CN114315073A - Starting method of anaerobic digestion reactor - Google Patents
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- CN114315073A CN114315073A CN202111533940.3A CN202111533940A CN114315073A CN 114315073 A CN114315073 A CN 114315073A CN 202111533940 A CN202111533940 A CN 202111533940A CN 114315073 A CN114315073 A CN 114315073A
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- 230000029087 digestion Effects 0.000 title claims abstract description 72
- 238000000034 method Methods 0.000 title claims abstract description 51
- 239000010802 sludge Substances 0.000 claims abstract description 82
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000004519 manufacturing process Methods 0.000 claims abstract description 20
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000000872 buffer Substances 0.000 claims abstract description 17
- 238000007789 sealing Methods 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims abstract description 14
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims abstract description 12
- 238000003756 stirring Methods 0.000 claims abstract description 12
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims abstract description 10
- 239000000395 magnesium oxide Substances 0.000 claims abstract description 10
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 9
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 6
- 238000010438 heat treatment Methods 0.000 claims abstract description 6
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims abstract description 6
- 229910000019 calcium carbonate Inorganic materials 0.000 claims abstract description 5
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000005416 organic matter Substances 0.000 claims description 24
- 238000000855 fermentation Methods 0.000 claims description 12
- 230000004151 fermentation Effects 0.000 claims description 12
- 239000011734 sodium Substances 0.000 claims description 11
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 8
- PXEDJBXQKAGXNJ-QTNFYWBSSA-L disodium L-glutamate Chemical compound [Na+].[Na+].[O-]C(=O)[C@@H](N)CCC([O-])=O PXEDJBXQKAGXNJ-QTNFYWBSSA-L 0.000 claims description 7
- 235000013923 monosodium glutamate Nutrition 0.000 claims description 7
- 229940073490 sodium glutamate Drugs 0.000 claims description 7
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 6
- 239000011668 ascorbic acid Substances 0.000 claims description 6
- 229910000366 copper(II) sulfate Inorganic materials 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 4
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims description 3
- 229910021580 Cobalt(II) chloride Inorganic materials 0.000 claims description 3
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 3
- 229910004619 Na2MoO4 Inorganic materials 0.000 claims description 3
- 229910021586 Nickel(II) chloride Inorganic materials 0.000 claims description 3
- KGBXLFKZBHKPEV-UHFFFAOYSA-N boric acid Chemical compound OB(O)O KGBXLFKZBHKPEV-UHFFFAOYSA-N 0.000 claims description 3
- 239000001110 calcium chloride Substances 0.000 claims description 3
- 229910001628 calcium chloride Inorganic materials 0.000 claims description 3
- 230000007423 decrease Effects 0.000 claims description 3
- BNIILDVGGAEEIG-UHFFFAOYSA-L disodium hydrogen phosphate Chemical compound [Na+].[Na+].OP([O-])([O-])=O BNIILDVGGAEEIG-UHFFFAOYSA-L 0.000 claims description 3
- 229910000397 disodium phosphate Inorganic materials 0.000 claims description 3
- 210000003608 fece Anatomy 0.000 claims description 3
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 3
- 239000010871 livestock manure Substances 0.000 claims description 3
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 3
- QMMRZOWCJAIUJA-UHFFFAOYSA-L nickel dichloride Chemical compound Cl[Ni]Cl QMMRZOWCJAIUJA-UHFFFAOYSA-L 0.000 claims description 3
- 244000144977 poultry Species 0.000 claims description 3
- 239000011684 sodium molybdate Substances 0.000 claims description 3
- TVXXNOYZHKPKGW-UHFFFAOYSA-N sodium molybdate (anhydrous) Chemical compound [Na+].[Na+].[O-][Mo]([O-])(=O)=O TVXXNOYZHKPKGW-UHFFFAOYSA-N 0.000 claims description 3
- 239000010902 straw Substances 0.000 claims description 3
- 235000013311 vegetables Nutrition 0.000 claims description 3
- 239000010806 kitchen waste Substances 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 239000002699 waste material Substances 0.000 claims description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 abstract description 60
- 235000019260 propionic acid Nutrition 0.000 abstract description 30
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 abstract description 30
- 241000894006 Bacteria Species 0.000 abstract description 13
- 238000009825 accumulation Methods 0.000 abstract description 12
- 239000002253 acid Substances 0.000 abstract description 12
- 230000000696 methanogenic effect Effects 0.000 abstract description 7
- 230000002503 metabolic effect Effects 0.000 abstract description 4
- 239000000243 solution Substances 0.000 description 7
