CN113121032A - Ship flue gas washing desulfurization wastewater treatment device and method - Google Patents
Ship flue gas washing desulfurization wastewater treatment device and method Download PDFInfo
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- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
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- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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Abstract
The invention provides a ship flue gas washing desulfurization wastewater treatment device which comprises a pre-settling tank, a membrane reactor, a cleaning tank, a dosing unit and a waste liquid collecting device. Through the treatment of the ship flue gas washing desulfurization wastewater treatment device provided by the invention, the ship flue gas washing desulfurization wastewater achieves that the produced water reaches the standard and is discharged to the sea, the concentrated solution and the residual solution generated by each unit are discharged into the waste liquid collection device and are recycled and treated by enterprises with port qualifications, the original desulfurization wastewater is greatly reduced, the economic burden can be reduced for ships, and the device has a good application prospect.
Description
Technical Field
The invention belongs to the technical field of water treatment, and relates to a method and a device for treating desulfurization wastewater generated in a ship flue gas washing process.
Background
At present, maritime transportation is the implementation of import and export trade in all countriesThe main means of easiness. Meanwhile, the problem of environmental pollution caused by marine ship transportation of various countries is also becoming more serious, wherein the atmospheric pollution is aggravated by diffusion of sulfur oxides caused by ship fuel oil smoke emission. At present, the number of huge ships sailing on public sea reaches tens of thousands, SO2The total amount of the discharged gas is huge, and the influence on the environment is not small. Therefore, in 2016, 10, 26 days, 70 th meeting (MEPC70) of the maritime environmental protection committee of the International Maritime Organization (IMO) held in London requires that from 2020, the sulfur content of fuel used by global ships is not more than 0.5% (part of emission control areas require 0.1%), and after the sulfur limit command is effective, all ships without desulfurization equipment are prohibited from carrying fuel with the exceeding sulfur content. In order to deal with sulfur limitation, adding a flue gas washing and desulfurizing system (EGC system) to a ship is one of the main choices of the shipowners.
A large amount of desulfurization washing wastewater can be generated by installing an EGC system, suspended substances and PAHs (polycyclic aromatic hydrocarbons) contained in the wastewater can influence the marine ecological environment, and therefore all countries actively limit the discharge of the wastewater to the marine water body, and a large amount of ships are additionally provided or base method closed systems are considered. The desulfurization waste water generated by the closed system of the basic method needs to occupy a large amount of space on a ship for storage and is handled by a shipowner, which brings great cost pressure to the shipowner.
Disclosure of Invention
In order to solve the problems, the invention aims to provide a ship flue gas washing desulfurization wastewater treatment device, which meets the application requirements of ship flue gas washing desulfurization wastewater reduction treatment, realizes great reduction of desulfurization wastewater, and has the advantages of small floor area, low fixed investment and short investment return period.
The invention also aims to provide a ship flue gas washing desulfurization wastewater treatment method based on the device, so as to effectively relieve the pressure caused by storage and treatment of a large amount of desulfurization wastewater on a ship.
