Comprehensive treatment system for sulfur-containing waste alkali

Abstract

The invention belongs to the technical field of sulfur-containing wastewater treatment, and provides a comprehensive treatment system for sulfur-containing waste alkali, one side of the waste liquid storage tank is connected with a waste alkali liquid storage tank through a pipeline, an anti-blocking assembly is arranged between the waste liquid storage tank I and the waste alkali liquid storage tank, and the waste alkali liquid storage tank is connected with a preheater through a pipeline; a pressurizing assembly is additionally arranged between the preheater and the waste alkali liquor storage tank, the other side of the preheater is connected with a reactor through a pipeline, the reactor is provided with a cooler connected through a pipeline, one side of the cooler is provided with a gas-liquid separator connected through a pipeline, one side of the gas-liquid separator is connected with a collecting tank through a pipeline, and the other side of the collecting tank is provided with an evaporator. A water treatment tank is arranged on the other side of the evaporator; by designing a double-path treatment mode, the sulfur-containing waste alkali liquid is divided into a high-sulfur type waste alkali liquid and a low-sulfur high-salt type waste alkali liquid, wet oxidation and chemical oxidation pretreatment are adopted respectively, cross interference is avoided, and the treatment effect is improved.

Description

Technical Field

[0001] The invention belongs to the technical field of sulfur-containing wastewater treatment, in particular to a comprehensive treatment system for sulfur-containing waste alkali. Background Art

[0002] Sulfur-containing waste alkali liquor mainly comes from the alkali washing process in industries such as petroleum refining, natural gas purification and coal chemical industry. During the processing, the sulfides in the raw materials (such as hydrogen sulfide, mercaptans, etc.) react with sodium hydroxide solution to produce salts such as sodium sulfide and sodium thiolate, and at the same time, unreacted alkali, oil substances and a small amount of heavy metal ions are mixed in.

[0003] With the rapid development of the petrochemical and refining industries, the discharge of sulfur-containing waste alkali liquor (mainly containing Na2S, NaHS, Na2SO3 and high COD organic matter) has increased sharply year by year. This type of wastewater is highly toxic, strongly corrosive, and easily releases highly toxic H2S gas. If not handled properly, it will cause serious environmental risks.

[0004] The current mainstream treatment technologies mainly use incineration and chemical precipitation.

[0005] However, the incineration method requires high temperatures above 800°C, consumes extremely high energy, and produces secondary pollutants such as SO2 and NOx, requiring a complex exhaust gas purification system.

[0006] Chemical precipitation removes sulfide by adding precipitants such as FeSO4, but the sludge output is large (accounting for 30% to 50% of the wastewater volume), and it cannot degrade COD, resulting in high disposal costs. Summary of the Invention

[0007] In order to solve the above technical problems, the present invention provides a comprehensive treatment system for sulfur-containing waste alkali to solve the problems such as poor treatment effect of sulfur-containing waste alkali in the prior art.

[0008] A comprehensive treatment system for sulfur-containing waste alkali, comprising a waste liquid storage tank 1 for storing high-sulfur waste alkali liquid, wherein one side of the waste liquid storage tank is connected to a waste alkali liquid storage tank via a pipeline, an anti-clogging component for filtering particles is provided between the waste liquid storage tank 1 and the waste alkali liquid storage tank, a preheater is connected to the waste alkali liquid storage tank via a pipeline, a booster component is added between the preheater and the waste alkali liquid storage tank, a reactor is connected to the other side of the preheater via a pipeline, a cooler connected via a pipeline is provided on the reactor, a gas-liquid separator connected via a pipeline is provided on one side of the cooler, a collection tank is connected to the other side of the gas-liquid separator via a pipeline, an evaporator is provided on the other side of the collection tank, and a treated water tank is provided on the other side of the evaporator via a pipeline;

[0009] It also includes a waste liquid storage tank 2 for passing low-sulfur wastewater. The waste liquid storage tank 2 is connected to a chemical oxidation reaction tank through a pipeline. A chemical oxidation component for reacting with the wastewater is provided on the other side of the chemical oxidation reaction tank. The chemical oxidation reaction tank is connected to the treated water tank through a pipeline.

