CN115520960A - Carbon-hydrogen mixed matrix biofilm reactor and method for purifying water containing oxidative pollutants - Google Patents
Carbon-hydrogen mixed matrix biofilm reactor and method for purifying water containing oxidative pollutants Download PDFInfo
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
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- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention provides a hydrocarbon mixed matrix biomembrane reactor and a method for purifying a water body containing oxidative pollutants, belonging to the technical field of water purification. The invention provides a hydrocarbon mixed matrix biofilm reactor, which comprises a raw water tank, a reaction tank, a water inlet pipeline system, a water outlet pipeline system, a return pipeline system and a gas supply system, wherein the raw water tank is connected with the reaction tank through a pipeline; wherein the gas supply system comprises H 2 Gas cylinder, H 2 With CO 2 A gas mixing cylinder and a gas supply pipeline, wherein one end of the gas supply pipeline is connected with the H 2 Gas cylinder and H 2 With CO 2 The mixed gas bottle is connected, and the other end of the gas supply pipeline is connected with two ports of the hollow fiber membrane component in the reaction tank. When the hydrocarbon mixed matrix biomembrane reactor provided by the invention is used for purifying water containing oxidative pollutants, H can be synchronously dispersed in the biomembrane through the hollow fiber membrane component without bubbles 2 With CO 2 The mixed gas can further realize the whole-area control of the pH value in the biomembrane.
Description
Technical Field
The invention relates to the technical field of water purification, in particular to a hydrocarbon mixed matrix biofilm reactor and a method for purifying a water body containing oxidative pollutants.
Background
Oxidative pollutants (including inorganic anions such as nitrate, nitrite, bromate, perchlorate and the like, heavy metal ions such as dichromate, selenate, arsenate and the like, and organic compounds such as trichloroethylene, chloroform and the like) are the most common pollutants in water body pollution, and seriously threaten the ecological safety and human health of the water body. Research and development of technologies for removing oxidative pollutants in water bodies are always a focus of attention of researchers at home and abroad. At present, methods for removing oxidative pollutants in water mainly comprise a physicochemical method and a biochemical method, wherein the physicochemical method can effectively separate or remove the pollutants from the water, but the problems of secondary pollution, high operation cost and the like generally exist, so that the large-scale engineering application of the pollutants is limited. Although the traditional biochemical method has certain advantages in environmental friendliness compared with a physicochemical method, an organic carbon source is often required to be additionally added, and if the operation management is not proper, the problem of secondary pollution is also caused. Therefore, there is an urgent need for a high-efficiency and low-cost treatment technique for developing oxidative pollutants in water.
Hydrogen based biofilm reactors (H) developed in recent years 2 MBfR) is an emerging water treatment technology based on the combination of bubble-free diffusion of hydrogen as an electron donor and autotrophic reduction of microorganisms through a hollow fiber membraneThe method has a plurality of advantages in treating the oxidative pollutants in the water body, such as: the method has the advantages of utilizing clean and cheap hydrogen as an electron donor, taking inorganic carbon as a carbon source, having high pollutant removal efficiency, no secondary pollutant, high hydrogen utilization rate (up to 100 percent) and the like, and is considered to be a water treatment technology with great prospect. However, the further development and engineering of this technology still faces a key technical challenge, namely the utilization of H 2 In the process of treating the oxidative pollutants in the water body by the MBfR, protons are consumed (for example, formula 1 for removing nitrate), which causes the pH value in the reactor to rise, and thus the removal efficiency of the pollutants is reduced, and precipitates are generated in the biofilm, for example, hydroxide precipitates, carbonate precipitates or phosphate precipitates are formed based on calcium ions and magnesium ions contained in the water body, so that the mass transfer efficiency of the substrate is reduced and membrane pollution is caused.
NO 3 - +4.48H 2 +0.86CO 2 +H + ＝0.41N 2 +0.17C 5 H 7 O 2 N+4.38H 2 O is represented by the formula 1.
H 2 The usual method for controlling the pH of the system in MBfR involves the addition of phosphate buffer, hydrochloric acid, bicarbonate and CO 2 And the like. Recent studies have shown that the addition of CO 2 Can simultaneously regulate the pH value of the system and serve as an inorganic carbon source, and is a more preferable choice (Jiang et al, water Research,2020, 184. However, the above method can effectively control the pH of the mixed liquid in the reactor and the pH outside the biofilm, but the pH inside the biofilm is still too high.
