Marine multi-stage anaerobic MBR device and ship multi-source sewage coordinated treatment method

Abstract

The invention discloses a multi-stage anaerobic MBR device for ships and a method for coordinating the treatment of multi-source sewage in ships, comprising: a reactor shell provided with sampling ports I, II and III; anaerobic chambers I, II and III which are sequentially connected to each other are provided in the shell; the sampling port I is connected to the anaerobic chamber I, the sampling port II is connected to the anaerobic chamber II, and the sampling port III is connected to the anaerobic chamber III; a stirrer is provided in the three anaerobic chambers, a membrane assembly and a cyclonic water distributor are provided in the anaerobic chamber III, and a drain outlet is provided at the bottom; baffles and vertical plates of the baffles are provided on both sides of the anaerobic chamber II; treated sewage flows out from the drain outlet and flows into the anaerobic chamber III through a backwashing water inlet pipe; exhaust holes are provided at the tops of the three anaerobic chambers, and treated gas is discharged from the exhaust holes and enters the anaerobic chamber III through a backwashing air inlet pipeline; the device sets pipelines for treated water and gas respectively, enhances the solubility of sulfide while backwashing the membrane assembly, reduces operating costs, strictly prevents membrane pollution, provides integrated ship sewage treatment equipment, and saves costs.

Description

Technical Field

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

[0002] Wastewater is no longer viewed as a source of pollution, but rather as a renewable resource with the potential to generate clean reused water, useful nutrients, and renewable energy. The resources extracted from wastewater treatment can effectively offset the operating costs of the treatment process, making it highly competitive. Ship organic wastewater (including domestic sewage and bilge oily water) contains large amounts of hazardous substances such as excreted organic matter and emulsified oil, while ship exhaust gas scrubbers contain large amounts of inorganic pollutants such as sulfates and nitrates. These substances can be recovered through appropriate on-site treatment technologies, effectively reducing waste.

[0003] Currently, membrane bioreactors (MBRs) are being used to treat domestic sewage on ships due to their ease of operation and small footprint, which improves water treatment efficiency. Traditional wastewater MBR processes are struggling to cope with the complex and diverse nature of wastewater treatment, and in-situ treatment technology on ships poses even greater challenges. Therefore, there is an urgent need to develop a cost-effective, stable, and compact in-situ treatment system for marine sewage to meet the increasingly stringent requirements of ship navigation. Summary of the Invention

[0004] The present invention proposes a ship-based multi-stage anaerobic MBR device and a method for co-treatment of ship-based multi-source sewage, so as to overcome the problems that traditional ship-based MBRs require frequent membrane cleaning, are complex to operate, and result in high energy consumption, high cost and low efficiency. It can also address the technical problems of insufficient backwash gas volume and insufficient carbon source.

[0005] In order to achieve the above object, the technical solution of the present invention is:

[0006] A marine multi-stage anaerobic MBR device comprises: a reactor shell, wherein the reactor shell is provided with an injection port I, an injection port II and an injection port III;

[0007] The reactor shell is provided with an anaerobic chamber I, an anaerobic chamber II and an anaerobic chamber III which are connected in sequence; the sample inlet I is connected to the anaerobic chamber I, the sample inlet II is connected to the anaerobic chamber II, and the sample inlet III is connected to the anaerobic chamber III; a stirrer is provided inside the anaerobic chamber I, the anaerobic chamber II and the anaerobic chamber III, and a membrane assembly and a cyclone water distributor are also provided inside the anaerobic chamber III; baffles and baffle vertical plates are provided on both sides of the anaerobic chamber II; a drain is also provided on the anaerobic chamber III; the treated sewage flows out of the drain through a suction pipe, a suction pump and a backwash inlet pipe into the anaerobic chamber III;

[0008] The tops of the anaerobic chambers I, II and III are all provided with exhaust holes, and the treated gas is discharged from the exhaust holes and enters the anaerobic chamber III through the gas collecting pipeline, gas circulation pipeline, gas peristaltic pump and backwashing air inlet pipeline.

[0009] 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 collecting pipeline through the gas three-way valve; the other end of the gas collecting device is connected to one end of the gas circulation pipeline; the other end of the gas circulation pipeline is connected to the backwash air inlet pipeline through a gas peristaltic pump.

[0010] Furthermore, it also includes an outlet pipe and a pressure sensor, the outlet pipe is externally connected to the water collecting tank; the pressure sensor is arranged on the suction pipeline; the treated sewage enters the water collecting tank through the liquid three-way valve and the outlet pipe, and the suction pump sucks liquid from the water collecting tank through the outlet pipe, passes through the liquid three-way valve and the backwash inlet pipe, and flows into the anaerobic chamber III.

[0011] Furthermore, the mixer includes a first stirring paddle and a second stirring paddle.