[0010] Preferably, the liquid inlet of the waste liquid storage tank 1 is connected to a delivery pump through a pipeline, the anti-clogging component is located between the delivery pump and the waste liquid storage tank 1, the anti-clogging component includes a primary filter, a secondary filter and a booster pump connected by pipelines, the liquid outlet of the delivery pump is connected to the primary filter, and the primary filter and the secondary filter adopt a basket filtering method.

[0011] Preferably, the liquid outlet of the booster pump is connected to the waste alkali liquid storage tank through a pipeline, the interior of the waste alkali liquid storage tank is divided into an oil removal area and a storage area, the top of the oil removal area is provided with an oil removal tank, the storage area is equipped with a liquid level gauge and an overflow port, and the interior of the waste alkali liquid storage tank is sealed with nitrogen.

[0012] Preferably, the boosting component includes a high-pressure gas storage tank and an air compressor, the external power supply of the air compressor is connected to the high-pressure gas storage tank, the boosting pump is connected to the high-pressure gas storage tank through a pipeline, and the other side of the boosting pump is connected to the liquid outlet of the waste alkali liquid storage tank through a pipeline.

[0013] Preferably, an alkali adding pump is provided before the boosting pump, the alkali adding pump is located between the boosting pump and the waste alkali liquid storage tank, and the other end of the alkali adding pump is connected to the solution tank through a pipeline.

[0014] Preferably, the other side of the reactor is connected to a desuperheater via a pipeline, and the desuperheater has two pipelines, which respectively convey high-pressure steam and high-pressure boiler water into the desuperheater to mix into medium-temperature steam.

[0015] Preferably, the gas-liquid mixture formed by the waste alkali liquid pressurized by the booster pump and the air is heat exchanged with the high-temperature reaction product discharged from the top outlet of the reactor in the preheater to produce an oxidation reaction. The product after the reaction of the reactor is discharged through the top outlet into the preheater. The preheater is heat exchanged with the gas-liquid mixture before the reaction. The cooler is heat exchanged through circulating cooling water, and the logistics are discharged into the gas-liquid separator for gas-liquid separation.

[0016] Preferably, a pipeline mixer connected via a pipeline is provided between the collecting tank and the gas-liquid separator, an acid adding pump connected via a pipeline is further provided on the pipeline mixer, and an acid adding tank is provided at the other end of the acid adding pump.

[0017] Preferably, the liquid inlet of the waste liquid storage tank 2 is also connected to a delivery pump through a pipeline, and the other end of the delivery pump is connected to the chemical oxidation reaction tank through a pipeline. The chemical oxidation component includes a dosing pump and an oxidant storage tank. The chemical oxidation reaction tank is connected to the dosing pump through a pipeline, and the other end of the dosing pump is connected to the oxidant storage tank through a pipeline.

[0018] Compared with the prior art, the present invention has the following beneficial effects:

[0019] 1. The present invention divides the sulfur-containing waste alkali liquor into high-sulfur waste alkali liquor and low-sulfur wastewater. The high-sulfur waste alkali liquor is treated by wet oxidation, and the low-sulfur wastewater is treated by chemical oxidation. The wastewater is separated according to the sulfur content. On the one hand, cross interference can be avoided. Compared with the traditional process that does not distinguish the sulfur content, the use of chemical oxidants can be reduced, thereby improving the treatment effect of the sulfur-containing waste alkali liquor. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] Figure 1 This is a schematic flow chart of the comprehensive treatment system for sulfur-containing waste alkali of the present invention;

[0021] Figure 2 This is a schematic diagram of the structural components of the comprehensive treatment system for sulfur-containing waste alkali according to the present invention.

