CN116143361B - Method for synchronously recycling protein and ammonia in anaerobic sludge by combining alkali pretreatment with electric fermentation system - Google Patents
Method for synchronously recycling protein and ammonia in anaerobic sludge by combining alkali pretreatment with electric fermentation system Download PDFInfo
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- 239000010802 sludge Substances 0.000 title claims abstract description 67
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 102000004169 proteins and genes Human genes 0.000 title claims abstract description 46
- 108090000623 proteins and genes Proteins 0.000 title claims abstract description 46
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 33
- 238000000855 fermentation Methods 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 30
- 230000004151 fermentation Effects 0.000 title claims abstract description 29
- 239000003513 alkali Substances 0.000 title claims abstract description 19
- 238000004064 recycling Methods 0.000 title claims abstract description 10
- 238000011084 recovery Methods 0.000 claims abstract description 19
- 235000019750 Crude protein Nutrition 0.000 claims abstract description 12
- 239000008186 active pharmaceutical agent Substances 0.000 claims description 24
- 239000011259 mixed solution Substances 0.000 claims description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- 239000010439 graphite Substances 0.000 claims description 10
- 229910002804 graphite Inorganic materials 0.000 claims description 10
- 238000005119 centrifugation Methods 0.000 claims description 9
- 239000000413 hydrolysate Substances 0.000 claims description 9
- 239000006228 supernatant Substances 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 238000005273 aeration Methods 0.000 claims description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- 230000001105 regulatory effect Effects 0.000 claims description 7
- 239000012153 distilled water Substances 0.000 claims description 6
- 239000008055 phosphate buffer solution Substances 0.000 claims description 6
- 238000001556 precipitation Methods 0.000 claims description 5
- 239000000243 solution Substances 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 5
- 230000001360 synchronised effect Effects 0.000 claims description 5
- 229910021607 Silver chloride Inorganic materials 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 238000005341 cation exchange Methods 0.000 claims description 4
- 238000007865 diluting Methods 0.000 claims description 4
- 230000007062 hydrolysis Effects 0.000 claims description 4
- 238000006460 hydrolysis reaction Methods 0.000 claims description 4
- 239000012528 membrane Substances 0.000 claims description 4
- 235000015097 nutrients Nutrition 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000002245 particle Substances 0.000 claims description 4
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- HKZLPVFGJNLROG-UHFFFAOYSA-M silver monochloride Chemical compound [Cl-].[Ag+] HKZLPVFGJNLROG-UHFFFAOYSA-M 0.000 claims description 4
- 239000000758 substrate Substances 0.000 claims description 4
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 claims description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 3
- 238000004108 freeze drying Methods 0.000 claims description 3
- 239000002054 inoculum Substances 0.000 claims description 3
- 235000016709 nutrition Nutrition 0.000 claims description 3
- 230000035764 nutrition Effects 0.000 claims description 3
- 235000017281 sodium acetate Nutrition 0.000 claims description 3
- 239000001632 sodium acetate Substances 0.000 claims description 3
- 229910052719 titanium Inorganic materials 0.000 claims description 3
- 239000010936 titanium Substances 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 2
- 238000006297 dehydration reaction Methods 0.000 claims description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims 2
- 239000011780 sodium chloride Substances 0.000 claims 1
- 238000011282 treatment Methods 0.000 abstract description 10
- 230000015556 catabolic process Effects 0.000 abstract description 2
- 238000006731 degradation reaction Methods 0.000 abstract description 2
- 230000000052 comparative effect Effects 0.000 description 7
- 238000002156 mixing Methods 0.000 description 5
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000002551 biofuel Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000012258 culturing Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000009997 thermal pre-treatment Methods 0.000 description 1
- 238000011269 treatment regimen Methods 0.000 description 1
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
- C02F11/00—Treatment of sludge; Devices therefor
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/006—Electrochemical treatment, e.g. electro-oxidation or electro-osmosis
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07K—PEPTIDES
- C07K1/00—General methods for the preparation of peptides, i.e. processes for the organic chemical preparation of peptides or proteins of any length
- C07K1/14—Extraction; Separation; Purification
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07K—PEPTIDES
- C07K1/00—General methods for the preparation of peptides, i.e. processes for the organic chemical preparation of peptides or proteins of any length
- C07K1/14—Extraction; Separation; Purification
- C07K1/30—Extraction; Separation; Purification by precipitation
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/27—Ammonia
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/50—Processes
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Electrochemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- Genetics & Genomics (AREA)
