CN107469597B - Electrochemical-based waste gas and waste water coupling purification system and purification method thereof - Google Patents
Electrochemical-based waste gas and waste water coupling purification system and purification method thereof Download PDFInfo
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- CN107469597B CN107469597B CN201710859882.0A CN201710859882A CN107469597B CN 107469597 B CN107469597 B CN 107469597B CN 201710859882 A CN201710859882 A CN 201710859882A CN 107469597 B CN107469597 B CN 107469597B
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- gas
- electrolytic tank
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- tank
- waste gas
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- 239000002351 wastewater Substances 0.000 title claims abstract description 62
- 238000000746 purification Methods 0.000 title claims abstract description 42
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- 238000010168 coupling process Methods 0.000 title claims abstract description 31
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 21
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Classifications
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- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
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Abstract
The invention discloses an electrochemical-based waste gas and waste water coupling purification system and a purification method thereof. The waste gas and waste water of the existing enterprises are treated independently, so that waste gas/waste water treatment needs waste water/waste gas secondary treatment, environmental protection facilities are repeatedly put into, and the investment and operation and maintenance costs are high. The invention pretreats the waste gas by a photoelectric treatment tower, and then the waste gas is purified and discharged up to the standard by electrochemical coupling of a gas phase oxidation tower and a liquid phase oxidation tower; the wastewater is purified by electrochemical coupling of a liquid-phase oxidation tower and a gas-phase oxidation tower to reach the standard and discharged. The photoelectric treatment tower is an exhaust gas purification technology based on an exhaust gas plasma catalytic system and a photocatalysis system; the gas-phase oxidation tower and the liquid-phase oxidation tower are both waste gas and wastewater electrochemical coupling oxidation-flocculation purification technologies based on Fe-C micro-electrolysis technology and electric-Fenton technology. The invention combines the advantages of Fe-C micro-electrolysis and electric-Fenton, and has low medicament input cost, low power consumption and large market space.
Description
Technical Field
The invention relates to a waste gas and waste water coupling purification method, in particular to a waste gas and waste water coupling purification system based on electrochemistry and a purification method thereof.
Background
Common enterprises have waste gas and waste water such as flue gas, VOCs (volatile organic compounds) and the like, but the waste gas and the waste water are often treated independently; the waste gas/waste water treatment needs waste water/waste gas secondary treatment, the environmental protection facilities are repeatedly input, the investment and operation and maintenance costs are high, and the enterprise burden is heavy. The current exhaust and waste water emission indexes of China are more and more strict, some provinces and cities are marked as local standards or industry standards on the basis of national standards, enterprises are heavy in burden due to failure to find suitable technologies, and environmental protection supervision is high when exceeding standard emission.
Most industries such as textile, wood, paint spraying, printing, shoemaking, slaughtering, medicines, chemical industry and the like have the problem of VOCs emission control; the photoelectric equipment such as photocatalysis, plasma and photocatalysis+plasma combined technology has high power consumption for decomposing VOCs, short service life of a photoelectric system and heavy enterprise burden; the activated carbon adsorption technology can generate a large amount of hazardous waste (waste activated carbon), and the subsequent disposal cost is high; using medicaments (e.g. H 2 O 2 、ClO 2 Etc.), the wet oxidation tower for spray washing has good technical effect, but the cost of the medicament is expensive. The single VOCs technology has poor adaptability, the wet oxidation tower technology integrates photocatalysis and plasma technology, which is a current development trend and makes good progress, but has the secondary troubles of low photocatalysis efficiency, high medicament cost, large sewage treatment facility investment and the like.
The emission indexes of desulfurization and denitration are continuously improved in the flue gas industry of thermal power plants, cement plants, steel plants and the like, and particularly the flue gas deodorization, desulfurization, denitration, dioxin removal and heavy metal removal cost of solid waste (garbage, sludge, hazardous waste and the like) incineration plants is high; the well-established flue gas denitration technologies which are widely used are SCR (selective catalytic reduction) and SNCR (selective non-catalytic reduction) technologies, which are to reduce and treat nitrogen oxides in flue gas by using ammonia gas or substances containing ammonia gas (ammonia water, urea which is decomposed at high temperature to generate ammonia gas, etc.). The typical reaction is as follows:
6NO+4NH 3 →5N 2 +6H 2 O
6NO 2 +8NH 3 →7N 2 +12H 2 O
the service life of the SCR denitration catalyst is generally three years, the deactivated catalyst contains chromium, beryllium, arsenic, mercury and other heavy metals besides vanadium dioxide, vanadium pentoxide and tungsten trioxide, and the deactivated catalyst is incorporated into the national hazardous waste directory (HW 50 spent catalyst: 772-007-50 waste vanadium-titanium catalyst generated in the flue gas denitration process), so that the hazardous waste disposal cost is high. SCR and SNCR flue gas denitration technique all have secondary pollution problems such as ammonia escape.
The waste gas and wastewater treatment of some enterprises adopts an ozone technology, so that secondary pollution problems such as ozone escape and the like are easily caused, no good solution is available at present, and upgrading and transformation are urgently needed.
Disclosure of Invention
The invention aims at:
(1) Waste gas and waste water of enterprises are treated independently, waste water and waste gas are treated secondarily, environmental protection facilities are repeatedly input, investment and operation and maintenance costs are high, and the enterprises are heavy in burden.
(2) The operation cost of the photoelectric catalysis facilities such as plasma, photocatalysis and the like is high, the efficiency is low, and the sewage treatment facilities are imperfect; the wet oxidation tower spray washing technology is adopted, so that the cost of the agent is high.
(3) The SCR and SNCR flue gas denitration technology of enterprises inevitably has the problems of secondary pollution and the like caused by ammonia escape in use; the applicable temperature of the V-Ti series catalyst for SCR denitration is 350 ℃, the energy consumption is huge, the device is difficult to miniaturize, and the deactivated catalyst is dangerous waste; although the SNCR denitration does not use a catalyst, the applicable temperature is 800-900 ℃, the energy consumption is high, the efficiency is low, and the environmental emission standard is often not met.
(4) Many provinces in China have begun to prevent ammonia and ozone escape problems of waste gas and wastewater treatment, and even limit the limit of time to ban the ozone oxidation technology.