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000010865 sewage Substances 0.000 description 6
- 239000010813 municipal solid waste Substances 0.000 description 5
- 230000003247 decreasing effect Effects 0.000 description 4
- 230000001590 oxidative effect Effects 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- 235000010323 ascorbic acid Nutrition 0.000 description 3
- 229960005070 ascorbic acid Drugs 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000020477 pH reduction Effects 0.000 description 3
- 230000001737 promoting effect Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 230000002411 adverse Effects 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 238000005034 decoration Methods 0.000 description 2
- 230000003301 hydrolyzing effect Effects 0.000 description 2
- 239000003112 inhibitor Substances 0.000 description 2
- 244000144972 livestock Species 0.000 description 2
- 239000002366 mineral element Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 230000033116 oxidation-reduction process Effects 0.000 description 2
- 230000036961 partial effect Effects 0.000 description 2
- -1 rare elements Substances 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 239000000758 substrate Substances 0.000 description 2
- NQPDZGIKBAWPEJ-UHFFFAOYSA-N valeric acid Chemical compound CCCCC(O)=O NQPDZGIKBAWPEJ-UHFFFAOYSA-N 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 229910015667 MoO4 Inorganic materials 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 239000012062 aqueous buffer Substances 0.000 description 1
- 239000006172 buffering agent Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 239000003623 enhancer Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000002829 reductive effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229940005605 valeric acid Drugs 0.000 description 1
Classifications
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Treatment Of Sludge (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention belongs to the technical field of anaerobic digestion, and particularly relates to a starting method of an anaerobic digestion reactor. The method comprises the following steps: a) pouring undigested sludge into an anaerobic digestion reactor, and sealing and placing for 24-48 h; b) adding a biological promoter and a buffer agent into the anaerobic digestion reactor, introducing nitrogen, deoxidizing, sealing, and fermenting at 36-45 ℃; the buffer is one or more of magnesium oxide, calcium carbonate and ferric oxide; c) and (3) heating the anaerobic digestion reactor to 55-60 ℃, stirring, and periodically adding fresh organic matters until the gas production is stable. The technical scheme provided by the invention has the advantages of no need of inoculating exogenous strains, low investment cost, shortened start time of high-temperature anaerobic digestion, rapid establishment of metabolic balance of acid-producing bacteria and methanogenic bacteria under a high-temperature condition, reduction of propionic acid accumulation in the start process, and realization of stability and high efficiency of the methane production process of a sludge high-temperature anaerobic digestion system.
Description
Technical Field
The invention belongs to the technical field of anaerobic digestion, and particularly relates to a starting method of an anaerobic digestion reactor.
Background
At present, the sludge recycling technology mainly comprises aerobic and anaerobic biological treatment methods, wherein anaerobic digestion can recover biomass energy while reducing sludge, and is a common method for realizing a sludge stabilization process.
The method for producing the biogas by utilizing the excess sludge in China has the engineering application, but the anaerobic digestion systems built in the sewage treatment plants are fewer, and even the phenomenon that part of the sewage treatment plants are not operated or stopped occurs, and the main reason is that the operation of the anaerobic digestion process of the sludge is complicated and the start-up period is too long. In the process of converting the mesophilic to the high-temperature environment, a great amount of dead bacteria and the increase of the hydrolysis acidification rate cause the concentration of volatile acid to be rapidly increased in a short time, and the accumulation of the volatile acid is easily caused due to the low methane production rate in the initial starting stage. In an anaerobic digestion system, the accumulation of volatile acids such as acetic acid, propionic acid, butyric acid and valeric acid to a certain concentration has an inhibitory effect on the methanogenesis process, wherein propionic acid is an important intermediate product of the anaerobic biological treatment process and is most difficult to degrade, and is of great concern. Research shows that when propionic acid exceeds 1800mg/L, the gas production of the system starts to obviously decrease, and when the propionic acid reaches 4000mg/L, the methane production process stops and the system is crashed.