- Environmental & Geological Engineering (AREA)
- Metallurgy (AREA)
- Hydrology & Water Resources (AREA)
- Health & Medical Sciences (AREA)
- Biochemistry (AREA)
- Biophysics (AREA)
- General Health & Medical Sciences (AREA)
- Water Supply & Treatment (AREA)
- Medicinal Chemistry (AREA)
- Molecular Biology (AREA)
- Proteomics, Peptides & Aminoacids (AREA)
- Inorganic Chemistry (AREA)
- Materials Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention discloses a method for synchronously recycling protein and ammonia in anaerobic sludge by utilizing an alkali pretreatment combined with an electric fermentation system, belongs to the field of sludge treatment and resource recycling, and particularly relates to a method for synchronously recycling protein and ammonia in anaerobic sludge by utilizing an alkali pretreatment combined with an electric fermentation system. The invention aims to solve the problem that protein and ammonia cannot be synchronously recovered at the same time during anaerobic sludge treatment. The method comprises the following steps: crude protein is recovered through the alkaline pretreatment of dehydrated sludge, and then the residual sludge is degraded by an electrofermentation system and ammonia is recovered at a cathode. The results of the study showed that the alkaline heat pretreatment achieved a protein recovery of 72.23%. The subsequent electric fermentation system realizes more thorough sludge COD removal than the conventional anaerobic fermentation: the SCOD degradation efficiency of the EFS system is improved by 28.80 percent. The TCOD removal rate is improved by 6.39%. In addition, EFS realizes higher ammonia recovery efficiency which reaches 71.3 percent. The ratio is improved by 1.73 times compared with the open-circuit anaerobic reactor.
Description
Technical Field
The invention belongs to the field of sludge treatment and resource recovery, and particularly relates to a method for synchronously recovering protein and ammonia in anaerobic sludge by combining alkaline pretreatment with an electric fermentation system.
Background
In recent years, the treatment of excess sludge generated in sewage treatment has attracted attention by researchers in terms of its increasing number and potential environmental problems. Thus, under stringent sludge management/disposal regulations, it is necessary to re-evaluate the sludge treatment strategy. Because of their high content of organics (59-88% w/v) and nutrients (N and P), the excess sludge is considered a renewable resource that can be converted into value added products such as biomass, biochemicals and biofuels. Protein as its main component (32-41% of TS) is of great interest in recovery from sludge. The protein is directly recovered from the sludge, rather than treating all sludge components as hazardous waste, providing a solution to overcome excessive energy and resource investment in sludge management. The extraction of crude proteins from WAS uses different techniques and processes, including physical, thermal, chemical, biological and comprehensive pretreatment methods. After sludge decomposition, inorganic salts, organic solvents and isoelectric precipitation methods are widely used to precipitate and recover proteins from sludge hydrolysates. Although various protein recovery methods have been evaluated, studies on protein recovery from dewatered sludge have been limited, and comprehensive treatment of sludge residue after protein recovery has not been studied; protein and ammonia cannot be synchronously recovered at the same time during anaerobic sludge treatment.
Disclosure of Invention
The invention aims to solve the problem that protein and ammonia cannot be synchronously recovered at the same time during anaerobic sludge treatment, and provides a method for synchronously recovering protein and ammonia in anaerobic sludge by combining alkaline pretreatment with an electric fermentation system.
The invention discloses a method for synchronously recycling protein and ammonia in anaerobic sludge by combining alkali pretreatment with an electric fermentation system, which comprises the following steps:
1. diluting the dehydrated sludge with distilled water to obtain DS mixed solution; regulating the pH value of the DS mixed solution to 12-13, then placing the DS mixed solution into a heat-collecting magnetic stirrer, stirring for 4-5 hours at 90-100 ℃, and centrifuging the sludge hydrolysate after hydrolysis to obtain protein supernatant; regulating the pH value of the protein supernatant to 3-4, performing isoelectric precipitation, centrifuging to recover crude protein, freeze-drying the crude protein particles, and recovering residual DS raffinate;
2. constructing a double-chamber EFS reactor which is separated by a cation exchange membrane; graphite felt is used as an anode and a cathode, and KCl saturated Ag/AgCl in an anode chamber is used as a reference electrode; enriching an active biological film on an anode by adopting an MFC method; the anode of the pre-acclimated biofilm is then maintained in the EFS reactor;
3. mixing DS raffinate with a nutrition phosphate buffer solution with the concentration of 100mmol/L to serve as a substrate of an electrofermentation system; the cathode chamber is added with a solution with the concentration of 100 mmol/LNaCl; removing oxygen by adopting a nitrogen aeration anode chamber; the anode potential of the EFS reactor is constant at 0.2V; and (3) operating the reactor for 15-20 days to complete synchronous recovery of protein and ammonia in the anaerobic sludge by combining the alkali pretreatment with the electric fermentation system.