Therefore, the invention provides an electrochemical-based waste gas and wastewater coupling purification system and a purification method thereof, wherein waste gas is pretreated by a photoelectric treatment tower and is purified to reach the emission standard by electrochemical coupling of a gas phase oxidation tower and a liquid phase oxidation tower; the wastewater is purified by electrochemical coupling of a liquid-phase oxidation tower and a gas-phase oxidation tower to reach the standard and discharged. The photoelectric treatment tower is an exhaust gas purification technology based on an exhaust gas plasma catalysis module and a photocatalysis module; the gas-phase oxidation tower and the liquid-phase oxidation tower are both waste gas and waste water electrochemical coupling oxidation-flocculation purification technologies based on Fe-C micro-electrolysis technology and electro-Fenton technology. The waste gas and waste water coupling purification method combines the advantages of Fe-C micro electrolysis and electric-Fenton, and has the advantages of low medicament input cost, low power consumption and large market space.
The invention discloses an electrochemical-based waste gas and wastewater coupling purification system which comprises a photoelectric treatment tower, a gas phase oxidation tower, a liquid phase oxidation tower, a gas-fall fan and a spray water pump. The photoelectric treatment tower comprises a plasma catalysis module arranged at the front and a photocatalysis module arranged at the rear; the plasma catalysis module comprises a multistage plasma generator and a plasma catalysis net which are alternately arranged; the photocatalysis module comprises a plurality of stages of ultraviolet lamp tubes and ultraviolet catalytic nets which are alternately arranged. The gas-phase oxidation tower comprises a gas collection box, a first electrolytic tank, a second electrolytic tank, a first filter layer, a second filter layer and a spray pipe; the first electrolytic tank consists of a grating plate, micro-electrolysis filler arranged on the grating plate and a first electrode group buried in the micro-electrolysis filler; the second electrolytic tank is composed of a grating plate, micro-electrolysis filler arranged on the grating plate and a second electrode group buried in the micro-electrolysis filler. The gas collecting header is divided into a first tank chamber, a second tank chamber and a third tank chamber, wherein the first tank chamber is communicated with the second tank chamber only at the top, and the second tank chamber is communicated with the third tank chamber only at the bottom; the first box chamber is divided into an upper part and a lower part by a grid plate of the first electrolytic tank, and the second box chamber is divided into an upper part and a lower part by a grid plate of the second electrolytic tank; the first filter layer and the second filter layer are arranged in the third box at intervals up and down. The liquid phase oxidation tower comprises a third electrolytic tank, a fourth electrolytic tank and a waterfall pipe; the third electrolytic cell is provided with a third electrode group; the fourth electrolytic cell is provided with a fourth electrode group and a reference electrode.
The outlet of the photoelectric treatment tower is communicated with a first port at the bottom of the first box chamber through a smoke pipeline; the air inlet of the air-fall fan is communicated with the first-interface smoke pipeline of the first box chamber by a smoke pipeline, and the air outlet is communicated with the twelve-interface of the third electrolytic tank and communicated with the air-fall pipeline. The spray water pump is communicated with a thirteenth interface of a third electrolytic tank and a sixth interface of the gas-phase oxidation tower through a water pipeline and is communicated with a spray pipe. The fifth interface at the top of the third box is a purified gas discharge port.
The third interface at the bottom of the first box chamber is a water outlet which is communicated with the tenth interface of the third electrolytic tank through a water pipeline; the third electrolytic tank and the fourth electrolytic tank are communicated with a second interface of the first box chamber by an air pipeline by taking an eleventh interface as an air outlet; the water outlet of the fourth interface at the bottom of the second box chamber is communicated with the eighth interface of the third electrolytic tank and the seventh interface of the fourth electrolytic tank through water pipelines respectively; the ninth interface of the third electrolytic tank is a wastewater inlet; the fourteen interfaces at the bottom of the fourth electrolytic tank are purified water discharge ports.
The plasma catalytic net is a double-layer wire net, and is internally filled with TiO 2 Platinum-based catalysts (e.g. Pt/Al 2 O 3 ) Proton zeolite, Y zeolite, naX zeolite, naY zeolite, laCoO 3 、Ag/CeO 2 、MnO 2 And gamma-Al 2 O 3 One or a combination of several catalysts.
The ultraviolet catalytic net is a double-layer wire net, and is internally filled with TiO 2 And a catalyst prepared from a mixture of activated carbon and iron oxide.
The micro-electrolysis filler is iron-carbon alloy (cast iron filings are more used), or inert carbon (such as graphite, coke, active carbon, coal and the like) particles are added into the cast iron filings.
The first electrode group and the second electrode group are made of iron plates or stainless steel plates; the anodes of the third electrode group and the fourth electrode group are DSA anodes, and the cathode is one of platinum, cu-Zn alloy or Ti; the reference electrode is a silver chloride electrode or a calomel electrode.
Each electrode group is connected with a corresponding wiring terminal of the direct current power supply, and the distance between the electrode plates of each electrode group is 1-10 cm; the voltage of the direct current power supply is 0-20V.
When the amount of wastewater is large, a small amount of micro-electrolysis filler is also added into the third electrolytic tank and the fourth electrolytic tank, so that coupling and electrochemical promotion are realizedAt the same time of chemical reaction, also serves as Fe 2+ Ion loss replenishment. The liquid phase oxidation tower adopts an electrochemical catalytic system and a high-grade oxidation technology, adopts a DSA anode to realize high electrocatalytic performance, and generates OH and HO with extremely strong oxidizing ability in the process of electrolysis of wastewater 2 Free radical, high-efficiency oxidative degradation of organic pollutants, and no toxic intermediate products.
The purifying gas discharge port is provided with a detector for monitoring concentration of SOx, NOx and VOCs, and the detector controls start and stop, voltage and frequency of the plasma generator through the concentration of the SOx, NOx and VOCs which are fed back, controls start and stop of the ultraviolet lamp tube, controls start and stop of the first electrode group and the second electrode group, voltage and current (the waste gas is controlled to reach standards), and controls start and stop of the third electrode group and the fourth electrode group, voltage and current (the waste water is controlled to reach standards).
