Composite anaerobic MBR ship multi-source sewage treatment device and cooperative treatment method

Abstract

The invention discloses a composite anaerobic MBR ship multi-source sewage treatment device and a cooperative treatment method, and the device comprises: a reactor shell provided with a water inlet I, a sampling port I, a water inlet II and a sampling port II; an anaerobic chamber and a membrane chamber which are communicated in sequence are arranged in the shell; the water inlet I is communicated with the bottom of the anaerobic chamber; the sampling port I is communicated with the top; the water inlet II is communicated with the bottom of the membrane chamber; stirrers are arranged in the anaerobic chamber and the membrane chamber, and a circulating air inlet, a membrane assembly and a membrane assembly water pipe are further arranged in the membrane chamber; the anaerobic chamber is communicated with the membrane chamber through an overflow plate and a baffle plate; the treated sewage passes through a membrane component water pipe, a suction pump, a liquid three-way valve and a water outlet pipe to carry out backwashing on the membrane component; gas outlets are formed in the top ends of the anaerobic chamber and the membrane chamber, treated gas is discharged from the gas outlets and enters the membrane assembly from a circulating gas inlet in the membrane chamber for backwashing, cleaner and more environment-friendly internal circulating backwashing is realized, membrane pollution is efficiently prevented and relieved, and synchronous removal of carbon, nitrogen and sulfur pollutants is promoted.

Description

Technical Field

[0001] The present invention relates to the technical field of ship sewage treatment, and in particular to a composite anaerobic MBR ship multi-source sewage treatment device and a coordinated treatment method. Background Art

[0002] With the increasing awareness of marine protection worldwide, the standards implemented by IMO have become more stringent, and higher requirements have been put forward for ship sewage treatment equipment, including the emission control of total nitrogen and total sulfur. In particular, MARPOL Annex I has more detailed restrictions and treatment requirements for oily sewage discharge. This move requires that almost all processes and devices based on the old resolution must be improved to meet the new standard requirements. The ship MBR domestic sewage treatment technology is an efficient sewage treatment method produced by the organic combination of membrane separation technology and biochemical treatment technology. It has strong impact resistance, anti-swaying ability and stable treatment capacity, and has broad application prospects in the field of ship sewage treatment.

[0003] Although marine MBR has many advantages mentioned above, from the perspective of maintenance and operating costs, membrane fouling and energy consumption during the operation of MBR are still bottlenecks that limit its efficient application. Membrane fouling requires the MBR to be cleaned or even replaced after a period of operation, which greatly increases the operating cost. The high energy consumption and high cost of aeration in traditional MBR, as well as the complex operation of multi-process treatment, have restricted the promotion and development of MBR. In order to reduce the volume of ship sewage treatment equipment, improve removal efficiency, maintain treatment stability, and reduce membrane fouling, it is necessary to study the integrated MBR of marine anaerobic equipment.

[0004] In addition, there is a problem of insufficient carbon source in the treatment process of ship exhaust gas washing waste liquid. If the ship's oily sewage and ship's domestic sewage are mixed and treated and then synergistically with the ship's exhaust gas washing liquid, it can not only overcome the problem of high cost of external carbon source, but also save space; while desulfurizing and denitrifying the washing liquid, it also achieves the effect of deep treatment of emulsified oil, that is, further removing residual protein and other organic matter and sulfide in ship's domestic sewage and ship's oily sewage. Therefore, it is urgent to develop resource-based, integrated, easy-to-operate and low-cost ship sewage treatment equipment. Summary of the invention

[0005] The present invention provides a composite anaerobic MBR ship multi-source sewage treatment device and a coordinated treatment method, so as to overcome the technical problems that the traditional sewage treatment technology is a multi-process combination device, the operation is complicated, the degree of automation is low, the occupation area is large, the energy consumption is high, the treatment efficiency is low, and the cost in the wastewater treatment process remains high.

[0006] In order to achieve the above object, the technical solution of the present invention is:

[0007] A composite anaerobic MBR ship multi-source sewage treatment device comprises: a reactor shell, wherein the reactor shell is provided with a water inlet I, a sampling port I, a sampling port II and a water inlet II;

[0008] The reactor shell is provided with an anaerobic chamber and a membrane chamber which are connected in sequence; the water inlet I is connected with the bottom of the anaerobic chamber, and the sampling port I is connected with the top of the anaerobic chamber; the water inlet II is connected with the bottom of the membrane chamber, and the sampling port II is connected with the top of the membrane chamber; the anaerobic chamber and the membrane chamber are provided with a stirrer, and the membrane chamber is also provided with a circulating air inlet and a membrane assembly; the anaerobic chamber and the membrane chamber are connected through an overflow plate and a baffle; a membrane assembly water pipe is provided in the membrane chamber, and the treated sewage is discharged to an external water collection tank through the membrane assembly water pipe, a suction pump, a liquid three-way valve and a water outlet pipe, and liquid is extracted from the water collection tank to backwash the membrane assembly;

[0009] The anaerobic chamber and the top of the membrane chamber are both provided with air outlets, and the treated gas is discharged from the air outlets through the gas pipeline, the circulation valve and the circulation gas pipeline, and enters from the circulation air inlet in the membrane chamber to backwash the membrane assembly.

[0010] Furthermore, it also includes a gas collecting device and a gas three-way valve; one end of the gas collecting device is connected to the gas pipeline through the gas three-way valve; the other end of the gas collecting device is connected to one end of the circulating gas pipeline through a circulating valve; the circulating gas pipeline is connected to the circulating gas inlet.

[0011] Furthermore, the anaerobic chamber further comprises a suspended filler device, and the suspended filler device is arranged on both sides of the mixer in the anaerobic chamber.