[0012] Furthermore, overflow weirs are provided on the upper parts of the anaerobic chamber I and the anaerobic chamber II. The anaerobic chamber I is connected to the baffle and the baffle vertical plate through the overflow weir, and the lower part of the baffle is connected to the anaerobic chamber II and the anaerobic chamber III in sequence.

[0013] A method for collaboratively treating multi-source sewage on ships, comprising:

[0014] S1: The acclimated anaerobic deoiling sludge is inoculated into anaerobic chamber I, sulfate reduction sludge is inoculated into anaerobic chamber II, and desulfurization and denitrification sludge is inoculated into anaerobic chamber III; the ship's oily wastewater enters anaerobic chamber I through inlet I, the ship's domestic sewage enters anaerobic chamber II through inlet II, and the ship's exhaust gas scrubbing liquid enters anaerobic chamber III through inlet III;

[0015] S2: Ship oily wastewater enters anaerobic chamber I through inlet I and is mixed with anaerobic deoiled sludge under the action of the mixer, undergoing hydrolysis and acidification reactions, oil degradation reactions, and sulfate reduction reactions. The treated ship oily wastewater overflows into anaerobic chamber II through the baffle plate and baffle between anaerobic chamber I and anaerobic chamber II. The generated gas is discharged from the exhaust hole and enters the gas collection device through the gas collection pipeline and gas three-way valve;

[0016] S3: The ship's domestic sewage enters anaerobic chamber II through inlet II. Under the action of the mixer, it is mixed with the treated ship's oily sewage and sulfate-reduced sludge, causing a sulfate reduction reaction. The treated ship's domestic sewage and the secondary-treated ship's oily sewage overflow into anaerobic chamber III through the baffle plate and baffle between anaerobic chamber II and anaerobic chamber III. The generated gas is discharged from the exhaust hole and enters the gas collection device through the gas collection pipeline and gas three-way valve.

[0017] S4: The ship exhaust gas scrubbing liquid enters the anaerobic chamber III through the sampling port III. Under the action of the mixer, it is mixed with the treated ship oily wastewater, ship domestic sewage and desulfurization and denitrification sludge, and an autotrophic / heterotrophic denitrification-sulfate reduction coupling reaction occurs. The generated gas is discharged from the exhaust hole and enters the gas collection device through the gas collection pipeline and the gas three-way valve;

[0018] S5: The sewage treated by S4 is filtered by the membrane assembly and flows out from the drain outlet. It passes through the suction pipeline and the liquid three-way valve and enters the water collecting tank through the outlet pipe under the action of the suction pump. After the membrane assembly is filtered, the suction pump is started to backwash the inside of the membrane assembly. When the pressure sensor reaches the set pressure value, the liquid three-way valve and the valve of the backwash inlet pipe are opened. The outlet water flows back to the bottom of the membrane assembly through the backwash inlet pipe under the action of the suction pump, and the outside of the membrane assembly is flushed through the cyclone water distributor; the gas in the gas collecting device reaches the bottom of the membrane assembly through the gas collecting pipeline and the gas circulation pipeline through the action of the gas peristaltic pump, and flushes the outside of the membrane assembly.

[0019] Furthermore, when the pressure sensor on the suction pipeline is at 30-40 KPa, the suction pump and the gas peristaltic pump are started to perform gas and liquid backwashing on the outside of the membrane assembly.

[0020] Furthermore, an intermittent reflux method is used to perform backwashing inside the membrane module, and the time when the membrane module is stopped is consistent with the time when the suction pump performs backwashing operation inside the membrane module.

[0021] Beneficial effects: The present invention proposes a marine multi-stage anaerobic MBR device, which has the following advantages:

[0022] 1. By setting up three anaerobic chambers, domestic sewage, oily sewage and exhaust gas scrubbing liquid can be placed in the same integrated device for simultaneous treatment. This overcomes the shortcomings of traditional processes that require external carbon sources, saves energy, reduces the space occupied by the hull, and achieves efficient in-situ synergistic removal of multiple pollutants under the action of enhanced microorganisms. It has the advantages of high resource utilization of carbon, nitrogen and sulfur in sewage, high treatment efficiency, low energy consumption, simple and integrated operation, etc.

[0023] 2. Use segmented treatment, that is, different sewage is introduced into each reaction chamber respectively. The sewage treated in the anaerobic chamber enters the anaerobic chamber III zone, i.e. the membrane chamber, directly through the baffle to supplement the degradation substrates required by heterotrophic denitrifying bacteria and autotrophic desulfurization and denitrifying bacteria, thereby improving the effluent effect and achieving the purpose of treating waste with waste;

[0024] 3. Each chamber is equipped with an air outlet connected to the gas collecting box to prevent harmful gases from being discharged into the environment. This solves the problem of insufficient circulating gas in traditional anaerobic processes and also enables the reuse of hydrogen sulfide gas.

[0025] 4. The treated water and gas are set up in different pipelines, which can be used to backwash the membrane components separately, reducing operating costs, preventing membrane pollution, and extending the service life of the membrane components. 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 is a brief introduction to 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 any creative labor.