In order to realize the aim, the invention provides a ship flue gas washing desulfurization wastewater treatment device which consists of a pre-settling tank, a membrane reactor, a cleaning tank, a dosing unit and a waste liquid collecting device, wherein the pre-settling tank is connected with the pre-settling tank;
wherein, the pre-settling tank, the membrane reactor, the cleaning tank, the dosing unit and the waste liquid collecting device are connected through pipelines;
the pre-settling tank is a hollow tank body, the top of the tank body is provided with a medicament inlet, the upper part of the tank body is provided with a supernatant outlet, the lower part of the tank body is provided with a wastewater inlet, and the bottom of the tank body is provided with a concentrated solution discharge port; the pre-settling tank is connected with the dosing unit through a medicament inlet at the top;
the membrane reactor consists of a cylindrical reactor shell, a hollow flat membrane array and a produced water collector; wherein the hollow flat membrane array is positioned at the middle lower part in the reactor shell, and the upper part of the hollow flat membrane array is connected with a water production collector; the bottom of the reactor shell is provided with a supernatant inlet, a raffinate discharge outlet and a compressed air connector; the top of the reactor shell is provided with a water outlet; a concentrated water return port is arranged at the position of the reactor shell corresponding to the water production collector; the hollow flat membrane array is formed by vertically arranging a plurality of hollow flat membranes along the circumference of a membrane reactor; the water production collector is formed by sequentially connecting a water production discharge pipe at the top, a water collecting tray at the middle part and a water production interface at the bottom;
the cleaning tank is a hollow tank body, the top of the tank body is provided with a chemical feeding port, the side wall of the tank body is provided with a tap water connector, a circulating inlet, a circulating outlet and a produced water discharge port from top to bottom, a produced water inlet is arranged on the opposite side between the circulating inlet and the circulating outlet, the bottom of the tank body is provided with a residual liquid discharge port, and a chemical cleaning liquid outlet is arranged close to the residual liquid discharge port;
the waste liquid collecting device is a hollow tank body or a sealed cabin;
the pre-settling tank is connected with the dosing unit through a medicament inlet at the top, a supernatant outlet of the pre-settling tank is connected with a supernatant inlet of the membrane reactor, a concentrated liquid discharge port of the pre-settling tank is connected with a waste liquid collecting device, and a residual liquid discharge port of the membrane reactor is connected with the waste liquid collecting device; a pipeline connected with a concentrated water return port of the membrane reactor branches off one pipeline to be converged with a pipeline between a residual liquid discharge port and a waste liquid collecting device of the membrane reactor, and the tail end of the pipeline connected with the concentrated water return port of the membrane reactor is converged to a pipeline connected with a waste water inlet of a pre-settling tank; a water production outlet of the membrane reactor is connected with a water production inlet of the cleaning tank; a pipeline connected with a medicine washing liquid outlet of the washing tank is converged with a pipeline between a residual liquid discharge port of the membrane reactor and the waste liquid collecting device; the residual liquid discharge port of the cleaning tank is connected with a waste liquid collecting device; the circulation outlet of the cleaning tank is connected with the circulation inlet.
Furthermore, the water collecting tray is of a hollow disc structure, the water producing ports are tubular and are arranged along the edge of the water collecting tray, and the lower ends of the water producing ports are connected with the upper end of the hollow flat membrane array and used for collecting water produced on the inner side of the hollow flat membrane array.
Further, the hollow flat membrane is a ceramic flat membrane.
Preferably, the material of the ceramic flat membrane is one or more of silicon carbide, aluminum oxide, zirconium oxide and silicon oxide.
Preferably, the pore diameter of the ceramic flat membrane plate is 0.1-1 micron.
The invention also provides a method for treating the ship flue gas washing desulfurization wastewater by adopting the ship flue gas washing desulfurization wastewater treatment device, which comprises the following steps:
1) desulfurization wastewater is introduced into the pre-settling tank from a wastewater inlet of the pre-settling tank, a medicament is added into the pre-settling tank by a medicament adding unit, partial particulate matters in the wastewater are quickly settled to the bottom of the pre-settling tank to form concentrated solution under the auxiliary action of the added medicament, and the concentrated solution is periodically discharged into a waste liquid collecting device through a concentrated solution discharge port of the pre-settling tank;
most particulate matters contained in desulfurization waste water can be settled by arranging the pre-settling tank, so that the content of the particulate matters in the waste water entering the membrane reactor is reduced, the content of the particulate matters in the waste water is less, the pollution blockage of the hollow flat membrane is difficult to cause, namely, the hollow flat membrane does not need to intercept a large number of particulate matters, and the particulate matters are less to be intercepted, so that the particulate matter interception pressure of the membrane reactor can be remarkably relieved by arranging the pre-settling tank.
