CN214383741U - Treatment device for anaerobic digestion liquid of pyrohydrolysis sludge - Google Patents
Treatment device for anaerobic digestion liquid of pyrohydrolysis sludge Download PDFInfo
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- CN214383741U CN214383741U CN202023032543.1U CN202023032543U CN214383741U CN 214383741 U CN214383741 U CN 214383741U CN 202023032543 U CN202023032543 U CN 202023032543U CN 214383741 U CN214383741 U CN 214383741U
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Abstract
The utility model belongs to the technical field of pyrohydrolysis mud anaerobic digestion liquid handles, a processing apparatus of pyrohydrolysis mud anaerobic digestion liquid is disclosed. The treatment device comprises a forward osmosis unit, a high-salt concentration unit, a water production tank and a PLC control unit which are operated independently or simultaneously; the high-salt concentration unit is used for dynamically circulating the membrane treatment process of the forward osmosis unit; the forward osmosis unit comprises a raw material liquid tank, a first filter, an infusion pump, a circulating pump, an FO membrane, a liquid drawing tank and a liquid level sensor. The utility model discloses can move simultaneously and just permeate unit and the concentrated unit of high salt, make just permeate unit's membrane treatment process dynamic cycle goes on. The concentration rate of the drawing liquid after concentration treatment can reach 80 percent. Solves the problem that the anaerobic digestion liquid of the thermal hydrolysis sludge is difficult to treat.
Description
Technical Field
The utility model belongs to the technical field of pyrohydrolysis mud anaerobic digestion liquid handles, specifically, relate to a processing apparatus of pyrohydrolysis mud anaerobic digestion liquid.
Background
The sludge pyrohydrolysis pretreatment technology is an effective sludge pretreatment method, can improve the sludge dewatering performance, reduce the sludge volume and generate higher-level organic destruction which is almost twice of the methane production. However, the thermal hydrolysis pretreatment of sludge also results in the Manndlar reaction, which produces refractory polyurethane, which makes the sludge liquor difficult to process in the subsequent anaerobic digestion process. At present, the commonly used method for treating the anaerobic digestion solution of the thermal hydrolysis sludge is mainly a biological treatment process, but the method requires a very large factory facility and is seriously dependent on environmental conditions. If thermal evaporation concentration is adopted, higher energy consumption is generated. In addition, the filtrate is refluxed to the front end of the water inlet of the sewage treatment plant again after biological treatment, so that the operation cost is increased, and pollutants are accumulated. The anaerobic digestion liquid of the thermal hydrolysis sludge contains rich nitrogen, so that the anaerobic digestion liquid can be concentrated to be used as a plant fertilizer, and the produced water can be recycled, thereby being beneficial to realizing sustainable utilization of resources. Therefore, it is necessary to treat the anaerobic digestion solution of the thermal hydrolysis sludge by a more effective and stable method.
Membrane separation techniques are increasingly gaining importance in wastewater treatment. However, there have been few studies on the treatment of anaerobic digestion liquid of thermal hydrolysis sludge using membrane treatment technology. The pyrohydrolysis sludge anaerobic digestion solution is a mixture containing high ammonia nitrogen and total dissolved solids, and the membrane can cause serious membrane pollution by common membrane separation such as reverse osmosis, nanofiltration and the like. While Forward Osmosis (FO) is an osmotic transmembrane process, the pressure gradient between the feed and draw solutions provides the driving force for separation, and the ability of FO to have high soil reversibility, a property that makes it promising for the treatment of anaerobic digests of thermally hydrolyzed sludge.
Therefore, it is desired to provide a method and an apparatus for treating anaerobic digestion liquid of thermal hydrolysis sludge, so that the anaerobic digestion liquid can be effectively treated and the apparatus can be stably and continuously operated.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a device and a method for treating the anaerobic digestion liquid of the pyrohydrolysis sludge aiming at the defects of the prior art. The utility model discloses can move simultaneously and just permeate unit and the concentrated unit of high salt, make just permeate unit's membrane treatment process dynamic cycle goes on. The concentration rate of the drawing liquid after concentration treatment can reach 80 percent. Solves the problem that the anaerobic digestion liquid of the thermal hydrolysis sludge is difficult to treat.