[0012] Furthermore, it also includes a backwash branch pipe, one end of which is connected to one end of the liquid three-way valve, and the other end of which is connected to an external water tank, for drawing clean water from the outside to backwash the membrane assembly.

[0013] Furthermore, it also includes a first pressure gauge, a second pressure gauge and a pressure relief valve; the first pressure gauge is arranged on the gas collecting device, and the second pressure gauge is arranged between the membrane module water pipe and the suction pump; the pressure relief valve is arranged on the gas collecting device to reduce the pressure of the gas collecting device.

[0014] A method for collaboratively treating sewage from multiple sources on a ship, comprising:

[0015] S1: Determine the anaerobic sludge to be inoculated, the anaerobic sludge includes oil degradation anaerobic sludge, sulfate reduction sludge and desulfurization and denitrification sludge; the oil degradation anaerobic sludge is used to treat ship oily sewage, the sulfate reduction sludge is used to treat ship domestic sewage and exhaust gas desulfurization and denitrification washing waste liquid, and the desulfurization and denitrification sludge is used to treat ship exhaust gas washing waste liquid;

[0016] S2: The domesticated oil-degrading anaerobic sludge is inoculated into the anaerobic chamber, the desulfurization and denitrification sludge is inoculated into the membrane chamber, and the sulfate-reducing sludge is randomly inoculated into the anaerobic chamber or the membrane chamber to obtain oil-removing mixed sludge or denitrification mixed sludge; the ship's oily sewage enters the anaerobic chamber through the water inlet Ⅰ, the ship's exhaust gas washing waste liquid enters the membrane chamber through the water inlet Ⅱ, and the ship's domestic sewage enters the anaerobic chamber or the membrane chamber where the sulfate-reducing sludge is located through the water inlet Ⅰ or the water inlet Ⅱ, and is mixed with the ship's oily sewage or the ship's exhaust gas washing waste liquid to obtain an oil-containing mixed liquid or a washing mixed liquid;

[0017] S3: The ship's oily sewage or oily mixed liquid is mixed with the oil-degrading anaerobic sludge or de-oiled mixed sludge under the action of the mixer, and hydrolysis and acidification reactions, oil degradation reactions and sulfate reduction reactions occur. The treated sewage overflows into the membrane chamber through the overflow plate and baffle between the anaerobic chamber and the membrane chamber, and the generated gas is discharged from the gas outlet and enters the gas collecting device through the gas pipeline and the gas three-way valve;

[0018] S4: The waste liquid from ship exhaust gas washing or the mixed washing liquid is mixed with the sewage treated in the anaerobic chamber and the desulfurization and denitrification sludge or the denitrification mixed sludge under the action of the mixer, and an autotrophic denitrification reaction, a heterotrophic denitrification reaction or an autotrophic / heterotrophic denitrification-sulfate reduction coupling reaction occurs, and the generated gas is discharged from the gas outlet and enters the gas collecting device through the gas pipeline and the gas three-way valve;

[0019] S5: The sewage treated in S4 is filtered by the membrane assembly and flows out from the water pipe of the membrane assembly, and enters the water collecting tank through the suction pump, the outlet pipe and the liquid three-way valve. The liquid is extracted from the water collecting tank under the action of the suction pump and flows back into the outlet pipe to backwash the membrane assembly; the gas in the gas collecting device reaches the bottom of the membrane assembly from the circulating air inlet through the circulating gas pipeline through the circulating valve to flush the membrane assembly.

[0020] Furthermore, when the value of the second pressure gauge is between 30 and 40 KPa, the suction pump and the circulation valve are started to perform gas and liquid backwashing on the membrane assembly.

[0021] Furthermore, the outlet water and backwashing of the membrane module share a suction pump, and the pumping and stopping time is consistent with the backwashing time.

[0022] Beneficial effects: The present invention provides a composite anaerobic MBR ship multi-source sewage treatment device, which has the following advantages:

[0023] 1. By optimizing the design of the anaerobic chamber and membrane chamber, this device can selectively mix and centrally treat the domestic sewage of ships with oily sewage or exhaust gas washing liquid. Adding fillers in the anaerobic chamber helps to promote the enrichment of microorganisms and prevent their loss, thereby fixing the functional bacterial flora. The membrane assembly combines the stirring mechanism on the inside of the membrane to form a cross-flow flow, which significantly reduces membrane fouling. The device can reduce energy consumption and save hull space. By strengthening the action of microorganisms, it achieves the goal of efficient in-situ synergistic removal of multiple pollutants.

[0024] 2. The anaerobic treated sewage enters the anaerobic membrane biological reactor area (MBR area) through the baffles, which can effectively prevent the sludge from flowing back and accumulating at the bottom of the baffle area.

[0025] 3. Improve the traditional membrane bioreactor (MBR) process and add multiple gas backwashing and effluent backwashing internal circulation systems. This not only maintains the reactor's efficient processing capacity, but also effectively prevents and reduces membrane pollution through green and environmentally friendly internal circulation backwashing technology. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative labor.

[0027] Figure 1 A schematic diagram of the structure of a composite anaerobic MBR ship multi-source sewage treatment device provided by the present invention;

[0028] Figure 2 A flow chart of a method for collaboratively treating multi-source sewage from ships provided by the present invention;

[0029] Figure 3 The oil removal rate and SO4 in the anaerobic chamber of an embodiment of the present invention are shown in FIG. 2- Removal rate and TOC removal rate diagram;

[0030] Figure 4 NO3 in the membrane chamber of an embodiment of the present invention - And TOC removal efficiency diagram;

[0031] Figure 5 It is a schematic diagram of oil removal rate and TOC removal rate in an anaerobic chamber in another embodiment of the present invention;

[0032] Figure 6 Another embodiment of the present invention is NO3 in the membrane chamber - 、SO4 2-Schematic diagram of removal efficiency and TOC removal rate.