Disclosure of Invention
The invention aims to provide a hydrocarbon mixed matrix biofilm reactor and a method for purifying a water body containing oxidative pollutants 2 MBfR maintains long-term efficient stable operation in the process of removing oxidative pollutants。
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides a hydrocarbon mixed matrix biofilm reactor, which comprises a raw water tank, a reaction tank, a water inlet pipeline system, a water outlet pipeline system, a return pipeline system and a gas supply system, wherein the raw water tank is connected with the reaction tank through a pipeline;
a hollow fiber membrane component is arranged in the reaction tank; one end of the reaction tank, the water inlet pipeline system and the return pipeline system are connected through a tee joint, and the other end of the reaction tank, the water outlet pipeline system and the return pipeline system are connected through a tee joint; the reaction tank, the water inlet pipeline system, the water outlet pipeline system and the return pipeline system form a circulation loop;
the gas supply system comprises H 2 Gas cylinder, H 2 With CO 2 A gas mixing cylinder and a gas supply pipeline, wherein one end of the gas supply pipeline is connected with the H 2 Gas cylinder and H 2 With CO 2 The mixed gas bottle is connected, and the other end of the gas supply pipeline is connected with two ports of the hollow fiber membrane component in the reaction tank.
Preferably, H 2 Gas cylinder and H 2 With CO 2 The gas mixing cylinder is independently provided with a gas pressure partial pressure valve.
Preferably, the reaction tank is vertically arranged, and the hollow fiber membrane module contains a plurality of hollow fiber membrane filaments.
Preferably, the hollow fiber membrane filaments are made of hydrophobic polypropylene materials; the outer diameter of the hollow fiber membrane yarn is 200-2000 mu m; the membrane aperture of the hollow fiber membrane filament is 0.01-0.02 μm.
Preferably, a reflux pump is arranged on the reflux pipeline system; and the water inlet pipeline system is provided with a water inlet pump.
The invention provides a method for purifying a water body containing oxidative pollutants by adopting the hydrocarbon mixed matrix biofilm reactor in the technical scheme, which comprises the following steps:
inoculating sludge into a hydrocarbon mixed matrix biomembrane reactor, continuously introducing raw water for domestication into a reaction tank through a water inlet pipeline system, and simultaneously supplying gasSystem providing H 2 The mixed liquid in the reaction tank flows back through a return pipeline system and is converged into the water inlet pipeline system, and the hydrocarbon mixed matrix biomembrane reactor is acclimated to form a biomembrane on the surface of the hollow fiber membrane component in the reaction tank;
continuously introducing water containing oxidative pollutants into the reaction tank through a water inlet pipeline system, and simultaneously providing H by using an air supply system 2 With CO 2 The mixed gas, the mixed liquid in the reaction tank flows back through the return pipeline system and is merged into the water inlet pipeline system, and the purification of the water body containing the oxidative pollutants is realized.
Preferably, said H 2 With CO 2 H in the mixed gas 2 With CO 2 The molar ratio of (2.5-10): 1.
preferably, during said purification, H 2 Is between 1 and 15psig.
Preferably, in the purification process, the pH of the mixed solution in the reaction tank is 7 to 8.
Preferably, during the purification process, the flow rate of the return flow is 50 to 150 times of the flow rate of the inlet water.
The invention provides a hydrocarbon mixed matrix biomembrane reactor (CO) 2 /H 2 -MBfR) comprising a raw water tank, a reaction cell, a water inlet pipe system, a water outlet pipe system, a return pipe system and a gas supply system; a hollow fiber membrane component is arranged in the reaction tank; one end of the reaction tank, the water inlet pipeline system and the return pipeline system are connected through a tee joint, and the other end of the reaction tank, the water outlet pipeline system and the return pipeline system are connected through a tee joint; the reaction tank, the water inlet pipeline system, the water outlet pipeline system and the return pipeline system form a circulation loop; the gas supply system comprises H 2 Gas cylinder, H 2 With CO 2 A gas mixing cylinder and a gas supply pipeline, one end of the gas supply pipeline is connected with the H 2 Gas cylinder and H 2 With CO 2 The mixing gas bottle is connected, and the other end of the gas supply pipeline is connected with two ports of the hollow fiber membrane component in the reaction tank. The carbon-hydrogen mixed matrix biological membrane reaction provided by the inventionWhen the device is used for purifying water containing oxidative pollutants, H can be synchronously diffused in a biological membrane without bubbles through the hollow fiber membrane component 2 With CO 2 The mixed gas can further realize the full-area control of the pH value in the biomembrane, and avoid the introduction of CO from the outer side of the biomembrane in the prior art 2 The existing problems that the removal efficiency of pollutants is reduced and the membrane pollution is caused by the fact that the pH value of the inner part of the biological membrane can not be effectively reduced only by controlling the pH value of the mixed liquid and the outer side of the biological membrane in the reactor are solved, and the method is favorable for ensuring H 2 The MBfR can maintain long-term high-efficiency stable operation in the process of removing the oxidative pollutants, and has good treatment efficiency on the oxidative pollutants. In addition, the hydrocarbon mixed matrix biofilm reactor provided by the invention has a simple structure, can be used for engineering amplification and can be used for H 2 The popularization and the large-scale application of the MBfR technology have important significance.
