CN212769942U - Treatment system for waste water generated by recycling of dry-process activated coke desulfurization and denitrification rich gas - Google Patents
Treatment system for waste water generated by recycling of dry-process activated coke desulfurization and denitrification rich gas Download PDFInfo
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Abstract
The utility model discloses a processing system of rich gas resource produced waste water of active burnt SOx/NOx control of dry process. The treatment system for the wastewater generated by recycling the dry-method activated coke desulfurization and denitrification rich gas comprises a pretreatment device, an atomization device, an evaporation device and a gas-solid separation device; the pretreatment device is communicated with the evaporation device through the atomization device, and the outlet of the evaporation device is connected with the inlet of the gas-solid separation device; the evaporation device is communicated with a flue gas outlet of a heat exchange tube of the desorption tower in the desulfurization and denitrification of the activated carbon flue gas, and the flue gas flowing into the evaporation device from the flue gas outlet of the heat exchange tube of the desorption tower is used as a heat source of the evaporation device. The utility model discloses effectively utilized the desulfurization waste heat, reduced the use amount of steam and electricity, reduced the running cost, realized the effective recycle of usable resource.
Description
Technical Field
The utility model belongs to the technical field of waste water treatment, concretely relates to processing system of rich gas resourceful produced waste water of active burnt SOx/NOx control of dry process.
Background
With the continuous improvement of the national environmental protection requirement, the control of the atmospheric pollutants represented by sulfur dioxide directly influences the quality of the atmospheric environment of China, and a series of desulfurization waste water can be generated in the current flue gas treatment and the resource recovery of rich gas. Because the desulfurization wastewater has high suspended matter content and fine particles, and contains two pollutants such as copper, zinc, fluoride, sulfide and the like, and heavy metal ions such as cadmium, mercury, chromium, lead, nickel and the like, the desulfurization wastewater has strong pollution to the environment.
The desulfurization wastewater treatment method mainly adopts a chemical precipitation method to remove pollutants in the desulfurization wastewater at present, but the method has high operation cost and limited removal rate of soluble salts such as chlorine salt and heavy metal ions such as selenium, suspended particulate matters, COD (chemical oxygen demand) and the like in effluent can not be stably discharged up to the standard, secondary pollution is easily caused, automatic control is difficult, and the operation result is not ideal. The treatment method has the problems of large floor area, high investment cost, complex process flow, large amount of chemical sludge generation, high energy consumption, incapability of removing chloride ions and the like, and the chloride ions have high corrosivity in a slightly acidic water environment, the treated wastewater cannot be recycled, and the application of the method is limited along with the improvement of environmental protection requirements.
The ultrafiltration reverse osmosis membrane method and the evaporation system are widely concerned by the proposal of the concept of zero discharge of wastewater. The concentrated wastewater produced by ultrafiltration reverse osmosis passes through an evaporation system to produce standard soft water external drainage, and the external drainage can be recycled, but the equipment investment cost is high, the consumed steam amount is large, the investment and operation cost is high, and the overall economy of the wastewater treatment system is poor.
SUMMERY OF THE UTILITY MODEL
The utility model discloses not enough and defect to prior art exists, the utility model aims to provide a processing system of rich gas resourceful produced waste water of active burnt SOx/NOx control of dry process.
At present, the most advanced countercurrent CSCR activated carbon flue gas desulfurization and denitration process in the world is realized by that flue gas is adsorbed and purified by activated carbon and then is discharged after reaching the standard, and the activated carbon adsorbing pollutants is analyzed by an analysis tower and then is recycled. The active carbon adsorbed with the pollutants enters an analytic tower which mainly comprises a heating section and a cooling section and consists of a multi-tube heat exchanger, and the analytic tower is used for removing SO2 and other adsorbed impurities in the active carbon. The activated carbon is heated to 390-450 ℃ in the heating section of the desorption tower, and adsorbed pollutants are released or decomposed, so that the purpose of activated carbon regeneration is achieved, and the adjustment of the heating section is realized by changing the temperature of a heating air inlet entering a heat exchanger. The heater for heating the air is a blast furnace gas burner system. The mixture of blast furnace gas and air is combusted to generate hot gas with the temperature as high as about 500 ℃, the hot gas enters a heat exchange tube, then the heat exchange is carried out on the active carbon in the desorption tower to ensure the complete desorption of the active carbon, SO2 adsorbed by the active carbon is released, and the generated gas rich in SO2 is sent to a salt making working section. The hot gas entering the desorption tower is cooled to 280 ℃ and 320 ℃ after heat exchange, and is discharged through the flue.
