CN107460111A - Organic solid castoff processing system and its method of disposal based on subcritical hydrolysis - Google Patents
Organic solid castoff processing system and its method of disposal based on subcritical hydrolysis Download PDFInfo
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- CN107460111A CN107460111A CN201710875165.7A CN201710875165A CN107460111A CN 107460111 A CN107460111 A CN 107460111A CN 201710875165 A CN201710875165 A CN 201710875165A CN 107460111 A CN107460111 A CN 107460111A
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- biogas
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- subcritical hydrolysis
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- 238000006460 hydrolysis reaction Methods 0.000 title claims abstract description 124
- 230000007062 hydrolysis Effects 0.000 title claims abstract description 120
- 239000007787 solid Substances 0.000 title claims abstract description 60
- 238000012545 processing Methods 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 24
- 238000006243 chemical reaction Methods 0.000 claims abstract description 35
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 238000000926 separation method Methods 0.000 claims abstract description 28
- 239000002918 waste heat Substances 0.000 claims abstract description 28
- 239000000706 filtrate Substances 0.000 claims abstract description 27
- 238000011084 recovery Methods 0.000 claims abstract description 25
- 238000000265 homogenisation Methods 0.000 claims abstract description 10
- 238000000746 purification Methods 0.000 claims abstract description 8
- 239000000463 material Substances 0.000 claims description 60
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- 230000003115 biocidal effect Effects 0.000 claims description 17
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- 239000010802 sludge Substances 0.000 claims description 15
- 230000033228 biological regulation Effects 0.000 claims description 13
- 238000007600 charging Methods 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 13
- 239000002351 wastewater Substances 0.000 claims description 11
- 230000018044 dehydration Effects 0.000 claims description 9
- 238000006297 dehydration reaction Methods 0.000 claims description 9
- 238000009272 plasma gasification Methods 0.000 claims description 9
- 238000003756 stirring Methods 0.000 claims description 7
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- 238000002474 experimental method Methods 0.000 description 3
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- 239000002028 Biomass Substances 0.000 description 2
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
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- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 230000003301 hydrolyzing effect Effects 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
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- 239000010841 municipal wastewater Substances 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 150000003384 small molecules Chemical class 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- GETQZCLCWQTVFV-UHFFFAOYSA-N trimethylamine Chemical compound CN(C)C GETQZCLCWQTVFV-UHFFFAOYSA-N 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- 241000219112 Cucumis Species 0.000 description 1
- 235000015510 Cucumis melo subsp melo Nutrition 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 1
- BUGBHKTXTAQXES-UHFFFAOYSA-N Selenium Chemical compound [Se] BUGBHKTXTAQXES-UHFFFAOYSA-N 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- FJJCIZWZNKZHII-UHFFFAOYSA-N [4,6-bis(cyanoamino)-1,3,5-triazin-2-yl]cyanamide Chemical compound N#CNC1=NC(NC#N)=NC(NC#N)=N1 FJJCIZWZNKZHII-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
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- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- 229910052788 barium Inorganic materials 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 229910052790 beryllium Inorganic materials 0.000 description 1
- ATBAMAFKBVZNFJ-UHFFFAOYSA-N beryllium atom Chemical compound [Be] ATBAMAFKBVZNFJ-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000012876 carrier material Substances 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
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- 238000001816 cooling Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
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- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
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- 239000000686 essence Substances 0.000 description 1
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- 239000000446 fuel Substances 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000000413 hydrolysate Substances 0.000 description 1
- 238000001027 hydrothermal synthesis Methods 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 239000010806 kitchen waste Substances 0.000 description 1
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- 238000011068 loading method Methods 0.000 description 1
- 208000020442 loss of weight Diseases 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 244000052769 pathogen Species 0.000 description 1
- 230000001717 pathogenic effect Effects 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000010908 plant waste Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 229910052711 selenium Inorganic materials 0.000 description 1