The invention discloses an electrochemical-based waste gas and waste water coupling purification method, which comprises the following steps: the waste gas is led into a photoelectric treatment tower, is decomposed and oxidized by a plasma catalytic module formed by a multistage plasma generator and a plasma catalytic net, is partially purified, is led into a photocatalysis module formed by a multistage ultraviolet lamp tube and an ultraviolet catalytic net, is purified again, enters a gas-phase oxidation tower along a part of a flue gas pipeline through a first interface for purification, and is led into a twelve-number interface of a liquid-phase oxidation tower along the flue gas pipeline through a gas-fall fan and is communicated with a gas-fall pipe for serving as gas fall.
In the gas-phase oxidation tower, the gas collecting header is divided into a first tank chamber, a second tank chamber and a third tank chamber, wherein the first tank chamber is communicated with the second tank chamber only at the top, and the second tank chamber is communicated with the third tank chamber only at the bottom; the first box chamber and the second box chamber are both divided into an upper part and a lower part by the grid plate; the first filter layer and the second filter layer are arranged in the third box at intervals up and down. The waste gas introduced into the gas-phase oxidation tower enters the first electrolytic tank through the grid plate after being homogenized by the gas collecting box, and spray pipe spray water is arranged above micro-electrolysis fillers in the first electrolytic tank and the second electrolytic tank. The spray water is from the third electrolytic tank, is pressurized and conveyed to the sixth interface of the gas-phase oxidation tower through a water pipeline by a spray water pump through a thirteenth interface and is communicated with a spray pipe. Waste gas is purified by the first electrolytic tank and then enters the top of the gas collection box, gas is homogenized and then enters the second electrolytic tank and then enters the bottom of the second box chamber of the gas collection box, and organic matters left by the photoelectric treatment tower are decomposed and purified through the combined action of the first electrolytic tank and the electrochemical coupling oxidation-flocculation reaction of the second electrolytic tank based on Fe-C micro electrolysis and electric-Fenton reaction and spray water with active groups from the third electrolytic tank. And the gas after the bottom of the second chamber of the gas collection header is uniformly mixed enters a first filter layer and a second filter layer to remove water mist, and the purified gas is discharged out of a fifth interface to finish the purification of the waste gas to reach the emission standard.
And (3) delivering the wastewater into a third electrolytic tank of the liquid phase oxidation tower from a ninth interface. The spray water of the first electrolytic tank flows out of the third interface and flows into the third electrolytic tank through the tenth interface, part of the spray water of the second electrolytic tank flows out of the fourth interface and flows into the third electrolytic tank through the eighth interface, and the other part of the spray water flows into the fourth electrolytic tank through the seventh interface; the third electrolytic tank is internally provided with a third electrode group, and the bottoms of the third electrolytic tank and the fourth electrolytic tank are provided with a waterfall pipe twelve-number connection port which is communicated with an outlet of a waterfall fan. The waste gas after the aeration of the third electrolytic tank and the fourth electrolytic tank reaches the second interface through the eleventh interface and enters the bottom of the first chamber of the gas collecting box through the flue gas pipeline, and is purified by the gas phase oxidation tower. After the third electrode group is electrified, the wastewater in the third electrolytic tank and iron ions in spray water of the gas phase oxidation tower are subjected to electrochemical coupling oxidation-flocculation reaction, and generated part of OH and H are subjected to electrochemical coupling oxidation-flocculation reaction 2 O 2 Flows out through the thirteen-th interface, is pressurized by a spray water pump along a water pipeline, is sent to a gas-phase oxidation tower to be used as spray water, is subjected to electrochemical coupling oxidation-flocculation reaction based on Fe-C micro-electrolysis and electric-Fenton reaction again, one part of the spray water returns to the third electrolytic tank of the liquid-phase oxidation tower to be continuously oxidized and decomposed, and the other part of the spray water is sent to the fourth electrolytic tank to be oxidized. The fourth electrolytic tank is provided with a fourth electrode group and a reference electrode, wherein the fourth electrode group is a working electrode group. And the spray water flowing into the fourth electrolytic tank through the seventh interface is subjected to potential difference of the reference electrode to judge the purification degree, and the purified water is discharged out of the fourteen interfaces to finish the purification of the wastewater to reach the discharge standard.
Compared with the prior art, the invention has the following beneficial effects:
(1) The invention integrates waste gas and waste water treatment into the same system, and plays an effect of increasing treatment stages when waste gas and waste water are purified in a coupling way, for example, waste water is purified in a liquid phase space and a gas phase space; the waste gas is purified not only in the gas phase space but also in the liquid phase space; the synergistic treatment effect is good, and the investment operation cost is low.
(2) The photoelectric treatment tower breaks through the bottleneck of low efficiency of traditional plasmas and photocatalysis, a plasma catalytic net is arranged at the rear section of the plasmas, and a catalyst is pertinently adjusted according to the components of inlet waste gas to form an efficient plasma catalytic module; an ultraviolet catalytic net is arranged at the rear section of the photocatalysis, and the catalyst is pertinently adjusted according to the components of the inlet waste gas to form an efficient plasma catalytic module. Under the same power consumption, the photoelectric treatment tower has higher efficiency.
(3) The photoelectric treatment tower is only used as a waste gas pretreatment means, and is combined with continuous purification of a multistage electrochemical coupling oxidation-flocculation technology of a gas phase oxidation tower and a liquid phase oxidation tower with lower subsequent power consumption, so that the energy-saving effect is remarkable.
(4) The gas phase oxidation tower integrates the synergistic effect of Fe-C micro-electrolysis technology, electric-Fenton technology, wet oxidation spray washing technology of spray water with active groups and the like, and the waste gas such as VOCs, NOx and the like is thoroughly purified; monitoring SOx, NOx and VOCs concentration of an exhaust port in real time, and controlling gas-phase electrochemical start-stop and voltage and frequency regulation conditions; the emission index of the purified gas is far lower than the industry standard, and the photoelectric treatment tower is verified to be a pretreatment link of the invention.