In order to obtain salt with higher purity, the rich gas is pre-washed by process water, and then a certain amount of wastewater is discharged periodically, so that the quality of the flue gas is ensured, and the salt precision is improved.
The quality of the wastewater (namely the water quality of the water inlet of the system) produced after the rich gas pre-washing is as follows:
| serial number | Item | Water inflow index |
| 1 | COD(mg/L) | 1200-1500 |
| 2 | Total hardness (mg/L) | 800-1200 |
| 3 | Chloride ion (mg/L) | 20000-40000 |
| 4 | Ammonia nitrogen (mg/L) | 400-600 |
| 5 | Turbidity (NTU) | 700-900 |
| 6 | F- | 100-200 |
| 7 | pH value | 3-4 |
The utility model provides a technical scheme that technical problem adopted as follows:
a treatment system for waste water generated by recycling of dry active coke desulfurization and denitrification rich gas comprises:
the device comprises a pretreatment device, an atomization device, an evaporation device and a gas-solid separation device; the pretreatment device is communicated with the evaporation device through the atomization device, and the outlet of the evaporation device is connected with the inlet of the gas-solid separation device; the evaporation device is communicated with a flue gas outlet of a heat exchange tube of the desorption tower in the desulfurization and denitrification of the activated carbon flue gas, and the flue gas flowing into the evaporation device from the flue gas outlet of the heat exchange tube of the desorption tower is used as a heat source of the evaporation device.
In the above system for treating wastewater generated by recycling rich gas through dry active coke desulfurization and denitrification, as a preferred embodiment, a flue gas circulation unit is arranged between the flue gas outlet of the heat exchange tube of the desorption tower and the flue gas inlet of the evaporation device, and preferably, the flue gas circulation unit is a heat circulation fan.
In the above system for treating wastewater generated by recycling rich gas through dry active coke desulfurization and denitrification, as a preferred embodiment, the pretreatment device comprises a buffer unit, a pH adjusting tank and a two-stage clarification unit along the wastewater flowing direction; and a wastewater inlet of the pH adjusting tank is connected with a wastewater outlet of the buffer unit, and a wastewater outlet of the pH adjusting tank is connected with a wastewater inlet of the two-stage clarification unit.
In the system for treating the wastewater generated by recycling the dry-process activated coke desulfurization and denitrification rich gas, as a preferred embodiment, the two-stage clarification unit comprises a first-stage flocculation reaction tank, a first-stage clarification tank, a second-stage flocculation reaction tank and a second-stage clarification tank which are sequentially connected along the wastewater flowing direction; preferably, the pretreatment device further comprises a filter press unit, more preferably, the filter press unit is a plate-and-frame filter press; further preferably, the bottom sludge outlets of the primary clarification tank and the secondary clarification tank are connected with the inlet of the plate-and-frame filter press, and the water outlet of the plate-and-frame filter press is connected with the water inlet of the primary clarification tank.
In the above system for treating wastewater generated by recycling rich gas in the dry active coke desulfurization and denitrification process, as a preferred embodiment, the atomization device comprises a compressed gas storage unit and an atomization nozzle, wherein the compressed gas storage unit is connected with the atomization nozzle; preferably, the atomizing nozzle is connected with the water outlet of the secondary clarifier.
In the above system for treating wastewater generated by recycling rich gas in dry active coke desulfurization and denitrification, as a preferred embodiment, the atomizing nozzle is disposed in the evaporation device, and preferably, the opening direction of the atomizing nozzle is opposite to the flow direction of flue gas flowing into the evaporation device; preferably, the diameter of the atomizing nozzles is less than 5mm, the number of the atomizing nozzles is multiple, and the distance between two adjacent atomizing nozzles is 0.2m-0.3 m; preferably, the diameter of the atomizing nozzle is 3-5 mm.