At present, the method for solving the problem of propionic acid focuses on adding propionic acid oxidizing bacteria or compound microbial agents after acid accumulation occurs in a system so as to promote propionic acid degradation and restore metabolic balance, and the main problems of the method include that the adaptability of exogenous strains to complex environmental conditions in an anaerobic system needs to be investigated, the ecological balance of the system is damaged, the flora structure is influenced, the investment cost is increased and the like. Therefore, in the starting process of the high-temperature anaerobic digestion system, the activity of propionic acid oxidizing bacteria is improved by a simple and effective method, the propionic acid accumulation of the system is reduced, and the practical application of the high-temperature anaerobic digestion of the sludge can be promoted.
Disclosure of Invention
In view of the above, the present invention provides a method for starting an anaerobic digestion reactor, which can quickly start anaerobic digestion of sludge at high temperature and reduce propionic acid accumulation, without inoculating exogenous strains.
The invention provides a starting method of an anaerobic digestion reactor, which comprises the following steps:
a) pouring undigested sludge into an anaerobic digestion reactor, and sealing and placing for 24-48 h;
b) adding a biological promoter and a buffer agent into the anaerobic digestion reactor, introducing nitrogen, deoxidizing, sealing, and fermenting at 36-45 ℃;
the buffer is one or more of magnesium oxide, calcium carbonate and ferric oxide;
c) and (3) heating the anaerobic digestion reactor to 55-60 ℃, stirring, and periodically adding fresh organic matters until the gas production is stable.
Preferably, in the step a), the water content of the sludge is 80-85%; the content of organic matters in the dry matter of the sludge is more than or equal to 40 wt%.
Preferably, in the step a), the temperature for sealing and placing is 20-30 ℃.
Preferably, in step b), the composition of the bio-promoter comprises FeS and CaCl2、MgCl2、 FeCl3、KCl、H3BO3、Na2HPO4、Na2CO3、NiCl2、CoCl2、Na2MoO4、CuSO4Ascorbic acid and sodium glutamate.
Preferably, in step b), the adding amount of the bio-promoter per kilogram of sludge organic matter in the anaerobic digestion reactor comprises: 0.25-1.5 g FeS, 0.2-1.8 g CaCl2，0.3～1.2g MgCl2，0.2～0.5g FeCl3，1～1.2g KCl，0.1～0.2g H3BO3，1.2～4.8g Na2HPO4，1.5～3.2g Na2CO3， 0.1～0.2g NiCl2，0.1～0.2g CoCl2，0.05～0.15g Na2MoO4，0.05～0.15g CuSO40.2-0.5 g ascorbic acid and 1.1-1.7 g sodium glutamate.
Preferably, in the step b), the adding amount of the buffering agent is 0.03-0.2 kg/ton of sludge.
Preferably, in step b), the methane content in the anaerobic digestion reactor is monitored during the fermentation, and the methane content continuously decreases after reaching a peak value as a fermentation end point.
Preferably, the peak value of the methane content is 65-75%; the fermentation time is 15-21 d.
Preferably, in the step c), the rotation speed of the stirring is 1-8 rpm.
Preferably, in step c), the fresh organic matter comprises one or more of fresh kitchen waste, fresh vegetable field waste, fresh livestock and poultry manure and fresh crop straw.