[0027] Figure 1 A structural diagram of a marine multi-stage anaerobic MBR 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 Schematic diagram of oil removal rate and TOC removal rate in anaerobic chamber 1 of the device of the present invention;

[0030] Figure 4 The SO4 in the anaerobic chamber II of the device of the present invention 2- Schematic diagram of removal rate and TOC removal rate;

[0031] Figure 5 The NO3 in the anaerobic chamber III of the device of the present invention - And a schematic diagram of TOC removal rate.

[0032] In the figure, 1. reactor shell; 2. anaerobic chamber I; 3. anaerobic chamber II; 4. anaerobic chamber III; 5. mixer; 6. exhaust hole; 7. overflow weir; 8. baffle vertical plate; 9. baffle; 10. suction pump; 11. gas peristaltic pump; 12. backwash air inlet pipeline; 13. gas collecting device; 14. gas three-way valve; 15. gas collecting pipeline; 16. gas circulation pipeline; 17. pressure sensor; 18. suction pipeline; 19. liquid three-way valve; 20. water outlet pipe; 21. injection port I; 22. injection port II; 23. injection port III; 24. membrane assembly; 25. drain outlet; 26. cyclone water distributor; 27. first stirring paddle; 28. second stirring paddle; 29. ​​backwash water inlet pipe; 30. air inlet. DETAILED DESCRIPTION

[0033] To make the objectives, technical solutions, and advantages of the embodiments of the present invention more clear, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the accompanying drawings of the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. All other embodiments obtained by ordinary technicians in this field based on the embodiments of the present invention without making any creative efforts shall fall within the scope of protection of the present invention.

[0034] This embodiment provides a marine multi-stage anaerobic MBR device, such as Figure 1 As shown, it includes: a reactor shell 1, wherein the reactor shell 1 is provided with an injection port I 21, an injection port II 22 and an injection port III 23;

[0035] The reactor shell 1 is provided with an anaerobic chamber I2, an anaerobic chamber II3 and an anaerobic chamber III4 which are connected in sequence; the sample inlet I 21 is connected to the anaerobic chamber I2, the sample inlet II 22 is connected to the anaerobic chamber II3, and the sample inlet III 23 is connected to the anaerobic chamber III4; a stirrer 5 is provided inside the anaerobic chamber I2, the anaerobic chamber II3 and the anaerobic chamber III4, and a membrane assembly 24 and a cyclone water distributor 26 are also provided inside the anaerobic chamber III4; baffles 9 and baffle vertical plates 8 are provided on both sides of the anaerobic chamber II3; a drain port 25 is also provided on the anaerobic chamber III4; the treated sewage flows out of the drain port 25 and flows into the anaerobic chamber III4 through the suction pipe 18, the suction pump 10 and the backwash inlet pipe 29;

[0036] The tops of the anaerobic chambers I2, II3 and III4 are all provided with exhaust holes 6. The treated gas is discharged from the exhaust holes 6 and enters the anaerobic chamber III4 through the gas collecting pipeline 15, the gas circulation pipeline 16, the gas peristaltic pump 11 and the backwashing air inlet pipeline 12.

[0037] Specifically, the reactor shell is closed, with exhaust holes at the tops of the three anaerobic chambers, an inlet at the bottom of each anaerobic chamber, and a stirrer inside each anaerobic chamber; anaerobic chamber III is an anaerobic MBR chamber, and a membrane assembly is provided inside anaerobic chamber III. The membrane assembly has a plate structure or an annular structure, and is composed of one or more curtain-shaped membranes. The membrane assembly is square and consistent with the shape of the reactor shell. The stirrer in anaerobic chamber III is provided inside the membrane assembly, and a cyclone water distributor is provided at the bottom of the membrane assembly for backwashing the outside of the membrane assembly; the anaerobic microorganisms themselves have a low yield, and the residues can be removed through microbial metabolism. Therefore, the device does not need to discharge excess sludge. If sludge discharge and maintenance are indeed necessary, it can be completed through the reverse operation of the inlet I 21, the inlet II 22 and the air inlet 30;

[0038] An overflow weir is provided at the top of anaerobic chamber I, which is connected to the baffle and the vertical plate of the baffle, and is connected to anaerobic chamber II and anaerobic chamber III in sequence through the lower part of the baffle; the vertical height of the overflow weir is 0.8cm-1.5cm, the inclination angle of the baffle is 45°-60°, and the distance between the baffle and the vertical plate of the baffle is 3-5cm.

[0039] In a specific embodiment, it also includes a gas collecting device 13 and a gas three-way valve 14; one end of the gas collecting device 13 is connected to the gas collecting pipeline 15 through the gas three-way valve 14; the other end of the gas collecting device 13 is connected to one end of the gas circulation pipeline 16; the other end of the gas circulation pipeline 16 is connected to the backwash air inlet pipeline 12 through a gas peristaltic pump 11.

