opening of the regulating valve 12, ensuring that when the regulating valve 12 is at its minimum opening, the natural gas flow rate in the natural gas pipe is not less than the waste gas flow rate in the organic waste gas pipe 4 when the flow meter 13 measures the upper limit. This means that even when the regulating valve 12 is at its minimum opening, the supplied natural gas is sufficient for the complete combustion of the organic gas mixture. Therefore, the adjustment of the natural gas supply, unlike traditional adjustment methods, aims to match the amount of organic gas mixture entering the incinerator 5 to ensure its complete combustion. Instead, the calorific value of the high-temperature flue gas exiting the high-temperature flue gas pipe 6 is adjusted. For example, if a large amount of organic mixed gas enters the incinerator 5, and this organic mixed gas undergoes sufficient combustion, the calorific value of the high-temperature flue gas produced is sufficient to generate steam in the waste heat boiler 7, then the natural gas supply is appropriately reduced. Conversely, if a small amount of organic mixed gas enters the incinerator 5, and the calorific value of the high-temperature flue gas produced is insufficient, then the natural gas supply is appropriately increased, because the temperature generated by the combustion of natural gas is higher than that generated by the combustion of organic mixed gas. This forms the third cycle. The arrangement of the exhaust gas nozzle 111 and the natural gas nozzle 112, as well as the arrangement of the combustion-supporting pipe 16, the air inlet pipe 17, and the blower 18, all contribute to the complete combustion of the organic mixed gas.

[0030] In summary, the high-concentration organic liquid treatment device provided in this embodiment forms three cycles, enabling the entire system to achieve dynamic balance. This is reflected in the continuous inflow of waste liquid, industrial water, natural gas, and air, and the continuous outflow of crystalline salt and high-temperature flue gas, making it a completely new organic liquid treatment system.

[0031] In one embodiment, the evaporation reactor 1 is an enamel-lined evaporation reactor.

[0032] In this embodiment, an enamel-lined evaporation reactor is used. The waste liquid mother liquor first enters the enamel-lined evaporation reactor, and the evaporation temperature is greater than 120°C. Considering that the evaporation and pyrolysis temperatures of organic matter in the waste liquid are currently unclear, the design pressure of the enamel-lined evaporation reactor is 0.5 MPa, and the temperature is 150°C, ensuring that the reaction pressure and temperature of the reactor are adjustable. The evaporation reactor adopts positive pressure evaporation.

[0033] In one embodiment, the waste heat boiler 7 is a shell-and-tube boiler.

[0034] In this embodiment, the flue gas after combustion and incineration enters the tubular waste heat boiler. After sufficient heat exchange, the flue gas generates saturated steam at 1.0 MPa, and the outlet flue gas temperature of the waste heat boiler is approximately 200°C. The high-temperature flue gas at 200°C can be vented into the sewage tank or to other locations via the induced draft fan 14.

[0035] In one embodiment, the evaporation reactor 1 is equipped with a stirrer 19.

[0036] In this embodiment, the stirrer 19 is provided to prevent sediment from settling at the bottom of the evaporation reactor 1.

[0037] In one embodiment, a circulation pump 20 is provided on the return pipe 3.

[0038] In this embodiment, centrifuge 2 is used to filter the waste liquid when the concentration is high, and circulation pump 20 is used to circulate the waste liquid.

[0039] In one implementation, such as Figure 1 and Figure 3 As shown.

[0040] The high-concentration organic liquid treatment device provided in this embodiment has a soft water tank 10 connected to a waste heat boiler 7 via a gas scrubbing device 21. The gas scrubbing device 21 includes a detachably connected pipe section 211. A first filter plate 212 and a second filter plate 213 are provided inside the pipe section 211. The first filter plate 212 is close to the upper end of the pipe section 211, and the second filter plate 213 is close to the lower end of the pipe section 211. A gas scrubbing space 214 is formed between the first filter plate 212 and the second filter plate 213. A heat-resistant layer 215 is provided inside the gas scrubbing space 214 and attached to the inner wall of the pipe section 211. An inlet branch pipe 216 and an outlet branch pipe 217 are provided on the outside of the pipe section 211. Both the inlet branch pipe 216 and the outlet branch pipe 217 are connected to the gas scrubbing space 214. The inlet branch pipe 216 is also connected to an induced draft fan 14, and the outlet branch pipe 217 is also connected to a gas collection tank 218.

[0041] In this embodiment, as mentioned earlier, the 200°C high-temperature flue gas can be introduced into the sewage tank or other locations via the induced draft fan 14. The technical solution adopted in this embodiment is to utilize the scrubbing space 214 of the high-temperature flue gas scrubbing device 21. In this embodiment, the condensate generated by the heat exchange in the evaporation reactor 1 is recovered by the soft water tank 10 and then supplied to the waste heat boiler 7. This low-temperature water directly contacts the high-temperature flue gas, which has already cooled to approximately 200°C, before indirectly contacting the 750-850°C high-temperature flue gas, thus preheating it. The condensate flows downwards within the pipe section 211, while the high-temperature flue gas is discharged upwards within the pipe section 211, ultimately reaching the gas collection tank 218. During the contact between the high-temperature flue gas and the condensate, scrubbing is achieved in addition to heat exchange. Heat exchange refers to the preheating of the condensate. The heat-resistant layer 215 installed within the scrubbing space 214 effectively isolates the high-temperature flue gas from direct contact with the pipe section 211. In the gas scrubbing space 214, the high-temperature flue gas can be cooled again and finally discharged into the gas collecting tank 218. The scrubbed gas is discharged into the gas collecting tank 218, while the scrubbed waste residue remains in the gas scrubbing space 214, which is separated by the first filter plate 212 and the second filter plate 213. The presence of the first filter plate 212 prevents the waste residue from entering the soft water tank 10. The presence of the second filter plate 213 prevents the waste residue from entering the waste heat boiler 7. Finally, when the high-concentration organic liquid treatment device stops operating, the pipe section 211 can be removed to clean its interior, and the gas collecting tank 218 can be opened to discharge the gas stored inside.