Drawings
FIG. 1 is a schematic structural diagram of a hydrocarbon mixed matrix biofilm reactor device in the invention, wherein 1 is a raw water tank, 2 is a water inlet pump, 3 is a reaction tank, 4 is a hollow fiber membrane component, 5 is a reflux pump, 6 is a water outlet pipe, 7 is a sampling port, and 8 is H 2 Gas cylinder, 9 is H 2 With CO 2 A mixed gas cylinder;
FIG. 2 example 1H 2 And CO 2 And (3) a system performance diagram of the hydrocarbon mixed matrix biofilm reactor under different molar ratio conditions.
Detailed Description
The invention provides a hydrocarbon mixed matrix biofilm reactor, which comprises a raw water tank, a reaction tank, a water inlet pipeline system, a water outlet pipeline system, a return pipeline system and a gas supply system, wherein the raw water tank is connected with the reaction tank;
a hollow fiber membrane component is arranged in the reaction tank; one end of the reaction tank, the water inlet pipeline system and the return pipeline system are connected through a tee joint, and the other end of the reaction tank, the water outlet pipeline system and the return pipeline system are connected through a tee joint; the reaction tank, the water inlet pipeline system, the water outlet pipeline system and the return pipeline system form a circulation loop;
the gas supply system comprises H 2 Gas cylinder, H 2 With CO 2 A mixed gas bottle and a gas supply pipeline,one end of the air supply pipeline is connected with the H 2 Gas cylinder and H 2 With CO 2 The mixed gas bottle is connected, and the other end of the gas supply pipeline is connected with two ports of the hollow fiber membrane component in the reaction tank.
In the present invention, unless otherwise specified, all the required devices or materials are commercially available products well known to those skilled in the art.
The invention provides a hydrocarbon mixed matrix biomembrane reactor, which comprises a raw water tank for storing water containing oxidative pollutants. The invention has no special limitation on the size and the material of the raw water tank, and can be selected according to the actual requirement.
The invention provides a hydrocarbon mixed matrix biomembrane reactor, which comprises a reaction tank, a water inlet pipeline system, a water outlet pipeline system and a return pipeline system, wherein one end of the reaction tank, the water inlet pipeline system and the return pipeline system are connected by a tee joint, and the other end of the reaction tank, the water outlet pipeline system and the return pipeline system are connected by a tee joint; the reaction tank, the water inlet pipeline system, the water outlet pipeline system and the return pipeline system form a circulation loop.
As an embodiment of the invention, the reaction tank is vertically arranged, a water inlet is arranged at the bottom end of the reaction tank, and the water inlet is connected with the water inlet pipeline system and the return pipeline system in a tee joint manner; and a water outlet is arranged at the top end of the reaction tank and is connected with the water outlet pipeline system and the return pipeline system in a tee joint mode. As an embodiment of the invention, both ends of the wall of the reaction tank are respectively provided with openings for installing hollow fiber membrane modules. As an embodiment of the invention, the reaction tank is processed by a square glass tube, the size of the inner wall is 10 x 10mm, and the length of the tube is 350mm.
In the invention, a hollow fiber membrane module is arranged in the reaction tank. In one embodiment of the present invention, the hollow fiber membrane module includes a plurality of hollow fiber membrane filaments, and specifically, may include 32 hollow fiber membrane filaments. In the invention, the material of the hollow fiber membrane filaments is preferably hydrophobic polypropylene material; the outer diameter of the hollow fiber membrane yarn is preferably 200-2000 μm, and more preferably 280 μm; the membrane pore diameter of the hollow fiber membrane filament is preferably 0.01 to 0.02 μm, and more preferably 0.02 μm. As an embodiment of the present invention, two ends of the hollow fiber membrane module are respectively bonded in the sleeves by epoxy resin glue, and then the sleeves are bonded in the openings on the tank wall of the reaction tank by epoxy resin glue, so as to fix the hollow fiber membrane module.