[0022] In the picture:

[0023] 1. Waste liquid storage tank 1; 2. Waste alkali liquid storage tank; 3. Preheater; 4. Reactor; 5. Cooler; 6. Gas-liquid separator; 7. Collection tank; 8. Evaporator; 9. Process water tank; 10. Waste liquid storage tank 2; 11. Chemical oxidation reaction tank; 12. Transfer pump; 13. Primary filter; 14. Secondary filter; 15. Booster pump; 16. High-pressure gas storage tank; 17. Air compressor; 18. Alkali dosing pump; 19. Solution tank; 20. Desuperheater; 21. Pipeline mixer; 22. Acid dosing pump; 23. Acid dosing tank; 24. Dosing pump; 25. Oxidant storage tank. DETAILED DESCRIPTION

[0024] The following embodiments of the present invention are described in further detail with reference to the accompanying drawings and examples. The following examples are used to illustrate the present invention but are not intended to limit the scope of the present invention.

[0025] As attached Figure 1 To the attached Figure 2 As shown:

[0026] Embodiment 1: The present invention provides a comprehensive treatment system for sulfur-containing waste alkali, comprising a waste liquid storage tank 1 for storing high-sulfur waste alkali liquid, wherein one side of the waste liquid storage tank 1 is connected to a waste alkali liquid storage tank 2 through a pipeline, an anti-clogging component for filtering particles is provided between the waste liquid storage tank 1 and the waste alkali liquid storage tank 2, a preheater 3 is connected to the waste alkali liquid storage tank 2 through a pipeline, a booster component is additionally provided between the preheater 3 and the waste alkali liquid storage tank 2, the other side of the preheater 3 is connected to a reactor 4 through a pipeline, a cooler 5 connected through a pipeline is provided on the reactor 4, a gas-liquid separator 6 connected through a pipeline is provided on one side of the cooler 5, a gas-liquid separator 6 connected through a pipeline is provided on one side of the gas-liquid separator 6, a collecting tank 7 is connected through a pipeline, an evaporator 8 is provided on the other side of the collecting tank 7, and a treated water tank 9 connected through a pipeline is provided on the other side of the evaporator 8;

[0027] It also includes a waste liquid storage tank 2 10 for passing low-sulfur wastewater. The waste liquid storage tank 2 10 is connected to a chemical oxidation reaction tank 11 through a pipeline. A chemical oxidation component for reacting with the wastewater is provided on the other side of the chemical oxidation reaction tank 11. The chemical oxidation reaction tank 11 is connected to the treated water tank 9 through a pipeline.

[0028] It should be noted that by dividing the sulfur-containing waste alkali into high-sulfur waste alkali liquor and low-sulfur wastewater, the high-sulfur waste alkali liquor is treated by wet oxidation, and the low-sulfur wastewater is treated by chemical oxidation, and the wastewater is diverted according to the sulfur content. On the one hand, cross-interference can be avoided. Compared with the traditional process that does not distinguish the sulfur content, the use of chemical oxidants can be reduced, and the treatment effect of the sulfur-containing waste alkali liquor can be improved.

[0029] It should be further explained that the principle of negative pressure evaporation is: at an absolute pressure of 0.15 to 0.30 bar, the wastewater is heated to 55 to 70° C. by water vapor continuously passing through the outer jacket of the evaporator 8 .

[0030] At this time, the wastewater begins to boil and evaporate, and the steam is continuously condensed and recovered. As the evaporation proceeds, the salt in the wastewater eventually crystallizes after reaching saturated solubility. The temperature of the evaporator 8 in the negative pressure evaporation crystallization device is 55-70°C, and the reaction pressure is 0.15-0.30 bar (absolute pressure); the wastewater in the device will boil and vaporize, and the salt in the wastewater will gradually crystallize.

[0031] After the negative pressure evaporation process, the produced water will be mixed with the condensed water and the advanced oxidation produced water, and then discharged into the treated water tank 9, and then pumped from the tank to the outside of the boundary area; the salts produced by the negative pressure evaporation crystallization will be directly transported out for disposal.

[0032] When a small amount of neutralized water passes through the bypass, the outlet water can meet the requirements. If the actual operating load is low and the outlet water requirements can be met without passing through the evaporation crystallization unit, all water flows can also be bypassed.