In order to achieve the aim, the utility model provides a treatment device for the anaerobic digestion liquid of the pyrohydrolysis sludge, which comprises a forward osmosis unit, a high-salt concentration unit, a water production tank and a PLC control unit which are operated independently or simultaneously;
the high-salt concentration unit is used for dynamically circulating the membrane treatment process of the forward osmosis unit;
the PLC control unit is used for controlling the chain reaction of the device.
Preferably, the first and second electrodes are formed of a metal,
the forward osmosis unit comprises a raw material liquid tank, a first filter, an infusion pump, a circulating pump, an FO membrane, a liquid drawing tank and a liquid level sensor;
two ends of the raw material liquid tank are respectively connected with a raw material liquid outlet pipe and a raw material liquid concentrated water circulating pipe, and the other end of the raw material liquid outlet pipe and the other end of the raw material liquid concentrated water circulating pipe are respectively connected with a raw material liquid side of the FO membrane;
the two ends of the drawing liquid box are respectively connected with a permeate inlet pipe and a drawing liquid circulating pipe, and the other end of the permeate inlet pipe and the other end of the drawing liquid circulating pipe are respectively connected with the drawing liquid side of the FO membrane;
the first filter and the infusion pump are sequentially arranged on the raw material liquid outlet pipe and are close to the raw material liquid outlet of the raw material liquid tank; the liquid level sensor is arranged on the raw material liquid concentrated water circulating pipe and is close to a raw material liquid concentrated water inlet of the raw material liquid tank; the circulating pump is arranged on the liquid-drawing circulating pipe and is close to a liquid-drawing water outlet of the liquid-drawing tank;
the positions of the raw material liquid outlet pipe, the raw material liquid concentrated water circulating pipe, the permeate inlet pipe and the draw liquid circulating pipe, which are close to the FO membrane, are provided with a conductivity sensor, an electromagnetic flowmeter and a forward osmosis pressure meter; thermometers are arranged at the positions of the raw material liquid concentrated water circulating pipe and the permeate liquid inlet pipe, which are close to the FO membrane.
Preferably, the FO membrane is a composite membrane or a protein membrane.
Preferably, the composite membrane comprises a cellulose triacetate membrane active layer and a polyester support layer.
Preferably, the high salt concentration unit comprises a membrane nanofiltration device and/or a membrane distillation device.
Preferably, the high-salt concentration unit is connected with the permeate water inlet pipe, the draw solution tank and the water production tank through a second filter, a draw solution concentration return pipe and a water production pipe respectively.
Preferably, a concentrate feed pressure gauge is disposed between the high salt concentration unit and the second filter.
Preferably, a concentrate reflux pressure gauge is arranged on the draw solution concentrate reflux pipe.
Preferably, the raw material liquid tank is provided with a first dosing cleaning tank for cleaning the raw material liquid tank.
Preferably, the liquid drawing tank is provided with a second dosing cleaning tank for cleaning the liquid drawing tank.
The technical scheme of the utility model following beneficial effect has:
(1) the utility model uses forward osmosis to treat the anaerobic digestion liquid of the pyrohydrolysis sludge, can realize low-energy-consumption concentration, and saves energy consumption; the membrane is not easy to pollute, has good cleaning and recovery effects and is not dependent on the environment; the returned raw material liquid concentrated water can be used as organic fertilizer, and the treated produced water has high quality and can be recycled; the utility model solves the problem that the anaerobic digestion liquid of the thermal hydrolysis sludge is difficult to treat.
(2) The utility model discloses can move simultaneously and just permeate unit and the concentrated unit of high salt, make it goes on to just permeate the dynamic cycle of processing.
(3) The utility model discloses the process the concentrated rate of drawing liquid that the concentrated unit of high salt carries out after the concentrated processing can reach 80%.
Other features and advantages of the present invention will be described in detail in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in more detail exemplary embodiments thereof with reference to the attached drawings, in which like reference numerals generally represent like parts throughout the exemplary embodiments of the present invention.
Fig. 1 shows a schematic diagram of a device for treating anaerobic digestion liquid of thermal hydrolysis sludge provided by the embodiment 1 of the utility model.
Fig. 2(a) shows the results of testing the flux change of the present invention in comparative examples 1 to 5, which were subjected to forward osmosis treatment.
Fig. 2(b) shows the results of testing the flux change of forward osmosis treatment performed in examples 3-7 of the present invention.