As an embodiment of the present invention, the water inlet pipeline system is provided with a water inlet pump for introducing the water containing the oxidative pollutants into the reaction tank through the water inlet pipeline system, and the water inlet flow rate can be adjusted and controlled.
As an embodiment of the invention, the return pipeline system is provided with a return pump for returning the mixed liquid in the reaction tank, and the return rate can be regulated and controlled to ensure that the mixed liquid in the hydrocarbon mixed matrix biomembrane reactor is fully mixed.
As an embodiment of the present invention, the water outlet pipeline system is provided with a water outlet pipe, and the water outlet pipe is provided with a sampling port.
The invention provides a hydrocarbon mixed matrix biomembrane reactor, which comprises a gas supply system, wherein the gas supply system comprises H 2 Gas cylinder, H 2 With CO 2 A gas mixing cylinder and a gas supply pipeline, wherein one end of the gas supply pipeline is connected with the H 2 Gas cylinder and H 2 With CO 2 The mixing gas bottle is connected, and the other end of the gas supply pipeline is connected with two ports of the hollow fiber membrane component in the reaction tank. As an embodiment of the present invention, the H 2 Gas cylinder and H 2 With CO 2 The gas mixing cylinder is independently provided with a gas pressure distributing valve for regulating and controlling gas pressure. In the present invention, said H 2 The gas cylinder can be used for acclimating the hydrocarbon mixed matrix biofilm reactor, so that a biofilm is formed on the surface of the hollow fiber membrane component in the reaction tank; said H 2 With CO 2 The mixed gas cylinder is used for purifying water containing oxidative pollutants, wherein H 2 With CO 2 Introducing the mixed gas into the hollow fiber membrane component, and then H 2 With CO 2 The mixed gas diffuses in a bubble-free manner through micropores on the filament wall of the hollow fiber membraneAnd the pH value in the biological membrane can be controlled in the whole area.
The invention provides a method for purifying a water body containing oxidative pollutants by adopting the hydrocarbon mixed matrix biofilm reactor in the technical scheme, which comprises the following steps:
inoculating sludge into a hydrocarbon mixed matrix biomembrane reactor, continuously introducing raw water for domestication into a reaction tank through a water inlet pipeline system, and simultaneously providing H by adopting an air supply system 2 The mixed liquid in the reaction tank flows back through a return pipeline system and is converged into the water inlet pipeline system, and the hydrocarbon mixed matrix biomembrane reactor is acclimated to form a biomembrane on the surface of the hollow fiber membrane component in the reaction tank;
continuously introducing water containing oxidative pollutants into the reaction tank through a water inlet pipeline system, and simultaneously providing H by using an air supply system 2 With CO 2 And mixed gas, wherein the mixed liquid in the reaction tank flows back through a return pipeline system and is merged into the water inlet pipeline system, so that the purification of the water body containing the oxidative pollutants is realized.
The invention inoculates sludge into a hydrocarbon mixed matrix biomembrane reactor, continuously feeds raw water for domestication into a reaction tank through a water inlet pipeline system, and simultaneously provides H through a gas supply system 2 And the mixed liquid in the reaction tank flows back through a return pipeline system and is converged into the water inlet pipeline system to acclimate the hydrocarbon mixed matrix biomembrane reactor, so that a biomembrane is formed on the surface of the hollow fiber membrane component in the reaction tank. The invention firstly starts and acclimates the hydrocarbon mixed matrix biofilm reactor to form a biofilm on the surface of the hollow fiber membrane component in the reaction tank and ensure the stable operation of the hydrocarbon mixed matrix biofilm reactor in the subsequent purification process.
