Waste water treatment device for semi-coke

Abstract

The application provides a device for treating semi-coke wastewater, which is characterized by the following steps: setting an oil separation tank to separate emulsified oil droplets in the wastewater by demulsification, setting a flocculation tank to flocculate and settle the sedimentable particles in the wastewater to improve the cleanliness of the wastewater, inputting the wastewater into a deacidification and deamination device to remove acid and ammonia, collecting the removed acid and ammonia in an acid gas collecting device and an ammonia gas collecting device respectively for treatment, inputting the wastewater after deacidification and deamination into an extraction device to extract and separate organic phenol, and finally inputting the wastewater after extraction into a biochemical treatment device for biochemical treatment. The device recycles acid, ammonia, organic phenol and other substances in the semi-coke wastewater by the cooperation of the above devices, and overcomes the waste of resources caused by the traditional incineration method for treating semi-coke wastewater.

Description

Technical Field

[0001] This application relates to wastewater treatment technology, and more particularly to a semi-coke wastewater treatment device. Background Technology

[0002] Semi-coke, also known as semi-coke, is a low-volatile solid carbonaceous product obtained by dry distilling non-caking or weakly caking high-volatile bituminous coal under medium and low temperature conditions, after which coal tar and coal gas are released. It possesses excellent characteristics such as high fixed carbon, high resistivity, high reactivity, high calorific value, and extremely low sulfur, aluminum, and phosphorus content. Semi-coke has a wide range of applications, serving as a raw material in industries such as metallurgy, calcium carbide, fertilizer, and activated carbon, and can also be used as a clean fuel in clean production processes.

[0003] Semi-coke wastewater mainly refers to the wastewater generated during the low-temperature (500-700℃) dry distillation of coal. Its main pollutants are phenols, CO2, H2S, ammonia, various fatty acids, and oils, making it a typical highly polluted and toxic industrial wastewater with high COD and ammonia nitrogen levels. The presence of these substances makes its treatment difficult, leading some companies to treat this wastewater through direct incineration. While this method is simple, the oils, phenols, and ammonia nitrogen in the wastewater are important raw materials in organic chemistry and have high utilization value; direct incineration leads to resource waste. Utility Model Content

[0004] This application provides a semi-coke wastewater treatment device to solve the problem of resource waste caused by the existing method of treating semi-coke wastewater by incineration.

[0005] This application provides a semi-coke wastewater treatment device, comprising a raw water tank, an oil separation tank, a flocculation tank, an intermediate water tank, an acid and ammonia removal device, a cooler, an extraction device, and a biochemical treatment device connected in series. The oil separator is also connected to the demulsifier metering pump and the oil separation collection tank, and the flocculation tank is connected to the flocculant metering pump. The acid and ammonia removal unit is also connected to an acid gas collection unit and an ammonia gas collection unit, respectively; The intermediate water tank and the deacidification and deammoniation unit are connected by a transfer pump.

[0006] Optionally, a coalescer is also provided between the flocculation tank and the intermediate water tank, and the coalescer is also connected to the oil collection tank.

[0007] Optionally, the deacidification and deammoniation unit includes a first heat exchanger, a second heat exchanger, and a deacidification tower connected in series. The bottom outlet of the deacidification tower is connected in sequence to the shell side of the second heat exchanger and the deammoniation tower; The bottom outlet of the ammonia removal tower is connected in sequence to the shell side of the first heat exchanger and the tube side of the cooler; The deacidification tower is connected to the acid gas collection device, and the deammoniation tower is connected to the ammonia gas collection device; The deammonia removal tower is also connected to the alkali storage tank.

[0008] Optionally, the extraction apparatus includes an extraction column and a solvent storage tank connected to the extraction column; The extraction tower is also connected to a biochemical treatment unit and a phenol recovery unit, respectively; The phenol recovery unit is also connected to a solvent storage tank.