- 239000011669 selenium Substances 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 238000009270 solid waste treatment Methods 0.000 description 1
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- 229910052725 zinc Inorganic materials 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
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- C12M23/00—Constructional details, e.g. recesses, hinges
- C12M23/36—Means for collection or storage of gas; Gas holders
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- C12M23/58—Reaction vessels connected in series or in parallel
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- C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
- C12M27/02—Stirrer or mobile mixing elements
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- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
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- C12M45/00—Means for pre-treatment of biological substances
- C12M45/02—Means for pre-treatment of biological substances by mechanical forces; Stirring; Trituration; Comminuting
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- C12M45/00—Means for pre-treatment of biological substances
- C12M45/04—Phase separators; Separation of non fermentable material; Fractionation
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- C12M45/00—Means for pre-treatment of biological substances
- C12M45/06—Means for pre-treatment of biological substances by chemical means or hydrolysis
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- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/18—Gas cleaning, e.g. scrubbers; Separation of different gases
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- 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
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Abstract
The present invention relates to a kind of organic solid castoff processing system and its method of disposal based on subcritical hydrolysis, including it is sequentially connected the homogenization system of setting, external heat subcritical hydrolysis system, solid-liquid separation system, anaerobic reaction system with waste heat recovery.Described anaerobic reaction system, include the IC reactors being sequentially connected, marsh gas purifying tower, reservoir hag and heat-conducting oil furnace, described IC reactors produce biogas by carrying out highly effective anaerobic reaction to filtrate, caused biogas is after marsh gas purifying tower purification, it is stored in the reservoir hag, biogas in the reservoir hag, which is delivered in the heat-conducting oil furnace, to burn, and provides thermal source for the external heat subcritical hydrolysis system with waste heat recovery.The present invention also provides the method for disposal using the system.The present invention organic solid castoff decrement it is higher, fermentation period is shorter, total system can heat self-balancing, and can realize organic solid castoff harmless treatment disposal.
Description
Technical field
The present invention relates to organic solid castoff processing technology field, and in particular to a kind of based on the organic of subcritical hydrolysis
Solid waste treatment system and its method of disposal.
Background technology
Organic solid castoff is often referred to the debirs that moisture content is less than 85%-90% bio-degradables, including animal
Excrement, crop residues, domestic sludge, food production discarded object, industrial organic wastes, timber processing discarded object, life
Rubbish living etc..Mainly include three burning, security landfill and recycling masters for the processing method of organic solid castoff at present
Want technological approaches.Burning method treating capacity is big, can eliminate medicament residue and pathogenic microorganism, reduce organic solid waste volume
95%, but for organic solid castoff, excess sludge especially caused by municipal wastewater biochemical treatment, chemicals manufacture row
Industry discards antibiotic bacterium dregs and urban life kitchen garbage, and its water content is big, needs extra fuel, causes burning disposal cost high
It is high, considerably increase processing cost.Security landfill construction and operating cost are low, but floor space be present and asked with secondary pollution greatly
Topic, and cause the wasting of resources of organic components.Organic principle can be changed into methane and realize recycling by anaerobic fermentation, and
And combination pyrohydrolysis pretreatment can improve anaerobic digestion performance, be the best class organic solid castoff that ferments of comprehensive benefit
Processing scheme.
Pyrohydrolysis anaerobic digestion techniques have obtained preferable ergonomic support in terms of municipal sludge disposal, but at anaerobic digestion
Reason unit the deficiencies of plant area is big, biogas output is low, fermentation period length (12-15d) be present, it is necessary to which modified technique is transported to improve
Line efficiency, reduce investment and operating cost.
In addition, under the background that socio-economic development emphasizes recycling economy and energy-saving low-carbon, there is an urgent need to by organic solid
Discarded object, especially antibiotic bacterium dregs, municipal sludge, realize that minimizing, innoxious final disposal and using energy source are maximized
Sustainable scheme.