[0040] In this solution, a gas collecting device is provided to collect various gases generated after sewage treatment. Through a gas peristaltic pump and a gas circulation pipeline, the generated high-flux gas is circulated inside the device, solving the problem of insufficient circulating gas in traditional anaerobic processes.

[0041] In a specific embodiment, it also includes an outlet pipe 20 and a pressure sensor 17, and the outlet pipe 20 is externally connected to the water collecting tank; the pressure sensor 17 is arranged on the suction pipeline 18; the treated sewage enters the water collecting tank through the liquid three-way valve 19 and the outlet pipe 20, and the suction pump 10 sucks liquid from the water collecting tank through the outlet pipe 20, passes through the liquid three-way valve 19 and the backwash inlet pipe 29 and flows into the anaerobic chamber III4.

[0042] The treated sewage flows into the external water collecting tank through the outlet pipe. When backwashing is performed, water is pumped from the water collecting tank through the suction pump and the outlet pipe. Intermittent reflux is used to backwash the inside of the membrane assembly. The time when the membrane assembly is pumped and stopped is consistent with the time when the suction pump performs the internal backwashing operation of the membrane assembly. The membrane assembly is internally backwashed and a pressure sensor is set. When the pressure exceeds the specified value, the backwashing operation is performed.

[0043] In a specific embodiment, the stirrer 5 includes a first stirring paddle 27 and a second stirring paddle 28 .

[0044] In this solution, the bottom stirring paddle is 5-8 cm away from the bottom of the shell and 2 cm-4 cm away from the upper stirring paddle; the double-paddle stirring is used to enhance the mass transfer capacity of the activated sludge, so that the sewage and the microorganisms in the activated sludge are fully mixed, thereby improving the system treatment efficiency.

[0045] In a specific embodiment, an overflow weir 7 is provided on the upper part of the anaerobic chamber I2 and the anaerobic chamber II3. The anaerobic chamber I2 is connected to the baffle 9 and the baffle vertical plate 8 through the overflow weir 7. The lower part of the baffle 9 is connected to the anaerobic chamber II3 and the anaerobic chamber III4 in sequence.

[0046] In this solution, baffles and baffle vertical plates are provided, which can push the treated sewage through the overflow weir into the next anaerobic chamber in an up-and-down manner, thereby increasing efficiency.

[0047] This embodiment also provides a method for coordinating treatment of multi-source sewage from ships, such as Figure 2 Shown, including:

[0048] S1: The acclimated anaerobic deoiling sludge is inoculated into anaerobic chamber I2, sulfate reduction sludge is inoculated into anaerobic chamber II3, and desulfurization and denitrification sludge is inoculated into anaerobic chamber III4; the ship's oily wastewater enters anaerobic chamber I2 through inlet I21, the ship's domestic sewage enters anaerobic chamber II3 through inlet II22, and the ship's exhaust gas scrubbing liquid enters anaerobic chamber III4 through inlet III23;

[0049] S2: The ship's oily wastewater enters the anaerobic chamber I2 through the inlet I21 and is mixed with the anaerobic deoiled sludge by the action of the mixer 5, causing hydrolysis and acidification reactions, oil degradation reactions, and sulfate reduction reactions. The treated ship's oily wastewater overflows into the anaerobic chamber II3 through the baffle plate 8 and baffle plate 9 between the anaerobic chambers I2 and II3. The generated gas is discharged from the exhaust port 6 and enters the gas collection device 13 through the gas collection pipeline 15 and the gas three-way valve 14;

[0050] S3: The ship's domestic sewage enters the anaerobic chamber II3 through the sampling port II 22. Under the action of the mixer 5, it is mixed with the treated ship's oily sewage and sulfate-reduced sludge, causing a sulfate reduction reaction. The treated ship's domestic sewage and the secondary-treated ship's oily sewage overflow into the anaerobic chamber III4 through the baffle plate 8 and baffle plate 9 between the anaerobic chambers II3 and III4. The generated gas is discharged from the exhaust port 6 and enters the gas collection device 13 through the gas collection pipeline 15 and the gas three-way valve 14.

[0051] S4: The ship exhaust gas scrubbing liquid enters the anaerobic chamber III4 through the sampling port III 23. Under the action of the mixer 5, it is mixed with the treated ship oily wastewater, ship domestic sewage and desulfurization and denitrification sludge, and an autotrophic / heterotrophic denitrification-sulfate reduction coupling reaction occurs. The generated gas is discharged from the exhaust port 6 and enters the gas collection device 13 through the gas collection pipeline 15 and the gas three-way valve 14.