[0009] Optionally, the acid gas collection device includes a condenser, an absorption tower, and an acid storage tank connected in series. The condenser is also connected to the acid storage tank; The ammonia collection device includes a multi-stage ammonia condenser, an ammonia scrubbing tower, an ammonia crystallization tower, an adsorption tank, an ammonia compressor, and an ammonia storage tank.

[0010] Optionally, the phenol recovery unit includes a phenol distillation column, a phenol cooler, and a crude phenol storage tank; The phenol distillation column is also connected to the solvent storage tank.

[0011] Optionally, the biochemical treatment device includes a wastewater equalization tank, an air flotation tank, a hydrolysis acidification tank, an IMC tank, an A / O tank, a secondary sedimentation tank, an ozone oxidation tank, a sand filter, and a clear water tank connected in series.

[0012] This application provides a semi-coke wastewater treatment device. It employs an oil separation tank to break down and separate emulsified oil droplets in the wastewater, and a flocculation tank to flocculate and settle settleable particles, improving the wastewater's cleanliness. The wastewater is then fed into a deacidification and deammoniation unit for further deacidification and deammoniation. Simultaneously, the released acid and ammonia gases are recovered and treated in separate acid and ammonia collection units. The deacidified and deammonerated wastewater is then fed into an extraction unit for extraction and separation of organic phenols. Finally, the extracted wastewater is fed into a biochemical treatment unit for further biochemical treatment. This device, through the combined use of the above equipment, recovers acids, ammonia, and organic phenols from semi-coke wastewater, overcoming the resource waste caused by traditional incineration methods. Attached Figure Description

[0013] To more clearly illustrate the technical solutions in the embodiments of this application or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0014] Figure 1 This is a schematic diagram of a semi-coke wastewater treatment device provided in an embodiment of this application; Figure 2A schematic diagram of a semi-coke wastewater treatment device provided in another embodiment of this application; Figure 3 This is a schematic diagram of an acid gas collection device provided in an embodiment of this application; Figure 4 This is a schematic diagram of an ammonia collection device provided in one embodiment of this application; Figure 5 This is a schematic diagram of a phenol recovery device provided in one embodiment of this application; Figure 6 This is a schematic diagram of a biochemical treatment apparatus provided in an embodiment of this application.

[0015] Explanation of reference numerals in the attached figures: 1. Raw water tank; 2. Oil separation tank; 3. Flocculation tank; 4. Deacidification and deammoniation unit; 5. Extraction unit; 6. Biochemical treatment unit; 7. Acid gas collection unit; 8. Ammonia gas collection unit; 10. Intermediate water tank; 20. Cooler; 21. Demulsifier metering pump; 22. Oil separation collection tank; 30. Transfer pump; 31. Flocculant metering pump; 32. Coalescer; 41. First heat exchanger; 42. Second heat exchanger; 43. Deacidification tower; 44. Deammoniation tower; 51. Extraction tower; 52. Solvent storage tank; 53. Phenol recovery unit; 61. Wastewater equalization tank; 62. Air flotation tank; 63. Hydrolysis acidification tank; 64. IMC tank; 65. A / O tank; 66. Secondary sedimentation tank; 67. Ozone oxidation tank; 68. Sand filter; 69. Clear water tank; 71. Condenser; 72. Absorption tower; 73. Acid storage tank; 81. Ammonia condenser; 82. Ammonia scrubbing tower; 83. Ammonia crystallization tower; 84. Adsorption tank; 85. Ammonia compressor; 86. Ammonia storage tank; 441. Alkali storage tank; 531. Phenol distillation tower; 532. Phenol cooler; 533. Crude phenol storage tank. Detailed Implementation

[0016] To make the objectives, technical solutions, and advantages of the embodiments of this application clearer, the technical solutions in the embodiments of this application are described clearly and completely below. Obviously, the described embodiments are only some embodiments of this application, not all embodiments. Based on the embodiments in this application, all other embodiments obtained by those skilled in the art without creative effort are also within the scope of protection of this application.