[0033] In this embodiment, the liquid inlet of the waste liquid storage tank 1 is connected to a delivery pump 12 through a pipeline. The anti-clogging component is located between the delivery pump 12 and the waste liquid storage tank 1. The anti-clogging component includes a primary filter 13, a secondary filter 14 and a booster pump 15 connected by pipelines. The liquid outlet of the delivery pump 12 is connected to the primary filter 13. The primary filter 13 and the secondary filter 14 adopt a basket-type filtering method.

[0034] It should be noted that, by providing the anti-clogging assembly, the primary filter 13 removes impurities larger than 1 mm, and the secondary filter 14 removes impurities larger than 0.5 mm, thereby removing particulate impurities and preventing the booster pump 15 from being clogged.

[0035] In this embodiment, the liquid outlet of the booster pump 15 is connected to the waste alkali liquid storage tank 2 through a pipeline. The interior of the waste alkali liquid storage tank 2 is divided into an oil removal area and a storage area. An oil removal tank is provided at the top of the oil removal area. The storage area is equipped with a liquid level gauge and an overflow port. The interior of the waste alkali liquid storage tank 2 is sealed with nitrogen.

[0036] It should be noted that the waste alkali liquid storage tank 2 is designed to be divided into two areas: an oil removal area and a storage area. The function of the oil removal area is to carry out static sedimentation, impurity separation and oil removal. Specifically, an oil removal tank is provided at the top of the oil removal area. When the oil level rises, the oil will overflow into the oil removal tank and be collected and discharged regularly; the solid impurities collected at the bottom are also discharged regularly.

[0037] The function of the storage area is to temporarily store the waste alkali liquid from which oil and impurities have been removed. The storage area is equipped with a liquid level gauge and an overflow port so that the liquid level in the storage area can be known.

[0038] The waste alkali liquid storage tank 2 is equipped with a nitrogen seal to prevent the risk of H2S leakage in the waste alkali liquid.

[0039] In this embodiment, the boosting component includes a high-pressure gas storage tank 16, a boosting pump 15 and an air compressor 17. The external power supply of the air compressor 17 is connected to the high-pressure gas storage tank 16. The boosting pump 15 is connected to the high-pressure gas storage tank 16 through a pipeline. The other side of the boosting pump 15 is connected to the liquid outlet of the waste alkali liquid storage tank 2 through a pipeline.

[0040] It should be noted that the waste alkali solution is 0.55m 3 / h, is pressurized to 60 bar by the booster pump 15, and then mixed with compressed air from the high-pressure gas storage tank 16.

[0041] The compressed air comes from the air compressor 17, and the compressed air parameters are: pressure 60bar, flow rate 230Nm 3 / h.

[0042] In this embodiment, an alkali adding pump 18 is provided before the boosting pump 15 . The alkali adding pump 18 is located between the boosting pump 15 and the waste alkali solution storage tank 2 . The other end of the alkali adding pump 18 is connected to a solution tank 19 through a pipeline.

[0043] It should be noted that a pipeline is provided before the booster pump 15 for thorough mixing with the sodium hydroxide solution (10 wt% concentration) delivered by the alkali pump 18 to adjust the alkalinity of the waste alkali liquor. Since the NaHS in the waste alkali liquor consumes a certain amount of NaOH during the reaction process (the reaction equation is NaHS + 2O2 + NaOH = Na2SO3 + H2O), calculations show that the amount of NaOH in the waste alkali liquor cannot meet the required consumption. Therefore, NaOH needs to be continuously added to the waste alkali liquor. The amount of sodium hydroxide solution added is adjusted within the range of 7-10 based on the pH value of the WO effluent. This pH range also prevents the generated acidic solution (NaHSO3) from corroding equipment.

[0044] In this embodiment, the other side of the reactor 4 is connected to a desuperheater 20 through a pipeline. The desuperheater 20 has two pipelines, which respectively transport high-pressure steam and high-pressure boiler water into the desuperheater 20 to mix into medium-temperature steam.