The content of the invention
For overcome the deficiencies in the prior art, the invention provides a kind for the treatment of effeciency height, energy consumption is low, occupation of land is small, and integrated
Meet the organic solid castoff processing system based on subcritical hydrolysis of the auxiliary disposal unit of environmental requirement.
Another object of the present invention is to provide a kind of above-mentioned organic solid castoff processing system of application to organic solid
The method of offal treatment disposal.
The technical solution adopted by the present invention is：Organic solid castoff processing system based on subcritical hydrolysis, including according to
The homogenization system of secondary connection setting, the external heat subcritical hydrolysis system with waste heat recovery, solid-liquid separation system, anaerobic reaction system
System；
Described homogenization system includes homogenate pond, is formed for organic solid castoff to be added to stir in homogenate pond
Possesses the material of mobility；
The described external heat subcritical hydrolysis system with waste heat recovery, includes the first-class heat exchanger being sequentially connected, two
Level heat exchanger and hydrolysis reactor, described hydrolysis reactor is used to carry out subcritical hydrolysis reaction to material after homogenate, described
First-class heat exchanger and secondary heat exchanger by be separately recovered hydrolysis after material waste heat, realize hydrolysis reactor external heat hydrolysate
Material；
Described solid-liquid separation system is provided with super-pressure filter press, and described super-pressure filter press is mechanically
Deep dehydration is carried out to the material after hydrolysis, further reduces volume；
Described anaerobic reaction system, include the IC reactors being sequentially connected, marsh gas purifying tower, reservoir hag and conduction oil
Stove, described IC reactors produce biogas by carrying out highly effective anaerobic reaction to filtrate, and caused biogas is net by the biogas
After changing tower purification, it is stored in the reservoir hag, the biogas in the reservoir hag, which is delivered in the heat-conducting oil furnace, to burn, and is
External heat subcritical hydrolysis system with waste heat recovery provides thermal source.
The homogenization system also include for convey technique supplement water submersible sewage pump, the output end of described submersible sewage pump with
Pond connection is homogenized, described homogenate pond is conveyed the mixed material after homogenate toward described first-class heat exchanger by plunger pump.
The hydrolysis reactor of the described external heat subcritical hydrolysis system with waste heat recovery is connected with pipe circle pump, institute
The output end for stating secondary heat exchanger is connected with hydrolysis reactor input, and the output end of hydrolysis reactor is connected by first-class heat exchanger
It is connected to pressure retaining valve.
The solid-liquid separation system includes also including the hydrolysis surge tank and press filtration feed pump being sequentially connected, described water
The pressure retaining valve of the input and upper level that solve surge tank is connected, and organic exhaust gas output is provided with the top of described hydrolysis surge tank
End, described organic exhaust gas output end are connected with spraying purification system；The output end of described press filtration feed pump and super-pressure pressure
The input connection of filter.
Described super-pressure filter press is provided with filter residue output end and filtrate output end, and described filter residue output end is connected with
Plasma gasification melts follow-up disposal plant.
The anaerobic reaction system also includes the IC chargings regulation tank being sequentially connected and IC feed pumps, and described IC chargings are adjusted
The input of section tank is connected with the filtrate output end of described super-pressure filter press, and is provided with vertical mixing in IC charging regulation tanks
Device.
The tank wall upper end of described IC reactors is provided with IC water sides, and described IC water sides are connected with waste water depth
Change processing system；Biogas output end, described biogas output end and marsh gas purifying tower are provided with the top of described IC reactors
Input connection, the input of the output end of marsh gas purifying tower and reservoir hag connects, and the reservoir hag conveys wind by biogas
Biogas is delivered in heat-conducting oil furnace by machine to burn；Described heat-conducting oil furnace is provided with conduction oil output end, and described conduction oil is defeated
Go out end to be connected with the input of secondary heat exchanger, described heat-conducting oil furnace output heat conduction oil carrier is external heat subcritical hydrolysis system
System provides thermal source.
Pressure sensor and flow sensor are provided with described reservoir hag, the biogas inside reservoir hag exceedes safety
Level, unnecessary biogas draw emergent burning through reservoir hag output end.