(5) The liquid phase oxidation tower supplies Fe ions by means of the Fe-C micro-electrolysis reaction backwater water of the gas phase oxidation tower, and forms an electric-Fenton reaction with the electrode group to generate H 2 O 2 No more medicament is added into the system; under the action of aeration, can promote H 2 O 2 The OH reactive groups rapidly decompose pollutants in the exhaust gas and wastewater; the discharge of the purified water is controlled by a fourth electrolytic tank, the change of the oxidation-reduction potential of the sewage is monitored in real time through a reference electrode, and the electrochemical start-stop and voltage and frequency regulation conditions of a liquid phase are controlled; purified water outletThe water quality is stable in emission and strong in impact resistance under working conditions, and the treated water quality meets the integrated wastewater emission standard and industry and local standards, such as 10mg/L of Suspended Substances (SS), 10mg/L of chemical oxygen demand (BOD 5) on five days, 50mg/L of chemical oxygen demand (CODcr), 5mg/L of ammonia nitrogen (calculated by total N) and 0.5mg/L of total phosphorus.
(6) The invention directly decomposes pollutants in waste gas and waste water into environmentally harmless substances such as sulfate, chloride and CO 2 And N 2 And the like, products such as ammonium nitrate, ammonium sulfate, ammonium bicarbonate and the like are not formed, the system is simple and reliable, and the manufacturing cost is low; the nitrate wastewater discharge problem of conventional plasma, wet and dry denitration is effectively solved.
(7) The Fe-C micro-electrolysis filler, the electrode group and the like used in the invention are all commonly supplied products in the market.
(8) The liquid phase electrolytic tank adopts the DSA anode, has small sludge amount, saves energy consumption, reduces pollution, reduces cost and effectively treats industrial wastewater, and meets the requirement of the current clean production.
(9) Waste gas and waste water treatment projects, in particular to technical improvement standard lifting projects, are limited in places, purification facilities are required to be arranged above roads in an overhead mode, and a photoelectric treatment tower, a gas phase oxidation tower and a liquid phase oxidation tower all adopt horizontal reactors and have unique market affinities.
(10) The photoelectric treatment tower, the gas phase oxidation tower and the liquid phase oxidation tower have low requirements on environmental conditions, and the problems of secondary environmental pollution such as ammonia escape, ozone escape and the like are avoided.
(11) The multi-layer Fe-C micro-electrolysis filler of the gas-phase oxidation tower, the washing of spray water, the repeated collection and deflection of air flow and the electrode capturing function of the filler layer have a good filtering effect on particulate matters in waste gas, and the dust reaches ultra-low emission.
Drawings
Fig. 1 is a schematic diagram of the system architecture of the present invention.
In the figure: 1. the device comprises an optoelectronic treatment tower, 2, a plasma catalytic net, 3, a plasma generator, 4, an ultraviolet lamp tube, 5, an ultraviolet catalytic net, 6, a first interface, 7, an electrolytic tank, 8, a gas phase oxidation tower, 9, a spray pipe, 10, a first electrode group, 11, a sixth interface, 12, a second electrolytic tank, 13, a second electrode group, 14, a fifth interface, 15, a second filter layer, 16, a first filter layer, 17, a fourth interface, 18, a third interface, 19, a second interface, 20, a liquid phase oxidation tower, 21, a twelve interface, 22, a waterfall fan, 23, a spray water pump, 24, a thirteen interface, 25, a third electrode group, 26, a third electrolytic tank, 27, a waterfall pipe, 28, a fourteen interface, 29, a fourth electrode group, 30, a reference electrode, 31, a fourth electrolytic tank, 32, a seventh interface, 33, a eighth interface, 34, a ninth interface, 35, a tenth interface, 36 and an eleventh interface.
Detailed Description
The invention is further described below with reference to the accompanying drawings.
As shown in fig. 1, an electrochemical-based waste gas and wastewater coupling purification system comprises a photoelectric treatment tower 1, a gas phase oxidation tower 8, a liquid phase oxidation tower 20, a gas-fall fan 22 and a spray water pump 23. The photoelectric treatment tower 1 comprises a plasma generator 3, a plasma catalysis net 2, an ultraviolet lamp tube 4 and an ultraviolet catalysis net 5. The gas-phase oxidation tower 8 comprises a gas collecting box, a first electrolytic tank 7, a second electrolytic tank 12, a first filter layer 16, a second filter layer 15 and a spray pipe 9; the first electrolytic tank 7 consists of a grating plate, micro-electrolysis filler arranged on the grating plate and a first electrode group 10 buried in the micro-electrolysis filler; the second electrolytic cell 12 is composed of a grid plate, a micro-electrolytic filler provided on the grid plate, and a second electrode group 13 buried in the micro-electrolytic filler. The liquid-phase oxidation tower 20 comprises a third electrolytic tank 26, a fourth electrolytic tank 31 and a waterfall pipe 27; the third electrolytic tank 26 is provided with a third electrode group 25; the fourth electrolytic cell 31 is provided with a fourth electrode group 29 and a reference electrode 30. The current density of each electrolytic tank is 0-250 mA/cm 2 (set point 50 mA/cm) 2 )。
As shown in fig. 1, an electrochemical-based waste gas and wastewater coupling purification method specifically comprises the following steps:
waste gas (VOCs, flue gas and the like) of enterprises is introduced into a photoelectric treatment tower 1, is decomposed and oxidized by a plasma catalytic module formed by a multistage plasma generator 3 and a plasma catalytic net 2 (the plasma generator 3 is arranged in front of the plasma catalytic net), is partially purified, is then introduced into a photocatalysis module formed by a multistage ultraviolet catalytic net 5 and an ultraviolet lamp tube 4 (the ultraviolet catalytic net 5 is arranged in front of the ultraviolet lamp tube 4), is purified again, enters a gas phase oxidation tower 8 from a first interface 6 along a flue gas pipeline to be finally purified, and is introduced into a twelve-number interface 21 of a liquid phase oxidation tower 20 along the flue gas pipeline through a waterfall fan 22 and is communicated with a waterfall pipe 27 to be used as waterfall.