2) Compressed air is used for aerating the membrane reactor through a compressed air interface, settled supernatant enters the membrane reactor from a supernatant inlet of the membrane reactor, is filtered by a hollow flat membrane, particulate matters in the supernatant are filtered and retained on the hollow flat membrane, produced water is filtered and enters the inner side of the hollow flat membrane, the concentration of the particulate matters retained on the outer side of the hollow flat membrane is improved to be concentrated water, and the concentrated water flows out from a concentrated water return port; returning one part of the outflow concentrated water from the wastewater inlet of the pre-settling tank to the pre-settling tank, and shunting and discharging the other part of the outflow concentrated water to a waste liquid collecting device;
in the filtering process of the membrane, particles can deposit on the surface of the membrane to cause the pollution blockage of the membrane, the membrane flux is reduced, and the polluted blocking layer can be washed away by inputting compressed air for aeration, so that the membrane flux is favorably maintained.
When the hollow flat membrane is used for filtration, the supernatant flows through the outer side surface, part of water in the supernatant enters the inner side through the small holes in the membrane wall, and the particulate matters are trapped on the outer side surface, so that the concentration of the particulate matters in the external liquid is increased.
The backflow of the concentrated water is used for increasing the flow, increasing the scouring flow velocity of the outer side surface of the hollow flat membrane and relieving the pollution and blockage of the membrane.
3) The produced water enters a produced water collector from the inner side of the hollow flat membrane and is discharged to a cleaning tank from a produced water outlet along the directions of a produced water interface, a water collecting tray and a produced water discharge pipe; the produced water stored in the cleaning tank flows back to the membrane reactor to carry out backwashing on the hollow flat membrane array from inside to outside in the backwashing period; the water is discharged out of the ship through a water production discharge port of the cleaning tank during the non-backwashing period;
4) the time period of drug washing: running water is injected into the cleaning tank through the tap water connector, the chemical adding port injects a chemical lotion into the cleaning tank, the chemical lotion is stirred and prepared in the cleaning tank through self circulation of the chemical lotion in the circulation outlet and the circulation inlet, then the chemical lotion enters the membrane reactor through the chemical lotion outlet of the cleaning tank to perform chemical washing on the hollow flat membrane, and residual liquid after the chemical washing is discharged into the waste liquid collecting device through a residual liquid discharge port of the cleaning tank.
Preferably, the medicament is an organic flocculant or an inorganic flocculant, and the organic flocculant is preferably polyacrylamide; the inorganic flocculant is preferably polyaluminium chloride.
Preferably, the medicinal lotion is a cleaning agent and a soaking agent, the cleaning agent is an aqueous solution containing hydrochloric acid and citric acid, wherein the mass concentration of the hydrochloric acid is 4%, and the mass concentration of the citric acid is 2%; the soaking agent is an aqueous solution with the sodium hypochlorite concentration of 1-5 mmol/L.
Wherein the cleaning agent is used for cleaning inorganic pollutants in the system, and the sodium hypochlorite used as the soaking agent is used for inhibiting the breeding of microorganisms on the surface of the hollow flat membrane.
The membrane reactor adopts a cross flow filtration mode, so that the supernatant vertically flows through the outer side of the hollow flat membrane for surface second, and the produced water passes through the membrane to enter the inner side and is concentrated towards the center, so that the flow direction of the supernatant and the produced water is vertical. The cross-flow filtration mode can lead the particles intercepted by the membrane to be taken away by the shearing force generated by the supernatant fluid flowing parallel to the surface of the membrane, thereby leading the pollution blocking layer formed by the residual particles on the surface of the membrane to be thinner. While the supernatant forms a concentrated water as the concentration of particulate increases.
The invention has the advantages that:
the invention provides a device for treating desulfurization waste water from washing of ship flue gas, which is adopted, desulfurization waste water firstly enters a pre-settling tank, partial particulate matters in the waste water are rapidly settled under the auxiliary action of adding a medicament, only supernatant enters a membrane reactor, and the particulate matter interception pressure of the membrane reactor is remarkably relieved; the membrane reactor adopts a cross-flow filtration mode based on a hollow flat membrane to be vertically arranged into a hollow flat membrane array, adopts the hollow flat membrane and can carry out filtration under lower external pressure so as to reduce energy consumption, and adopts the cross-flow filtration and aeration modes so as to realize continuous scouring on the outer surface of the membrane and obviously reduce membrane pollution; the cleaning tank integrates the functions of water production backwashing and drug washing, and the membrane reactor is cleaned regularly to ensure the long-term stable operation of the process device. Through the treatment of the process device, the produced water of the flue gas washing desulfurization wastewater of the ship reaches the standard and is discharged to the sea, the concentrated solution and the residual solution generated by each unit are discharged into a waste liquid collecting device on the ship and are recovered and treated by a qualified enterprise at a port, the amount of the original desulfurization wastewater is greatly reduced, and the economic burden of the ship is reduced.