[0042] In this embodiment, the high-concentration organic liquid treatment device not only cleverly utilizes washing gas for preheating but also achieves zero emissions. During operation, apart from the production of crystalline salt, there are no other waste gas or waste liquid emissions, greatly enhancing the safety of workshop operations.

[0043] In one embodiment, the upper end of pipe segment 211 is provided with an upper threaded connection end 219. The lower end of pipe segment 211 is provided with a lower threaded connection end 2110.

[0044] In this embodiment, the pipe section 211 is detachably connected via an upper threaded connection end 219 and a lower threaded connection end 2110.

[0045] The specific embodiments described above further illustrate the inventive purpose, technical solution, and beneficial effects of the present invention. It should be understood that the above descriptions are merely specific embodiments of the present invention and are not intended to limit the scope of protection of the present invention. In particular, it should be noted that any modifications, equivalent substitutions, or improvements made by those skilled in the art within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A high-concentration organic liquid treatment device, characterized in that: It comprises an evaporation reactor (1), wherein a first feed port of the evaporation reactor (1) is connected to waste liquid, a discharge port of the evaporation reactor (1) is connected to a centrifuge (2), and a water outlet of the centrifuge (2) is connected to a second feed port of the evaporation reactor (1) via a reflux pipe (3); The evaporation reactor (1) is connected to an incinerator (5) via an organic waste gas pipe (4); the incinerator (5) is connected to a waste heat boiler (7) via a high-temperature flue gas pipe (6); the waste heat boiler (7) is connected to a steam inlet of the evaporation reactor (1) via a steam pipe (8); the condensate outlet of the evaporation reactor (1) is connected to a soft water tank (10) via a water pipe (9); and the soft water tank (10) is connected to the waste heat boiler (7); The incinerator (5) is provided with a combined burner (11), the burner (11) is provided with an exhaust gas nozzle (111) connected to the organic exhaust gas pipe (4) and a plurality of natural gas nozzles (112) surrounding the exhaust gas nozzle (111), the natural gas nozzle (112) is connected to a natural gas pipe (15), the natural gas pipe (15) is provided with a regulating valve (12), the outer periphery of the incinerator (5) is provided with a plurality of combustion-supporting pipes (16) inserted into the incinerator, the combustion-supporting pipes (16) are connected to an air intake pipe (17), the air intake pipe (17) is provided with a blower (18); the organic exhaust gas pipe (4) is provided with A flow meter (13), wherein the flow meter (13) is provided with an upper limit value and a lower limit value for comparison, and when the flow meter (13) measures that the flow rate in the organic waste gas pipe (4) is greater than the upper limit value, the opening of the regulating valve (12) is reduced, and when the flow meter (13) measures that the flow rate in the organic waste gas pipe (4) is less than the lower limit value, the opening of the regulating valve (12) is increased, wherein when the regulating valve (12) is at a minimum adjustment opening, the natural gas flow rate in the natural gas pipe is not less than the waste gas flow rate in the organic waste gas pipe (4) when the flow rate in the organic waste gas pipe (4) measured by the flow meter (13) reaches the upper limit value; The waste heat boiler (7) is connected to an induced draft fan (14), and the soft water tank (10) is connected to industrial water; The soft water tank (10) is connected to the waste heat boiler (7) via a scrubber (21); the scrubber (21) comprises a detachably connected pipe section (211); a first filter plate (212) and a second filter plate (213) are provided in the pipe section (211); the first filter plate (212) is close to the upper end of the pipe section (211); the second filter plate (213) is close to the lower end of the pipe section (211); and a filter element (212) is formed between the first filter plate (212) and the second filter plate (213). An air washing space (214) is formed, wherein a temperature-resistant layer (215) attached to the inner wall of the pipe section (211) is provided in the air washing space (214), and an air inlet branch pipe (216) and an air outlet branch pipe (217) are provided on the outer side of the pipe section (211), wherein the air inlet branch pipe (216) and the air outlet branch pipe (217) are both connected to the air washing space (214), the air inlet branch pipe (216) is also connected to the induced draft fan (14), and the air outlet branch pipe (217) is also connected to an air collecting tank (218).

2. The high-concentration organic liquid treatment device according to claim 1, characterized in that: The evaporation reactor (1) is an enamel evaporation reactor.

3. The high-concentration organic liquid treatment device according to claim 1, characterized in that: The waste heat boiler (7) is a shell and tube boiler.

4. The high-concentration organic liquid treatment device according to claim 1, characterized in that: The evaporation reactor (1) is provided with a stirrer (19).

5. The high-concentration organic liquid treatment device according to claim 1, characterized in that: The reflux pipe (3) is provided with a circulation pump (20).

6. The high-concentration organic liquid treatment device according to claim 1, characterized in that: An upper threaded connection end (219) is provided at the upper end of the pipe section (211).

7. The high-concentration organic liquid treatment device according to claim 1, characterized in that: The lower end of the pipe section (211) is provided with a lower threaded connection end (2110).

8. The high-concentration organic liquid treatment device according to claim 1, characterized in that: The gas collecting tank (218) is a long cylindrical tank.

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