The gas collecting header is divided into a first tank chamber, a second tank chamber and a third tank chamber, wherein the first tank chamber is communicated with the second tank chamber only at the top, and the second tank chamber is communicated with the third tank chamber only at the bottom; the first box chamber and the second box chamber are both divided into an upper part and a lower part by the grid plate; the first interface 6 is arranged at the bottom of the first box chamber; the waste gas introduced into the gas-phase oxidation tower 8 enters the first electrolytic tank 7 through the grid plate after being evenly homogenized (gas is evenly homogenized) by the gas collecting box, and spray pipes 9 are arranged above micro-electrolysis fillers in the first electrolytic tank 7 and the second electrolytic tank 12 to evenly spray water. The spray water is delivered from the third electrolytic tank 26 to the sixth interface 11 of the gas-phase oxidation tower 8 through the water pipeline by the spray water pump 23 through the thirteenth interface 24 and is communicated with the spray pipe 9. The waste gas is purified by the first electrolytic tank 7 and then enters the top of the gas collecting box, the gas is homogenized and then enters the second electrolytic tank 12 and then enters the bottom of the second chamber of the gas collecting box, the gas is homogenized and then enters the first filter layer 16 and the second filter layer 15 (the first filter layer 16 and the second filter layer 15 are both water mist filter layers) to remove water mist, and the purified gas is discharged out of the fifth interface 14 to finish the purification of the waste gas to reach the emission standards.
The waste water of the enterprises is sent to the third electrolytic tank 26 of the liquid phase oxidation tower 20 through the ninth interface 34. The shower water of the first electrolytic tank 7 flows out of the third interface 18 and flows into the third electrolytic tank 26 through the tenth interface 35, and the shower water of the second electrolytic tank 12 flows out of the fourth interface 17, one part flows into the third electrolytic tank 26 through the eighth interface 33 and the other part flows into the fourth electrolytic tank 31 through the seventh interface 32; the third electrode group 25 is arranged in the third electrolytic tank 26, and the waterfall air pipes 27 are arranged at the bottoms of the third electrolytic tank and the fourth electrolytic tank 31, are connected with the twelve interfaces 21 and are communicated with the outlet of the waterfall air blower. Waste after aeration of the third electrolytic tank 26 and the fourth electrolytic tank 31The gas reaches the second port 19 through the eleventh port 36 and enters the bottom of the first tank of the gas collecting tank to be purified by the gas phase oxidation tower 8. After the third electrode group 25 is electrified, the wastewater in the third electrolytic tank 26 and iron ions (generated by micro-electrolysis filler) in the spray water of the gas-phase oxidation tower 8 are subjected to electrochemical coupling oxidation-flocculation reaction, pollutants in the wastewater are oxidized and decomposed, and generated parts of OH and H are formed 2 O 2 Flows out through thirteen connectors 24, is pressurized by a spray water pump 23 along a water pipeline, is sent to a sixth connector 11 of the gas-phase oxidation tower 8 and is communicated with a spray pipe 9 to be used as spray water of the gas-phase oxidation tower 8.
The fourth electrolytic cell 31 is arranged with a fourth electrode group 29 and a reference electrode 30, wherein the fourth electrode group 29 is a working electrode group. The fourth electrolytic tank 31 is used as the second-stage disposal of the third electrolytic tank 26, the principle is the same, the wastewater flowing into the fourth electrolytic tank 31 through the seventh interface 32 is subjected to potential difference judgment of the purifying degree by the reference electrode, and the purified water is discharged out of the fourteen interfaces 28 to finish the purification of the wastewater to reach the standard and discharge. The oxidation-reduction potential change of the water body is monitored in real time by the working electrode and the reference electrode of the fourth electrolytic tank, and when the change value of the measured potential is 100-300 mV (set value is 200mV and is regulated and set according to the drainage water quality control requirement), the sewage CODcr, nitrate and other pollutants are completely decomposed, and the purified water is discharged after reaching the standard.
The spray pipe 9 is composed of a main pipeline and a spray header.
The electro-Fenton reaction conditions of the liquid phase oxidation tower are as follows: PH=4-9, water temperature 5-35 ℃, and reaction time 2-50 min.
Plasma is the fourth state of matter, and there are two main ways of directly removing NOx from plasma: one is the decomposition route, i.e. electron and N 2 The collision generates N atoms, which then react to convert NO to N 2 . The other is the oxidation pathway, i.e. NO is oxidized to NO under the action of plasma 2 Then with H 2 The OH free radical generated by O discharge acts to finally remove NO in the form of nitric acid or nitrite. The direct removal of VOCs by plasma mainly depends on a large number of chemical active species including high-energy electrons, ions, excited molecules, free radicals and the like, and the energy of the active species is highAt the bond energy of the gas molecules, the gas molecules frequently collide with the VOCs molecules, so that the molecules are broken and dissociated to degrade the VOCs. In addition, when oxygen exists in the reaction, oxygen molecules collide with high-energy electrons in the plasma to generate oxygen atoms and excited oxygen molecules, and the particles with strong oxidability react with VOCs molecules to oxidize the VOCs molecules into non-toxic CO 2 。H 2 O generates a large amount of active particles under the action of a plasma field, such as H, OH and HO 2 Etc., which can directly react with the reactant gas molecules in an oxidation reaction.
The combination of the plasma and the catalyst improves the energy efficiency, and therefore, the plasma and the catalyst show obvious superiority compared with the single use of the plasma or the single use of the catalyst.
The photocatalysis consists of ultraviolet lamp tube and ultraviolet catalytic net, such as TiO catalyst 2 Radicals, also known as TiO 2 The photocatalytic oxidation technology has good purifying effect on NOx in the flue gas, and the degradation rate is up to 97 percent, so that HNO is generated 3 。
TiO 2 The mechanism of removing NOx by photocatalytic oxidation is similar to that of oxidizing VOCs, namely TiO 2 When irradiated by optical radiation exceeding the band gap energy, electrons in the valence band are excited, enter the conduction band across the forbidden band, and generate corresponding holes in the valence band. Electrons and holes migrate to different positions on the surface of the particles, and the holes have strong electron-obtaining capability, so that electrons in a NOx and VOCs system can be extracted, activated and oxidized. The electrons react with water and oxygen in the air to generate OH and O with stronger oxidizing ability 2 A first part Etc., is to finally oxidize NOx and VOCs to form NO 3 A first part 、CO 2 And H 2 The most predominant oxidant of O.