Drawings
FIG. 1 is a schematic view of a ship flue gas scrubbing desulfurization wastewater treatment device provided by the invention.
FIG. 2 is a schematic view of a water-producing collector in the ship flue gas scrubbing desulfurization wastewater treatment device provided by the invention.
Reference numerals
1: a pre-settling tank; 11: a medicament inlet; 12: a supernatant outlet; 13: a wastewater inlet; 14: a concentrated solution discharge port; 2: a membrane reactor; 21: a reactor housing; 211: a supernatant inlet; 212: a raffinate discharge port; 213: a compressed air interface; 214: a water production outlet; 215: a concentrated water return port; 22: a hollow flat sheet membrane array; 221: a hollow flat membrane; 23: a produced water collector; 231: a produced water discharge pipe; 232: a water collection tray; 233: a water producing interface; 3: cleaning the tank; 31: a medicine adding port; 32: a tap water interface; 33: a recycle inlet; 34: a recycle outlet; 35: a water production discharge port; 36: a water production inlet; 37: a raffinate discharge port; 38: a medicine washing liquid outlet; 4: a dosing unit; 5: waste liquid collection device.
Detailed Description
The invention will be further described with reference to the following figures and examples, but the invention is not limited thereto.
Example 1
As shown in figure 1, the invention provides a ship flue gas washing desulfurization wastewater treatment device, which consists of a pre-settling tank 1, a membrane reactor 2, a cleaning tank 3, a dosing unit 4 and a waste liquid collecting device 5;
wherein, the pre-sedimentation tank 1, the membrane reactor 2, the cleaning tank 3, the dosing unit 4 and the waste liquid collecting device 5 are connected through a pipeline 9;
the pre-settling tank 1 is a hollow tank body, the top of the tank body is provided with a medicament inlet 11, the upper part of the tank body is provided with a supernatant outlet 12, the lower part of the tank body is provided with a wastewater inlet 13, and the bottom of the tank body is provided with a concentrated solution discharge port 14; the pre-settling tank 1 is connected with the dosing unit 4 through a medicament inlet 11 at the top;
the membrane reactor 2 consists of a cylindrical reactor shell 21, a hollow flat membrane array 22 and a produced water collector 23; wherein, the hollow flat membrane array 22 is positioned at the middle lower part in the reactor shell 21, and the upper part of the hollow flat membrane array 22 is connected with a water production collector 23; the bottom of the reactor shell 21 is provided with a supernatant inlet 211, a concentrated solution discharge port 212 and a compressed air interface 213; the top of the reactor shell 21 is provided with a water outlet 214; a concentrated water return port 215 is arranged at the position of the reactor shell 21 corresponding to the water production collector 23; the hollow flat membrane array 22 is formed by vertically arranging a plurality of hollow flat membranes 221 along the circumference of the membrane reactor 2; as shown in fig. 2, the produced water collector 23 is formed by sequentially connecting a produced water discharge pipe 231 at the top, a water collecting tray 232 at the middle and a produced water interface 233 at the bottom; the water collecting tray 232 is of a hollow disc structure, the water producing connectors 233 are tubular and are formed by being arranged along the edge of the water collecting tray 232, the lower ends of the water producing connectors 233 are connected with the upper end of the hollow flat membrane array 22, the upper ends of the water producing connectors 233 are connected with the bottom of the water collecting tray 232 and are used for collecting water produced on the inner side of the hollow flat membrane array, the water is collected into the water collecting tray and finally discharged through a water producing discharge pipe, the length of the water producing connectors 233 can be adjusted according to the space size of the membrane reactor 2, for example, the length of the water producing connectors 233 in fig. 1 is long, and for example, the. The hollow flat membrane 221 is a ceramic flat membrane, and is made of one or more of silicon carbide, aluminum oxide, zirconium oxide, and silicon oxide, in this embodiment, silicon carbide is preferred, and the pore size is 0.1 micron to 1 micron, in this embodiment, 0.1 micron.