[0052] S5: The sewage treated by S4 is filtered by the membrane assembly 24 and flows out from the drain port 25, passes through the suction pipe 18 and the liquid three-way valve 19, and enters the water collecting tank through the outlet pipe 20 under the action of the suction pump 10. After the membrane assembly 24 is filtered, the suction pump 10 is started to backwash the inside of the membrane assembly 24. When the pressure sensor 17 reaches the set pressure value, the liquid three-way valve 19 and the valve of the backwashing water inlet pipe 29 are opened. The outlet water flows back to the bottom of the membrane assembly 24 through the backwashing water inlet pipe 29 under the action of the suction pump 10, and the outside of the membrane assembly 24 is flushed through the cyclone water distributor 26; the gas in the gas collecting device 13 reaches the bottom of the membrane assembly 24 through the gas collecting pipe 15 and the gas circulation pipe 16 through the action of the gas peristaltic pump 11, and flushes the outside of the membrane assembly 24.

[0053] Specifically, first, the acclimated anaerobic deoiling sludge is inoculated into anaerobic chamber I, sulfate reduction sludge is inoculated into anaerobic chamber II, and desulfurization and denitrification sludge is inoculated into anaerobic chamber III; the ship's oily sewage enters anaerobic chamber I through inlet I, the ship's domestic sewage enters anaerobic chamber II through inlet II, and the ship's exhaust gas scrubbing liquid enters anaerobic chamber III through the inlet pipe of inlet III;

[0054] The ship's oily wastewater enters the anaerobic chamber I through the inlet port I and is mixed with the anaerobic deoiling sludge under the action of the mixer, and oil degradation reaction, hydrolysis acidification reaction and sulfate reduction reaction occur. Under the action of high-concentration anaerobic deoiling sludge, the oil and other macromolecular organic matter in the ship's oily wastewater is degraded into CO2 and water by acid-producing bacteria, fermentation bacteria, and sulfate-reducing bacteria. At the same time, SO4 2- Restore to S 2- , hydrogen sulfide gas and a small amount of methane gas are generated, and the gas rises to the exhaust hole and enters the gas collecting device; the treated ship oily wastewater overflows into anaerobic chamber II through the baffle vertical plate and baffle between anaerobic chamber I and anaerobic chamber II; the combined effect of water flow and uniform stirring of the agitator causes the high-concentration sulfate-reduced sludge in the system to mix with the ship's domestic sewage and the treated ship oily wastewater, thereby improving the treatment efficiency;

[0055] The domestic sewage from the ship enters the anaerobic chamber II through the sampling port II, and is mixed with the treated ship oily sewage and sulfate-reducing sludge under the action of the mixer, and a sulfate reduction reaction occurs. Under the action of microorganisms mainly composed of sulfate-reducing bacteria, the organic matter in the mixed sewage is removed, and the sulfate is reduced to sulfide, part of which exists in the form of hydrogen sulfide gas. The treated domestic sewage from the ship and the secondary treated oily sewage from the ship overflow into the anaerobic chamber III through the baffle vertical plate and baffle between anaerobic chamber II and anaerobic chamber III; the generated gas is discharged from the exhaust hole and enters the gas collecting device through the gas collecting pipeline and the gas three-way valve; in this area, the effluent from the anaerobic chamber I brings incompletely degraded hydrocarbons, and the domestic sewage brings in organic pollutants such as proteins and sugars, which overcomes the problem of insufficient carbon source for the sulfate reduction reaction and promotes SO4 2- While restoring, it also deeply treats ship oily wastewater and domestic sewage, using waste to treat waste;

[0056] The ship exhaust gas washing liquid enters the anaerobic chamber III through the sampling port III. The ship exhaust gas washing liquid is mixed with the high-concentration desulfurization and denitrification sludge through hydraulic flow and uniform stirring in the mixer, and the autotrophic / heterotrophic denitrification-sulfate reduction coupling reaction occurs. The S generated in the anaerobic chamber II is 2- It flows into the anaerobic chamber III with the water flow, providing electron donors for autotrophic denitrifying bacteria. The remaining undegraded organic matter in the effluent serves as a substrate for heterotrophic denitrifying bacteria, desulfurizing and denitrifying the ship exhaust gas scrubbing liquid. While deeply treating the effluent from the anaerobic chamber II, it also avoids the problem of secondary pollution caused by the addition of external carbon sources.

[0057] The treated sewage is filtered through the membrane module and enters the water collection tank through the outlet pipe under the action of the suction pump. The hydrogen sulfide and other gases generated in the anaerobic chamber III enter the gas collecting device through the exhaust hole and the gas collecting pipeline. The membrane module is backwashed while the pumping is stopped. The outlet water is returned to the inside of the membrane module by the suction pump through the backwash inlet pipe. The gas reaches the bottom of the membrane module through the backwash inlet pipe through the gas peristaltic pump and is backwashed through the aeration pipe. When the transmembrane pressure difference of the pressure sensor is 30-40kPa, the membrane module is externally flushed online through the cyclone water distributor.