Fig. 2(c) shows the results of testing the flux change of the present invention in comparative examples 6 to 9, which were subjected to forward osmosis treatment.
Fig. 2(d) shows the results of testing the flux change of forward osmosis treatment performed in examples 8-11 of the present invention.
Fig. 2(e) shows the results of testing the flux change of the present invention comparative examples 10 to 12 for forward osmosis treatment. Wherein: the forward osmosis liquid flux curves with the dotted lines at 1.5L/min and 0.5L/min, respectively, and the forward osmosis liquid flux curves with the solid lines at 2L/min and 1L/min, respectively
Fig. 2(f) shows the results of testing the flux change of forward osmosis treatments performed in examples 12-14 of the present invention. (wherein: curves of forward osmosis liquid flux with time for dotted lines of 1.5L/min and 0.5L/min, respectively, and curves of forward osmosis liquid flux with time for solid lines of 2L/min and 1L/min, respectively.)
Among them, Flux (L/m) in FIG. 22h) Represents the flux of the fluid being permeated; time (min) represents time.
The reference numerals are explained below:
1-raw material liquid tank; 2-a first filter; 3-an infusion pump; 4-a circulating pump; a 5-FO membrane; 6-liquid drawing tank; 7-a liquid level sensor; 8-high salt concentration unit; 9-a raw material liquid outlet pipe; 10-raw material liquid concentrated water circulating pipe; 11-permeate inlet pipe; 12-draw liquid circulating pipe; 13-a conductivity sensor; 14-an electromagnetic flow meter; 15-forward osmometer; 16-a thermometer; 17-a water production tank; 18-a second filter; 19-concentrated reflux tube of drawing liquid; 20-a water production pipe; 21-a first dosing cleaning box; 22-a second dosing cleaning box; 23-the concentrate enters the water pressure gauge; 24-concentrate reflux manometer.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the following describes preferred embodiments of the present invention, it should be understood that the present invention may be embodied in various forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.
The utility model provides a device for treating the anaerobic digestion liquid of the pyrohydrolysis sludge, which comprises a forward osmosis unit, a high-salt concentration unit, a water production tank and a PLC control unit which are operated independently or simultaneously;
the high-salt concentration unit is used for dynamically circulating the membrane treatment process of the forward osmosis unit;
the PLC control unit is used for controlling the chain reaction of the device.
In one example of the use of a magnetic resonance imaging system,
the forward osmosis unit comprises a raw material liquid tank, a first filter, an infusion pump, a circulating pump, an FO membrane, a liquid drawing tank and a liquid level sensor;
two ends of the raw material liquid tank are respectively connected with a raw material liquid outlet pipe and a raw material liquid concentrated water circulating pipe, and the other end of the raw material liquid outlet pipe and the other end of the raw material liquid concentrated water circulating pipe are respectively connected with a raw material liquid side of the FO membrane;
the two ends of the drawing liquid box are respectively connected with a permeate inlet pipe and a drawing liquid circulating pipe, and the other end of the permeate inlet pipe and the other end of the drawing liquid circulating pipe are respectively connected with the drawing liquid side of the FO membrane;
the first filter and the infusion pump are sequentially arranged on the raw material liquid outlet pipe and are close to the raw material liquid outlet of the raw material liquid tank; the liquid level sensor is arranged on the raw material liquid concentrated water circulating pipe and is close to a raw material liquid concentrated water inlet of the raw material liquid tank; the circulating pump is arranged on the liquid-drawing circulating pipe and is close to a liquid-drawing water outlet of the liquid-drawing tank;
the positions of the raw material liquid outlet pipe, the raw material liquid concentrated water circulating pipe, the permeate inlet pipe and the draw liquid circulating pipe, which are close to the FO membrane, are provided with a conductivity sensor, an electromagnetic flowmeter and a forward osmosis pressure meter; thermometers are arranged at the positions of the raw material liquid concentrated water circulating pipe and the permeate liquid inlet pipe, which are close to the FO membrane.
In one example, the FO membrane is a composite membrane or a protein membrane.
In one example, the composite membrane includes a cellulose triacetate membrane active layer and a polyester support layer.
In one example, the high salt concentration unit comprises a membrane nanofiltration device and/or a membrane distillation device.