The cleaning tank 3 is a hollow tank body, the top of the tank body is provided with a chemical feeding port 31, the side wall of the tank body is provided with a tap water connector 32, a circulating inlet 33, a circulating outlet 34 and a water production discharge port 35 from top to bottom, the opposite side between the circulating inlet 33 and the circulating outlet 34 is provided with a water production inlet 36, the bottom of the tank body is provided with a residual liquid discharge port 37, and a chemical cleaning liquid outlet 38 is arranged close to the residual liquid discharge port;
the waste liquid collecting device 5 is a hollow tank body or a sealed cabin; when the ship is small and the voyage is short, the hollow tank body can be used for storing when the waste liquid is less generated, and when the ship is large and the voyage is long, the sealed cabin of the ship can be used as a waste liquid collecting device when the waste liquid is more generated.
The pre-settling tank 1 is connected with a dosing unit 4 through a medicament inlet 11 at the top, a supernatant outlet 12 of the pre-settling tank 1 is connected with a supernatant inlet 211 of the membrane reactor 2, a concentrated solution discharge port 14 of the pre-settling tank 1 is connected with a waste solution collecting device 5, and a residual solution discharge port 212 of the membrane reactor 2 is connected with the waste solution collecting device 5; a pipeline connected with the concentrated water return port 215 of the membrane reactor 2 branches off one pipeline to be converged with a pipeline between the residual liquid discharge port 212 of the membrane reactor 2 and the waste liquid collecting device 5, and the tail end of the pipeline connected with the concentrated water return port 215 of the membrane reactor 2 is converged to a pipeline connected with the waste water inlet 13 of the pre-settling tank 1; the water production outlet 214 of the membrane reactor 2 is connected with the water production inlet 36 of the cleaning tank 3; a pipeline connected with the drug washing liquid outlet 38 of the washing tank 3 is converged with a pipeline between the residual liquid discharge port 212 of the membrane reactor 2 and the waste liquid collecting device 5; the residual liquid discharge port 37 of the cleaning tank 3 is connected with the waste liquid collecting device 5; the circulation outlet 34 of the purge tank 3 is connected to the circulation inlet 33.
The method for treating the ship flue gas washing desulfurization wastewater by using the ship flue gas washing desulfurization wastewater treatment device comprises the following steps:
1) desulfurization wastewater is introduced into the pre-settling tank 1 from a wastewater inlet 13 of the pre-settling tank 1, a medicament is added into the pre-settling tank 1 by a medicament adding unit 4, partial particulate matters in the wastewater are quickly settled to the bottom of the pre-settling tank 1 to form concentrated solution under the auxiliary action of the added medicament, and the concentrated solution is periodically discharged into a waste liquid collecting device through a concentrated solution discharge port 14 of the pre-settling tank 1;
the dosing unit continuously adds a medicament during the operation of the device, mainly adds an organic flocculant polyacrylamide or an inorganic flocculant polyaluminium, mainly enables small particles in wastewater to be agglomerated into large particles, and can reduce the pollution and blockage of the membrane.
Most of particulate matters contained in desulfurization wastewater can be settled by arranging the pre-settling tank 1, so that the content of the particulate matters in the wastewater entering the membrane reactor 2 is reduced, the content of the particulate matters in the wastewater is less, the pollution blockage of the hollow flat membrane is difficult to cause, namely, the hollow flat membrane 212 does not need to intercept a lot of particulate matters, and only fewer particulate matters need to be intercepted, and therefore the particulate matter interception pressure of the membrane reactor 2 can be remarkably relieved by arranging the pre-settling tank 1.