The electric-Fenton method combines the electrochemical process and the oxidization process of Fenton reagent, and fully utilizes the oxidization capability of the electrochemical process and the oxidization process of Fenton reagent.
The electric Fenton technology has the following advantages: (1) Automatic generation of H 2 O 2 The mechanism of (2) is relatively perfect; (2) Oxygen or air sprayed on the cathode can improve the mixing effect of the reaction solution; (3) Fe (Fe) 2+ Can be regenerated by cathode, fe 3+ And Fe (Fe) 2+ Can keep good cyclic reaction and has small sludge amount; (4) organic matter degradation factors are as follows: indirect oxidation of hydroxyl radical OH, direct oxidation of the anode, electrocoagulation and electrocoagulation.
And the spray water after the reaction in the gas-phase oxidation tower is entrained with VOCs, nitrate, sulfate and dust and flows back to the liquid-phase oxidation tower.
The electro-Fenton reaction is as follows:
Fe 2+ +H 2 O 2 →Fe 3+ +OH — +·OH
Fe 2+ +·OH→Fe 3+ +OH —
·OH+H 2 O 2 →·HO 2 +H 2 O
DSA anode arranged in the liquid phase oxidation tower is electrified to generate electrochemical reaction, and H is generated under the condition of aeration 2 O 2 。
The iron-carbon micro-electrolysis technology mainly utilizes the combined action of the reducibility of iron, the electrochemistry of iron and the flocculation adsorption of iron ions to purify the wastewater.
The iron-carbon micro-electrolysis electrochemical reaction process is as follows:
anode of Fe-2 e- & gtFe 2+ E(Fe/Fe2+)＝0.44V
Cathode 2H + +2e→H 2 E(H+/H2)＝0.00V
Nascent Fe produced 2+ And atoms H, which have high chemical activity and can change the structure and characteristics of a plurality of organic matters in the wastewater, so that the organic matters have the effects of chain scission, ring opening and the like.
If there is a waterfall, the following reaction also occurs:
O 2 +4H + +4e→2H 2 O E(O2)＝1.23V
O 2 +2H2O+4e→4OH — E(O2/OH — )＝0.41V
Fe 2+ +O 2 +4H + →2H 2 O+Fe 3+
OH produced — Is the reason for the rise of the pH value of the effluent water and is made of Fe 2+ Oxidation of formed Fe 3+ Gradually hydrolyzing to obtain Fe (OH) with high polymerization degree 3 The colloid flocculant can effectively adsorb and coagulate suspended matters and heavy metal ions in water, thereby enhancing the purification effect on wastewater, and being similar to Fe generated by Fenton reagent 3+ Mechanism of action.
The DSA anode of the third electrode group and the fourth electrode group of the liquid phase oxidation tower is a titanium-based metal oxide anode (Ti/IrO) 2 /IrO 2 -SnO 2 ) Can efficiently catalyze strong oxide ClO — And formation of OH.
The cathodes of the third electrode group and the fourth electrode group of the liquid-phase oxidation tower are platinum cathodes (Pt), cu-Zn alloy or Ti and are opposite to NO 3 — Has high catalytic reduction efficiency, stable electrolytic performance and long service life of the electrode.
CODcr and SO in liquid phase oxidation tower waste water 3 2— And nitrogen-containing pollutant (mainly in two forms of ammonia nitrogen and nitrate nitrogen), and the nitrate and nitrite in the wastewater are reduced into NO by utilizing the cathode of the electrolytic tank through the circulation action of a circulating pump, the circulation electrochemical coupling oxidation-flocculation action of the first electrolytic tank, the second electrolytic tank and the third electrolytic tank of the liquid phase oxidation tower, and the final controlled disposal of the fourth electrolytic tank of the liquid phase oxidation tower 2 — 、NH 4 + 、OH — And N 2 The method comprises the steps of carrying out a first treatment on the surface of the Generation of highly oxidizing species ClO using DSA anode region — And OH, CODcr and SO in the wastewater are treated 3 2— 、NH 4 + 、NO 2 — Oxidation to SO 4 2— 、Cl — 、NO 3 — And N 2 、CO 2 The aim of purifying the wastewater is fulfilled; adding a certain amount of Cl into the wastewater — Can promote ClO — Is generated.
The multi-layer Fe-C micro-electrolysis filler of the gas-phase oxidation tower, the washing of spray water, the repeated collection and deflection of air flow and the electrode capturing function of the filler layer have a good filtering effect on particulate matters in waste gas, and the dust reaches ultra-low emission.
By adopting the scheme, the smoke treatment is aimed atThe sulfur dioxide removal rate can reach more than 99 percent, the nitrogen oxide removal rate can reach more than 90 percent, and the VOCs emission concentration aiming at VOCs treatment is lower than 20mg/m 3 The methanol emission concentration is lower than 10mg/m 3 The non-methane total hydrocarbon emission concentration is lower than 5mg/m 3 。
The examples are preferred embodiments of the present invention, but the present invention is not limited to the above-described embodiments, and any obvious modifications, substitutions or variations that can be made by one skilled in the art without departing from the spirit of the present invention are within the scope of the present invention.