In the above system for treating wastewater generated by recycling rich gas in the dry active coke desulfurization and denitrification process, as a preferred embodiment, the evaporation device is a flash mixer.
In the above system for treating wastewater generated by recycling rich gas through dry active coke desulfurization and denitrification, as a preferred embodiment, the gas-solid separation device is a cyclone separator.
Compared with the prior art, the utility model discloses following beneficial effect has:
(1) compared with the prior art, the system adopts the waste heat of the heating section of the desorption tower to evaporate the waste water, so that zero discharge of the desulfurization waste water is realized, the desulfurization waste heat is effectively utilized, the use amount of steam and electricity is reduced, the operation cost is reduced, and effective recycling of available resources is realized.
(2) The waste water evaporation system of this system, equipment is small in quantity, and inner structure is simple, and the mixed back flue gas temperature is high simultaneously, and the system does not scale deposit, not block up, has reduced area, has reduced the investment cost, has reduced the maintenance cost of later stage system simultaneously.
(3) The system realizes zero discharge of the desulfurization wastewater and does not cause secondary pollution. The method has low operation cost.
Drawings
FIG. 1 is a structural diagram of a treatment system for the waste water generated by the recycling of the dry active coke desulfurization and denitrification rich gas of the utility model;
wherein, 1 is the buffer tank, 2 is the pH equalizing basin, 3 is the one-level flocculation reaction, 4 is the one-level depositing reservoir, 5 is the second grade flocculation reaction pond, 6 is the second grade depositing reservoir, 7 is the plate and frame filter press, 8 is the atomizing nozzle, 9 is the compressed gas storage tank, 10 is the flash distillation blender, 11 is analysis tower thermal desorption device, 11-1 is the analysis tower, 11-2 is the hot-blast furnace, 12 is the hot circulating fan, 13 is cyclone.
Detailed Description
In order to highlight the objects, technical solutions and advantages of the present invention, the present invention will be further described with reference to the following embodiments, examples of which are provided by way of illustration rather than limitation of the present invention. The technical solution of the present invention is not limited to the following specific embodiments, but also includes any combination between the specific embodiments.
A method for treating wastewater generated by recycling rich gas through dry-process activated coke desulfurization and denitrification comprises the following steps:
a pretreatment step: pretreating the wastewater to obtain purified wastewater;
atomizing: atomizing the purified wastewater to obtain atomized wastewater;
and (3) an evaporation step: and (3) evaporating the atomized wastewater by using hot flue gas flowing out of a heat exchange tube of an analytic tower in the activated carbon flue gas desulfurization and denitrification to obtain mixed flue gas and solid particles, and then carrying out gas-solid separation on the mixed flue gas and the solid particles.
In the method for treating wastewater generated by recycling rich gas in the dry-process activated coke desulfurization and denitrification process, as a preferred embodiment, in the pretreatment step, the pretreatment specifically comprises the following steps: and adding lime slurry into the wastewater to adjust the pH value of the wastewater, then adding carbonate to react, and then performing precipitation and clarification.
In the method for treating the wastewater generated by recycling the dry-method activated coke desulfurization and denitrification rich gas, as a preferred embodiment, in the pretreatment step, the pH of the wastewater is adjusted to 9-10.
In the method for treating wastewater generated by recycling rich gas in the dry active coke desulfurization and denitrification process, as a preferred embodiment, in the pretreatment step, the carbonate is sodium carbonate.
In the method for treating the wastewater generated by recycling the dry-method activated coke desulfurization and denitrification rich gas, as a preferred embodiment, in the pretreatment step, the precipitation is carried out by adding a flocculating agent and a coagulant aid; preferably, the flocculating and coagulant aids are PAC and PAM.
In the method for treating wastewater generated by recycling rich gas in the dry-process activated coke desulfurization and denitrification process, as a preferred embodiment, in the atomization step, the atomization process specifically comprises: mixing compressed air with the purified wastewater, and then passing through an atomizing nozzle to obtain the atomized wastewater.
In the method for treating wastewater generated by recycling rich gas in the dry active coke desulfurization and denitrification process, as a preferred embodiment, in the atomization step, the atomized wastewater has a droplet diameter of 30 μm to 50 μm.