In one example, the high-salt concentration unit is connected with the permeate water inlet pipe, the draw solution tank and the water production tank through a second filter, a draw solution concentration return pipe and a water production pipe respectively.
In one example, a concentrate feed pressure gauge is disposed between the high salt concentration unit and the second filter.
In one example, a concentrate return pressure gauge is provided on the draw solution concentrate return line.
In one example, the feed solution tank is provided with a first dosing cleaning tank for cleaning the feed solution tank.
In one example, the draw solution tank is provided with a second dosing cleaning tank for cleaning the draw solution tank.
In the utility model, the thermometer, the conductivity sensor, the electromagnetic flowmeter, the forward osmosis pressure gauge, the concentrate inflow pressure gauge and the concentrate return pressure gauge are used for recording the states of various feed liquids, and then the PLC control unit is combined to realize the adjustment of pressure, flow velocity and flow; automatic recording of conductance, throughput, yield; the high salt concentration unit is started, and the dosing cleaning is carried out.
The utility model also provides a processing method of pyrohydrolysis mud anaerobic digestion liquid, this method adopts the processing apparatus of pyrohydrolysis mud anaerobic digestion liquid, including following step:
s1: injecting the thermal hydrolysis sludge anaerobic digestion solution into the raw material solution tank, injecting the drawing solution into the drawing solution tank, starting the infusion pump and the circulating pump, filtering the thermal hydrolysis sludge anaerobic digestion solution through the first filter, performing forward osmosis on the raw material solution side of the FO membrane, obtaining a permeate on the drawing solution side of the FO membrane, obtaining a raw material solution concentrated water on the raw material solution side of the FO membrane, and refluxing the raw material solution concentrated water into the raw material solution tank through the raw material solution concentrated water circulating pipe;
s2: when the TDS difference between the mixed liquid of the drawing liquid and the raw material permeate and the thermal hydrolysis sludge anaerobic digestion liquid is smaller than a threshold value, the high-salt concentration unit is started, the mixed liquid of the drawing liquid and the raw material permeate is concentrated to obtain the drawing liquid and the produced water after the concentration treatment, the drawing liquid after the concentration treatment flows back to the drawing liquid box through the drawing liquid concentration return pipe, and the produced water flows into the production water box.
In one example, in step S1:
the drawing solution is a sodium chloride solution, and the concentration of the sodium chloride is 0.5-4 mol/L;
the temperature of the thermal hydrolysis sludge anaerobic digestion liquid is 20-40 ℃;
the flow rate of the thermal hydrolysis sludge anaerobic digestion liquid injected into the raw material liquid tank is 0.5-20L/min.
In one example, in step S2:
the threshold value is 1000-6000 TDS;
the concentration treatment method carried out by the high-salt concentration unit comprises a membrane nanofiltration treatment method and/or a membrane distillation treatment method.
In one example, the anaerobic digestion solution of the thermal hydrolysis sludge comprises TOC, TN and NH3-N, TP, Fe, Mn, Ca, Mg, with an overall rejection of 85-99% for each component after passing through the FO membrane.
In one example, the concentration rate of the draw solution after the concentration treatment is 20 to 80%.
In one example, the water quality index of the produced water is SDI less than or equal to 1, turbidity less than or equal to 0.2, SS less than 0.2mg/L, and microorganism removal rate greater than 99%.
The present invention will be described in detail with reference to examples.
The calculation formula of the retention rate of each substance in the thermal hydrolysis sludge anaerobic digestion solution after passing through the FO membrane is as follows:
the FO membrane was purchased from Hydration Technology Innovations (USA Hydration Technology Innovations Co., Ltd.)