The method of disposal of organic solid castoff processing based on subcritical hydrolysis, comprises the following steps：
Step 1：Homogenate, pending organic solid castoff is added to homogenization system, by organic solid castoff and
Process water is added in homogenate pond, and the agitating device by being homogenized pond stirs to form the material for possessing mobility, the thing after homogenate
Material is conveyed by plunger pump toward the external heat subcritical hydrolysis system with waste heat recovery；
Step 2：Subcritical hydrolysis, the material after homogenate complete hydrolytic decomposition pot successively by first-class heat exchanger, secondary heat exchanger
External heat, enter in hydrolysis reactor after external heat, subcritical hydrolysis reaction, profit are carried out to material after homogenate by HTHP
In follow-up dehydration and anaerobic digestion, while eliminate residual antibiotic, thalline or pathogenic microorganism；
Step 3：Separation of solid and liquid, the material after hydrolysis first pass through surge tank, and caused organic exhaust gas delivers to spray cleaning system
System, followed by super-pressure filter press, deep dehydration mechanically is carried out to material, further reduces volume, produced
Filtrate enter anaerobic reaction system, caused filter residue outward transport landfill or deliver to plasma gasification melting disposal system；
Step 4：Anaerobic reaction, only carries out Anaerobic Digestion to filtrate caused by solid-liquid separation system, and filtrate first passes through
IC charging regulation tank, it is quenched after filtrate be delivered to by IC feed pumps in IC reactors, pass through in IC reactors carry out height
Imitate anaerobic reaction and produce biogas, caused biogas is stored in reservoir hag after first passing through the purification of marsh gas purifying tower, in reservoir hag
Biogas is the external heat subcritical hydrolysis system with waste heat recovery by being burnt in biogas conveying fan methane conveying to heat-conducting oil furnace
System provides thermal source；Wastewater deepening processing system is delivered in caused IC water outlets, handles rear discharge up to standard；Caused anaerobic activated sludge
It is periodically outer to arrange.
The parameter of described step 2 subcritical hydrolysis is as follows：The external heat subcritical hydrolysis system with waste heat recovery of control
Pressure be maintained at 0.8-1.5MPa, the temperature control of hydrolysis reactor is set in the range of 150 DEG C -200 DEG C, after making homogenate
Material keeps liquid, heat-insulation pressure keeping 30-60min；First-class heat exchanger in described step 2 is to thing after material after hydrolysis and homogenate
Material is exchanged heat, and waste heat recovery is carried out to material after hydrolysis；Secondary heat exchanger in described step 2 is added with heat transfer oil heat carrier
Material before pyrohydrolysis.
Beneficial effects of the present invention include following：
(1) under the high temperature and high pressure environment of hydrolysis system, cellular material is destroyed, and long-chain macromolecule is broken to small molecule,
To liquid phase organic matter availability is greatly improved, to be in nearly 90% organic matter dissolving conversion in organic solid castoff
The recycling for follow-up anaerobic reaction system of uniting is laid a good foundation, meanwhile, be advantageous to improve follow-up dehydration depth, with moisture content
80% organic solid castoff decrement is dehydrated moisture content than being used as benchmark for 0, after hydrolysis can drop to less than 50%, and directly dry
Moisture content is 60%-65% after change, and by contrast, decrement ratio improves 20%-40%.
(2) material passes through solid-liquid separation system after hydrolyzing, and realizes separation of solid and liquid, only carries out anaerobic digestion to filtrate afterwards,
IC reactor volumes load, digestion rate are improved, hydraulic detention time shorten to 24h, and is adopted mostly on engineer applied at present
With complete poor anaerobic fermentation, its fermentation period is 12-15d, and by contrast, fermentation period shortens more than 90%, and subtracts significantly
Lack processing equipment space, meanwhile, the biogas yield and fire damp purity of anaerobic system are improved, with reference to pyrohydrolysis
Conditioning effect, the operational efficiency of total system substantially increase.