The invention has the beneficial effects that:
the invention realizes the treatment of dehydrated sludge by combining alkali pretreatment with an electric fermentation system and synchronous recovery of protein and ammonia, and the result shows that the recovery rate of 72.23 percent of protein is realized by alkali thermal pretreatment; compared with the conventional anaerobic fermentation, the subsequent electric fermentation system not only realizes more thorough sludge COD removal, but also realizes more efficient ammonia recovery at the same time; the SCOD degradation efficiency of the EFS system is improved by 28.80%, the TCOD removal rate is improved by 6.39%, the ammonia recovery efficiency is up to 71.3%, and the efficiency is improved by 1.73 times compared with that of an open-loop anaerobic reactor.
Drawings
FIG. 1 is a graph showing the comparison of protein content of the hydrolysate before and after the step one of the example; wherein 1 represents dehydrated sludge, 2 represents protein supernatant, and 3 represents DS raffinate;
FIG. 2 is a graph showing SCOD change under various conditions according to an embodiment of the present invention; wherein 1 represents example one, 2 represents comparative example;
FIG. 3 is a graph showing TCOD removal under various conditions according to an embodiment of the present invention; wherein 1 represents the removal rate of example one, 2 represents the removal rate of comparative example, a represents the initial state, and B represents water;
FIG. 4 is a graph showing the variation of the concentration of ammonia nitrogen at the anode under different conditions in the examples; wherein 1 represents example one, 2 represents comparative example;
FIG. 5 is a graph showing the concentration of ammonia nitrogen at the cathode under different conditions in the examples; wherein 1 represents example one and 2 represents comparative example.
Detailed Description
The first embodiment is as follows: the method for synchronously recycling protein and ammonia in anaerobic sludge by combining alkali pretreatment with an electric fermentation system in the embodiment specifically comprises the following steps:
1. diluting the dehydrated sludge with distilled water to obtain DS mixed solution; regulating the pH value of the DS mixed solution to 12-13, then placing the DS mixed solution into a heat-collecting magnetic stirrer, stirring for 4-5 hours at 90-100 ℃, and centrifuging the sludge hydrolysate after hydrolysis to obtain protein supernatant; regulating the pH value of the protein supernatant to 3-4, performing isoelectric precipitation, centrifuging to recover crude protein, freeze-drying the crude protein particles, and recovering residual DS raffinate;
2. constructing a double-chamber EFS reactor which is separated by a cation exchange membrane; graphite felt is used as an anode and a cathode, and KCl saturated Ag/AgCl in an anode chamber is used as a reference electrode; enriching an active biological film on an anode by adopting an MFC method; the anode of the pre-acclimated biofilm is then maintained in the EFS reactor;
3. mixing DS raffinate with a nutrition phosphate buffer solution with the concentration of 100mmol/L to serve as a substrate of an electrofermentation system; the cathode chamber is added with a solution with the concentration of 100 mmol/LNaCl; removing oxygen by adopting a nitrogen aeration anode chamber; the anode potential of the EFS reactor is constant at 0.2V; and (3) operating the reactor for 15-20 days to complete synchronous recovery of protein and ammonia in the anaerobic sludge by combining the alkali pretreatment with the electric fermentation system.
The second embodiment is as follows: the first difference between this embodiment and the specific embodiment is that: in the first step, the volume ratio of the dehydrated sludge to the distilled water is 1:2. The other is the same as in the first embodiment.
And a third specific embodiment: the first difference between this embodiment and the specific embodiment is that: the dehydration rate of the dehydrated sludge in the first step is 79-80%, and the TCOD content is 103-114 g/L. The other is the same as in the first embodiment.
The specific embodiment IV is as follows: the present embodiment is different from the specific embodiment one by one in that: the moisture content of the DS mixed solution in the first step is 92-95%. The other is the same as in the first embodiment.
Fifth embodiment: the first difference between this embodiment and the specific embodiment is that: centrifugation parameters for centrifuging the sludge hydrolysate in step one: the temperature is 4 ℃, the rotating speed is 10000r/min, and the centrifugation time is 30min. The other is the same as in the first embodiment.
Specific embodiment six: the first difference between this embodiment and the specific embodiment is that: centrifugation parameters for recovering crude protein by centrifugation in step one: the temperature was 4℃and the rotational speed was 12000r/min, and the centrifugation time was 30min. The other is the same as in the first embodiment.