Compared with the prior art, the invention provides a starting method of an anaerobic digestion reactor. The starting method provided by the invention comprises the following steps: a) pouring undigested sludge into an anaerobic digestion reactor, and sealing and placing for 24-48 h; b) adding a biological promoter and a buffer agent into the anaerobic digestion reactor, introducing nitrogen for deoxidation, sealing, and fermenting at 36-45 ℃; the buffer is one or more of magnesium oxide, calcium carbonate and ferric oxide; c) and (3) heating the anaerobic digestion reactor to 55-60 ℃, stirring, and periodically adding fresh organic matters until the gas production is stable. The technical scheme provided by the invention firstly realizes partial hydrolytic acidification of the sludge in a microaerobic environment, and provides a small amount of volatile acid substrate for methanogenic flora; raising the temperature to a medium temperature, promoting the rapid enrichment of methanogenic flora through various mineral elements, rare elements, oxygen inhibitors and the like in a biological promoter in an anaerobic environment, establishing a stable medium-temperature anaerobic digestion system, particularly adding FeS to promote the enrichment of sulfate reducing bacteria and improve the oxidation-reduction potential of an anaerobic digestion system, further maintaining the buffer performance of the anaerobic digestion system through MgO, and simultaneously ensuring that propionic acid oxidizing bacteria have a good growth environment from multiple aspects and improving the abundance of related flora; when the basic consumption of the organic matter of the seed sludge is finished, the seed sludge is directly heated to high temperature, new organic matter is added, the mesophilic anaerobic digestion system in a substrate-lacking state is quickly converted into the thermophilic anaerobic digestion system, the propionic acid degradation in the process is ensured by rich propionic acid oxidation flora, and the adverse effect of propionic acid accumulation on anaerobic digestion gas production is effectively avoided. The technical scheme provided by the invention has the advantages of wide sources of inoculated sludge, low investment cost, shortened start time of high-temperature anaerobic digestion, rapid establishment of metabolic balance of acid-producing bacteria and methanogenic bacteria under a high-temperature condition, reduction of propionic acid accumulation in the start process, realization of stability and high efficiency of the methane production process of a sludge high-temperature anaerobic digestion system, and good practical significance for resource utilization of organic solid wastes and popularization and application of a high-temperature anaerobic digestion technology.
Detailed Description
The technical solutions in the embodiments of the present invention are clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. 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.
The invention provides a starting method of an anaerobic digestion reactor, which comprises the following steps:
a) pouring undigested sludge into an anaerobic digestion reactor, and sealing and placing;
b) adding a biological promoter and a buffer agent into the anaerobic digestion reactor, introducing nitrogen, deoxidizing and then sealing and fermenting;
c) and heating the anaerobic digestion reactor, stirring, and periodically adding fresh organic matters until the gas production is stable.
In the starting method provided by the invention, in the step a), the water content of the sludge is preferably 80-85%, and specifically can be 80%, 80.5%, 81%, 81.5%, 82%, 82.6%, 83%, 83.5%, 84%, 84.5% or 85%; the organic matter content in the dry matter of the sludge is more than or equal to 40 wt%, and specifically can be 40 wt%, 41 wt%, 42 wt%, 43 wt%, 44 wt%, 45 wt%, 46 wt%, 46.5 wt%, 47 wt%, 48 wt%, 48.2 wt%, 49 wt% or 50 wt%; the source of the sludge is preferably undigested dewatered sludge of a sewage treatment plant.
In the starting method provided by the invention, in the step a), the temperature for sealing and placing is preferably 20-30 ℃, and specifically can be 20 ℃, 21 ℃, 22 ℃, 23 ℃, 24 ℃, 25 ℃ (room temperature), 26 ℃, 27 ℃, 28 ℃, 29 ℃ or 30 ℃; the time for the sealing and placing is 24-48 h, and specifically can be 24h, 26h, 28h, 30h, 32h, 34h, 36h, 38h, 40h, 42h, 44h, 46h or 48 h.