[0017] like Figure 1 As shown, this application provides a semi-coke wastewater treatment device, including a raw water tank 1, an oil separation tank 2, a flocculation tank 3, an intermediate water tank 10, an acid and ammonia removal device 4, a cooler 20, an extraction device 5, and a biochemical treatment device 6 connected in series. Oil separator 2 is also connected to demulsifier metering pump 21 and oil separation collection tank 22 respectively, and flocculation tank 3 is connected to flocculant metering pump 31. The acid and ammonia removal device 4 is also connected to the acid gas collection device 7 and the ammonia gas collection device 8, respectively. The intermediate water tank 10 and the deacidification and deammoniation unit 4 are connected by a transfer pump 30.

[0018] In use, the device of this application transfers the semi-coke wastewater stored in the raw water tank 1 to the oil separation tank 2. A demulsifier (such as a surfactant) is added by the demulsifier metering pump 21 and stirred to break up the emulsified oil droplets in the wastewater. After settling, the oil and water are separated. The separated oil (floating on the liquid surface) is collected in the oil separation collection tank 22, while the water at the bottom is discharged into the flocculation tank 3 through the outlet at the bottom of the oil separation tank 2. A flocculant (such as an aqueous solution of polyacrylamide) is added by the flocculant metering pump 31 to flocculate, adsorbing and settling the fine dust and other solid particles in the wastewater.

[0019] The separated upper wastewater is transferred to the intermediate water tank 10, and then the wastewater is transferred to the deacidification and deammoniation device 4 through the transfer pump 30 for treatment. During the treatment process, the separated acid gas enters the acid gas collection device 7 for treatment and recovery, and the ammonia gas enters the ammonia gas collection device 8 for treatment and recovery.

[0020] The wastewater after deacidification and deammoniation treatment is then fed into cooler 20 to cool down (to about 30°C; multiple coolers 20 can also be connected in series to improve the heat exchange effect). The cooled wastewater is then transferred to extraction device 5 for extraction to extract the organic phenols. The extracted wastewater is then transferred to biochemical treatment device 6 for biochemical treatment and reuse.

[0021] This application provides a semi-coke wastewater treatment device. It employs an oil separation tank 2 to break down and separate emulsified oil droplets in the wastewater, and a flocculation tank 3 to flocculate and settle settleable particulate matter, improving the wastewater's cleanliness. The wastewater is then fed into a deacidification and deammoniation device 4 for deacidification and deammoniation, while the released acid and ammonia gases are recovered and treated in an acid gas collection device 7 and an ammonia gas collection device 8, respectively. The deacidified and deammonerated wastewater is then fed into an extraction device 5 for extraction to separate organic phenols. Finally, the extracted wastewater is fed into a biochemical treatment device 6 for biochemical treatment. This device, through the combined use of the above equipment, recovers acids, ammonia, and organic phenols from semi-coke wastewater, overcoming the resource waste caused by traditional incineration methods.

[0022] like Figure 2 As shown, optionally, a coalescer 32 is also provided between the flocculation tank 3 and the intermediate water tank 10, and the coalescer 32 is also connected to the oil collection tank 22.

[0023] In this application, since the wastewater still contains a small amount of oil droplets, the supernatant of the flocculated wastewater is transferred to the coalescer 32 to further separate the oil droplets from the wastewater, and the separated oil is transferred to the oil collection tank 22 for recovery.

[0024] like Figure 2 As shown, optionally, the deacidification and deammoniation device 4 includes a first heat exchanger 41, a second heat exchanger 42 and a deacidification tower 43 connected in series. The bottom outlet of the deacidification tower 43 is connected in sequence to the shell side of the second heat exchanger 42 and the deammoniation tower 44; The bottom outlet of the ammonia removal tower 44 is connected in sequence to the shell side of the first heat exchanger 41 and the tube side of the cooler 20. The acid removal tower 43 is connected to the acid gas collection device 7, and the ammonia removal tower 44 is connected to the ammonia gas collection device 8; The deammonia removal tower 44 is also connected to the alkali storage tank 441.