2) Compressed air aerates the membrane reactor 2 through a compressed air interface 213, settled supernatant enters the membrane reactor 2 from a supernatant inlet 211 of the membrane reactor 2, is filtered by the hollow flat membrane 221, particulate matters in the supernatant are filtered and trapped on the hollow flat membrane 221, water is produced after being filtered and enters the inner side of the hollow flat membrane 221, concentrated water is obtained after the concentration of the particulate matters trapped on the outer side of the hollow flat membrane 221 is improved, and the concentrated water flows out from a concentrated water return port 215; part of the outflow concentrated water reflows from the wastewater inlet 13 of the pre-settling tank 1 to enter the pre-settling tank 1 again, and the other part of the outflow concentrated water is shunted and discharged to the waste liquid collecting device 5;
in the filtering process of the membrane, particles can deposit on the surface of the membrane to cause the pollution blockage of the membrane, the membrane flux is reduced, and the polluted blocking layer can be washed away by inputting compressed air for aeration, so that the membrane flux is favorably maintained.
When the hollow flat membrane is used for filtration, the supernatant flows through the outer side surface, part of water in the supernatant enters the inner side through the small holes in the membrane wall, and the particulate matters are trapped on the outer side surface, so that the concentration of the particulate matters in the external liquid is increased.
The backflow of the concentrated water is used for increasing the flow, increasing the scouring flow velocity of the outer side surface of the hollow flat membrane and relieving the pollution and blockage of the membrane.
The material balance of the system can be realized by controlling the liquid inlet flow (equal to the flow of the concentrated water discharged by shunting and the flow of the produced water) at the wastewater inlet of the pre-settling tank; the concentration proportion of the original desulfurization wastewater can be controlled by adjusting the proportion of the concentrated water flow and the produced water flow discharged in a shunting manner.
3) The produced water enters the produced water collector 23 from the inner side of the hollow flat membrane 221 and is discharged to the cleaning tank 3 from the produced water outlet 214 along the directions of the produced water interface 233, the water collecting tray 232 and the produced water discharge pipe 231; the produced water stored in the cleaning tank 3 flows back to the membrane reactor 2 to carry out backwashing on the hollow flat membrane array 22 from inside to outside in the backwashing period; the water is discharged out of the ship through a water production discharge port 35 of the cleaning tank 3 in the non-backwashing period;
4) the time period of drug washing: tap water is injected into the cleaning tank 3 through the tap water connector 32, the chemical lotion is injected into the cleaning tank 3 through the chemical adding port 31, the chemical lotion is stirred and prepared in the cleaning tank 3 through self circulation of the chemical lotion realized through the circulation outlet 33 and the circulation inlet 32, then the chemical lotion enters the membrane reactor 2 through the chemical lotion outlet 38 of the cleaning tank 3 to perform chemical cleaning on the hollow flat membrane 221, and residual liquid after the chemical cleaning is discharged into a waste liquid collecting device through a residual liquid discharge port 37 of the cleaning tank 3.
The medicinal lotion is divided into a cleaning agent and a soaking agent, wherein the cleaning agent is an aqueous solution containing hydrochloric acid and citric acid, the mass concentration of the hydrochloric acid is 4%, and the mass concentration of the citric acid is 2%; the soaking agent is an aqueous solution with the sodium hypochlorite concentration of 1-5 mmol/L. The drug washing function is that when the device stops running, the pipeline and the membrane surface in the system are washed by a cleaning agent, and the flat membrane array is soaked by a soaking agent, so that the influence of microorganism breeding on the service life of the membrane is prevented. If the device has a long period of stoppage, the soaking agent should be replaced periodically.