[0033] In the figure, 1, reactor shell; 2, anaerobic chamber; 3, membrane chamber; 4, mixer; 5, air outlet; 6, gas collecting device; 7, first pressure gauge; 8, gas three-way valve; 9, circulation valve; 10, membrane module water pipe; 11, suction pump; 12, water outlet pipe; 13, circulation gas pipeline; 14, second pressure gauge 15, liquid three-way valve; 16, backwash branch pipe; 17, gas pipeline; 18, overflow plate; 19, baffle; 21, water inlet I; 22, mud outlet; 23, sampling port I; 24, suspended filler device; 25, sampling port II; 26, circulation air inlet; 27, water inlet II; 28, membrane module; 29, overflow weir; 30, first stirring paddle; 31, second stirring paddle; 32, pressure relief valve. DETAILED DESCRIPTION

[0034] In order to make the purpose, technical solution and advantages of the embodiments of the present invention clearer, the technical solution in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0035] This embodiment provides a composite anaerobic MBR ship multi-source sewage treatment device, such as Figure 1 As shown, the reactor shell 1 is provided with a water inlet Ⅰ21, a sampling port Ⅰ23, a sampling port Ⅱ25 and a water inlet Ⅱ27;

[0036] The reactor shell 1 is provided with an anaerobic chamber 2 and a membrane chamber 3 which are connected in sequence; the water inlet I 21 is connected to the bottom of the anaerobic chamber 2, and the sampling port I 23 is connected to the top of the anaerobic chamber 2; the water inlet II 27 is connected to the bottom of the membrane chamber 3, and the sampling port II 25 is connected to the top of the membrane chamber 3; a stirrer 4 is provided inside the anaerobic chamber 2 and the membrane chamber 3, and a circulating air inlet 26 and a membrane assembly 28 are also provided in the membrane chamber 3; the anaerobic chamber 2 and the membrane chamber 3 are connected through an overflow plate 18 and a baffle 19; a membrane assembly water pipe 10 is provided in the membrane chamber 3, and the treated sewage is discharged to an external water collection tank through the membrane assembly water pipe 10, a suction pump 11, a liquid three-way valve 15 and a water outlet pipe 12, and liquid is extracted from the water collection tank to backwash the membrane assembly 28;

[0037] The tops of the anaerobic chamber 2 and the membrane chamber 3 are both provided with gas outlets 5. The treated gas is discharged from the gas outlets 5 through the gas pipeline 17, the circulation valve 9 and the circulation gas pipeline 13, and enters the membrane assembly 28 from the circulation air inlet 26 in the membrane chamber for backwashing.

[0038] Specifically, the reactor shell is closed, and air outlets and exhaust pipes are provided at the top of the anaerobic chamber and the membrane chamber. Water inlets are provided at the bottom of the anaerobic chamber and the membrane chamber, and wastewater enters the anaerobic chamber and the membrane chamber from the water inlets; sampling ports are provided at the top of the left and right sides for sampling and testing the treated wastewater; a sludge discharge port is provided at the bottom of the anaerobic chamber, and the residual sludge in the anaerobic chamber after treatment can be discharged from the sludge discharge port; an air circulation air inlet is provided at the bottom of the membrane chamber, which can be used as a sludge discharge port. The yield of anaerobic microorganisms themselves is low, and the residue can be removed through microbial metabolism. Therefore, the device does not need to discharge the residual sludge. If sludge discharge and maintenance are required, they can be completed through the reverse operation of the circulating air inlet. The gas collected after treatment enters from the circulating air inlet to backwash the membrane assembly; a stirrer is provided inside the anaerobic chamber and the membrane chamber to promote full mixing of sludge and wastewater, and at the same time make the fluid in the membrane chamber in a dynamic form, which can reduce membrane pollution; the membrane chamber environment is anaerobic, and a membrane assembly is provided in the membrane chamber, which is a plate structure or a ring structure, and is composed of one or more curtain-like membranes;

[0039] An overflow weir 29 is provided at the top of the anaerobic chamber, which is connected to the overflow plate and the baffle plate. The overflow plate and the baffle plate are staggered up and down, so that the water flows into the membrane chamber in a push flow manner, which is more efficient; the vertical height of the overflow weir 29 is 0.5cm-1.0cm, and an inclined plate is provided at the bottom of the baffle plate, with an inclination angle of 45°-60°, and the distance between the baffle plate and the overflow plate is 3-5cm.

[0040] In a specific embodiment, it also includes a gas collecting device 6 and a gas three-way valve 8; one end of the gas collecting device 6 is connected to the gas pipeline 17 through the gas three-way valve 8; the other end of the gas collecting device 6 is connected to one end of the circulating gas pipeline 13 through the circulating valve 9; the circulating gas pipeline 13 is connected to the circulating gas inlet 26.

[0041] This solution sets up a gas collection device that can collect various gases generated after sewage treatment. Through the circulation valve and the circulating gas pipeline, the generated gas is circulated inside the device to backwash the membrane components, reduce membrane pollution, and realize a cleaner, greener and more environmentally friendly internal circulation backwashing treatment method.