[0025] In this application, during use, the wastewater in the intermediate water tank 10 is transferred to the first heat exchanger 41 via the transfer pump 30 and preheated to a first temperature (e.g., 50~60℃), and then enters the second heat exchanger 42 for heat exchange to a second temperature (e.g., 110~120℃). The wastewater obtained after heat exchange in the second heat exchanger 42 is transferred to the deacidification tower 43 for distillation and deacidification (the bottom temperature of the tower is 160~165℃).

[0026] The deacidification wastewater from the bottom of the tower is first transferred to the second heat exchanger 42 for heat exchange and cooling to about 130°C. Then it is transferred to the deammoniation tower 44, where alkaline solution (such as a 5-10% sodium hydroxide aqueous solution) is added through the alkaline solution storage tank 441 to adjust the alkali, so that the ammonium ions are converted into free ammonia molecules for evaporation. During the ammonia evaporation process, the temperature of the bottom of the deammoniation tower 44 is controlled at 130-135°C. Ammonia and vapor are evaporated from the top of the tower and then enter the ammonia collection device 8. The deammoniation wastewater (at about 130°C) output from the bottom of the deammoniation tower 44 enters the first heat exchanger 41 to preheat the wastewater from the intermediate water tank 10. At the same time, the deammoniation wastewater is cooled to about 100°C. Then the cooled deammoniation wastewater is fed into the cooler 20 for further cooling (to about 30°C; multiple coolers 20 can be connected in series to improve the heat exchange effect).

[0027] like Figure 2 As shown, optionally, the extraction apparatus 5 includes an extraction tower 51 and a solvent storage tank 52 connected to the extraction tower 51; Extraction tower 51 is also connected to biochemical treatment unit 6 and phenol recovery unit 53 respectively; The phenol recovery unit 53 is also connected to the solvent storage tank 52.

[0028] In this application, the wastewater cooled by the cooler 20 is transferred to the extraction tower 51 and mixed with the solvent (such as ethyl acetate) in the solvent storage tank 52 to extract the organic phenols. The extracted phenol solution enters the phenol recovery device 53 for processing. After processing by the phenol recovery device 53, the solvent and phenol are separated, and the separated solvent is transferred to the solvent storage tank 52 for recycling.

[0029] like Figure 3 and Figure 4 As shown, optionally, the acid gas collection device 7 includes a condenser 71, an absorption tower 72 and an acid storage tank 73 connected in series. Condenser 71 is also connected to acid storage tank 73; The ammonia collection device 8 includes a multi-stage ammonia condenser 81, an ammonia scrubbing tower 82, an ammonia crystallization tower 83, an adsorption tank 84, an ammonia compressor 85, and an ammonia storage tank 86.

[0030] In this application, during use, the distilled acid gas (vapor mixed with sulfur dioxide) enters the acid gas collection device 7, is cooled and condensed by the condenser 71, and then enters the absorption tower 72 for absorption by clean water. The absorbed acid liquid and the acidic condensate obtained in the condenser 71 are fed together into the acid storage tank 73 for storage.

[0031] In the ammonia collection device 8, the ammonia gas obtained after being condensed by the ammonia condenser 81 is then fed into the ammonia scrubbing tower 82 to remove impurities such as hydrogen sulfide and phenol. It is then further purified by the ammonia crystallization tower 83 and the adsorption tank 84 to obtain clean ammonia gas. The clean ammonia gas is then compressed by the ammonia compressor 85 and fed into the ammonia storage tank 86 for storage.

[0032] like Figure 5 As shown, optionally, the phenol recovery device 53 includes a phenol distillation column 531, a phenol cooler 532, and a crude phenol storage tank 533; The phenol distillation column 531 is also connected to the solvent storage tank 52.