In the starting method provided by the invention, in the step b), the component of the biological promoter is a substance capable of promoting the growth of microorganisms, including but not limited to FeS and CaCl2、MgCl2、FeCl3、KCl、H3BO3、 Na2HPO4、Na2CO3、NiCl2、CoCl2、Na2MoO4、CuSO4Ascorbic acid and sodium glutamate; the feeding amount of the FeS corresponding to each kilogram of sludge organic matters in the anaerobic digestion reactor is preferably 0.25-1.5 g, and specifically can be 0.25g, 0.5g, 0.75g, 1g, 1.25g or 1.5 g; the CaCl corresponds to organic matters in each kilogram of sludge2The addition amount of (b) is preferably 0.2-1.8 g, and specifically may be 0.2g, 0.4g, 0.6g, 0.8g, 1g, 1.2g, 1.4g, 1.6g or 1.8 g; the MgCl corresponding to the organic matter per kilogram of sludge2The addition amount of (b) is preferably 0.3-1.2 g, and specifically may be 0.3g, 0.4g, 0.5g, 0.6g, 0.7g, 0.8g, 0.9g, 1g, 1.1g or 1.2 g; the FeCl corresponding to the organic matter per kilogram of sludge3The addition amount of (b) is preferably 0.2-0.5 g, and specifically may be 0.2g, 0.25g, 0.3g, 0.35g, 0.4g, 0.45g or 0.5 g; the addition amount of the KCl corresponding to each kilogram of sludge organic matters is preferably 1-1.2 g, and specifically can be 1g, 1.02g, 1.04g, 1.06g, 1.08g, 1.1g, 1.12g, 1.14g, 1.16g, 1.18g or 1.2 g; the H corresponds to the organic matter per kilogram of sludge3BO3The amount of (b) is preferably 0.1 to 0.2g, and specifically may be 0.1g, 0.11g, 0.12g, 0.13g, 0.14g, 0.15g, 0.16g, 0.17g, 0.18g, 0.19g or 0.2 g; the Na corresponding to the organic matter per kilogram of sludge2HPO4The addition amount of (b) is preferably 1.2-4.8 g, and specifically may be 1.2g, 1.6g, 2g, 2.4g, 2.8g, 3.2g, 3.6g, 4g, 4.4g or 4.8 g; the Na corresponding to the organic matter per kilogram of sludge2CO3The addition amount of (b) is preferably 1.5-3.2 g, and specifically may be 1.5g, 1.7g, 2g, 2.3g, 2.5g, 2.7g, 3g or 3.2 g; the NiCl corresponding to the organic matter per kilogram of sludge2The addition amount of (c) is preferably 0.1 &0.2g, specifically 0.1g, 0.11g, 0.12g, 0.13g, 0.14g, 0.15g, 0.16g, 0.17g, 0.18g, 0.19g or 0.2 g; the CoCl corresponding to the organic matter per kilogram of sludge2The amount of (b) is preferably 0.1 to 0.2g, and specifically may be 0.1g, 0.11g, 0.12g, 0.13g, 0.14g, 0.15g, 0.16g, 0.17g, 0.18g, 0.19g or 0.2 g; the Na corresponding to the organic matter per kilogram of sludge2MoO4The addition amount of (b) is preferably 0.05-0.15 g, and specifically may be 0.05g, 0.06g, 0.07g, 0.08g, 0.09g, 0.1g, 0.11g, 0.12g, 0.13g, 0.14g or 0.15 g; the CuSO corresponding to organic matters in per kilogram of sludge4The addition amount of (b) is preferably 0.05-0.15 g, and specifically may be 0.05g, 0.06g, 0.07g, 0.08g, 0.09g, 0.1g, 0.11g, 0.12g, 0.13g, 0.14g or 0.15 g; the adding amount of the ascorbic acid corresponding to each kilogram of sludge organic matters is preferably 0.2-0.5 g, and specifically can be 0.2g, 0.25g, 0.3g, 0.35g, 0.4g, 0.45g or 0.5 g; the adding amount of the sodium glutamate corresponding to each kilogram of sludge organic matters is preferably 1.1-1.7 g, and specifically can be 1.1g, 1.2g, 1.3g, 1.4g, 1.5g, 1.6g or 1.7 g.
In the starting method provided by the invention, in the step b), the buffer is one or more of magnesium oxide, calcium carbonate and iron oxide, preferably magnesium oxide; the amount of the buffer is preferably 0.03 to 0.2 kg/ton of sludge, and specifically may be 0.03 kg/ton of sludge, 0.04 kg/ton of sludge, 0.05 kg/ton of sludge, 0.06 kg/ton of sludge, 0.07 kg/ton of sludge, 0.08 kg/ton of sludge, 0.09 kg/ton of sludge, 0.1 kg/ton of sludge, 0.11 kg/ton of sludge, 0.12 kg/ton of sludge, 0.13 kg/ton of sludge, 0.14 kg/ton of sludge, 0.15 kg/ton of sludge, 0.16 kg/ton of sludge, 0.17 kg/ton of sludge, 0.18 kg/ton of sludge, 0.19 kg/ton of sludge or 0.2 kg/ton of sludge.