[0045] It should be noted that, through the provided desuperheater 20, two pipes are connected to the desuperheater 20, through which high-pressure steam and high-pressure boiler water are introduced respectively. Specifically, at the start of the reaction, high-pressure steam (400°C, 42 bar) and high-pressure boiler water (110°C, 62.5 bar) need to be introduced from outside the boundary area. They are mixed in the desuperheater 20 to become medium-temperature steam (250°C, 40 bar). The medium-temperature steam directly enters the reactor 4 and heats the gas-liquid mixture in the reactor 4 to the required temperature. On the one hand, it avoids local overheating of the reactor 4 due to the direct introduction of 400°C steam, and on the other hand, it provides a suitable temperature for wet oxidation.

[0046] In this embodiment, the gas-liquid mixture formed by the waste alkali liquid pressurized by the booster pump 15 and the air is heat exchanged with the high-temperature reaction product discharged from the top outlet of the reactor 4 in the preheater 3, and an oxidation reaction occurs. The product after the reaction of the reactor 4 is discharged through the top outlet into the preheater 3, and the preheater 3 is heat exchanged with the gas-liquid mixture before the reaction. The cooler 5 performs heat exchange through circulating cooling water, and the logistics is discharged into the gas-liquid separator 6 for gas-liquid separation.

[0047] It should be noted that the gas-liquid mixture formed by the pressurized waste alkali liquid and air is heat-exchanged with the high-temperature reaction product discharged from the top outlet of the reactor 4 in the preheater 3 and is heated to about 178°C.

[0048] The gas-liquid mixture undergoes an oxidation reaction in reactor 4 and releases heat. The main reaction equations are: 2NaHS+2O2->Na2S2O3+H2O (partial oxidation), Na2S+2O2->Na2SO4 (complete oxidation), NaHS+2O2->NaHSO4 (acidic conditions). The operating pressure of reactor 4 is controlled at 60 bar, and the operating temperature is controlled at 200-240°C.

[0049] The product after the reaction is discharged through the outlet at the top of the reactor 4 and enters the preheater 3. In the preheater 3, it exchanges heat with the gas-liquid mixture before the reaction to reduce its temperature to about 100°C. Then, it exchanges heat with the circulating cooling water through the cooler 5 to further reduce its temperature to 55°C. Then, the logistics will be discharged into the gas-liquid separator 6 for gas-liquid separation.

[0050] Since sodium sulfide and sodium hydrosulfide react easily with oxygen, no special catalyst is required. However, in order to make the gas-liquid mixing more uniform (oxygen and liquid mixing more uniformly) and make the reaction more efficient, titanium-based distributed fillers can be filled in the reactor 4.

[0051] After the gas phase is decompressed by the pressure control valve, it is discharged from the top outlet of the gas-liquid separator 6 into the atmosphere 15 meters above the top of the device platform; after the liquid phase passes through the liquid level control valve (which has a decompression function) at the bottom outlet of the gas-liquid separator 6, it is mixed with the sulfuric acid solution from the acid addition tank 23 in the pipeline mixer 21, neutralized to a pH of 6.5-8.5, and then discharged into the collection tank 7.

[0052] The reactor 4 is a vertical pressure vessel with a gas distributor (not shown) at the bottom and a gas-liquid mixture outlet at the top. The reactor 4 can be filled with titanium-based random packing or structured packing to promote gas-liquid mass transfer.

[0053] In this embodiment, a pipeline mixer 21 connected by a pipeline is provided between the collecting tank 7 and the gas-liquid separator 6. The pipeline mixer 21 is also provided with an acid adding pump 22 connected by a pipeline. The other end of the acid adding pump 22 is provided with an acid adding tank 23.

[0054] It should be noted that an inline mixer 21 is installed in front of the storage tank to thoroughly mix the 98 wt% H2SO4 solution delivered by the acid addition pump 22 to adjust the pH of the wet oxidation product effluent. After adjustment, the pH of the wet oxidation product effluent is within the range of 6.5 to 8.5, and the wet oxidation product effluent is then sent to the collection tank 7 for storage.