In the method for treating wastewater generated by recycling rich gas in the dry active coke desulfurization and denitrification process, as a preferred embodiment, in the atomization step, the fog drop velocity of the atomized wastewater is 40-60 m/s.
In the method for treating wastewater generated by recycling rich gas in the dry-method activated coke desulfurization and denitrification process, as a preferred embodiment, in the evaporation step, the temperature of the hot flue gas is 280-320 ℃.
In the method for treating wastewater generated by recycling rich gas through dry active coke desulfurization and denitrification, as a preferred embodiment, in the evaporation step, the hot flue gas and the atomized wastewater are mixed in a counter-current manner to perform evaporation.
In the method for treating wastewater generated by recycling rich gas in the dry-method activated coke desulfurization and denitrification process, as a preferred embodiment, in the evaporation step, the temperature of the mixed flue gas is 120-150 ℃.
A system and a method for treating waste water generated by recycling dry active coke desulfurization and denitrification rich gas,
the treatment system of the waste water generated by recycling the dry active coke desulfurization and denitrification rich gas comprises: the device comprises a pretreatment device, an atomization device, an evaporation device and a gas-solid separation device; the pretreatment device is communicated with the evaporation device through the atomization device, and the outlet of the evaporation device is connected with the inlet of the gas-solid separation device; the evaporation device is connected with a flue gas outlet of a heat exchange tube of the desorption tower in the desulfurization and denitrification of the activated carbon flue gas, and the flue gas flowing into the evaporation device from the flue gas outlet of the heat exchange tube of the desorption tower is used as a heat source of the evaporation device.
As a preferred embodiment, the pretreatment device comprises, in the wastewater flow direction: the device comprises a buffer tank 1, a pH adjusting tank 2, a two-stage clarification unit and a filter pressing unit; preferably, the two-stage clarification unit comprises a first-stage flocculation reaction tank 3, a first-stage clarification tank 4, a second-stage flocculation reaction tank 5 and a second-stage clarification tank 6 which are connected in sequence along the flowing direction of the wastewater; preferably, the filter press unit is a plate and frame filter press 7. The wastewater inlet of the pH adjusting tank 2 is connected with the wastewater outlet of the buffer tank 1, and the wastewater outlet of the pH adjusting tank 2 is connected with the wastewater inlet of the primary flocculation reaction tank 3. The bottom sludge outlet of the first-stage clarification tank 4 and the bottom sludge outlet of the second-stage clarification tank 6 are connected with the inlet of the plate-and-frame filter press 7, and the water outlet of the plate-and-frame filter press 7 is connected with the water inlet of the first-stage clarification tank 4.
The specific process of the wastewater in the pretreatment device is as follows: the wastewater is sent to a buffer tank 1 for water quality and water quantity adjustment, the adjusted wastewater enters a pH adjusting tank 2, the pH of the wastewater is adjusted to 9-10 by adding lime slurry into the pH adjusting tank 2, partial acid radicals and halogen ions of the wastewater are neutralized into corresponding inorganic salt after the pH adjustment, and partial light and heavy metal ions react to generate hydroxide so as to be precipitated. Meanwhile, the alkalescent atmosphere after the neutralization of the wastewater is favorable for further complexing and crystallizing and precipitating heavy metal ions. After the reaction is completed, the wastewater automatically flows to a first-stage flocculation reaction tank 3, sodium carbonate is added into the first-stage flocculation reaction tank 3 to combine the sodium carbonate and calcium and magnesium ions in the wastewater into calcium carbonate and magnesium carbonate, then a flocculating agent and a coagulant aid (PAC and PAM) are added into the first-stage flocculation reaction tank 3 to coagulate small particles such as the calcium carbonate and the magnesium carbonate into large particles, and then the wastewater is subjected to mud-water separation through a first-stage clarifier 4, so that the effect of reducing the hardness is achieved. Meanwhile, the coagulating sedimentation can also remove a part of organic matters. Considering that the solid content of the project is large, the process flow adopts two-stage clarification, the wastewater passing through the primary clarification tank 4 enters the secondary flocculation reaction tank 5, PAC and PAM are added into the secondary flocculation reaction tank 5 to form coagulation flocculation reaction, and the wastewater passing through the coagulation flocculation reaction enters the secondary clarification tank 6 to further remove impurities, so that the clarification of clear liquid is ensured. The sludge at the bottom of the primary clarifier 4 and the secondary clarifier 6 enters a plate-and-frame filter press 7 to form a sludge cake and filtered clear liquid, and the filtered clear liquid automatically flows to the primary clarifier 4. The pretreatment device can ensure that the wastewater is not easy to scale and block when passing through the atomization device, and the system maintenance amount is reduced.