[0033] like Figure 6 As shown, optionally, the biochemical treatment device 6 includes a wastewater equalization tank 61, an air flotation tank 62, a hydrolysis acidification tank 63, an IMC tank 64, an A / O tank 65, a secondary sedimentation tank 66, an ozone oxidation tank 67, a sand filter 68, and a clear water tank 69 connected in series.

[0034] A semi-coke wastewater treatment device, the working process of which is as follows: In operation, the semi-coke wastewater stored in the raw water tank 1 is transferred to the oil separator 2. A demulsifier (such as a surfactant) is added through the demulsifier metering pump 21 and stirred to break up the emulsified oil droplets in the wastewater. After settling, the oil and water are separated. The separated oil (floating on the surface of the liquid) is collected in the oil collection tank 22, while the water at the bottom is discharged into the flocculation tank 3 through the outlet at the bottom of the oil separator 2. A flocculant (such as an aqueous solution of polyacrylamide) is added through the flocculant metering pump 31 to flocculate, adsorbing and settling fine dust and other solid particles in the wastewater. Since the wastewater still contains a small amount of oil droplets, the supernatant of the flocculated wastewater is transferred to the coalescer 32 to further separate the oil droplets from the wastewater. The separated oil is then transferred to the oil collection tank 22 for recovery.

[0035] The separated wastewater is transferred to the intermediate water tank 10, and then transferred to the first heat exchanger 41 via the transfer pump 30 to be preheated to the first temperature (e.g., 50~60℃). It then enters the second heat exchanger 42 to be heated to the second temperature (e.g., 110~120℃). The wastewater obtained after heat exchange in the second heat exchanger 42 is transferred to the deacidification tower 43 for distillation and deacidification (the tower bottom temperature is 160~165℃). The distilled acid gas (vapor mixed with sulfur dioxide) enters the acid gas collection device 7, and after being cooled and condensed by the condenser 71, it enters the absorption tower 72 for absorption with clean water. The acid liquid obtained from absorption and the acidic condensate obtained from condensation in the condenser 71 are fed into the acid storage tank 73 for storage.

[0036] The deacidification wastewater from the bottom of the tower is first transferred to the second heat exchanger 42 for heat exchange and cooling to about 130°C, and then transferred to the deammoniation tower 44. Then, alkaline solution (such as a 5-10% sodium hydroxide aqueous solution) is transferred into the alkaline storage tank 441 to adjust the alkali, so that the ammonium ions are converted into free ammonia molecules for evaporation. During the ammonia evaporation process, the temperature of the bottom of the deammoniation tower 44 is controlled at 130-135°C. Ammonia and vapor are distilled from the top of the tower and enter the ammonia collection device 8. After being condensed by the ammonia condenser 81, the ammonia gas is then fed into the ammonia scrubbing tower 82 to remove impurities such as hydrogen sulfide and phenol. Then, it is further purified by the ammonia crystallization tower 83 and the adsorption tank 84 to obtain clean ammonia gas. The clean ammonia gas is then compressed by the ammonia compressor 85 and fed into the ammonia storage tank 86 for storage. The deammoniation wastewater (around 130°C) output from the bottom of deammoniation tower 44 enters the first heat exchanger 41 to preheat the wastewater from the intermediate water tank 10. Simultaneously, the deammoniation wastewater is cooled to around 100°C. The cooled wastewater is then fed into cooler 20 for further cooling (around 30°C; multiple coolers 20 can be connected in series to improve heat exchange efficiency). The cooled wastewater is then transferred to extraction tower 51, where it is mixed with solvent (e.g., ethyl acetate) in solvent storage tank 52 to extract the organic phenols. The extracted phenol solution enters the phenol recovery unit 53 for further processing. This phenol solution first enters the phenol distillation tower 531 for distillation to recover the solvent, which is then returned to solvent storage tank 52. The crude phenol obtained after distillation is cooled by phenol cooler 532 and then transferred to crude phenol storage tank 533 for storage.