Seventh embodiment: this embodiment differs from the first or fourth embodiment in that: in the second stepThe MFC method is to take activated sludge as anode inoculum, 1g/L sodium acetate as anolyte, 50mmol/LK 3 Fe(CN) 6 Mixing with 100mmol/LPBS to obtain catholyte. The others are the same as in the first or fourth embodiment.
Eighth embodiment: the first difference between this embodiment and the specific embodiment is that: in the second step, the length of the graphite felt is 45mm, the width is 25mm, and the thickness is 3mm; the graphite felt is connected by titanium wires. The other is the same as in the first embodiment.
Detailed description nine: the first difference between this embodiment and the specific embodiment is that: and in the third step, the aeration time of nitrogen aeration is 30min. The other is the same as in the first embodiment.
Detailed description ten: the first difference between this embodiment and the specific embodiment is that: the pH of the nutrient phosphate buffer solution with the concentration of 100mmol/L in the third step is 7. The other is the same as in the first embodiment.
The following examples are used to verify the benefits of the present invention:
embodiment one: the method for synchronously recycling protein and ammonia in anaerobic sludge by combining alkali pretreatment with an electric fermentation system comprises the following steps:
1. diluting the dehydrated sludge with distilled water with the volume twice that of the dehydrated sludge to obtain DS mixed solution; regulating the pH of the DS mixed solution to 12.5, then placing the DS mixed solution in a heat-collecting magnetic stirrer, stirring for 4.5 hours at 100 ℃, centrifuging the sludge hydrolysate after hydrolysis (the temperature is 4 ℃, the rotating speed is 10000r/min, and the centrifuging time is 30 min) to obtain a hydrolyzed precipitate and a protein supernatant; the Hydrolyzed Precipitate (HP) is stored for subsequent electrofermentation treatment; regulating pH of the protein supernatant to 3, performing isoelectric precipitation, stirring for 15min, centrifuging (at 4deg.C and rotational speed of 12000r/min for 30 min), recovering crude protein, lyophilizing the crude protein particles, and recovering residual DS raffinate; the moisture content of the DS mixed solution is 93%; detecting that the protein content in the hydrolysate reaches 4171.25 +/-23.75 mg/L after the alkaline heat treatment, and reducing the protein content in the hydrolysate to 1158.12 +/-16.87 mg/L after isoelectric point sedimentation under the condition that the pH value is 3, so that the protein recovery rate of 72.23% is realized;
2. construction of double ChamberEFS reactor, each room liquid volume is 120mL, separated by cation exchange membrane; graphite felt as anode and cathode, KCl saturated Ag/AgCl in the anode chamber as reference electrode (+199 mV compared to standard hydrogen electrode SHE); taking activated sludge as an anode inoculum, 1g/L sodium acetate as anolyte, 50mmol/LK 3 Fe(CN) 6 Mixing with 100mmol/LPBS to obtain catholyte, and enriching active biological film on anode by MFC method; determining an anode CV curve after culturing for 30 days to verify that the biofilm has been enriched, and then retaining the anode of the pre-acclimated biofilm in the EFS reactor; the length of the graphite felt is 45mm, the width is 25mm, and the thickness is 3mm; the graphite felt is connected by titanium wires;
3. mixing DS raffinate with 120mL of a nutrient phosphate buffer solution with the concentration of 100mmol/L, pH of 7 to serve as a substrate of an electrofermentation system; the cathode chamber is added with a solution with the concentration of 100 mmol/LNaCl; aerating the anode chamber with nitrogen (99.999%) for 30min to remove oxygen; the anode potential of the EFS reactor is constant at 0.2V; the EFS reactor is operated for 17 days, and the synchronous recovery of protein and ammonia in the anaerobic sludge by combining the alkaline pretreatment with the electric fermentation system is completed; after 17 days of fermentation, the TCOD removal rate of the sludge is measured to reach 75.91%. EFS-TS anode chamber NH 4 + The N concentration is reduced to 100.00.+ -. 5.56mg-N/L, and the cathodic NH 4 + The concentration of the-N is increased to 248.80 +/-28.11 mg-N/L, so that 71.3% recovery rate of ammonia in the sludge fermentation liquor is realized.
Comparative example: this embodiment differs from the first embodiment in that the dual chambers are set to open circuits without an applied potential. After 17 days of fermentation, the TCOD removal rate was 71.35%. Is arranged to open circuit for conventional anaerobic fermentation, NH in sludge suspension 4 + The N concentration increased to 326.85.+ -. 6.25mg-N/L after 17 days. At the same time, NH in catholyte due to diffusion of concentration gradients 4 + N is 115.74 + -8.64 mg-N/L.