(3) anaerobic reaction system produces biogas, burns into heat-conducting oil furnace, with reference to Multi-stage heat-exchanging device, realizes organic solid
The recycling of biomass energy contained by body discarded object, thermal source is provided for hydrolysis, and realize total system heat self-balancing.
(4) organic solid castoff eliminates residual antibiotic, thalline or pathogenic microorganism through hydrolysis, through anaerobic digestion
Afterwards, filter residue land use or can need to melt follow-up disposing technique through plasma gasification, and heavy metal ion be changed into stable glass
Glass body reduces its harmfulness, finally realizes the harmless treatment disposal of organic solid castoff.
Brief description of the drawings
Fig. 1 is the process chart of organic solid castoff processing system of the present invention.
Label is shown in figure：
1- submersible sewage pumps, 2- homogenate pond, 3- plunger pumps, 4- first-class heat exchangers, 5- secondary heat exchangers, 6- hydrolysis reactors, 7-
Pipe circle pump, 8- pressure retaining valves, 9- hydrolysis surge tank, 10- press filtrations feed pump, 11- super-pressure filter press, 12-IC charging regulations
Tank, 13-IC feed pumps, 14-IC reactors, 15- marsh gas purifyings tower, 16- reservoir hags, 17- biogas conveying fan, 18- conduction oils
Stove.
Embodiment
In order to illustrate the embodiments of the present invention more clearly, the embodiment of the present invention is done into one below in conjunction with the accompanying drawings
The explanation of step.
Reference picture 1, the organic solid castoff processing system based on subcritical hydrolysis, including it is sequentially connected the homogenate of setting
System, external heat subcritical hydrolysis system, solid-liquid separation system, anaerobic reaction system with waste heat recovery.
Homogenization system includes submersible sewage pump 1, homogenate pond 2 and the plunger pump 3 for conveying technique supplement water, described latent dirt
The output end of pump 1 is connected with homogenate pond 2, and described homogenate pond 2 is by plunger pump 3 by the mixed material after homogenate toward described one
Level heat exchanger 4 conveys.Described homogenization system possesses stream for organic solid castoff to be added into stirring formation in homogenate pond 2
The material of dynamic property.
External heat subcritical hydrolysis system with waste heat recovery, includes the first-class heat exchanger 4 being sequentially connected, secondary heat exchange
Device 5 and hydrolysis reactor 6, described hydrolysis reactor 6 are connected with pipe circle pump 7, the output end of the secondary heat exchanger 5 with
The input of hydrolysis reactor 6 connects, and the output end of hydrolysis reactor 6 is connected with pressure retaining valve 8 by first-class heat exchanger 4.Described
Hydrolysis reactor 6 is used to carry out subcritical hydrolysis reaction, described first-class heat exchanger 4 and secondary heat exchanger 5 to material after homogenate
By be separately recovered hydrolysis after material waste heat, realize the external heat of hydrolysis reactor 6 hydrolyze material.
Breaking-wall cell occurs for material in hydrolysis reactor 6, organic matter is discharged, while long-chain macromolecule is broken to small point
Son so that organic substance can be decomposed by the microorganisms utilization, possess efficient anaerobic digestion necessary condition；More particularly, to chemical drugs
Product manufacturing discards antibiotic bacterium dregs, and residual antibiotic no longer possesses bactericidal action, thalline warp because of the destruction of chemical constitution
Heat inactivation, so as to realize the innoxious of antibiotic bacterium dregs.
Solid-liquid separation system includes the hydrolysis surge tank 9 being sequentially connected, press filtration feed pump 10 and super-pressure filter press 11.
The input of described hydrolysis surge tank 9 and the pressure retaining valve 8 of external heat subcritical hydrolysis system of the upper level with waste heat recovery connect
Connect, the described top of hydrolysis surge tank 9 is provided with organic exhaust gas output end, and it is net that described organic exhaust gas output end is connected with spray
Change system；The output end of described press filtration feed pump 10 is connected with the input of super-pressure filter press 11；Described super-pressure pressure
Filter 11 mechanically carries out deep dehydration to the material after hydrolysis, further reduces volume；Described super-pressure pressure
Filter 11 is provided with filter residue output end and filtrate output end, and described filter residue output end is connected with the follow-up place of plasma gasification melting
Put device.