The source of the sludge in the present invention is not particularly limited, and sludge known to those skilled in the art may be used. In the embodiment of the invention, the sludge is preferably anoxic pond sludge from a municipal sewage treatment plant by taking the example of purifying the nitrate-containing water body by using a hydrocarbon mixed matrix biofilm reactor. In the bookIn the invention, the inoculation amount of the sludge is preferably 10% of the total effective volume of the hydrocarbon mixed matrix biofilm reactor. In the invention, the raw water for domestication is preferably additionally added with an inorganic carbon source and a buffer solution on the basis of a water body containing oxidative pollutants so as to meet the growth of microorganisms and control the pH value of a system within a proper range; in the present invention, the inorganic carbon source is preferably NaHCO 3 The buffer solution is preferably phosphate buffer solution, in particular KH 2 PO 4 With Na 2 HPO 4 And (4) preparing a buffer solution. In the embodiment of the present invention, for example, the nitrate-containing water is purified by using a hydrocarbon mixed matrix biofilm reactor, the raw water for acclimation preferably includes: 20mgN/L NaNO 3 100mg/L NaHCO 3 128mg/L KH 2 PO 4 And 434mg/L of Na 2 HPO 4 (ii) a Preferably, the fertilizer also comprises trace elements, specifically: 1mg/L MgSO of 4 ·7H 2 O, 80mg/L FeSO 4 ·7H 2 O, 1mg/L CaCl 2 ·2H 2 O, 0.013mg/L ZnSO 4 ·7H 2 O, 0.038mg/L H 3 BO 3 0.001mg/L of CuCl 2 ·2H 2 O, 0.004mg/L Na 2 MoO 4 ·2H 2 O, 0.004mg/L MnCl 2 ·4H 2 O, 0.025mg/L CoCl 2 ·6H 2 O, 0.001mg/L NiCl 2 ·6H 2 O and 0.004mg/L of Na 2 SeO 3 。
In the invention, in the process of starting and domesticating the hydrocarbon mixed matrix biomembrane reactor, H 2 Preferably 1 to 15psig, more preferably 5psig. In the invention, in the process of starting and domesticating the hydrocarbon mixed matrix biomembrane reactor, the flow rate of the backflow is preferably 50-150 times of the flow rate of the inflow so as to achieve the purpose that the mixed liquid in the reaction tank is in a completely mixed state; preferably, the domestication raw water is continuously introduced into the reaction tank through a water inlet pipeline system by a water inlet pump, and the mixed liquid in the reaction tank is refluxed by a reflux pipeline system by a reflux pump and is converged into the water inlet pipeline system; in an embodiment of the present invention, it is,the flow rate of the feed pump is preferably 0.63mL/min, and the flow rate of the reflux pump is preferably 80mL/min.
In the present invention, the thickness of the biofilm is preferably 500 to 900 μm, and more preferably 650 to 700 μm. After the biofilm is formed, the nitrate concentration in the water is preferably monitored, and when the nitrate concentration in the effluent is kept stable, the start-up and acclimation of the hydrocarbon mixed matrix biofilm reactor are considered to be completed. In the embodiment of the invention, when the nitrate concentration in the effluent is stable for at least 5 continuous days, the start-up and acclimation of the hydrocarbon mixed matrix biofilm reactor are considered to be completed.
In the invention, after the start and the domestication of the hydrocarbon mixed matrix biomembrane reactor are finished, the water containing the oxidative pollutants is continuously introduced into the reaction tank through the water inlet pipeline system, and the gas supply system is adopted to provide H 2 With CO 2 The mixed gas, the mixed liquid in the reaction tank flows back through the return pipeline system and is merged into the water inlet pipeline system, and the purification of the water body containing the oxidative pollutants is realized. In the invention, the oxidative pollutants in the water body containing the oxidative pollutants preferably comprise one or more of inorganic anions, heavy metal ions and organic compounds, the inorganic anions preferably comprise one or more of nitrate, nitrite, bromate and perchlorate, the heavy metal ions preferably comprise one or more of dichromate, selenate and arsenate, and the organic compounds preferably comprise one or more of trichloroethylene and chloroform; in the embodiment of the present invention, the nitrate-containing water is specifically exemplified. In the invention, the concentration of nitrate in the nitrate-containing water body is preferably 10-100 mgN/L; in the embodiment of the invention, the concentration of the nitrate in the nitrate-containing water body is specifically 20mgN/L.
In the present invention, said H 2 With CO 2 H in the mixed gas 2 With CO 2 The molar ratio of (2.5 to 10): 1, more preferably 5.2; in the course of said purification, H 2 Preferably 1 to 15psig, more preferably 5psig. In the invention, in the purification process, the pH value of the mixed liquid in the reaction tankPreferably 7 to 8, more preferably 7.4. In the invention, in the purification process, the flow rate of the reflux is preferably 50 to 150 times, more preferably 120 to 130 times of the flow rate of the inlet water, so as to achieve the purpose that the mixed liquid in the reaction tank is in a completely mixed state; according to the invention, preferably, a water body containing oxidative pollutants is continuously introduced into the reaction tank through a water inlet pipeline system by a water inlet pump, and a mixed liquid in the reaction tank is refluxed by a reflux pipeline system by a reflux pump and is converged into the water inlet pipeline system; in embodiments of the present invention, the inlet pump flow rate is preferably 0.63mL/min and the return pump flow rate is preferably 80mL/min.