As can be seen from fig. 1-5, the first example achieved a protein recovery of 72.23%. Compared with the comparative example, the efficiency of degrading SCOD is improved by 28.80%, the removal rate of TCOD is improved by 6.39%, and the embodiment realizes higher ammonia recovery rate which reaches 71.3%. The ratio of the preparation is improved by 1.73 times compared with the comparative example.
Claims (10)
1. A method for synchronously recovering protein and ammonia in anaerobic sludge by combining alkali pretreatment with an electric fermentation system is characterized by comprising the following steps:
1. diluting the dehydrated sludge with distilled water to obtain DS mixed solution; adjusting the pH of the DS mixed solution to 12-13, then placing the DS mixed solution in a heat-collecting magnetic stirrer, stirring for 4-5 hours at 90-100 ℃, and centrifuging the sludge hydrolysate after hydrolysis to obtain protein supernatant; regulating the pH value of the protein supernatant to 3-4, performing isoelectric precipitation, centrifuging to recover crude protein, freeze-drying the crude protein particles, and recovering residual DS raffinate;
2. constructing a double-chamber EFS reactor which is separated by a cation exchange membrane; graphite felt is used as an anode and a cathode, and KCl saturated Ag/AgCl in an anode chamber is used as a reference electrode; enriching an active biological film on an anode by adopting an MFC method; the anode of the pre-acclimated biofilm is then maintained in the EFS reactor;
3. the DS raffinate and a mixed solution of a nutrition phosphate buffer solution with the concentration of 100mmol/L are used as substrates of an electrofermentation system; adding NaCl solution with the concentration of 100mmol/L into the cathode chamber; removing oxygen by adopting a nitrogen aeration anode chamber; the anode potential of the EFS reactor is constant at 0.2V; and (3) operating the reactor for 15-20 days to complete synchronous recovery of protein and ammonia in the anaerobic sludge by combining the alkali pretreatment with the electric fermentation system.
2. The method for synchronously recovering protein and ammonia in anaerobic sludge by combining alkali pretreatment and an electric fermentation system according to claim 1, wherein the volume ratio of the dewatered sludge to distilled water in the step one is 1:2.
3. The method for synchronously recycling protein and ammonia in anaerobic sludge by combining alkaline pretreatment and an electric fermentation system according to claim 1, wherein the dehydration rate of the dehydrated sludge in the step one is 79-80%, and the TCOD content is 103-114 g/L.
4. The method for synchronously recycling protein and ammonia in anaerobic sludge by combining alkaline pretreatment with an electric fermentation system according to claim 1, wherein the DS mixed solution in the step one has a water content of 92-95%.
5. The method for synchronously recovering protein and ammonia in anaerobic sludge by combining alkaline pretreatment with an electric fermentation system according to claim 1, wherein the centrifugation parameters of the sludge hydrolysate centrifugation in the step one are as follows: the temperature is 4 ℃, the rotating speed is 10000r/min, and the centrifugation time is 30min.
6. The method for synchronously recovering protein and ammonia in anaerobic sludge by combining alkali pretreatment with an electric fermentation system according to claim 1, wherein the centrifugal parameters of centrifugally recovering crude protein in the step one are as follows: the temperature was 4℃and the rotational speed was 12000r/min, and the centrifugation time was 30min.
7. The method for synchronously recovering protein and ammonia in anaerobic sludge by combining alkali pretreatment and electric fermentation system as claimed in claim 1, wherein in the step two, the MFC method is characterized in that activated sludge is used as an anodic inoculum, 1g/L sodium acetate is used as anolyte, and 50mmol/L K 3 Fe(CN) 6 Mixed with 100mmol/L PBS to obtain catholyte.
8. The method for synchronously recovering protein and ammonia in anaerobic sludge by combining alkali pretreatment and an electric fermentation system according to claim 1, wherein the length of the graphite felt in the second step is 45mm, the width is 25mm and the thickness is 3mm; the graphite felt is connected by titanium wires.
9. The method for synchronously recovering protein and ammonia in anaerobic sludge by combining alkali pretreatment and an electric fermentation system according to claim 1, wherein the aeration time of nitrogen aeration in the step three is 30min.
10. The method for synchronously recovering protein and ammonia in anaerobic sludge by combining alkali pretreatment with an electric fermentation system according to claim 1, wherein in the third step, the pH of the 100mmol/L nutrient phosphate buffer solution is 7.
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