[0042] In a specific embodiment, the anaerobic chamber 2 further includes a suspended filler device 24, and the suspended filler device 24 is arranged on both sides of the mixer 4 in the anaerobic chamber 2;

[0043] The mixer 4 includes a first stirring paddle 30 and a second stirring paddle 31. The bottom stirring paddle is 5-8 cm away from the bottom of the shell, and is 2 cm-4 cm away from the upper stirring paddle. The double-paddle stirring is used to enhance the mass transfer capacity of the reaction device, so that the sewage is fully in contact with the activated sludge microorganisms, thereby improving the system treatment efficiency.

[0044] In this scheme, a suspended filler device is set up to dynamically fix sulfate-reducing bacteria, prevent sludge loss, and at the same time increase the contact area between sewage and microorganisms to improve degradation efficiency.

[0045] In a specific embodiment, a backwash branch pipe 16 is further included, one end of which is connected to one end of the liquid three-way valve 15, and the other end of which is connected to an external water tank for drawing clean water from the outside to backwash the membrane assembly 28.

[0046] In this scheme, an external backwash branch is connected, and clean water can be pumped from the outside to backwash the membrane components when the internal circulating sewage is insufficient.

[0047] In a specific embodiment, it also includes a first pressure gauge 7, a second pressure gauge 14 and a pressure relief valve 32; the first pressure gauge 7 is arranged on the gas collecting device 6, and the second pressure gauge 14 is arranged between the membrane module water pipe 10 and the suction pump 11; the pressure relief valve 32 is arranged on the gas collecting device 6, and is used to reduce the pressure of the gas collecting device 6.

[0048] A first pressure gauge is set to judge the air pressure in the gas collecting device. When the air pressure exceeds the specified value, the pressure relief valve is opened to release the pressure. A second pressure gauge is set. When the pressure difference between the inside and outside of the membrane chamber reaches 30-40Kpa, the circulation valve and the suction pump are opened to continuously backwash the membrane chamber.

[0049] This embodiment also provides a method for coordinating treatment of multi-source sewage from ships, such as Figure 2 As shown, including:

[0050] S1: Determine the anaerobic sludge to be inoculated, the anaerobic sludge includes oil degradation anaerobic sludge, sulfate reduction sludge and desulfurization and denitrification sludge; the oil degradation anaerobic sludge is used to treat ship oily sewage, the sulfate reduction sludge is used to treat ship domestic sewage and exhaust gas desulfurization and denitrification washing waste liquid, and the desulfurization and denitrification sludge is used to treat ship exhaust gas washing waste liquid;

[0051] S2: the domesticated oil-degrading anaerobic sludge is inoculated into the anaerobic chamber 2, the desulfurization and denitrification sludge is inoculated into the membrane chamber 3, and the sulfate-reducing sludge is randomly inoculated into the anaerobic chamber 2 or the membrane chamber 3 to obtain the oil-removing mixed sludge or the denitrification mixed sludge; the ship's oily sewage enters the anaerobic chamber 2 through the water inlet Ⅰ21, the ship's exhaust gas washing waste liquid enters the membrane chamber 3 through the water inlet Ⅱ27, and the ship's domestic sewage enters the anaerobic chamber 2 or the membrane chamber 3 where the sulfate-reducing sludge is located through the water inlet Ⅰ21 or the water inlet Ⅱ27, and is mixed with the ship's oily sewage or the ship's exhaust gas washing waste liquid to obtain an oil-containing mixed liquid or a washing mixed liquid;

[0052] S3: The ship's oily sewage or oily mixed liquid is mixed with the oil-degrading anaerobic sludge or the de-oiled mixed sludge under the action of the mixer 4, and hydrolysis and acidification reaction, oil degradation reaction and sulfate reduction reaction occur. The treated sewage overflows into the membrane chamber 3 through the overflow plate 18 and the baffle plate 19 between the anaerobic chamber 2 and the membrane chamber 3, and the generated gas is discharged from the gas outlet 5 and enters the gas collecting device 6 through the gas pipeline 17 and the gas three-way valve 8;

[0053] S4: The waste liquid from ship exhaust gas washing or the mixed washing liquid is mixed with the sewage treated in the anaerobic chamber 2 and the desulfurization and denitrification sludge or the denitrification mixed sludge under the action of the mixer 4, and an autotrophic denitrification reaction, a heterotrophic denitrification reaction or an autotrophic / heterotrophic denitrification-sulfate reduction coupling reaction occurs, and the generated gas is discharged from the gas outlet 5 and enters the gas collecting device 6 through the gas pipeline 17 and the gas three-way valve 8;

[0054] S5: The sewage treated by S4 is filtered by the membrane assembly 28, flows out from the membrane assembly water pipe 10, and enters the water collecting tank through the suction pump 11, the outlet pipe 12 and the liquid three-way valve 15. Under the action of the suction pump 11, the liquid is extracted from the water collecting tank and returned to the outlet pipe 12 to backwash the membrane assembly 28; the gas in the gas collecting device 6 reaches the bottom of the membrane assembly 28 from the circulating gas inlet 26 through the circulating gas pipeline 13 through the circulating valve 9 to flush the membrane assembly 28.

[0055] Specifically, one of the methods is:

[0056] The domesticated de-oiling sludge and sulfate-reducing sludge are inoculated into the anaerobic chamber and mixed in a one-to-one ratio. The desulfurization and denitrification sludge is inoculated into the membrane chamber. The ship's oily sewage and ship's domestic sewage enter the anaerobic chamber through the water inlet Ⅰ, and the ship's exhaust gas scrubbing liquid enters the membrane chamber through the water inlet Ⅱ.