In the start-up method provided by the present invention, in step b), the bio-enhancer and the buffer are preferably both added to the anaerobic digestion reactor in the form of an aqueous solution; wherein the concentration of the aqueous solution of the biological promoter is not particularly limited, and each solute component may be dissolved; the concentration of the aqueous buffer solution is preferably 2 to 5 wt%, and specifically may be 2 wt%, 2.5 wt%, 3 wt%, 3.5 wt%, 4 wt%, 4.5 wt%, or 5 wt%.
In the starting method provided by the invention, in the step b), after the biological promoter and the buffer are added, the biological promoter and the buffer are uniformly mixed with the sludge in the reactor.
In the starting method provided by the invention, in the step b), the oxygen content of the anaerobic digestion reactor after nitrogen introduction and deoxidation is preferably less than or equal to 0.5%, and specifically can be 0.05%, 0.1%, 0.15%, 0.2%, 0.25%, 0.3%, 0.35%, 0.4%, 0.45% or 0.5%.
In the starting method provided by the invention, in the step b), the fermentation mode can be static fermentation or low-speed stirring; the fermentation temperature is 36-45 deg.C, specifically 36 deg.C, 36.5 deg.C, 37 deg.C, 37.5 deg.C, 38 deg.C, 38.5 deg.C, 39 deg.C, 39.5 deg.C, 40 deg.C, 40.5 deg.C, 41 deg.C, 41.5 deg.C, 42 deg.C, 42.5 deg.C, 43 deg.C, 43.5 deg.C, 44 deg.C, 44.5 deg.C or 45 deg.C; preferably, monitoring the methane content in the anaerobic digestion reactor in the fermentation process, and taking the continuous reduction of the methane content after the methane content reaches a peak value as a fermentation end point; the peak value of the methane content is preferably 65-75%, and specifically can be 68% and 70.8%; the fermentation time is preferably 15-21 d, and specifically can be 15d, 16d, 17d, 18d, 19d, 20d or 21 d.
In the starting method provided by the invention, in the step c), the temperature rise end point temperature is 55-60 ℃, and specifically can be 55 ℃, 56 ℃, 57 ℃, 58 ℃, 59 ℃ or 60 ℃; the rotation speed of the stirring is preferably 1-8 rpm, and specifically may be 1rpm, 1.5rpm, 2rpm, 2.5rpm, 3rpm, 3.5rpm, 4rpm, 4.2rpm, 4.5rpm, 4.7rpm, 5rpm, 5.5rpm, 6rpm, 6.5rpm, 7rpm, 7.5rpm or 8 rpm.
In the starting method provided by the invention, in step c), the fresh organic matter comprises one or more of but not limited to fresh kitchen garbage, fresh vegetable field garbage, fresh livestock and poultry manure and fresh crop straws; the fresh organic matter is preferably selected according to 1-5 kgVS/(m)3D) organic charge, more preferably 2.2 kgVS/(m)3Organic charge addition of d), where VS denotes volatile solids.
In the starting method provided by the invention, the stepsc) The stable gas production refers to that the methane production potential (the volume number of methane produced by degrading 1kg of VS fresh organic matter) of two adjacent days is continuously higher than 0.3m for 3 times3/kgVSREMOr the gas yield, namely the methane yield of each kilogram of fresh organic matters added reaches more than 80L/(kg.d). In the invention, after the gas production is stable, the starting process of the anaerobic digestion reactor is completed.