[0058] In this embodiment, the stirring speed of the stirrer is 150 rpm, stirring is performed intermittently, the operating temperature is 25-35°C, and the hydraulic retention time of each reaction zone is 10h-48h;

[0059] The sludge acclimation method is as follows: the hydraulic retention time is 48 hours, and natural seawater is used in all cases; the influent components of sulfate-reducing sludge are peptone and sodium bicarbonate; the influent components of oil-degrading anaerobic sludge are emulsified diesel and sodium bicarbonate; the influent components of denitrifying sludge are sodium sulfide, peptone, sodium nitrate, and sodium bicarbonate; the activated sludge for inoculation should be taken from anaerobic sludge tanks or fermentation tanks;

[0060] Sludge acclimation uses natural seawater to create a high-salinity environment, which promotes the rapid development of high-salinity-tolerant microbial flora, facilitating efficient operation of the desulfurization and denitrification process under high-load, high-salinity conditions. Furthermore, sludge acclimation can be carried out onshore in advance, with successfully acclimated activated sludge directly inoculated into the vessel's reactor. This significantly shortens the start-up time of the vessel's equipment, making it suitable for the vessel's operating environment and eliminating the need to occupy limited space resources onboard for sludge acclimation.

[0061] The concentration of sludge in each anaerobic zone is:

[0062] The volatile suspended solids concentration (MLVSS) of the denitrifying sludge inoculated in the anaerobic membrane zone is 2500-4500 mg / L; the sludge inoculation concentration in the sulfate reducing anaerobic zone is 2200-3900 mgMLVSS / L; the MLVSS inoculation concentration of the desulfurization denitrification activated sludge is 2500-4500 mg / L.

[0063] In a specific embodiment, when the pressure sensor 17 on the suction pipeline 18 is at 30-40 KPa, the suction pump 10 and the gas peristaltic pump 11 are started to perform gas and liquid backwashing on the outside of the membrane assembly 24 .

[0064] In a specific embodiment, intermittent reflux is used to perform backwashing inside the membrane assembly 24 , and the time when the membrane assembly 24 is stopped is consistent with the time when the suction pump 10 performs the backwashing operation inside the membrane assembly 24 .

[0065] The pumping time of the membrane component is 8 minutes, and the stopping time is 1 minute; the filtration time during backwashing is 8 minutes, and the backwashing time is 1 minute; in this scheme, the filtration time of the membrane component is consistent with the backwashing operation time, and the membrane component can be cleaned at the same time as the filtration of the membrane component is completed, thereby improving the effect and efficiency of sewage treatment.

[0066] The overall processing process of this device is as follows:

[0067] (1) Acclimation of activated sludge

[0068] Anaerobic sludge was inoculated from the secondary sedimentation tank of the municipal sewage treatment plant and inoculated into a continuous stirred reactor. After the addition of seawater with organic matter, 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 components of ship oily wastewater were: oil concentration, sodium bicarbonate 3.2g / L; the components of ship domestic sewage were peptone 1.2g / L, sodium bicarbonate 8g / L; the components of ship exhaust gas scrubbing liquid were: peptone 0.17g / L, sodium nitrate 0.93g / L, sodium sulfide 3.33g / L, bicarbonate Sodium 8g / L, where the overall environment is alkaline, is dissolved in natural seawater, and the HRT is first 48h and then changed to 24h. When the oil removal rate of the activated sludge treating oily wastewater is above 90%, it indicates successful acclimation; seawater contains a large amount of sulfate, and this method only needs to remove the sulfate generated by flue gas scrubbing. Therefore, the sulfate removal rate of sulfate-reducing activated sludge is above 70%, indicating successful acclimation; the sulfide removal rate of desulfurization and denitrification sludge is 90% and the nitrate removal rate is above 90%, indicating successful acclimation;

[0069] (2) Device startup

[0070] The acclimated activated sludge was inoculated into different chambers of the reactor, i.e., the desulfurization and oil removal activated sludge was inoculated into anaerobic chamber I, the sulfate reduction activated sludge SRB was inoculated into anaerobic chamber II, and the desulfurization and denitrification activated sludge was inoculated into anaerobic chamber III. The ship's oily sewage entered the anaerobic chamber I from the inlet I at the bottom of the shell, the ship's domestic sewage was introduced into the bottom of the anaerobic chamber II shell, and the ship's exhaust gas scrubbing liquid was introduced into the bottom of the anaerobic chamber III. The water inlet time and composition were consistent with those in the acclimation stage. The operating temperature was 25-35°C, stirring was continued at a stirring speed of 150rpm, stirring was continued, the hydraulic retention time of anaerobic chamber II, anaerobic chamber I and anaerobic chamber III was 24h, and the membrane assembly was backwashed while being filtered, i.e., filtration for 8min and backwashing for 1min.