Example 1
The embodiment provides a treatment device for the anaerobic digestion liquid of the thermal hydrolysis sludge, which comprises a forward osmosis unit, a high-salt concentration unit 8, a water production tank 17 and a PLC (programmable logic controller) control unit which are operated independently or simultaneously, as shown in figure 1;
the high-salt concentration unit 8 is used for dynamically circulating the membrane treatment process of the forward osmosis unit;
the forward osmosis unit comprises a raw material liquid tank 1, a first filter 2, an infusion pump 3, a circulating pump 4, an FO membrane 5, a liquid drawing tank 6 and a liquid level sensor 7; two ends of the raw material liquid tank 1 are respectively connected with a raw material liquid outlet pipe 9 and a raw material liquid concentrated water circulating pipe 10, and the other end of the raw material liquid outlet pipe 9 and the other end of the raw material liquid concentrated water circulating pipe 10 are respectively connected with the raw material liquid side of the FO membrane 5; both ends of the drawing liquid tank 6 are respectively connected with a permeate inlet pipe 11 and a drawing liquid circulating pipe 12, and the other end of the permeate inlet pipe 11 and the other end of the drawing liquid circulating pipe 12 are respectively connected with the drawing liquid side of the FO membrane 5; the first filter 2 and the infusion pump 3 are sequentially arranged on the raw material liquid outlet pipe 9 and are close to the raw material liquid outlet of the raw material liquid tank 1; the liquid level sensor 7 is arranged on the raw material liquid concentrated water circulating pipe 10 and is close to the raw material liquid concentrated water inlet of the raw material liquid tank 1; the circulating pump 4 is arranged on the draw solution circulating pipe 12 and is close to the draw solution outlet of the draw solution tank 6; a conductivity sensor 13, an electromagnetic flow meter 14 and a forward osmosis pressure gauge 15 are arranged at the positions of the raw material liquid outlet pipe 9, the raw material liquid concentrated water circulating pipe 10, the permeate liquid inlet pipe 11 and the draw liquid circulating pipe 12 close to the FO membrane 5; thermometers 16 are arranged at the positions of the raw material liquid concentrated water circulating pipe 10 and the permeate inlet pipe 11 close to the FO membrane 5; the FO membrane 5 is a composite membrane comprising a cellulose triacetate membrane active layer and a polyester support layer.
The high-salt concentration unit 8 comprises a membrane nanofiltration device and a membrane distillation device, and the high-salt concentration unit 8 is respectively connected with the permeate water inlet pipe 11, the draw solution tank 6 and the water production tank 17 through a second filter 18, a draw solution concentration return pipe 19 and a water production pipe 20; a concentrated solution inlet pressure gauge 23 is arranged between the high-salt concentration unit 8 and the second filter 18; and a concentrated reflux pressure gauge 24 is arranged on the drawing liquid concentrated reflux pipe 19. Neither the membrane nanofiltration device nor the membrane distillation device is shown.
The raw material liquid tank 1 is provided with a first dosing cleaning tank 21 for cleaning the raw material liquid tank 1; the liquid drawing tank 6 is provided with a second dosing cleaning tank 22 for cleaning the liquid drawing tank 6.
The PLC control unit is used for controlling the chain reaction of the device.
Example 2
This example provides a method for treating a thermally hydrolyzed sludge anaerobic digestion solution, which uses the device for treating a thermally hydrolyzed sludge anaerobic digestion solution described in example 1, as shown in fig. 1, and includes the following steps:
s1: injecting the thermal hydrolysis sludge anaerobic digestion solution into the raw material solution tank 1, injecting the draw solution into the draw solution tank 6, starting the infusion pump 3 and the circulating pump 4, filtering the thermal hydrolysis sludge anaerobic digestion solution by the first filter 2, performing forward osmosis on the raw material solution side of the FO membrane 5, obtaining a permeate on the draw solution side of the FO membrane 5, obtaining a raw material solution concentrated water on the raw material solution side of the FO membrane 5, and returning the raw material solution concentrated water into the raw material solution tank 1 through the raw material solution concentrated water circulating pipe 10;
s2: when the TDS difference between the mixed solution of the draw solution and the raw material permeate and the thermal hydrolysis sludge anaerobic digestion solution is smaller than a threshold value, the high-salt concentration unit 8 is started to concentrate the mixed solution of the draw solution and the raw material permeate to obtain the concentrated draw solution and the product water, the concentrated draw solution flows back to the draw solution tank 6 through the draw solution concentration return pipe 19, and the product water flows into the product water tank 17.
The drawing solution is a sodium chloride solution, and the concentration of the sodium chloride is 2 mol/L;
the temperature of the thermal hydrolysis sludge anaerobic digestion liquid is 25 ℃;
the flow rate of the thermal hydrolysis sludge anaerobic digestion liquid injected into the raw material liquid tank is 2L/min.
The threshold value is 3000-5000 TDS;
the concentration treatment method performed by the high-salt concentration unit 8 includes a membrane nanofiltration treatment method and a membrane distillation treatment method.