The membrane reactor adopts a cross flow filtration mode, so that the supernatant vertically flows through the outer side of the hollow flat membrane for surface second, and the produced water passes through the membrane to enter the inner side and is concentrated towards the center, so that the flow direction of the supernatant and the produced water is vertical. The cross-flow filtration mode can lead the particles intercepted by the membrane to be taken away by the shearing force generated by the supernatant fluid flowing parallel to the surface of the membrane, thereby leading the pollution blocking layer formed by the residual particles on the surface of the membrane to be thinner. While the supernatant forms a concentrated water as the concentration of particulate increases.
Through the above process, the treatment of the desulfurization wastewater of the flue gas washing of the ship is realized, the produced water is discharged out of the ship after reaching the standard, the concentrated solution and the waste solution generated by each unit are discharged into the waste solution collecting device, and finally the concentrated solution and the waste solution are delivered to the qualified enterprises in ports for recovery treatment, so that the amount of the original desulfurization wastewater is greatly reduced, and the economic burden of the ship is reduced.
The invention provides a ship flue gas washing desulfurization wastewater treatment device and a washing desulfurization wastewater treatment method, wherein a membrane reactor is vertically arranged into a hollow flat membrane array in a cross-flow filtration mode based on a hollow flat membrane, and the hollow flat membrane is adopted and can be used for filtering under lower external pressure, so that the energy consumption is reduced; the cleaning tank integrates the functions of water production backwashing and drug washing, and the membrane reactor is cleaned regularly to ensure the long-term stable operation of the process device.
Claims (9)
1. A ship flue gas washing desulfurization wastewater treatment device is characterized by comprising a pre-settling tank, a membrane reactor, a cleaning tank, a dosing unit and a waste liquid collecting device;
wherein, the pre-settling tank, the membrane reactor, the cleaning tank, the dosing unit and the waste liquid collecting device are connected through pipelines;
the pre-settling tank is a hollow tank body, the top of the tank body is provided with a medicament inlet, the upper part of the tank body is provided with a supernatant outlet, the lower part of the tank body is provided with a wastewater inlet, and the bottom of the tank body is provided with a concentrated solution discharge port; the pre-settling tank is connected with the dosing unit through a medicament inlet at the top;
the membrane reactor consists of a cylindrical reactor shell, a hollow flat membrane array and a produced water collector; wherein the hollow flat membrane array is positioned at the middle lower part in the reactor shell, and the upper part of the hollow flat membrane array is connected with a water production collector; the bottom of the reactor shell is provided with a supernatant inlet, a raffinate discharge outlet and a compressed air connector; the top of the reactor shell is provided with a water outlet; a concentrated water return port is arranged at the position of the reactor shell corresponding to the water production collector; the hollow flat membrane array is formed by vertically arranging a plurality of hollow flat membranes along the circumference of a membrane reactor; the water production collector is formed by sequentially connecting a water production discharge pipe at the top, a water collecting tray at the middle part and a water production interface at the bottom, the top of the water production discharge pipe penetrates out of a water production outlet of the membrane reactor and is fixed and sealed by adopting a rotary locking structure, and the water production interface at the bottom of the water production collector is connected with a water production port at the top end of the hollow flat membrane;
the waste liquid collecting device is a hollow tank body or a sealed cabin;
the pre-settling tank is connected with the dosing unit through a medicament inlet at the top, a supernatant outlet of the pre-settling tank is connected with a supernatant inlet of the membrane reactor, a concentrated liquid discharge port of the pre-settling tank is connected with a waste liquid collecting device, and a residual liquid discharge port of the membrane reactor is connected with the waste liquid collecting device; a pipeline connected with a concentrated water return port of the membrane reactor branches off one pipeline to be converged with a pipeline between a residual liquid discharge port and a waste liquid collecting device of the membrane reactor, and the tail end of the pipeline connected with the concentrated water return port of the membrane reactor is converged to a pipeline connected with a waste water inlet of a pre-settling tank; a water production outlet of the membrane reactor is connected with a water production inlet of the cleaning tank; a pipeline connected with a medicine washing liquid outlet of the washing tank is converged with a pipeline between a residual liquid discharge port of the membrane reactor and the waste liquid collecting device; the residual liquid discharge port of the cleaning tank is connected with a waste liquid collecting device; the circulation outlet of the cleaning tank is connected with the circulation inlet.