[0071] (3) Device operation

[0072] Under the action of microorganisms, ship sewage in anaerobic chamber I degrades large molecules such as oil into small molecular hydrocarbons, CO2 and water; ship oily sewage enters anaerobic chamber II in an upward and downward push flow through the baffle, and ship domestic sewage is introduced into the bottom of the anaerobic chamber II shell. Under the action of sulfate-reducing bacteria, organic matter in the mixed sewage is removed and sulfate is reduced to sulfide; ship exhaust gas scrubbing liquid is introduced into the bottom of anaerobic chamber III and mixed with the effluent of anaerobic chamber II to carry out deep desulfurization and denitrification and degradation of organic matter. The pumping and stopping time of the effluent of anaerobic chamber III is consistent with the backwashing time, with the pumping / stopping time of 8 min / 1 min, that is, 8 min of filtration and 1 min of backwashing; at the same time, when the pressure sensor is at 30-40Kpa, the valve is opened and the outside of the membrane assembly is backwashed for 5 minutes through the backwashing pipe.

[0073] Hydrolysis and acidification, oil degradation, and sulfate reduction reactions occur within Anaerobic Chamber I. Oil in the oily wastewater is adsorbed by microorganisms onto their surfaces or enters their cells, undergoing biochemical metabolism. Complex organic compounds are broken down into simpler, small-molecule organic matter. The microorganisms use the remaining organic compounds as a carbon and energy source to carry out their physiological activities, releasing end products such as carbon dioxide and water.

[0074] Sulfate reduction reaction occurs in anaerobic chamber II. Macromolecular organic matter such as proteins, sugars, and fats in the ship's domestic sewage provide electron donors for sulfate-reducing bacteria, and sulfate and organic matter are efficiently converted into sulfide and small molecular organic matter.

[0075] In the anaerobic chamber III, autotrophic / heterotrophic denitrification-sulfate reduction coupling reaction occurs, sulfide and nitrate are converted into elemental sulfur and nitrogen, and pollutants in the sewage are removed. After membrane filtration, the turbidity of the effluent is guaranteed. Figure 3 As shown in Figure 1, the oil removal rate in anaerobic chamber I can reach more than 90%, and the organic matter removal rate can reach 94%. Figure 4 As shown in the figure, the organic matter removal rate in the anaerobic chamber II can reach more than 98%, SO 24 - The removal rate can reach more than 74%; Figure 5 As shown, in anaerobic chamber III, NO3 - The removal rates of effluent and TOC can reach over 99%.

[0076] This invention synergistically treats multiple types of ship wastewater, saving space and recycling multiple harmful gases. The internal gas circulation system within the device also effectively promotes desulfurization and denitrification. The annular membrane assembly, combined with a stirrer, increases membrane flux and hydraulic cross-flow flushing reduces membrane fouling. Internal and external membrane assembly backwashing devices also effectively reduce and prevent membrane fouling. The synergistic treatment of multiple sources of ship wastewater promotes the synergistic effects of various reactions, thereby improving overall treatment efficiency and achieving deep purification.

[0077] 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 above embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the above 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 marine multi-stage anaerobic MBR device, characterized in that: include: A reactor shell (1), wherein the reactor shell (1) is provided with an injection port I (21), an injection port II (22) and an injection port III (23); The reactor shell (1) is provided with an anaerobic chamber I (2), an anaerobic chamber II (3) and an anaerobic chamber III (4) which are connected in sequence; the sample inlet I (21) is connected to the anaerobic chamber I (2), the sample inlet II (22) is connected to the anaerobic chamber II (3), and the sample inlet III (23) is connected to the anaerobic chamber III (4); the anaerobic chamber I (2), the anaerobic chamber II (3) and the anaerobic chamber III (4) are provided with A mixer (5), a membrane assembly (24) and a cyclone water distributor (26) are further provided inside the anaerobic chamber III (4); baffles (9) and baffle vertical plates (8) are provided on both sides of the anaerobic chamber II (3); a drain port (25) is further provided on the anaerobic chamber III (4); the treated sewage flows out from the drain port (25) through a suction pipe (18), a suction pump (10) and a backwash water inlet pipe (29) and flows into the anaerobic chamber III (4); The tops of the anaerobic chamber I (2), anaerobic chamber II (3) and anaerobic chamber III (4) are all provided with exhaust holes (6). The treated gas is discharged from the exhaust holes (6) and enters the anaerobic chamber III (4) through the gas collecting pipeline (15), the gas circulation pipeline (16), the gas peristaltic pump (11) and the backwashing air inlet pipeline (12).

2. The marine multi-stage anaerobic MBR device according to claim 1, characterized in that: It also includes a gas collecting device (13) and a gas three-way valve (14); one end of the gas collecting device (13) is connected to a gas collecting pipeline (15) via the gas three-way valve (14); the other end of the gas collecting device (13) is connected to one end of a gas circulation pipeline (16); the other end of the gas circulation pipeline (16) is connected to the backwashing air inlet pipeline (12) via a gas peristaltic pump (11).