The technical scheme provided by the invention is that partial hydrolytic acidification of sludge is realized under a microaerobic environment, and a small amount of volatile acid substrates are provided for methanogenic flora; raising the temperature to medium temperature, promoting the rapid enrichment of methanogenic flora through various mineral elements, rare elements, oxygen inhibitors and the like in a biological promoter in an anaerobic environment, establishing a stable medium-temperature anaerobic digestion system, particularly adding FeS to promote the enrichment of sulfate reducing bacteria and improve the oxidation-reduction potential of the anaerobic digestion system, further maintaining the buffer performance of the anaerobic digestion system through MgO, simultaneously ensuring that propionic acid oxidizing bacteria have good growth environment from multiple aspects and improving the abundance of related flora; when the organic matter of the seed sludge is basically consumed, the seed sludge is directly heated to high temperature, new organic matter is added, the mesophilic anaerobic digestion system in a substrate-lacking state is quickly converted into the thermophilic anaerobic digestion system, the propionic acid degradation in the process is ensured by rich propionic acid oxidation flora, and the adverse effect of propionic acid accumulation on anaerobic digestion gas production is effectively avoided. The technical scheme provided by the invention has the advantages of wide sources of inoculated sludge, low investment cost, shortened start time of high-temperature anaerobic digestion, rapid establishment of metabolic balance of acid-producing bacteria and methanogenic bacteria under a high-temperature condition, reduction of propionic acid accumulation in the start process, realization of the stability and high efficiency of the methane production process of the sludge high-temperature anaerobic digestion system, and good practical significance for resource utilization of organic solid wastes and popularization and application of the high-temperature anaerobic digestion technology.
For the sake of clarity, the following examples are given in detail.
In the following examples of the present invention, the solute component of the bio-accelerator solution per kg of sludge organic matter is added in the following amounts: 0.75g FeS, 1.8g CaCl2，1.2g MgCl2，0.5g FeCl3，1.2g KCl， 0.15g H3BO3，4.8g Na2HPO4，3.2g Na2CO3，0.1g NiCl2，0.1g CoCl2，0.15g Na2MoO4，0.15g CuSO40.5g ascorbic acid, 1.7g sodium glutamate.
Example 1
A method for rapidly starting high-temperature anaerobic digestion of sludge and reducing propionic acid accumulation is completed according to the following steps:
a) conveying 600kg of undigested dewatered sludge of a sewage treatment plant back to an anaerobic digestion reactor, measuring that the water content of the sludge is 82.6 percent and VS/TS is 46.5 percent (VS represents volatile solid, TS represents total solid, and VS/TS is organic matter content in sludge dry matter), and sealing and placing for 36 hours at normal temperature;
b) adding a biological promoter solution into sludge according to 48kg of organic matter content, adding 2.4L of 2 wt% magnesium oxide solution, uniformly mixing, introducing nitrogen until the oxygen content is 0.3%, statically fermenting at the temperature of 36-40 ℃ for 21 days after a reactor is sealed, wherein the methane proportion is 68% at most in 18 th day, then slowly decreasing, wherein propionic acid is increased and then decreased in the period, the concentration is 231mg/L at the end, and the total volatile acid is 874 mg/L;
c) directly raising the temperature of the anaerobic digestion reactor to 55-60 ℃, starting a stirring device at the rotating speed of 3rpm according to 2.2 kgVS/(m)3And d) adding the organic load, adding the crushed fresh kitchen garbage periodically, wherein in a feeding period, the gas production rate of the reactor reaches 86-104L/(kg d), and the concentration of propionic acid is always lower than 300mg/L and is in a descending trend, thus finishing the starting of the anaerobic digestion reactor.
Example 2
A method for rapidly starting high-temperature anaerobic digestion of sludge and reducing propionic acid accumulation is completed according to the following steps:
a) conveying 1500kg of undigested dewatered sludge of a sewage treatment plant back to an anaerobic digestion reactor, measuring to obtain sludge with water content of 83.5% and VS/TS of 48.2%, and sealing and placing for 24h at normal temperature;
b) adding a biological promoter solution into the sludge according to the organic matter content of 120kg, adding 6L of a 5 wt% magnesium oxide solution, uniformly mixing, introducing nitrogen until the oxygen content is 0.2%, statically fermenting at the temperature of 38-42 ℃ for 20 days after a reactor is sealed, wherein the methane proportion is 70.8% at the maximum at day 18, then slowly decreasing, wherein the propionic acid is increased and then decreased, the concentration is 17mg/L at the end, and the total volatile acid is 406 mg/L;
c) directly raising the temperature of the anaerobic digestion reactor to 55-60 ℃, starting a stirring device at the rotating speed of 4.2rpm according to 2.2 kgVS/(m)3And d) adding the organic load, adding the crushed fresh kitchen garbage periodically, wherein in a feeding period, the gas production rate of the reactor reaches 92-116L/(kg d), the concentration of propionic acid is always lower than 100mg/L, and the starting of the anaerobic digestion reactor is finished without increasing trend.