Claims (9)
1. An electrochemical-based waste gas and wastewater coupling purification system comprises a photoelectric treatment tower, a gas phase oxidation tower, a liquid phase oxidation tower, a gas-fall fan and a spray water pump; the method is characterized in that: the photoelectric treatment tower comprises a plasma catalysis module arranged at the front and a photocatalysis module arranged at the rear; the plasma catalysis module comprises a multistage plasma generator and a plasma catalysis net which are alternately arranged; the photocatalysis module comprises a plurality of stages of ultraviolet lamp tubes and an ultraviolet catalysis net which are alternately arranged; the gas-phase oxidation tower comprises a gas collection box, a first electrolytic tank, a second electrolytic tank, a first filter layer, a second filter layer and a spray pipe; the first electrolytic tank consists of a grating plate, micro-electrolysis filler arranged on the grating plate and a first electrode group buried in the micro-electrolysis filler; the second electrolytic tank consists of a grating plate, micro-electrolysis filler arranged on the grating plate and a second electrode group buried in the micro-electrolysis filler; the gas collecting header is divided into a first tank chamber, a second tank chamber and a third tank chamber, wherein the first tank chamber is communicated with the second tank chamber only at the top, and the second tank chamber is communicated with the third tank chamber only at the bottom; the first box chamber is divided into an upper part and a lower part by a grid plate of the first electrolytic tank, and the second box chamber is divided into an upper part and a lower part by a grid plate of the second electrolytic tank; the first filter layer and the second filter layer are arranged in the third box at intervals up and down; the liquid phase oxidation tower comprises a third electrolytic tank, a fourth electrolytic tank and a waterfall pipe; the third electrolytic cell is provided with a third electrode group; a fourth electrode group and a reference electrode are arranged in the fourth electrolytic tank;
the outlet of the photoelectric treatment tower is communicated with a first port at the bottom of the first box chamber through a smoke pipeline; the air inlet of the air-fall fan is communicated with a first-port smoke pipeline of a first box chamber by a smoke pipeline, and the air outlet is communicated with a twelve-port of a third electrolytic tank and communicated with an air-fall pipeline; the spray water pump is communicated with a thirteenth interface of a third electrolytic tank and a sixth interface of the gas-phase oxidation tower through a water pipeline and is communicated with a spray pipe; the fifth interface at the top of the third box chamber is a purified gas discharge port;
the third interface at the bottom of the first box chamber is a water outlet which is communicated with the tenth interface of the third electrolytic tank through a water pipeline; the third electrolytic tank and the fourth electrolytic tank are communicated with a second interface of the first box chamber by an air pipeline by taking an eleventh interface as an air outlet; the water outlet of the fourth interface at the bottom of the second box chamber is communicated with the eighth interface of the third electrolytic tank and the seventh interface of the fourth electrolytic tank through water pipelines respectively; the ninth interface of the third electrolytic tank is a wastewater inlet; the fourteen interfaces at the bottom of the fourth electrolytic tank are purified water discharge ports.
2. An electrochemical-based waste gas and wastewater coupled purification system as claimed in claim 1, wherein: the plasma catalytic net is a double-layer wire net, and is internally filled with TiO 2 Platinum-based catalyst, proton zeolite, Y zeolite, naX zeolite, naY zeolite, laCoO 3 、Ag/CeO 2 、MnO 2 And gamma-Al 2 O 3 One or a combination of several catalysts.
3. An electrochemical-based waste gas and wastewater coupled purification system as claimed in claim 1, wherein: the ultraviolet catalytic net is a double-layer wire net, and is internally filled with TiO 2 And a catalyst prepared from a mixture of activated carbon and iron oxide.
4. An electrochemical-based waste gas and wastewater coupled purification system as claimed in claim 1, wherein: the micro-electrolysis filler is iron-carbon alloy.
5. An electrochemical-based waste gas and wastewater coupled purification system as claimed in claim 1, wherein: the first electrode group and the second electrode group are made of iron plates or stainless steel plates; the anodes of the third electrode group and the fourth electrode group are DSA anodes, and the cathode is one of platinum, cu-Zn alloy or Ti; the reference electrode is a silver chloride electrode or a calomel electrode.
6. An electrochemical-based waste gas and wastewater coupled purification system as claimed in claim 1, wherein: each electrode group is connected with a corresponding wiring terminal of the direct current power supply, and the distance between the electrode plates of each electrode group is 1-10 cm; the voltage of the direct current power supply is 0-20V.
7. An electrochemical-based waste gas and wastewater coupled purification system as claimed in claim 1, wherein: the third electrolytic tank and the fourth electrolytic tank are also added with micro-electrolysis filler.
8. An electrochemical-based waste gas and wastewater coupled purification system as claimed in claim 1, wherein: the purifying gas discharge port is provided with a detector for monitoring the concentration of SOx, NOx and VOCs, and the detector controls the start and stop, voltage and frequency of the plasma generator through the concentration of the SOx, NOx and VOCs which are fed back, controls the start and stop of the ultraviolet lamp tube, controls the start and stop, voltage and current of the first electrode group and the second electrode group, and controls the start and stop, voltage and current of the third electrode group and the fourth electrode group.
9. An electrochemical-based waste gas and waste water coupling purification method is characterized by comprising the following steps of: introducing the waste gas into a photoelectric treatment tower, decomposing and oxidizing the waste gas by a plasma catalytic module formed by a multistage plasma generator and a plasma catalytic net, partially purifying the waste gas, introducing a photocatalytic module formed by a multistage ultraviolet lamp tube and an ultraviolet catalytic net, purifying the waste gas again, introducing one part of the waste gas into a gas-phase oxidation tower along a flue gas pipeline through a first interface for purification, introducing the other part of the waste gas into a twelve interface of a liquid-phase oxidation tower along the flue gas pipeline through a gas-fall fan, and communicating the twelve interface with a gas-fall pipe for gas fall;