3. The marine multi-stage anaerobic MBR device according to claim 1, characterized in that: The apparatus further comprises an outlet pipe (20) and a pressure sensor (17), wherein the outlet pipe (20) is externally connected to a water collecting tank; the pressure sensor (17) is arranged on the suction pipe (18); the treated sewage enters the water collecting tank through a liquid three-way valve (19) and the outlet pipe (20); the suction pump (10) draws liquid from the water collecting tank through the outlet pipe (20), and the liquid flows through the liquid three-way valve (19) and the backwash inlet pipe (29) into the anaerobic chamber III (4).

4. The marine multi-stage anaerobic MBR device according to claim 1, characterized in that: The stirrer (5) comprises a first stirring paddle (27) and a second stirring paddle (28).

5. The marine multi-stage anaerobic MBR device according to claim 1, characterized in that: The anaerobic chamber I (2) and the anaerobic chamber II (3) are both provided with overflow weirs (7) at their upper parts. The anaerobic chamber I (2) is communicated with the baffle (9) and the baffle vertical plate (8) through the overflow weir (7). The lower part of the baffle (9) is communicated with the anaerobic chamber II (3) and the anaerobic chamber III (4) in sequence.

6. A method for co-treatment of multi-source sewage from ships based on the ship-based multi-stage anaerobic MBR device according to claim 1, characterized in that: include: S1: The acclimated anaerobic deoiling sludge is inoculated into the anaerobic chamber I (2), the sulfate reducing sludge is inoculated into the anaerobic chamber II (3), and the desulfurization and denitrification sludge is inoculated into the anaerobic chamber III (4); the ship's oily sewage enters the anaerobic chamber I (2) through the sampling port I (21), the ship's domestic sewage enters the anaerobic chamber II (3) through the sampling port II (22), and the ship's exhaust gas scrubbing liquid enters the anaerobic chamber III (4) through the sampling port III (23); S2: The ship's oily wastewater enters the anaerobic chamber I (2) through the inlet I (21), and is mixed with the anaerobic deoiling sludge under the action of the mixer (5), and undergoes hydrolysis and acidification reaction, oil degradation reaction and sulfate reduction reaction. The treated ship's oily wastewater overflows into the anaerobic chamber II (3) through the baffle plate (8) and the baffle plate (9) between the anaerobic chamber I (2) and the anaerobic chamber II (3). The generated gas is discharged from the exhaust hole (6) and enters the gas collecting device (13) through the gas collecting pipeline (15) and the gas three-way valve (14); S3: The domestic sewage from the ship enters the anaerobic chamber II (3) through the inlet II (22), and is mixed with the treated ship oily sewage and sulfate reduction sludge under the action of the mixer (5), and a sulfate reduction reaction occurs. The treated ship domestic sewage and the secondary treated ship oily sewage overflow into the anaerobic chamber III (4) through the baffle vertical plate (8) and the baffle (9) between the anaerobic chamber II (3) and the anaerobic chamber III (4); the generated gas is discharged from the exhaust hole (6) and enters the gas collecting device (13) through the gas collecting pipeline (15) and the gas three-way valve (14); S4: The ship exhaust gas scrubbing liquid enters the anaerobic chamber III (4) through the sampling port III (23), and is mixed with the treated ship oily sewage, ship domestic sewage and desulfurization and denitrification sludge under the action of the mixer (5), and an autotrophic / heterotrophic denitrification-sulfate reduction coupling reaction occurs. The generated gas is discharged from the exhaust hole (6) and enters the gas collection device (13) through the gas collection pipeline (15) and the gas three-way valve (14); S5: The sewage treated in S4 flows out from the drain port (25) through the suction pipe (18) and the liquid three-way valve (19), and enters the water collection tank through the outlet pipe (20) under the action of the suction pump (10). After the membrane assembly (24) is filtered, the suction pump (10) is started to backwash the inside of the membrane assembly (24). When the pressure sensor (17) reaches the set pressure value, the liquid three-way valve (19) is opened and the pressure sensor (17) is opened. The valve of the backwash water inlet pipe (29) allows the outlet water to flow back to the bottom of the membrane assembly (24) through the backwash water inlet pipe (29) under the action of the suction pump (10), and flush the outside of the membrane assembly (24) through the cyclone water distributor (26); the gas in the gas collecting device (13) reaches the bottom of the membrane assembly (24) through the gas collecting pipeline (15) and the gas circulation pipeline (16) through the action of the gas peristaltic pump (11), and flushes the outside of the membrane assembly (24).

7. The method for coordinating treatment of multi-source sewage from ships according to claim 6, characterized in that: When the pressure sensor (17) on the suction pipeline (18) is at 30-40KPa, the suction pump (10) and the gas peristaltic pump (11) are started to perform gas and liquid backwashing on the outside of the membrane assembly (24).

8. The method for coordinating treatment of multi-source sewage from ships according to claim 6, characterized in that: The membrane assembly (24) is backwashed internally by an intermittent reflux method, and the time when the membrane assembly (24) is pumped and stopped is consistent with the time when the suction pump (10) performs the backwashing operation inside the membrane assembly (24).

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