[0057] The oily sewage from ships and the domestic sewage from ships are mixed under the action of a mixer to achieve full mixing of sludge and wastewater, and sulfate reduction reaction, hydrolysis acidification reaction and oil degradation reaction occur. The generated gases such as hydrogen sulfide, carbon dioxide and methane are discharged through the exhaust port and recycled; the sewage treated in the anaerobic chamber flows into the membrane chamber through the baffle plate and is mixed with the ship exhaust gas washing waste liquid in the membrane chamber, and an autotrophic denitrification reaction with sulfide as an electron donor and a heterotrophic denitrification reaction with the aforementioned residual organic matter as an electron donor occur; the generated various gases enter the gas collecting device through the gas pipeline, and the gas is controlled by the circulation valve to enter the circulating gas pipeline to backwash the membrane assembly;

[0058] The treated sewage is filtered by the membrane assembly through the outlet pipe and flows into the water collecting tank under the action of the suction pump. The membrane assembly stops pumping and backwashing starts at the same time. The valve is opened, and the outlet water flows back to the membrane assembly through the outlet pipe by the suction pump. The gas reaches the bottom of the membrane assembly through the circulating valve and the circulating gas pipeline, and the membrane assembly is flushed by the cyclone water distributor.

[0059] Another method is:

[0060] The anaerobic chamber is inoculated with domesticated oil-degrading anaerobic sludge, and the membrane chamber is inoculated with domesticated sulfate-reducing sludge and desulfurization and denitrification sludge. The waste liquid from ship exhaust gas washing and domestic sewage from the ship are passed into the membrane chamber. The ship's oily sewage is pumped into the anaerobic chamber. The sludge and wastewater in each chamber are fully mixed by a stirring paddle, and the organic matter is biochemically degraded. Hydrolysis and acidification reactions, oil degradation reactions, and sulfate reduction reactions occur in the reaction device. The generated gases such as hydrogen sulfide, carbon dioxide, and methane are discharged through the exhaust port and then recycled. The sewage treated in the anaerobic chamber flows into the membrane chamber through the baffle, and an autotrophic denitrification reaction, a heterotrophic denitrification reaction, or an autotrophic / heterotrophic denitrification-sulfate reduction coupling reaction occurs in the membrane chamber. The generated gas is collected to a gas collecting device through a gas pipeline.

[0061] The treated sewage is filtered by the membrane assembly through the outlet pipe and flows into the water collecting tank under the action of the suction pump. The membrane assembly stops pumping and backwashing starts at the same time. The valve is opened, and the outlet water flows back to the membrane assembly through the outlet pipe by the suction pump. The gas reaches the bottom of the membrane assembly through the circulating valve and the circulating gas pipeline, and the membrane assembly is flushed through the aeration pipe.

[0062] In this embodiment, the stirring speed of the stirrer is 150 rpm, the stirring is intermittent, the operating temperature is 25-35°C, and the hydraulic retention time of each reaction zone is 10-48h;

[0063] The sludge acclimation method is:

[0064] The sludge is domesticated by artificially simulating ship sewage. The HRT at the initial stage of domestication is 48 hours, and the HRT is reduced to 24 hours after the pollutant removal effect is stable. Natural seawater is used for both. The influent formula of sulfate reduction sludge is peptone and NaHCO3; the influent components of oil degradation sludge are emulsified diesel and NaHCO3; the denitrification sludge uses Na2S·9H2O, peptone, NaNO3, and NaHCO3; the pollutant removal rate of the denitrification and oil degradation sludge is more than 90%. Because seawater contains a large amount of sulfate, this method only needs to remove the sulfate generated by flue gas washing. Therefore, the sulfate removal rate of the anaerobic chamber sludge mainly composed of sulfate-reducing bacteria reaches 70% or more, which means that the sludge is successfully domesticated.

[0065] The concentration of the desulfurization and denitrification sludge inoculated into the membrane chamber is 2500-4500 mg / L MLVSS; the concentration of the anaerobic chamber sludge mainly containing sulfate-reducing bacteria inoculated into the anaerobic chamber is 2000-4000 mgMLVSS / L.

[0066] In a specific embodiment, when the value of the second pressure gauge 14 is between 30 and 40 KPa, the suction pump 11 and the circulation valve 9 are started to perform gas and liquid backwashing on the membrane assembly 28 .

[0067] A second pressure gauge is provided to monitor the transmembrane pressure difference. When the pressure difference is 30-40 KPa, the suction pump and the circulation valve are started to perform gas and liquid backwashing on the membrane assembly 28. Backwashing can be strengthened during normal operation to prevent excessive internal and external pressure difference and incomplete cleaning.

[0068] In a specific embodiment, the water outlet and backwashing of the membrane assembly 28 share a suction pump 11, and the pumping stop time is consistent with the backwashing time.

[0069] The pumping and stopping time of the membrane assembly is consistent with the backwashing time. The pumping time of the membrane assembly is 8 minutes, and the pumping and stopping time is 1 minute.

[0070] In this scheme, the membrane assembly suction stop time is consistent with the backwashing start time, and the membrane assembly can be backwashed immediately after the membrane assembly suction is completed, thereby improving the efficiency of sewage treatment.

[0071] The processing flow of this device is:

[0072] (1) Activated sludge acclimation

[0073] Anaerobic sludge is inoculated from the secondary sedimentation tank of the municipal sewage plant, inoculated into a continuous stirring reactor, and then seawater with organic matter is introduced and left to stand for 15 days. The first stirring is carried out while the water is changed. After 15 days, simulated wastewater is added to the sewage. The components of ship oily sewage: emulsified diesel 212mg / L, NaHCO3 is added in appropriate amounts according to pH; the components of ship domestic sewage: peptone 1.92g / L, NaHCO3 is added in appropriate amounts according to pH; ship exhaust gas washing waste liquid: peptone 0.17g / L, NaNO3 0.93g / L, Na2S 9H2O3.25g / L, NaHCO3 is added in appropriate amounts according to pH. Among them, the overall environment is alkaline, and the influent is diluted with natural seawater. The HRT is 48h. When the oil removal rate of oily sewage is above 90%, it means that the activated sludge has been successfully domesticated, and the SO4 of ship domestic sewage 2- A removal rate of more than 90% indicates that the domestication of sulfate-reducing bacteria SRB is successful. 2- The removal rate is more than 90%, NO3 -A removal rate of more than 90% indicates that the desulfurization and denitrification bacteria have been successfully domesticated. At this time, the HRT is reduced to 24h and the domestication is completed.