[0037] The wastewater extracted in extraction tower 51 is transferred to biochemical treatment device 6 for biochemical treatment. During treatment, the wastewater is transferred to wastewater equalization tank 61 to be mixed and conditioned with biochemically treatable wastewater from other parts of the factory. The conditioned wastewater is then fed into flotation tank 62 for flotation treatment to remove impurities. The flotation wastewater is then transferred to hydrolysis acidification tank 63 for acidification treatment. The treated wastewater is then transferred to IMC tank 64 and A / O tank 65 for biochemical treatment. The treated wastewater enters secondary sedimentation tank 66 to settle particulate matter generated during biochemical treatment. The supernatant is transferred to ozone oxidation tank 67 for ozone oxidation treatment and sterilization. The treated wastewater is then transferred to sand filter 68 for filtration and then transferred to clear water tank 69 for temporary storage and reuse.

[0038] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this application, and are not intended to limit them. Although this application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of this application.

Claims

1. A semi-coke wastewater treatment device, characterized in that, It includes a raw water tank (1), an oil separation tank (2), a flocculation tank (3), an intermediate water tank (10), a deacidification and deammoniation device (4), a cooler (20), an extraction device (5), and a biochemical treatment device (6) connected in series. The oil separation tank (2) is also connected to the demulsifier metering pump (21) and the oil separation collection tank (22), respectively, and the flocculation tank (3) is connected to the flocculant metering pump (31); The deacidification and deammoniation device (4) is also connected to the acid gas collection device (7) and the ammonia gas collection device (8), respectively; The intermediate water tank (10) and the deacidification and deammoniation device (4) are connected by a transfer pump (30).

2. The semi-coke wastewater treatment device according to claim 1, characterized in that, A coalescer (32) is also provided between the flocculation tank (3) and the intermediate water tank (10), and the coalescer (32) is also connected to the oil collection tank (22).

3. The semi-coke wastewater treatment device according to claim 1, characterized in that, The deacidification and deammoniation device (4) includes a first heat exchanger (41), a second heat exchanger (42), and a deacidification tower (43) connected in series. The bottom outlet of the deacidification tower (43) is connected in sequence to the shell side of the second heat exchanger (42) and the deammoniation tower (44); The bottom outlet of the deammoniation tower (44) is connected in sequence to the shell side of the first heat exchanger (41) and the tube side of the cooler (20); The deacidification tower (43) is connected to the acid gas collection device (7), and the deammonia removal tower (44) is connected to the ammonia gas collection device (8); The deammonia removal tower (44) is also connected to the alkali storage tank (441).

4. The semi-coke wastewater treatment device according to claim 1, characterized in that, The extraction device (5) includes an extraction tower (51) and a solvent storage tank (52) connected to the extraction tower (51). The extraction tower (51) is also connected to the biochemical treatment device (6) and the phenol recovery device (53), respectively; The phenol recovery device (53) is also connected to the solvent storage tank (52).

5. The semi-coke wastewater treatment device according to claim 3, characterized in that, The acid gas collection device (7) includes a condenser (71), an absorption tower (72) and an acid storage tank (73) connected in series. The condenser (71) is also connected to the acid storage tank (73); The ammonia collection device (8) includes a multi-stage ammonia condenser (81), an ammonia scrubbing tower (82), an ammonia crystallization tower (83), an adsorption tank (84), an ammonia compressor (85), and an ammonia storage tank (86).

6. The semi-coke wastewater treatment device according to claim 4, characterized in that, The phenol recovery unit (53) includes a phenol distillation column (531), a phenol cooler (532), and a crude phenol storage tank (533). The phenol distillation column (531) is also connected to the solvent storage tank (52).

7. The semi-coke wastewater treatment device according to any one of claims 1 to 6, characterized in that, The biochemical treatment device (6) includes a wastewater equalization tank (61), an air flotation tank (62), a hydrolysis acidification tank (63), an IMC tank (64), an A / O tank (65), a secondary sedimentation tank (66), an ozone oxidation tank (67), a sand filter (68), and a clear water tank (69) connected in series.

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