[0055] In this embodiment, the liquid inlet of the waste liquid storage tank 2 10 is also connected to a delivery pump 12 through a pipeline, and the other end of the delivery pump 12 is connected to the chemical oxidation reaction tank 11 through a pipeline. The chemical oxidation component includes a dosing pump 24 and an oxidant storage tank 25. The chemical oxidation reaction tank 11 is connected to the dosing pump 24 through a pipeline, and the other end of the dosing pump 24 is connected to the oxidant storage tank 25 through a pipeline.

[0056] It should be noted that the wastewater from the waste gas treatment system is directly sent to the waste liquid storage tank 2 10 within the boundary area, and then sent to the chemical oxidation reaction tank 11 through the feed pump.

[0057] At the same time, the liquid oxidant from the oxidant storage tank 25 is also fed into the chemical oxidation reaction tank 11 through the dosing pump 24. The oxidant fully reacts with the wastewater in the chemical oxidation reaction tank 11 at ambient temperature and atmospheric pressure.

[0058] The main reaction equation is: HS-+4H2O2->SO4 2 -+4H2O+H + (H2O2 oxidation), S 2 -+4ClO-+4H + ->SO4 2 -+4Cl-+2H + The liquid oxidant is a conventional industrial liquid reagent such as sodium hypochlorite solution or hydrogen peroxide (30 wt%).

[0059] The main purpose of oxidation is to reduce the COD in the wastewater. The reaction time is about 1 hour. The amount of oxidant added is adjusted according to the COD value in the wastewater. The water produced after the chemical oxidation reaction is directly pumped into the pipeline through the delivery pump 12. After mixing with the water produced by negative pressure evaporation crystallization and cooling water, it will be introduced into the treated water tank 9 and then pumped out of the boundary area.

[0060] The evaporation crystallization process is described in detail.

[0061] Liquid filling process:

[0062] Start the vacuum pump and open the vacuum pump refill valve for 5 seconds. This will evacuate the still through the pipeline. When the pressure reaches -70 kPa, the valve in the equipment's raw water metering tank opens, allowing the raw liquid to enter the tank. The float in the tank rises to the measured high liquid level, and the inlet valve closes.

[0063] The pressure of the still is monitored by a vacuum pressure transmitter, and its liquid level is measured by the raw water metering tank to measure the water inlet, while the recycled water metering tank measures the water outlet.

[0064] Open the waste liquid inlet valve and press the raw liquid into the distillation kettle under negative pressure. When the float drops to the low liquid level, close the waste liquid inlet valve to complete one liquid inlet process. After the set number of liquid inlets is reached, the distillation process should be continued.

[0065] Distillation process:

[0066] After the liquid inlet process is completed, the steam valve opens and steam will enter the heating jacket with a steam pressure of about 1 barg. The vacuum pump will remain in operation, the stirring motor will start, and the stirring shaft will run in a forward and reverse intermittent manner.

[0067] The pressure in the reduced pressure environment is maintained at -80 to -90 kPa, with a boiling point of 40 to 50°C. The evaporated water vapor enters the condenser, where the secondary steam condenses into clean condensate. The condensate enters the recycled water metering tank for internal collection and metering. When the water level reaches the high level float position in the recycled water metering tank, the condensate is discharged.

[0068] Check valves NO-1 and NO-2 will close, the exhaust valve of the recycled water metering tank will open, and the drain valve of the recycled water metering tank will open. The condensed water of the secondary steam will be discharged into the buffer tank by gravity, completing the metering of the primary recycled water. When the water in the buffer tank rises to the high level, the recycled water discharge pump will discharge the water in the buffer tank until the water level reaches the low level, at which point the pump will stop.

[0069] The steam used is converted into steam condensate, which flows through a steam trap into a steam condensate tank. When the water level in the tank reaches the high level, the steam pump starts and continues until the water level drops to the low level. When the distillation reaches the designed time and frequency, the boiling process begins.