Anaerobic reaction system, include the IC charging regulations tank 12 being sequentially connected, IC feed pumps 13, IC reactors 14, natural pond
Gas purifying column 15, reservoir hag 16 and heat-conducting oil furnace 18.The input of described IC charging regulation tanks 12 and described super-pressure pressure
The filtrate output end connection of filter 11, and it is provided with vertical stirrer in IC charging regulation tanks 12.The tank of described IC reactors 14
Body sidewall upper end is provided with IC water sides, and described IC water sides are connected with wastewater deepening processing system；Described IC reactors
14 top is provided with biogas output end, and described biogas output end is connected with the input of marsh gas purifying tower, marsh gas purifying tower
Output end be connected with the input of reservoir hag 16, biogas is delivered to heat conduction by the reservoir hag 16 by biogas conveying fan 17
Burnt in oil oven 18；Described heat-conducting oil furnace 18 is provided with conduction oil output end, described conduction oil output end and secondary heat exchange
The input connection of device 5.
Pressure sensor and flow sensor are provided with reservoir hag 16, the biogas inside reservoir hag 16 exceedes safe water
Flat, unnecessary biogas draws emergent burning through the output end of reservoir hag 16.
IC reactors 14 produce biogas by carrying out highly effective anaerobic reaction to filtrate, and caused biogas is net by the biogas
After changing the purification of tower 15, it is stored in the reservoir hag 16, the biogas in the reservoir hag 16 is delivered in the heat-conducting oil furnace 18
Burning, described heat-conducting oil furnace 18 output heat conduction oil carrier provide heat for the external heat subcritical hydrolysis system with waste heat recovery
Source.
Anaerobic reaction system only carries out anaerobic digestion to filtrate, improves the volumetric loading of IC reactors 14, digestion rate, water
Power shorter residence time is 24h, so as to greatly reduce processing equipment space, meanwhile, the biogas yield of anaerobic system and
Fire damp purity is improved, and with reference to pyrohydrolysis conditioning effect, the operational efficiency of total system substantially increases.
Anaerobic reaction system produces biogas, is burnt into heat-conducting oil furnace 18, with reference to Multi-stage heat-exchanging device, realizes antibiotic bacterium
The recycling of biomass energy contained by slag, thermal source is provided for hydrolysis, and realize total system heat self-balancing.
The method of disposal of organic solid castoff processing based on subcritical hydrolysis, including homogenate, subcritical hydrolysis, solid-liquid
Separation and 4 steps of anaerobic reaction：
Step 1：Homogenate, pending organic solid castoff is added to homogenization system, by organic solid castoff and
Process water is added in homogenate pond 2, and the agitating device by being homogenized pond 2 stirs to form the material for possessing mobility, if processing meal
Kitchen rubbish, added after can first kitchen waste disintegrating apparatus be crushed in homogenate pond.Material after homogenate is past by plunger pump 3
External heat subcritical hydrolysis system conveying with waste heat recovery；
Step 2：Subcritical hydrolysis, the material after homogenate complete hydrolysis successively by first-class heat exchanger 4, secondary heat exchanger 5
Tank external heat, enter in hydrolysis reactor 6 after external heat, first-class heat exchanger 4 is changed material after material after hydrolysis and homogenate
Heat, waste heat recovery is carried out to material after hydrolysis.The material before heat transfer oil heat carrier heating hydrolysis of secondary heat exchanger 5.More than control band
The pressure of the external heat subcritical hydrolysis system of recuperation of heat is maintained at 0.8-1.5MPa, sets the temperature control of hydrolysis reactor 6
In the range of 150 DEG C -200 DEG C, the material after homogenate is set to keep liquid, heat-insulation pressure keeping 30-60min.By HTHP to even
Material carries out subcritical hydrolysis reaction after slurry, beneficial to follow-up separation of solid and liquid and anaerobic digestion, while eliminates residual antibiotic and bacterium
Body.