Comparative example
A method for starting sludge high-temperature anaerobic digestion is completed according to the following steps:
1000kg of undigested dewatered sludge of a sewage treatment plant is transported back to be poured into an anaerobic digestion reactor, the water content of the sludge is 83.2 percent, and VS/TS is 45.7 percent; introducing nitrogen to enable the oxygen content to be 0.2%, then sealing the reactor, directly heating to 55-60 ℃, starting a stirring device, and setting the rotating speed to be 3 rpm; the following are shown by the multipoint measurements: after 3 days, the propionic acid in the reactor increased to 2500mg/L, and after 30 days, the propionic acid increased to 4000 mg/L; after 90 days, the propionic acid is 4500-4800 mg/L, and the total volatile acid is approximately 10000 mg/L; during the period, fresh kitchen garbage is added at 1.5 kgVS/(m)3D) is operated under an organic load, and the gas production rate in 103 days is 31-65L/(kg d).
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 decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (10)
1. A method of starting up an anaerobic digestion reactor comprising the steps of:
a) pouring undigested sludge into an anaerobic digestion reactor, and sealing and placing for 24-48 h;
b) adding a biological promoter and a buffer agent into the anaerobic digestion reactor, introducing nitrogen, deoxidizing, sealing, and fermenting at 36-45 ℃;
the buffer is one or more of magnesium oxide, calcium carbonate and ferric oxide;
c) and (3) heating the anaerobic digestion reactor to 55-60 ℃, stirring, and periodically adding fresh organic matters until the gas production is stable.
2. The starting method according to claim 1, characterized in that in step a), the water content of the sludge is 80-85%; the content of organic matters in the dry matter of the sludge is more than or equal to 40 wt%.
3. The starting method according to claim 1, wherein the temperature of the sealing and placing in step a) is 20-30 ℃.
4. The method of starting according to claim 1, wherein in step b), the composition of the bio-promoter comprises FeS, CaCl2、MgCl2、FeCl3、KCl、H3BO3、Na2HPO4、Na2CO3、NiCl2、CoCl2、Na2MoO4、CuSO4Ascorbic acid and sodium glutamate.
5. The start-up method of claim 4, wherein in step b), the adding of the bio-promoter per kg of organic matter in the sludge in the anaerobic digestion reactor comprises: 0.25-1.5 g FeS, 0.2-1.8 g CaCl2，0.3～1.2g MgCl2，0.2～0.5g FeCl3，1～1.2g KCl，0.1～0.2gH3BO3，1.2～4.8g Na2HPO4，1.5～3.2g Na2CO3，0.1～0.2g NiCl2，0.1～0.2g CoCl2，0.05～0.15g Na2MoO4，0.05～0.15g CuSO40.2 to 0.5g of an antioxidant1.1 to 1.7g of sodium glutamate.
6. The starting method according to claim 1, wherein the amount of the buffer added in step b) is 0.03 to 0.2 kg/ton of sludge.
7. The start-up method of claim 1, wherein in step b), the methane content in the anaerobic digestion reactor is monitored during the fermentation, and the methane content continuously decreases after reaching a peak value to reach the fermentation end point.
8. The start-up method of claim 7, wherein the peak methane content is 65-75%; the fermentation time is 15-21 d.
9. The starting method according to claim 1, wherein in step c), the rotation speed of the stirring is 1-8 rpm.
10. The start-up method of claim 1, wherein in step c) the fresh organic matter comprises one or more of fresh kitchen waste, fresh vegetable field waste, fresh poultry manure and fresh crop straw.
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