[0074] (2) Reactor startup and operation

[0075] The domesticated SRB and desulfurized and oil-removed sludge are added to the reactor in a ratio of 1:1. The water inlet time and components are consistent with the sludge domestication stage. After mixing in the water inlet tank, they are pumped into the anaerobic chamber with a continuous stirring speed of 150rpm. The organic matter is biochemically degraded, and hydrolysis acidification, oil degradation and sulfate reduction reactions occur in the reaction device. The desulfurized and denitrified sludge is inoculated into the membrane chamber of the reactor with an MLVSS of 2500-4500mg / L and a stirring speed of 150rpm. The pumping and stopping time of the membrane chamber outlet pipe is consistent with the backwashing time, 8min for filtration and 1min for backwashing. The hydraulic retention time of the reaction zone is 24h at first, and water is fed intermittently first. After the pollutant removal rate is stable, continuous water inflow is switched.

[0076] (3) Reaction mechanism and removal rate

[0077] In the anaerobic chamber, hydrolysis and acidification reactions and oil degradation reactions mainly occur. Organic matter in oily wastewater is adsorbed by microorganisms on the surface of microorganisms and then enters the cells, where it is gradually metabolized and degraded by microorganisms. Complex organic compounds are decomposed into simple metabolites, releasing harmless substances such as carbon dioxide and water. In addition, the macromolecular organic matter provided by ship sewage provides electron donors for sulfate-reducing bacteria. Sulfate and organic matter are efficiently converted into sulfide and carbon dioxide, and nitrate is heterotrophically denitrified into nitrogen. Desulfurization and denitrification reactions occur in the membrane chamber, and sulfide and nitrate are converted into elemental sulfur and nitrogen. Figure 3 As shown, in the anaerobic chamber, the oil removal rate can reach more than 90%, the organic matter removal rate can reach 95%, and the SO4 2- The removal rate can reach more than 77%; Figure 4 As shown, in the membrane chamber NO3 - The removal rate can reach over 99%, and the organic matter removal rate can reach over 99%.

[0078] Another processing flow of this device is as follows:

[0079] (1) Domestication of activated sludge

[0080] Anaerobic sludge was inoculated from the sewage plant and inoculated into a stirred reactor. After the seawater was introduced, it was allowed to stand for 15 days. The first stirring was carried out while the water was changed. After 15 days, simulated wastewater was added to the sewage. The formulas were as follows: ship oily sewage: oil concentration 212 mg / L, NaHCO3 was added in appropriate amount according to pH; ship domestic sewage: peptone 1.92 g / L, NaHCO3 was added in appropriate amount according to pH; ship exhaust gas scrubbing liquid: peptone 0.17 g / L, NaNO3 0.93 g / L, Na2S 9H2O3.33 g / L, NaHCO3 was added in appropriate amount according to pH. The overall environment was alkaline, and the influent was natural seawater. The initial hydraulic retention time was 48 h, and the pollutant removal rate was changed to 24 h after it stabilized. When the oil removal rate of the activated sludge treating oily sewage was above 90%, it indicated that the acclimation was successful. SRB, that is, the activated sludge SO4 2- A removal rate of more than 70% indicates successful acclimatization. The desulfurization and denitrification sludge of ship exhaust gas scrubbing liquid is acclimatized to treat S 2- The removal rate is more than 90%, NO3 - A removal rate of more than 90% indicates successful acclimatization.

[0081] (2) Device startup

[0082] The domesticated activated sludge is inoculated into the reactors respectively, that is, the domesticated desulfurization and oil removal activated sludge is inoculated into the anaerobic chamber, the desulfurization and denitrification sludge and SRB are inoculated into the membrane chamber, the ship's oily sewage enters the anaerobic chamber from the bottom, and the ship's domestic sewage and ship's exhaust gas washing liquid are passed through the bottom of the membrane chamber. The water inlet time and formula are consistent with the sludge training stage, the operating temperature is 25-35℃, the stirring speed is 150rpm, and the stirring is continuous. The hydraulic retention time in the anaerobic chamber is 48h, and the hydraulic retention time in the membrane chamber is 24h. The membrane components are backwashed while filtering, that is, 8min of pumping, 1min of stopping, and starting the air-water backwashing device.

[0083] (3) Device operation

[0084] Under the action of microorganisms, the ship sewage in the anaerobic chamber degrades oil and other macromolecules into CO2 and water. The ship oily sewage enters the membrane chamber through the baffle in an up-and-down push flow manner, and the ship domestic sewage and ship exhaust gas washing liquid are introduced into the bottom of the membrane chamber shell. Under the action of microorganisms mainly composed of sulfate-reducing bacteria and denitrifying bacteria, the organic matter in the mixed sewage is removed, and the influent is desulfurized and denitrified. The pumping and stopping time of the membrane chamber outlet pipe and the suction pump is consistent with the backwashing time, and the pumping / stopping time is 8min / 1min, that is, 8min of filtration and 1min of backwashing; when the value of the first pressure gauge is at 30-40Kpa, start the suction pump to backwash the membrane assembly for 5min.