2. The process and the device for treating the wastewater generated by washing and desulfurizing the flue gas of the ship according to claim 1 are characterized in that: the water collecting tray is of a hollow disc structure, the water producing interfaces are tubular and are arranged along the edge of the water collecting tray, and the lower ends of the water producing interfaces are connected with the upper end of the hollow flat membrane array and used for collecting water produced on the inner side of the hollow flat membrane array.
3. The process and the device for treating the wastewater generated by washing and desulfurizing the flue gas of the ship according to claim 1 are characterized in that: the hollow flat membrane is a ceramic flat membrane.
4. The process and the device for treating the wastewater generated by washing and desulfurizing the flue gas of the ship according to claim 1 are characterized in that: the ceramic flat plate membrane is made of one or more of silicon carbide, aluminum oxide, zirconium oxide and silicon oxide.
5. The process and the device for treating the wastewater generated by washing and desulfurizing the flue gas of the ship according to claim 1 are characterized in that: the aperture of the ceramic flat membrane plate is 0.1-1 micron.
6. The method for treating the ship flue gas washing desulfurization wastewater by using the ship flue gas washing desulfurization wastewater treatment device as set forth in any one of claims 1 to 5, is characterized by comprising the following steps:
1) desulfurization wastewater is introduced into a pre-settling tank from a wastewater inlet of the pre-settling tank, a medicine adding unit adds a medicine into the pre-settling tank, partial particles in the wastewater rapidly settle to the bottom of the pre-settling tank to form a concentrated solution under the auxiliary action of the added medicine, the concentrated solution is periodically discharged into a waste liquid collecting device through a concentrated solution discharge port of the pre-settling tank, and supernatant liquid with lower content of the particles at the upper part after settlement is obtained;
2) compressed air is used for aerating the membrane reactor through a compressed air interface, settled supernatant enters the membrane reactor from a supernatant inlet of the membrane reactor and is filtered by a hollow flat membrane, particulate matters in the supernatant are filtered and retained on the hollow flat membrane, water filtered and entering the inner side of the hollow flat membrane is produced water, water with the concentration of the particulate matters retained on the outer side of the hollow flat membrane being improved is concentrated water, and the concentrated water flows out from a concentrated water return port; returning one part of the outflow concentrated water from the wastewater inlet of the pre-settling tank to the pre-settling tank, and shunting and discharging the other part of the outflow concentrated water to a waste liquid collecting device;
3) the produced water enters a produced water collector from the inner side of the hollow flat membrane and is discharged to a cleaning tank from a produced water outlet along the directions of a produced water interface, a water collecting tray and a produced water discharge pipe; the produced water stored in the cleaning tank flows back to the membrane reactor to carry out backwashing on the hollow flat membrane array from inside to outside in the backwashing period; the water is discharged out of the ship through a water production discharge port of the cleaning tank during the non-backwashing period;
4) the time period of drug washing: running water is injected into the cleaning tank through the tap water connector, the chemical adding port injects a chemical lotion into the cleaning tank, the chemical lotion is stirred and prepared in the cleaning tank through self circulation of the chemical lotion in the circulation outlet and the circulation inlet, then the chemical lotion enters the membrane reactor through the chemical lotion outlet of the cleaning tank to perform chemical washing on the hollow flat membrane, and residual liquid after the chemical washing is discharged into the waste liquid collecting device through a residual liquid discharge port of the cleaning tank.
7. The method of claim 6, wherein the agent is an organic flocculant or an inorganic flocculant.
8. The method of claim 7, wherein the organic flocculant is polyacrylamide; the inorganic flocculant is polyaluminium chloride.
9. The method as claimed in claim 6, wherein the medicinal lotion is a cleaning agent and a soaking agent, the cleaning agent is an aqueous solution containing hydrochloric acid and citric acid, wherein the hydrochloric acid mass concentration is 4%, and the citric acid mass concentration is 2%; the soaking agent is an aqueous solution with the sodium hypochlorite concentration of 1-5 mmol/L.
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