Under the high temperature and high pressure environment of hydrolysis system, cellular material is destroyed, and long-chain macromolecule is broken to small molecule, organic
The organic matter dissolving conversion of solid waste nearly 90% is greatly improved organic matter availability, is that system is follow-up to liquid phase
The recycling of anaerobic reaction system is laid a good foundation, meanwhile, be advantageous to improve follow-up dehydration depth, finally cut down solid
Rate can reach more than 75%.
Step 3：Separation of solid and liquid, material passes through solid-liquid separation system after hydrolysis, realizes separation of solid and liquid.Material after hydrolysis is first
By surge tank, caused organic exhaust gas delivers to spraying purification system, followed by super-pressure filter press 11, passes through the side of machinery
Formula carries out deep dehydration to material, further reduces volume, and caused filtrate enters anaerobic reaction system, caused filter residue outward transport
Fill or deliver to plasma gasification melting disposal system；
Step 4：Anaerobic reaction, only carries out Anaerobic Digestion to filtrate caused by solid-liquid separation system, and filtrate first passes through
IC charging regulation tank 12, it is quenched after filtrate be delivered to by IC feed pumps 13 in IC reactors 14, by IC reactors 14
Interior progress highly effective anaerobic reaction produces biogas, and caused biogas is first passed through after marsh gas purifying tower 15 is evolved and is stored in reservoir hag,
Biogas in reservoir hag is with the additional of waste heat recovery by being burnt in the methane conveying of biogas conveying fan 17 to heat-conducting oil furnace 18
Hot subcritical hydrolysis system provides thermal source；Wastewater deepening processing system is delivered in caused IC water outlets, and water quality treatment reaches country
Primary standard discharges；Caused anaerobic activated sludge is periodically outer to be arranged.
Discharging standards《Integrated wastewater discharge standard》(GB8978-1996) such as following table：
| Sequence number | Pollutant | Primary standard | Secondary standard | Grade III Standard |
| 1 | Suspension (SS) | 70 | 150 | 400 |
| 2 | COD (COD) | 100 | 300 | 1000 |
| 3 | Ammonia nitrogen | 15 | 50 | - |
Caused organic exhaust gas can reach national secondary discharge standard, specific standards after spray system purifies in step 2
It is as follows：
| Sequence number | Item controlled | Unit | Secondary standard |
| 1 | Ammonia | mg/m3 | 1.5 |
| 2 | Trimethylamine | mg/m3 | 0.08 |
| 3 | Hydrogen sulfide | mg/m3 | 0.06 |
| 4 | Methyl mercaptan | mg/m3 | 0.007 |
| 5 | Methyl sulfide | mg/m3 | 0.07 |
| 6 | Methyl disulfide | mg/m3 | 0.06 |
| 7 | Carbon disulfide | mg/m3 | 3.0 |
| 8 | Styrene | mg/m3 | 5.0 |
| 9 | Odor concentration | Dimensionless | 20 |
The present invention makes organic solid castoff eliminate residual antibiotic, thalline or pathogenic microorganism through hydrolysis, through anaerobism
After digestion, filter residue land use or can need to melt follow-up disposing technique through plasma gasification, and heavy metal ion is changed into stabilization
Vitreum reduce its harmfulness, finally realize organic solid castoff harmless treatment disposal.
The criterion of filter residue outward transport disposal is as follows：
1st, pollutant load meets agricultural less than the carry out of following table standard.