[0085] (4) Reaction mechanism and removal rate

[0086] Hydrolysis and acidification reactions, oil degradation reactions, and sulfate reduction reactions occur in the anaerobic chamber. Organic compounds in oily wastewater are first adsorbed or contacted by microorganisms. After being adsorbed on the surface of microorganisms or entering their cells, they begin to be degraded through metabolic processes. Complex organic compounds are broken down into simpler metabolites. Microorganisms use these newly degraded organic matter as a carbon source and energy source to promote their growth and metabolism. Microorganisms convert organic matter into simple and harmless substances such as carbon dioxide and water, and finally complete the degradation process. Autotrophic denitrification reactions, heterotrophic denitrification reactions, or autotrophic-heterotrophic denitrification-sulfate reduction coupling reactions mainly occur in the membrane chamber. Through the hydrocarbons provided by the ship's oily wastewater, sulfate-reducing bacteria resist the inhibition of the high-salt environment and shorten the startup time. At the same time, sulfate and organic matter are efficiently converted into sulfide and carbon dioxide, NO x The pollutants are converted into nitrogen. The pollutants in the sewage are removed in all directions, and the effluent is filtered through the membrane to ensure the turbidity and suspended solids concentration of the effluent. Figure 5 As shown in the figure, the oil removal rate in the anaerobic chamber can reach more than 90%, and the organic matter removal rate can reach 90%; Figure 6 As shown, in the membrane chamber NO3 - The removal rate can reach more than 99%, the organic matter removal rate can reach more than 95%, SO4 2- The removal rate can reach over 70%.

[0087] The beneficial effects of the device and the processing method are:

[0088] 1. The centralized treatment of domestic sewage and oily sewage or exhaust gas washing liquid from ships overcomes the waste caused by the addition of external carbon sources in traditional processes, saves energy consumption and reduces floor space, and realizes the efficient and coordinated removal of multiple pollutants under the action of enhanced microorganisms;

[0089] 2. The sewage treated in the anaerobic chamber directly enters the membrane chamber through the baffle plate, replenishing the nutrients of heterotrophic denitrifying bacteria and desulfurization denitrifying bacteria, improving the effluent effect and achieving the purpose of treating waste with waste;

[0090] 3. The composite anaerobic MBR process is adopted. The anaerobic chamber filler can enrich sulfate-reducing bacteria and oil-degrading bacteria, which can greatly improve the treatment efficiency, overcome the problems of high cost of traditional ship sewage treatment process and incomplete degradation of harmful substances, and has economic feasibility;

[0091] 4. Improve the traditional MBR process, use a variety of harmful gases for gas backwashing and effluent for liquid backwashing in an internal circulation device, while maintaining the high removal efficiency of the reactor, achieving a cleaner, greener and more environmentally friendly internal circulation backwashing treatment method.

[0092] 5. The present invention adopts bypass water inlet and backwashing, and stirs at the same time, so that the membrane system is in a dynamic form, which can effectively prevent and reduce membrane pollution;

[0093] 6. The sludge domestication of the present invention uses seawater to domesticate sulfate-reducing bacteria, desulfurization and denitrification bacteria and oil-degrading bacteria directly in a high-salt environment, promote the rapid formation of high-salt-tolerant microbial flora, and facilitate the efficient operation of the desulfurization and denitrification process under high-load and high-salt conditions. At the same time, sludge domestication can be carried out in advance on land, and the successfully domesticated activated sludge is directly inoculated into the reaction device on the ship, which greatly shortens the startup time of the device on the ship, is suitable for the ship operating environment, and does not need to occupy the limited space resources on the ship for sludge domestication.

[0094] 7. The device and treatment method of the present invention place ship domestic sewage, ship oily sewage and ship exhaust gas washing liquid in the same device for coordinated treatment, replacing the oil-water separator, secondary sedimentation tank, aeration tank and traditional biochemical tank, integrating the resource utilization of carbon, nitrogen and sulfur elements into one, and can simultaneously remove multiple pollutants in the water while effectively collecting resources such as methane, nitrogen and sulfur. It has the advantages of high degree of carbon, nitrogen and sulfur resource utilization in sewage, high treatment efficiency, low energy consumption, simple operation and integration.

[0095] 8. The H2S generated in the system is circulated to the membrane chamber as a supplementary substance to provide S for the autotrophic denitrifying bacteria. 2- , promoting the reaction.

[0096] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or replace some or all of the technical features therein with equivalents. However, these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A composite anaerobic MBR ship multi-source sewage treatment device, characterized in that: include: A reactor shell (1), wherein the reactor shell (1) is provided with a water inlet I (21), a sampling port I (23), a sampling port II (25) and a water inlet II (27); The reactor shell (1) is provided with an anaerobic chamber (2) and a membrane chamber (3) which are connected in sequence; the water inlet I (21) is connected to the bottom of the anaerobic chamber (2), and the sampling port I (23) is connected to the top of the anaerobic chamber (2); the water inlet II (27) is connected to the bottom of the membrane chamber (3), and the sampling port II (25) is connected to the top of the membrane chamber (3); a stirrer (4) is provided inside the anaerobic chamber (2) and the membrane chamber (3); (3) is also provided with a circulating air inlet (26) and a membrane assembly (28); the anaerobic chamber (2) and the membrane chamber (3) are connected via an overflow plate (18) and a baffle (19); a membrane assembly water pipe (10) is provided in the membrane chamber (3); the treated sewage is discharged to an external water collection tank via the membrane assembly water pipe (10), a suction pump (11), a liquid three-way valve (15) and a water outlet pipe (12), and liquid is extracted from the water collection tank to backwash the membrane assembly (28); The tops of the anaerobic chamber (2) and the membrane chamber (3) are both provided with gas outlets (5), and the treated gas is discharged from the gas outlets (5) through a gas pipeline (17), a circulation valve (9) and a circulation gas pipeline (13), and enters from a circulation air inlet (26) in the membrane chamber to backwash the membrane assembly (28).