The wastewater passing through the pretreatment unit can reach the following water quality standards:
as a preferred embodiment, the atomizing device includes: a compressed gas storage unit and an atomizing nozzle 8; the compressed gas storage unit is preferably a compressed gas storage tank 9; the compressed gas storage tank 9 is connected with the atomizing nozzle 8; the atomizing nozzle is connected with the water outlet of the secondary clarification tank 6; the diameter of the atomizing nozzles is less than 5mm (such as 2mm, 3mm and 4mm), the number of the atomizing nozzles is multiple (such as 5-10), and the installation distance between adjacent atomizing nozzles is 0.2m-0.3 m. Waste water flowing out of a water outlet of the secondary clarification tank 6 and gas flowing out of a compressed air gas storage tank 9 are mixed and then enter an atomizing nozzle 8, pretreated desulfurization waste water enters the atomizing nozzle after being subjected to high-pressure treatment, the waste water is atomized into fog drops after passing through the atomizing nozzle 8, the diameter range of the fog drops is 30-50 mu m, the speed of the fog drops is 40-60m/s, the fog drops can be rapidly and completely heated and evaporated to dryness, meanwhile, the fog drops are prevented from being enriched on the inner wall of an evaporation device, and the evaporation device is prevented from being corroded and scaled.
As a preferred embodiment, the evaporation device is a flash mixer 10, and the flash mixer 10 of the present invention has a simple structure, low cost and easy processing; preferably, the atomizing nozzles 8 are arranged inside the flash mixer 10, the number of atomizing nozzles depending on the cross-sectional area of the flash mixer; the flue gas inlet of the flash evaporation mixer 10 is connected with the flue gas outlet of the heat exchange tube of the desorption tower. The desorption tower is a desorption tower 11-1 in a desorption tower thermal desorption device 11 used in a countercurrent CSCR activated carbon flue gas desulfurization and denitration process, in the countercurrent CSCR activated carbon flue gas desulfurization and denitration process, flue gas is adsorbed and purified by activated carbon and then is discharged up to the standard, and the activated carbon adsorbed with pollutants is desorbed by the desorption tower and then is recycled. The active carbon adsorbed with the pollutants enters an analytic tower which mainly comprises a heating section and a cooling section and consists of a multi-tube heat exchanger, and the analytic tower is used for removing SO2 and other adsorbed impurities in the active carbon. The activated carbon is heated to 390-450 ℃ in the heating section of the desorption tower, and adsorbed pollutants are released or decomposed, so that the purpose of activated carbon regeneration is achieved, and the adjustment of the heating section is realized by changing the temperature of a heating air inlet entering a heat exchanger. The heater for heating the air is a blast furnace gas burner system, such as a hot blast stove 11-2. The mixture of blast furnace gas and air is combusted in the hot blast stove 11-2, hot gas with the temperature as high as about 500 ℃ is generated and enters the heat exchange tube of the desorption tower 11-1, then the heat exchange is carried out on the active carbon in the desorption tower to ensure that the active carbon is completely desorbed, SO2 adsorbed by the active carbon is released, and the generated gas rich in SO2 is sent to a salt making working section. The temperature of the hot flue gas entering the desorption tower 11-1 is reduced to 280-320 ℃ after heat exchange, and then the hot flue gas flows out of the heat exchange pipe of the desorption tower 11-1 and flows into the flash evaporation mixer 10 through the heat circulation fan 12.