The water quality parameters of the thermal hydrolysis sludge anaerobic digestion solution and the raw material permeate are shown in table 1. The water quality parameters are obtained by testing through a three-dimensional fluorescence spectrometer. Table 1 also includes the rejection rates of each substance in the thermally hydrolyzed sludge anaerobic digester after passing through the FO membrane 5, which are calculated according to the above formula.
TABLE 1 Water quality parameters
The concentration rate of the draw solution after the concentration treatment is 80%. The water quality index of the produced water is that SDI is less than or equal to 1, turbidity is less than or equal to 0.2, SS is less than 0.2mg/L, and microorganism removal rate is 99.99%.
Examples 3 to 7
The draw solution of examples 3-7 was a sodium chloride solution, and the concentrations of the sodium chloride were 0.5mol/L, 1.0mol/L, 2.0mol/L, 3.0mol/L, and 4.0mol/L in this order;
the flow rate of the thermal hydrolysis sludge anaerobic digestion liquid injected into the raw material liquid tank is 1.5L/min;
the temperature of the thermal hydrolysis sludge anaerobic digestion liquid is 25 ℃;
other steps and conditions were the same as in example 2.
Examples 8 to 11
The temperature of the thermal hydrolysis sludge anaerobic digestion solution of the embodiment 8-11 is 20 ℃, 25 ℃, 30 ℃ and 40 ℃ in sequence;
the flow rate of the thermal hydrolysis sludge anaerobic digestion liquid injected into the raw material liquid tank is 1.5L/min.
The drawing solution is a sodium chloride solution, and the concentration of the sodium chloride is 2.0 mol/L;
other steps and conditions were the same as in example 2.
Examples 12 to 14
The flow rates of the thermal hydrolysis sludge anaerobic digestion solution of examples 12 to 14 injected into the raw material liquid tank were 0.5L/min, 1.0L/min, and 1.5L/min in this order.
The drawing solution is a sodium chloride solution, and the concentration of the sodium chloride is 2.0 mol/L;
the temperature of the thermal hydrolysis sludge anaerobic digestion liquid is 25 ℃;
other steps and conditions were the same as in example 2.
Comparative examples 1 to 5
Comparative examples 1-5 the thermo-hydrolyzed sludge anaerobic digest was replaced with deionized water and the procedure described in example 2 was followed.
The drawing solution is a sodium chloride solution, and the concentration of the sodium chloride is 0.5mol/L, 1.0mol/L, 2.0mol/L, 3.0mol/L and 4.0mol/L in sequence;
the temperature of the deionized water is 25 ℃;
the flow rate of injecting the deionized water into the raw material liquid tank is 1.5L/min.
Comparative examples 6 to 9
Comparative examples 6-9 the thermal hydrolysis sludge anaerobic digester was replaced with deionized water and the procedure described in example 2 was followed.
The drawing solution is a sodium chloride solution, and the concentration of the sodium chloride is 2.0 mol/L;
the temperature of the deionized water is 20 ℃, 25 ℃, 30 ℃ and 40 ℃ in sequence;
the flow rate of injecting the deionized water into the raw material liquid tank is 1.5L/min.
Comparative examples 10 to 12
Comparative examples 10-12 the thermo-hydrolyzed sludge anaerobic digester was replaced with deionized water and the procedure described in example 2 was followed.
The drawing solution is a sodium chloride solution, and the concentration of the sodium chloride is 2.0 mol/L;
the temperature of the deionized water is 25 ℃;
the flow rate of the deionized water injected into the raw material liquid tank is 0.5L/min, 1.0L/min and 1.5L/min in sequence.
Test examples 1 to 5
This test example shows the results of testing the flux change of the forward osmosis treatment of comparative examples 1 to 5 and examples 3 to 7 in FIGS. 2(a) and (b), respectively. The test results are recorded by a thermometer, a conductivity sensor, an electromagnetic flow meter, a forward osmosis pressure gauge, a concentrated solution water inlet pressure gauge and a concentrated reflux pressure gauge.
Test examples 6 to 9
This test example shows the results of testing the flux change of the forward osmosis treatment of comparative examples 6 to 9 and examples 8 to 11 in FIGS. 2(c) and (d), respectively. The test results are recorded by a thermometer, a conductivity sensor, an electromagnetic flow meter, a forward osmosis pressure gauge, a concentrated solution water inlet pressure gauge and a concentrated reflux pressure gauge.