2. The composite anaerobic MBR ship multi-source sewage treatment device according to claim 1 is characterized in that: It also includes a gas collecting device (6) and a gas three-way valve (8); one end of the gas collecting device (6) is connected to a gas pipeline (17) via the gas three-way valve (8); the other end of the gas collecting device (6) is connected to one end of a circulating gas pipeline (13) via a circulating valve (9); and the circulating gas pipeline (13) is connected to the circulating gas inlet (26).

3. The composite anaerobic MBR ship multi-source sewage treatment device according to claim 1 is characterized in that: The anaerobic chamber (2) further comprises a suspended filler device (24), and the suspended filler device (24) is arranged on both sides of the mixer (4) in the anaerobic chamber (2).

4. The composite anaerobic MBR ship multi-source sewage treatment device according to claim 1 is characterized in that: It also includes a backwash branch pipe (16), one end of which is connected to one end of the liquid three-way valve (15), and the other end of which is connected to an external water tank, for drawing clean water from the outside to backwash the membrane assembly (28).

5. The composite anaerobic MBR ship multi-source sewage treatment device according to claim 2 is characterized in that: It also includes a first pressure gauge (7), a second pressure gauge (14) and a pressure relief valve (32); the first pressure gauge (7) is arranged on the gas collecting device (6), and the second pressure gauge (14) is arranged between the membrane module water pipe (10) and the suction pump (11); the pressure relief valve (32) is arranged on the gas collecting device (6) and is used to reduce the pressure of the gas collecting device (6).

6. A method for coordinating treatment of multi-source sewage from ships based on the composite anaerobic MBR ship multi-source sewage treatment device according to claim 1, characterized in that: include: S1: Determine the anaerobic sludge to be inoculated, wherein the anaerobic sludge includes oil degradation anaerobic sludge, sulfate reduction sludge and desulfurization and denitrification sludge; The oil-degrading anaerobic sludge is used to treat ship oily sewage, the sulfate-reducing sludge is used to treat ship domestic sewage and waste gas desulfurization and denitrification washing waste liquid, and the desulfurization and denitrification sludge is used to treat ship exhaust gas washing waste liquid; S2: the domesticated oil-degrading anaerobic sludge is inoculated into the anaerobic chamber (2), the desulfurization and denitrification sludge is inoculated into the membrane chamber (3), and the sulfate-reducing sludge is randomly inoculated into the anaerobic chamber (2) or the membrane chamber (3) to obtain oil-removing mixed sludge or denitrification mixed sludge; the ship's oily sewage enters the anaerobic chamber (2) through the water inlet Ⅰ (21), the ship's exhaust gas washing waste liquid enters the membrane chamber (3) through the water inlet Ⅱ (27), and the ship's domestic sewage enters the anaerobic chamber (2) or the membrane chamber (3) where the sulfate-reducing sludge is located through the water inlet Ⅰ (21) or the water inlet Ⅱ (27), and is mixed with the ship's oily sewage or the ship's exhaust gas washing waste liquid to obtain an oil-containing mixed liquid or a washing mixed liquid; S3: The ship's oily sewage or oily mixed liquid is mixed with the oil-degrading anaerobic sludge or the de-oiled mixed sludge under the action of the mixer (4), and a hydrolysis and acidification reaction, an oil degradation reaction and a sulfate reduction reaction occur. The treated sewage overflows into the membrane chamber (3) through the overflow plate (18) and the baffle plate (19) between the anaerobic chamber (2) and the membrane chamber (3), and the generated gas is discharged from the gas outlet (5) and enters the gas collecting device (6) through the gas pipeline (17) and the gas three-way valve (8); S4: The waste liquid from ship exhaust gas washing or the mixed washing liquid is mixed with the sewage treated in the anaerobic chamber (2) and the desulfurization denitrification sludge or the denitrification mixed sludge under the action of the mixer (4), and an autotrophic denitrification reaction, a heterotrophic denitrification reaction or an autotrophic / heterotrophic denitrification-sulfate reduction coupling reaction occurs, and the generated gas is discharged from the gas outlet (5) and enters the gas collecting device (6) through the gas pipeline (17) and the gas three-way valve (8); S5: The sewage treated by S4 flows out from the water pipe (10) of the membrane assembly through the suction filtration action of the membrane assembly (28), enters the water collecting tank through the suction pump (11), the water outlet pipe (12) and the liquid three-way valve (15), and the liquid is drawn out from the water collecting tank under the action of the suction pump (11) and flows back into the water outlet pipe (12) to backwash the membrane assembly (28); the gas in the gas collecting device (6) reaches the bottom of the membrane assembly (28) from the circulation inlet (26) through the circulation valve (9) and the circulation gas pipeline (13), so as to flush the membrane assembly (28).

7. The method for coordinating treatment of multi-source sewage from ships according to claim 6, characterized in that: When the value of the second pressure gauge (14) is between 30 and 40 KPa, the suction pump (11) and the circulation valve (9) are started to perform gas and liquid backwashing on the membrane assembly (28).

8. The method for coordinating treatment of multi-source sewage from ships according to claim 6, characterized in that: The water outlet and backwashing of the membrane assembly (28) share a suction pump (11), and the suction stop time is consistent with the backwashing time.

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