Preferably, the hot flue gas flowing into the flash mixer 10 through the hot circulation fan 12 is mixed with the atomized waste water (mist droplets) in a counter-current manner, so that the contact area can be increased, and the evaporation area can be enlarged. The atomized wastewater and the hot gas with the temperature of 280-320 ℃ which is led out from the desorption tower are fully mixed in the flash evaporation mixer 10, the atomized desulfurization wastewater is evaporated into mixed flue gas and solid particles (which can contain trace water, such as less than 1 wt%), the mixed flue gas and the solid particles formed by evaporation enter a gas-solid separation device, such as a cyclone separator 13, with the flue gas, so as to carry out gas-solid separation, and the main components of the obtained solid particles are calcium sulfate and sodium sulfate. The temperature of the mixed flue gas at the outlet of the flash evaporation mixer is slightly changed according to the difference of water quantity, the temperature range is 120-150 ℃, and the temperature of the flue gas is higher than the acid dew point, so that the corrosion of equipment can not be caused.
Claims (10)
1. The utility model provides a processing system of rich gas resource produced waste water of active burnt SOx/NOx control of dry process which characterized in that includes:
the device comprises a pretreatment device, an atomization device, an evaporation device and a gas-solid separation device; the pretreatment device is communicated with the evaporation device through the atomization device, and the outlet of the evaporation device is connected with the inlet of the gas-solid separation device; the evaporation device is communicated with a flue gas outlet of a heat exchange tube of the desorption tower in the desulfurization and denitrification of the activated carbon flue gas, and the flue gas flowing into the evaporation device from the flue gas outlet of the heat exchange tube of the desorption tower is used as a heat source of the evaporation device.
2. The system for treating the wastewater generated by the resource utilization of the dry activated coke, the desulfurization and the denitrification rich gas as recited in claim 1, wherein a thermal circulating fan is arranged between the flue gas outlet of the heat exchange tube of the desorption tower and the flue gas inlet of the evaporation device.
3. The system for treating the wastewater generated by recycling the rich gas through the desulfurization and denitrification by the dry activated coke as claimed in claim 1, wherein the pretreatment device comprises a buffer unit, a pH adjusting tank and a two-stage clarification unit along the wastewater flowing direction; and a wastewater inlet of the pH adjusting tank is connected with a wastewater outlet of the buffer unit, and a wastewater outlet of the pH adjusting tank is connected with a wastewater inlet of the two-stage clarification unit.
4. The system for treating the wastewater generated by the resource utilization of the rich gas through the desulfurization and denitrification by the dry method activated coke as claimed in claim 3, wherein the two-stage clarification unit comprises a first-stage flocculation reaction tank, a first-stage clarification tank, a second-stage flocculation reaction tank and a second-stage clarification tank which are connected in sequence along the flowing direction of the wastewater.
5. The system for treating wastewater generated by recycling rich gas through desulfurization and denitrification by using dry activated coke as claimed in claim 4, wherein the pretreatment device further comprises a plate-and-frame filter press; the bottom sludge outlets of the primary clarification tank and the secondary clarification tank are connected with the inlet of the plate-and-frame filter press, and the water outlet of the plate-and-frame filter press is connected with the water inlet of the primary clarification tank.
6. The system for treating wastewater generated by recycling of desulfurization and denitrification rich gas by using dry activated coke as claimed in claim 4 or 5, wherein the atomization device comprises a compressed gas storage unit and an atomization nozzle, and the compressed gas storage unit is connected with the atomization nozzle.
7. The system for treating the wastewater generated by recycling the rich gas through the desulfurization and denitrification by the dry activated coke as claimed in claim 6, wherein the atomizing nozzle is connected with a water outlet of the secondary clarifier; the atomizing nozzle is arranged in the evaporation device, and the opening direction of the atomizing nozzle is opposite to the flow direction of the flue gas flowing into the evaporation device.
8. The system for treating wastewater generated by recycling of desulfurization and denitrification rich gas by using dry activated coke as claimed in claim 6, wherein the diameter of the atomizing nozzles is 3-5mm, the number of the atomizing nozzles is multiple, and the distance between two adjacent atomizing nozzles is 0.2-0.3 m.
9. The system for treating wastewater generated by recycling of desulfurization and denitrification rich gas of dry activated coke according to claim 1, wherein the evaporation device is a flash mixer.
10. The system for treating wastewater generated by recycling rich gas through desulfurization and denitrification by using dry activated coke as claimed in claim 1, wherein the gas-solid separation device is a cyclone separator.
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