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
In this example, the most typical oxidizing pollutant nitrate in water is degraded by using a hydrocarbon mixed matrix biofilm reactor, and the specific steps are as follows:
(1) Constructing a hydrocarbon mixed matrix biomembrane reactor according to the figure 1, wherein a reaction tank is formed by processing a square glass tube, the size of the inner wall is 10 multiplied by 10mm, the length of the tube is 350mm, and both ends of the tank wall of the reaction tank are respectively provided with an opening; a hollow fiber membrane assembly is arranged in the reaction tank, the hollow fiber membrane assembly contains 32 hollow fiber membrane filaments, the hollow fiber membrane filaments are made of hydrophobic polypropylene materials, the inner diameter of each hollow fiber membrane filament is 200 micrometers, the outer diameter of each hollow fiber membrane filament is 280 micrometers, and the membrane aperture is 0.02 micrometer; two ends of the hollow fiber membrane component are respectively bonded in the sleeve by epoxy resin glue, and then the sleeve is bonded in the opening on the wall of the reaction tank by the epoxy resin glue to realize the fixation of the hollow fiber membrane component;
(2) Starting and domesticating a hydrocarbon mixed matrix biofilm reactor: inoculating 10mL of anoxic pond sludge from a municipal sewage treatment plant to a reactionIn the reactor (the inoculation amount is 10 percent of the total effective volume of the reactor); preparing first simulated wastewater, wherein the components of the first simulated wastewater comprise: 20mgN/L NaNO 3 100mg/L NaHCO 3 (as inorganic carbon source for microbial growth), 128mg/L KH 2 PO 4 And 434mg/L of Na 2 HPO 4 (as buffer solution to control system pH), 1mg/L MgSO 4 ·7H 2 O, 80mg/L FeSO 4 ·7H 2 O, 1mg/L CaCl 2 ·2H 2 O, 0.013mg/L ZnSO 4 ·7H 2 O, 0.038mg/L H 3 BO 3 0.001mg/L of CuCl 2 ·2H 2 O, 0.004mg/L Na 2 MoO 4 ·2H 2 O, 0.004mg/L MnCl 2 ·4H 2 O, 0.025mg/L CoCl 2 ·6H 2 O, 0.001mg/L NiCl 2 ·6H 2 O and 0.004mg/L Na 2 SeO 3 (providing trace elements required for microbial growth); the first simulated wastewater enters the hydrocarbon mixed matrix biofilm reactor from the bottom of the reaction tank through a water inlet pump and a water inlet pipeline, and the flow rate of the water inlet pump is set to be 0.63mL/min; starting a reflux pump, and setting the flow rate of the reflux pump to be 80mL/min; simultaneously starting a gas supply system to provide high-purity hydrogen (more than or equal to 99 percent) and setting the hydrogen pressure to be 5psig; when a macroscopic biological membrane (the thickness is 700 mu m specifically) is formed on the surface of the hollow fiber membrane in the reactor, monitoring the concentration of nitrate in the effluent every day, and when the concentration of nitrate in the effluent is kept stable for 5 continuous days, the start and the domestication of the hydrocarbon mixed matrix biological membrane reactor can be considered to be finished;
(3) A continuous operation stage:
preparing a second simulated wastewater which is different from the first simulated wastewater only in that NaHCO is not contained 3 、KH 2 PO 4 And Na 2 HPO 4 (ii) a Pumping the second simulated wastewater serving as wastewater to be treated into a reactor for treatment according to the method in the step (2), and providing H by the gas supply system 2 And CO 2 Gas mixture, monitored at H 2 And CO 2 When the operation of the hydrocarbon mixed matrix biomembrane reactor reaches stability under the condition of different molar ratios, the method is suitable for the conditions of high temperature and high pressure of the hydrocarbon mixed matrix biomembrane reactorNitrate removal performance and change in system pH to determine H 2 And CO 2 The optimal molar ratio; wherein in the process H 2 And CO 2 During experiments with different molar ratios, H is always maintained 2 The same partial pressure, i.e., 5.0psig, with different CO settings 2 Partial pressure to maintain available H in a mixed hydrocarbon matrix biofilm reactor 2 The content is consistent;
specific arrangement H 2 With CO 2 The molar ratio of (a).