in the gas-phase oxidation tower, the gas collecting header is divided into a first tank chamber, a second tank chamber and a third tank chamber, wherein the first tank chamber is communicated with the second tank chamber only at the top, and the second tank chamber is communicated with the third tank chamber only at the bottom; the first box chamber and the second box chamber are both divided into an upper part and a lower part by the grid plate; the first filter layer and the second filter layer are arranged in the third box at intervals up and down; introducing the waste gas of the gas-phase oxidation tower, homogenizing the waste gas by a gas collecting box, then introducing the waste gas into a first electrolytic tank by a grid plate, and arranging spray pipe spray water above micro-electrolysis fillers in the first electrolytic tank and a second electrolytic tank; the spray water is from the electrolytic tank III, pressurized and conveyed to the port six of the gas-phase oxidation tower through a water pipeline by a spray water pump through the port thirteen and communicated with a spray pipe; waste gas is purified by the first electrolytic tank and then enters the top of the gas collection box, gas is homogenized and then enters the second electrolytic tank and then enters the bottom of the second box chamber of the gas collection box, and organic matters left by the photoelectric treatment tower are decomposed and purified through the electrochemical coupling oxidation-flocculation reaction of the first electrolytic tank and the second electrolytic tank based on Fe-C micro electrolysis and electric-Fenton reaction and the combined action of the waste gas and spray water with active groups from the third electrolytic tank; the gas after uniform gas at the bottom of the second tank chamber of the gas collecting tank enters a first filter layer and a second filter layer to remove water mist, and the purified gas is discharged out of a fifth interface to finish the purification of the waste gas to reach the emission standard;
delivering the wastewater into a third electrolytic tank of a liquid phase oxidation tower from a ninth interface; the spray water of the first electrolytic tank flows out of the third interface and flows into the third electrolytic tank through the tenth interface, part of the spray water of the second electrolytic tank flows out of the fourth interface and flows into the third electrolytic tank through the eighth interface, and the other part of the spray water flows into the fourth electrolytic tank through the seventh interface; a third electrode group is arranged in the third electrolytic tank, and the bottoms of the third electrolytic tank and the fourth electrolytic tank are provided with a waterfall pipe twelve-number connection port which is communicated with an outlet of a waterfall fan; waste gas after the aeration of the third electrolytic tank and the fourth electrolytic tank reaches the second interface through the eleventh interface through a flue gas pipeline and enters the bottom of the first chamber of the gas collecting box, and is purified by the gas phase oxidation tower; after the third electrode group is electrifiedThe wastewater in the third electrolytic tank and iron ions in spray water of the gas phase oxidation tower are subjected to electrochemical coupling oxidation-flocculation reaction, and generated part of OH and H 2 O 2 Flows out through a thirteen-th interface, is pressurized by a spray water pump along a water pipeline, is sent to a gas-phase oxidation tower to be used as spray water, is subjected to electrochemical coupling oxidation-flocculation reaction based on Fe-C micro-electrolysis and electric-Fenton reaction again, one part of the spray water returns to a third electrolytic tank of a liquid-phase oxidation tower to be continuously oxidized and decomposed, and the other part of the spray water is sent to a fourth electrolytic tank to be oxidized; the fourth electrolytic tank is provided with a fourth electrode group and a reference electrode, wherein the fourth electrode group is a working electrode group; and the spray water flowing into the fourth electrolytic tank through the seventh interface is subjected to potential difference of the reference electrode to judge the purification degree, and the purified water is discharged out of the fourteen interfaces to finish the purification of the wastewater to reach the discharge standard.
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Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004204739A (en) * | 2002-12-24 | 2004-07-22 | Toshiba Corp | Exhaust emission control system and exhaust emission control method |
| WO2010149147A1 (en) * | 2009-06-24 | 2010-12-29 | Cetec Destillationstechnik Gmbh | Method and device for the combined physical/chemical purification of exhaust air, purification of waste water, and disinfection of potable water, and for the simultaneous treatment of exhaust air and waste water |
| CN104671592A (en) * | 2015-01-26 | 2015-06-03 | 常州大学 | Comprehensive treatment system for waste gas and PO wastewater |
| CN104826462A (en) * | 2015-05-06 | 2015-08-12 | 胡志勇 | Garbage station waste gas processing and deodorizing system |
| CN205145942U (en) * | 2015-10-28 | 2016-04-13 | 天津中天和庆环保科技有限公司 | VOCs volatility waste gas treatment equipment |
| CN105601002A (en) * | 2015-12-29 | 2016-05-25 | 宁磊 | A treatment system and method for purifying organic wastewater |
| CN106178874A (en) * | 2016-08-11 | 2016-12-07 | 上海洗霸科技股份有限公司 | Water solublity VOCs Zero-discharge treating process |
| CN106351765A (en) * | 2016-09-19 | 2017-01-25 | 马加德 | Power and heat co-supply system based on Stirling engine and power and heat co-supply method of system |
| WO2017071515A1 (en) * | 2015-10-29 | 2017-05-04 | 清华大学 | Device and method enabling industrial coal-fired boiler to concurrently absorb nox and so2 |
| CN106823724A (en) * | 2017-02-21 | 2017-06-13 | 浙江大维高新技术股份有限公司 | A kind of flue gas integrated purification system for realizing wastewater zero discharge |
| CN207307579U (en) * | 2017-09-21 | 2018-05-04 | 马加德 | A kind of exhaust gas waste water coupling purification system based on electrochemistry |
-
2017
- 2017-09-21 CN CN201710859882.0A patent/CN107469597B/en active Active
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004204739A (en) * | 2002-12-24 | 2004-07-22 | Toshiba Corp | Exhaust emission control system and exhaust emission control method |
| WO2010149147A1 (en) * | 2009-06-24 | 2010-12-29 | Cetec Destillationstechnik Gmbh | Method and device for the combined physical/chemical purification of exhaust air, purification of waste water, and disinfection of potable water, and for the simultaneous treatment of exhaust air and waste water |
| CN104671592A (en) * | 2015-01-26 | 2015-06-03 | 常州大学 | Comprehensive treatment system for waste gas and PO wastewater |
| CN104826462A (en) * | 2015-05-06 | 2015-08-12 | 胡志勇 | Garbage station waste gas processing and deodorizing system |
| CN205145942U (en) * | 2015-10-28 | 2016-04-13 | 天津中天和庆环保科技有限公司 | VOCs volatility waste gas treatment equipment |
| WO2017071515A1 (en) * | 2015-10-29 | 2017-05-04 | 清华大学 | Device and method enabling industrial coal-fired boiler to concurrently absorb nox and so2 |
| CN105601002A (en) * | 2015-12-29 | 2016-05-25 | 宁磊 | A treatment system and method for purifying organic wastewater |
| CN106178874A (en) * | 2016-08-11 | 2016-12-07 | 上海洗霸科技股份有限公司 | Water solublity VOCs Zero-discharge treating process |
| CN106351765A (en) * | 2016-09-19 | 2017-01-25 | 马加德 | Power and heat co-supply system based on Stirling engine and power and heat co-supply method of system |
| CN106823724A (en) * | 2017-02-21 | 2017-06-13 | 浙江大维高新技术股份有限公司 | A kind of flue gas integrated purification system for realizing wastewater zero discharge |
| CN207307579U (en) * | 2017-09-21 | 2018-05-04 | 马加德 | A kind of exhaust gas waste water coupling purification system based on electrochemistry |
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