[0070] Boiling process:

[0071] The distillation process can be set to a certain number of times, allowing for multiple distillations. Once distillation is complete, raw water is replenished. Boiling is performed only once, during which the water output rate or condensate volume is monitored. Slag discharge can only be performed when the boiling process meets the slag discharge conditions. The specific slag discharge conditions should be adjusted based on actual conditions. Ideally, the majority of the material should be discharged by the slag discharge device within approximately 10 minutes.

[0072] The slag discharge time will be set according to the appropriate time obtained during and after commissioning. If the slag is discharged at a reasonable time setting, the slag discharge is basically normal; at the same time, the operator needs to regularly inspect and check whether the slag discharge is normal.

[0073] No raw liquid is introduced during the boiling process. The concentrated raw water in the still is crystallized and dried to a state suitable for discharge. Specific discharge conditions will be determined during commissioning. During the boiling process, when the liquid level in the recovered water metering tank reaches the highest level within the programmed time (this time will be determined during commissioning), the raw water in the still has completely evaporated and the discharge process begins.

[0074] Slag discharge process:

[0075] Stop the vacuum pump, open the atmospheric balance valve, and raise the system pressure to atmospheric pressure. Open the check valve, the exhaust valve and drain valve of the recycled water metering tank, and the slag discharge drum. Start the agitator motor and rotate the agitator shaft counterclockwise in the discharge direction. When the slag discharge time reaches the set time, stop the agitator shaft and the discharge is complete. Open the steam valve and the slag discharge cleaning valve. When the opening time reaches the set value, close the steam valve. Close the slag discharge drum, and the batch operation is complete.

[0076] Continuous operation mode: After completing a complete batch project, the device automatically enters the next batch operation.

[0077] Batch run detection detects the number of batch runs. When the set number of runs is reached, the device will enter the standby mode set in the control program; if the set number of batch runs is not reached, it will continue to run the next batch.

[0078] other:

[0079] The water ring vacuum pump requires liquid circulation in the buffer tank to achieve vacuum. In order to remove the heat generated by the liquid circulation, a vacuum pump heat exchanger is set up and circulated with cooling water to remove the heat.

[0080] Steam pressure relief valve to prevent steam pressure from being too high. When the equipment is stopped, the jacket steam is vented.

[0081] The evaporator 8 water storage tank cleaning water valve can discharge the cooling water into the distillation kettle cleaning water tank.

[0082] The slag discharge barrel has two states: extended and retracted.

[0083] Whether foam will be generated during the low-temperature distillation of wastewater should be determined based on the wastewater composition and pilot test results. If foam is generated during commissioning and operation, a defoamer line should be installed, the defoamer line valve should be opened, and defoamer should be injected.

[0084] The embodiments of the present invention are provided for the purpose of illustration and description. Although the embodiments of the present invention have been shown and described above, it can be understood that the above embodiments are exemplary and cannot be understood as limitations of the present invention. Ordinary technicians in this field can change, modify, replace and modify the above embodiments within the scope of the present invention.

Claims

1. A comprehensive treatment system for sulfur-containing waste alkali, characterized by: include: A waste liquid storage tank (1) for storing high-sulfur waste alkali liquid is provided. One side of the waste liquid storage tank (1) is connected to a waste alkali liquid storage tank (2) via a pipeline. An anti-clogging component for filtering particles is provided between the waste liquid storage tank (1) and the waste alkali liquid storage tank (2). A preheater (3) is connected to the waste alkali liquid storage tank (2) via a pipeline. A booster component is provided between the preheater (3) and the waste alkali liquid storage tank (2). The other side of the preheater (3) is connected to a reactor (4) via a pipeline. The reactor (4) is provided with a cooler (5) connected via a pipeline. One side of the cooler (5) is provided with a gas-liquid separator (6) connected via a pipeline. One side of the gas-liquid separator (6) is connected to a collecting tank (7) via a pipeline. An evaporator (8) is provided on the other side of the collecting tank (7). A treated water tank (9) is provided on the other side of the evaporator (8). The invention also includes a second waste liquid storage tank (10) for introducing low-sulfur waste water, wherein the second waste liquid storage tank (10) is connected to a chemical oxidation reaction tank (11) via a pipeline, and a chemical oxidation component for reacting with the waste water is provided on the other side of the chemical oxidation reaction tank (11), and the chemical oxidation reaction tank (11) is connected to the treated water tank (9) via a pipeline.