With CO 2 Reduction of partial pressure, NO in the reactor effluent 3 - The concentration of N gradually decreases from H 2 And CO 2 7.17mg/L at a molar ratio of 2.5 2 4.14mg/L. From NO 3 - Reduction of CO from the viewpoint of removal rate of-N 2 The input of (2) will increase the reactor to NO 3 - Removal efficiency of-N, but when H 2 With CO 2 When the molar ratio of (b) is less than 5.2, the pH of the mixed liquid in the reactor may exceed 8, increasing the risk of precipitation of hardness ions (such as calcium ions and magnesium ions) in the biofilm, and generating an accumulation of nitrite that is more toxic than nitrate. However, when CO is present 2 Excessive input directly results in NO 3 - The removal effect of-N decreases. In summary, when H is used 2 With CO 2 At a molar ratio of 5.2 3 - Concentration of-N6.19 mg/L, NO 3 - The N is kept at a higher removal rate and no nitrite is accumulated, and meanwhile, the pH value of the mixed liquid in the reactor is kept at about 7.4, and the molar ratio can meet the requirement of the long-term growth metabolic process of the hydrogen autotrophic microorganisms on H by combining with theoretical calculation 2 And inorganic carbon, can ensure that the reactor maintains long-term high-efficiency stable operation in the pollutant removal process.
Comparative example 1
After step (3) was completed according to the method of example 1, the operation mode was changed by supplying high-purity hydrogen gas using a gas supply system while feeding the first simulated wastewater as wastewater to be treatedLine treatment, i.e. using NaHCO during the continuous operation phase 3 Use of KH as inorganic carbon source for microbial growth 2 PO 4 And Na 2 HPO 4 The pH value of the system is controlled by using the buffer solution.
The experimental results show that NaHCO is adopted 3 When the pH value of the system is controlled by phosphate buffer solution as a carbon source and the operation mode is changed, NO in the effluent of the reactor 3 - The concentration of-N is 6.5mg/L, NO 3 - Removal of-N relative to H 2 With CO 2 The difference was not large when the mixture was fed at a molar ratio of 5.2:1, but 0.97mg N/L of nitrite was accumulated in the effluent and the pH of the mixture in the reactor was about 8.3. After the reactor is operated for 3 months in the mode for a long time, NO in effluent 3 - Increase of the concentration of-N to 8.6mg/L, NO 3 - -N removal rate compared to H 2 With CO 2 The molar ratio was 5.2, which decreased by 12% when the mixed gas was supplied. Probably because the pH value cannot be effectively controlled in the biological membrane along with the long-term operation of the reactor, hardness ions (such as calcium ions and magnesium ions) generate precipitates in the biological membrane, thereby reducing the mass transfer efficiency of the substrate in the biological membrane and influencing the denitrification activity.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and amendments can be made without departing from the principle of the present invention, and these modifications and amendments should also be considered as the protection scope of the present invention.
Claims (10)
1. A hydrocarbon mixed matrix biomembrane reactor is characterized by comprising a raw water tank, a reaction tank, a water inlet pipeline system, a water outlet pipeline system, a return pipeline system and a gas supply system;
a hollow fiber membrane component is arranged in the reaction tank; one end of the reaction tank, the water inlet pipeline system and the return pipeline system are connected through a tee joint, and the other end of the reaction tank, the water outlet pipeline system and the return pipeline system are connected through a tee joint; the reaction tank, the water inlet pipeline system, the water outlet pipeline system and the return pipeline system form a circulation loop;
the gas supply system comprises H 2 Gas cylinder, H 2 With CO 2 A gas mixing cylinder and a gas supply pipeline, wherein one end of the gas supply pipeline is connected with the H 2 Gas cylinder and H 2 With CO 2 The mixed gas bottle is connected, and the other end of the gas supply pipeline is connected with two ports of the hollow fiber membrane component in the reaction tank.
2. The hydrocarbon mixed matrix biofilm reactor of claim 1, wherein said H is 2 Gas cylinder and H 2 With CO 2 The gas mixing cylinder is independently provided with a gas pressure distributing valve.
3. The hydrocarbon mixed matrix biofilm reactor of claim 1, wherein the reaction tank is vertically disposed and the hollow fiber membrane module comprises a plurality of hollow fiber membrane filaments.
4. The hydrocarbon mixed matrix biofilm reactor of claim 3, wherein the hollow fiber membrane filaments are made of a hydrophobic polypropylene material; the outer diameter of the hollow fiber membrane yarn is 200-2000 mu m; the membrane aperture of the hollow fiber membrane filament is 0.01-0.02 μm.