Test examples 10 to 12
This test example shows the results of the tests of the flux change of the forward osmosis treatment of comparative examples 10 to 12 and examples 12 to 14 in FIGS. 2(e) and (f), respectively. The test results are recorded by a thermometer, a conductivity sensor, an electromagnetic flow meter, a forward osmosis pressure gauge, a concentrated solution water inlet pressure gauge and a concentrated reflux pressure gauge.
While various embodiments of the present invention have been described above, the above description is intended to be illustrative, not exhaustive, and not limited to the disclosed embodiments. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (10)
1. The device for treating the anaerobic digestion liquid of the thermal hydrolysis sludge is characterized by comprising a forward osmosis unit, a high-salt concentration unit, a water production tank and a PLC (programmable logic controller) control unit which are operated independently or simultaneously;
the high-salt concentration unit is used for dynamically circulating the membrane treatment process of the forward osmosis unit;
the PLC control unit is used for controlling the chain reaction of the device.
2. The apparatus for treating pyrohydrolysis sludge anaerobic digester according to claim 1, wherein the forward osmosis unit comprises a raw material liquid tank, a first filter, an infusion pump, a circulation pump, an FO membrane, a draw liquid tank, and a liquid level sensor;
two ends of the raw material liquid tank are respectively connected with a raw material liquid outlet pipe and a raw material liquid concentrated water circulating pipe, and the other end of the raw material liquid outlet pipe and the other end of the raw material liquid concentrated water circulating pipe are respectively connected with a raw material liquid side of the FO membrane;
the two ends of the drawing liquid box are respectively connected with a permeate inlet pipe and a drawing liquid circulating pipe, and the other end of the permeate inlet pipe and the other end of the drawing liquid circulating pipe are respectively connected with the drawing liquid side of the FO membrane;
the first filter and the infusion pump are sequentially arranged on the raw material liquid outlet pipe and are close to the raw material liquid outlet of the raw material liquid tank; the liquid level sensor is arranged on the raw material liquid concentrated water circulating pipe and is close to a raw material liquid concentrated water inlet of the raw material liquid tank; the circulating pump is arranged on the liquid-drawing circulating pipe and is close to a liquid-drawing water outlet of the liquid-drawing tank;
the positions of the raw material liquid outlet pipe, the raw material liquid concentrated water circulating pipe, the permeate inlet pipe and the draw liquid circulating pipe, which are close to the FO membrane, are provided with a conductivity sensor, an electromagnetic flowmeter and a forward osmosis pressure meter; thermometers are arranged at the positions of the raw material liquid concentrated water circulating pipe and the permeate liquid inlet pipe, which are close to the FO membrane.
3. The apparatus for processing the pyro lytic sludge anaerobic digester effluent of claim 2, wherein the FO membrane is a composite membrane or a protein membrane.
4. The apparatus of claim 3, wherein the composite membrane comprises a cellulose triacetate membrane active layer and a polyester support layer.
5. The apparatus for treating pyro lytic sludge anaerobic digestion solution of claim 2, wherein said high salt concentration unit comprises a membrane nano-filtration apparatus and/or a membrane distillation apparatus.
6. The device for treating the anaerobic digestion solution of the pyrohydrolysis sludge as claimed in claim 5, wherein the high-salt concentration unit is connected with the permeate inlet pipe, the draw solution tank and the water production tank through a second filter, a draw solution concentration return pipe and a water production pipe respectively.
7. The apparatus for treating thermally hydrolyzed sludge anaerobic digestion liquid according to claim 6, wherein a concentrate water inflow pressure gauge is provided between the high salt concentration unit and the second filter.
8. The apparatus for treating a pyrohydrolysis sludge anaerobic digestion solution as claimed in claim 6, wherein a concentrate reflux pressure gauge is provided on the draw solution concentrate reflux pipe.
9. The apparatus of claim 2, wherein the feed tank is equipped with a first chemical-adding cleaning tank for cleaning the feed tank.
10. The device for treating the anaerobic digestion solution of the pyrohydrolysis sludge as claimed in claim 2, wherein the liquid-drawing tank is provided with a second chemical-adding cleaning tank for cleaning the liquid-drawing tank.
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