2. The comprehensive treatment system for sulfur-containing waste alkali according to claim 1, wherein: The liquid inlet of the waste liquid storage tank (1) is connected to a delivery pump (12) through a pipeline. The anti-clogging component is located between the delivery pump (12) and the waste liquid storage tank (1). The anti-clogging component includes a primary filter (13), a secondary filter (14) and a booster pump (15) connected through a pipeline. The liquid outlet of the delivery pump (12) is connected to the primary filter (13). The primary filter (13) and the secondary filter (14) adopt a basket-type filtering method.

3. The comprehensive treatment system for sulfur-containing waste alkali according to claim 1, wherein: The liquid outlet of the booster pump (15) is connected to the waste alkali liquid storage tank (2) through a pipeline. The interior of the waste alkali liquid storage tank (2) is divided into an oil removal area and a storage area. The top of the oil removal area is provided with an oil removal tank. The storage area is equipped with a liquid level gauge and an overflow port. The interior of the waste alkali liquid storage tank (2) is sealed with nitrogen.

4. The comprehensive treatment system for sulfur-containing waste alkali according to claim 1, wherein: The boosting assembly comprises a high-pressure gas storage tank (16) and an air compressor (17); the air compressor (17) is connected to the high-pressure gas storage tank (16) via an external power supply; the boosting pump (15) is connected to the high-pressure gas storage tank (16) via a pipeline; and the other side of the boosting pump (15) is connected to the liquid outlet of the waste alkali liquid storage tank (2) via a pipeline.

5. The comprehensive treatment system for sulfur-containing waste alkali according to claim 4, characterized in that: An alkali adding pump (18) is provided before the boosting pump (15). The alkali adding pump (18) is located between the boosting pump (15) and the waste alkali liquid storage tank (2). The other end of the alkali adding pump (18) is connected to a solution tank (19) through a pipeline.

6. The comprehensive treatment system for sulfur-containing waste alkali according to claim 1, characterized in that: The other side of the reactor (4) is connected to a desuperheater (20) via a pipeline. The desuperheater (20) has two pipelines, which respectively transport high-pressure steam and high-pressure boiler water into the desuperheater (20) to mix and form medium-temperature steam.

7. The comprehensive treatment system for sulfur-containing waste alkali according to claim 1, characterized in that: The gas-liquid mixture formed by the waste alkali liquid pressurized by the booster pump (15) and air is heat-exchanged in the preheater (3) with the high-temperature reaction product discharged from the top outlet of the reactor (4). The product after the reaction of the reactor (4) is discharged through the top outlet into the preheater (3). The preheater (3) is heat-exchanged with the gas-liquid mixture before the reaction. The cooler (5) is heat-exchanged by circulating cooling water, and the logistics are discharged into the gas-liquid separator (6) for gas-liquid separation.

8. The comprehensive treatment system for sulfur-containing waste alkali according to claim 7, characterized in that: A pipeline mixer (21) connected via a pipeline is provided between the collecting tank (7) and the gas-liquid separator (6). An acid addition pump (22) connected via a pipeline is also provided on the pipeline mixer (21). An acid addition tank (23) is provided at the other end of the acid addition pump (22).

9. The comprehensive treatment system for sulfur-containing waste alkali according to claim 1, wherein: The liquid inlet of the second waste liquid storage tank (10) is also connected to a delivery pump (12) through a pipeline, and the other end of the delivery pump (12) is connected to the chemical oxidation reaction tank (11) through a pipeline. The chemical oxidation component includes a dosing pump (24) and an oxidant storage tank (25). The chemical oxidation reaction tank (11) is connected to the dosing pump (24) through a pipeline, and the other end of the dosing pump (24) is connected to the oxidant storage tank (25) through a pipeline.

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