5. The hydrocarbon mixed matrix biofilm reactor of claim 1, wherein a return pump is provided on the return piping system; and a water inlet pump is arranged on the water inlet pipeline system.
6. A method for purifying a water body containing oxidative pollutants by using the hydrocarbon mixed matrix biofilm reactor of any of claims 1 to 5, comprising the following steps:
inoculating sludge into a hydrocarbon mixed matrix biomembrane reactor, continuously introducing raw water for domestication into a reaction tank through a water inlet pipeline system, and simultaneously providing H by adopting an air supply system 2 The mixed liquid in the reaction tank is refluxedThe pipeline system reflows and converges into the water inlet pipeline system to acclimate the hydrocarbon mixed matrix biomembrane reactor, so that a biomembrane is formed on the surface of a hollow fiber membrane component in the reaction tank;
continuously introducing water containing oxidative pollutants into the reaction tank through a water inlet pipeline system, and simultaneously providing H by adopting a gas supply system 2 With CO 2 The mixed gas, the mixed liquid in the reaction tank flows back through the return pipeline system and is merged into the water inlet pipeline system, and the purification of the water body containing the oxidative pollutants is realized.
7. The method of claim 6, wherein H is 2 With CO 2 H in the mixed gas 2 With CO 2 The molar ratio of (2.5-10): 1.
8. the method according to claim 6 or 7, wherein during the purification, H 2 Is in the range of 1 to 15psig.
9. The method according to claim 6, wherein the pH of the mixed solution in the reaction tank is 7 to 8 during the purification.
10. The method of claim 6, wherein the flow rate of the return water during the purification is 50 to 150 times the flow rate of the feed water.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080302720A1 (en) * | 2007-03-30 | 2008-12-11 | Reid Bowman | Membrane biofilm reactor for removing contaminants from ground water |
| US20090095675A1 (en) * | 2007-09-13 | 2009-04-16 | Applied Process Technology | Water treatment bioreactor using hollow filaments |
| CN103043777A (en) * | 2012-12-07 | 2013-04-17 | 同济大学 | Backflow type hydrogen matrix bio-membrane reactor with carbon dioxide serving as carbon source |
| CN103771588A (en) * | 2013-12-18 | 2014-05-07 | 同济大学 | Reverse-flow type horizontal flow hydrogen substrate bio-membrane reactor based on carbon dioxide as carbon source |
| CN111072137A (en) * | 2020-01-14 | 2020-04-28 | 浙江大学 | Membrane biofilm reactor device and method for sewage treatment |
| CN111186905A (en) * | 2019-04-17 | 2020-05-22 | 麦王环境技术股份有限公司 | Membrane biological reduction reactor and process with hydrogen as electron donor |
| CN114751515A (en) * | 2022-05-05 | 2022-07-15 | 浙江大学 | Stable and efficient short-cut denitrification method and treatment device |
| CN114790037A (en) * | 2022-05-16 | 2022-07-26 | 桂林电子科技大学 | Control of CO 2 Hydrogen-based biomembrane reactor combination device with additive amount and method for treating nitrate-containing sewage |
-
2022
- 2022-09-01 CN CN202211061292.0A patent/CN115520960A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080302720A1 (en) * | 2007-03-30 | 2008-12-11 | Reid Bowman | Membrane biofilm reactor for removing contaminants from ground water |
| US20090095675A1 (en) * | 2007-09-13 | 2009-04-16 | Applied Process Technology | Water treatment bioreactor using hollow filaments |
| CN103043777A (en) * | 2012-12-07 | 2013-04-17 | 同济大学 | Backflow type hydrogen matrix bio-membrane reactor with carbon dioxide serving as carbon source |
| CN103771588A (en) * | 2013-12-18 | 2014-05-07 | 同济大学 | Reverse-flow type horizontal flow hydrogen substrate bio-membrane reactor based on carbon dioxide as carbon source |
| CN111186905A (en) * | 2019-04-17 | 2020-05-22 | 麦王环境技术股份有限公司 | Membrane biological reduction reactor and process with hydrogen as electron donor |
| CN111072137A (en) * | 2020-01-14 | 2020-04-28 | 浙江大学 | Membrane biofilm reactor device and method for sewage treatment |
| CN114751515A (en) * | 2022-05-05 | 2022-07-15 | 浙江大学 | Stable and efficient short-cut denitrification method and treatment device |
| CN114790037A (en) * | 2022-05-16 | 2022-07-26 | 桂林电子科技大学 | Control of CO 2 Hydrogen-based biomembrane reactor combination device with additive amount and method for treating nitrate-containing sewage |
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