2nd, pollutant load carries out plasma gasification melting disposal, converts the leachate of vitreum beyond upper table standard
Constituent concentration is endangered less than the limitation of following table regulation, into household refuse landfill sites, otherwise into hazardous waste landfill.
| Sequence number | Pollutant project | Concentration limit (mg/L) |
| 1 | Mercury | 0.05 |
| 2 | Copper | 40 |
| 3 | Zinc | 100 |
| 4 | Lead | 0.25 |
| 5 | Cadmium | 0.15 |
| 6 | Beryllium | 0.02 |
| 7 | Barium | 25 |
| 8 | Nickel | 0.5 |
| 9 | Arsenic | 0.3 |
| 10 | Total chromium | 4.5 |
| 11 | Cr VI | 1.5 |
| 12 | Selenium | 0.1 |
Case study on implementation 1
Chemicals manufacturing discards antibiotic bacterium dregs：Antibiotic bacterium dregs can pass through because it contains left drug composition
Environment and food chain are shifted and accumulated, and bacteria residue is classified as hazardous waste by country from 2008.
The technology of present invention processing antibiotic bacterium dregs and the designed capacity index of equipment：
Technology：By the antibiotic bacterium dregs of solid content 30.5%, add in 6.1% solid content mixed liquor supplement process water ratio
Into homogenate pond, 200-300r/min is stirred, stirs the 30min/ cycles, the material after homogenate is entered in subcritical hydrolysis system
Hydrolysis, sets the temperature control of hydrolysis reactor in the range of 150 DEG C -200 DEG C, and pressure is in 1.0-1.2MPa, after making homogenate
Material keeps liquid, heat-insulation pressure keeping 50min.Material after hydrolysis enters solid-liquid separation system, sets the pressure of super-pressure filter press
Power is 5-6MPa.Filter residue after separation carries out outward transport disposal, and filtrate enters anaerobic reaction system, and setting IC reactor pressures are
Normal pressure, 40 DEG C of temperature, hydraulic detention time 17.5h, caused anaerobic sludge is periodically outer to be arranged, and caused IC discharges water to wastewater deepening
Processing system, national grade one discharge standard discharge is reached after wastewater treatment.
By experiment, the case study on implementation 1 is under the treatment scale in 100.0kg/ cycles, to the antibiotic bacterium of solid content 30.5%
Slag, process water is supplemented by 6.1% solid content mixed liquor, after integrated system is handled, generation 10.0kg (solid content 50%) filter cake,
2.7m3Biogas and 488.5kg waste water, antibiotic bacterium dregs can reach 90% minimizing, and system can realize that energy is certainly flat
Weighing apparatus.Case study on implementation 2
Excess sludge caused by municipal wastewater biochemical treatment：
Sludge is caused solid waste in sewage disposal process, and its main component is pathogen, organic matter, bacterium
Deng.
The technology of present invention processing sludge and the designed capacity index of equipment：
Technology：Moisture percentage in sewage sludge of the sewage plant after belt filter press is dehydrated is transported to homogenate pond, led to below 80%
Cross submersible sewage pump and extract secondary clarifier effluent mixed liquor, adjust according to a certain ratio to moisture content to 93-95%；The sludge of moisture content 94%
Conveyed by plunger pump, first pass through first-class heat exchanger and exchanged heat with hydrolysis reactor discharging, then by secondary heat exchanger with leading
Deep fat is exchanged heat, and eventually enters into 1.0-1.2MPa, in 170 DEG C of hydrolysis reactors, heat-insulation pressure keeping 60min；Material is arranged after hydrolysis
Put and enter surge tank after heat exchange, 6 hours residence times, then plate and frame filter press is pumped into by feeding plunger, filtrate is discharged into IC tune
Save tank and carry out homogeneous cooling with IC reactors recirculation water；Lower water temperature is pumped into anaeration in normal temperature IC reactions to 40 DEG C, by feed pump
Device system, water outlet are discharged into sewage plant biochemical system and reprocessed, and biogas is delivered to by reservoir hag, spark arrester and booster fan
Heat conducting oil boiler burning heat production, tail gas high altitude discharge, while the emptying of the unnecessary biogas of bypass progress is set；IC anaerobic reactors are determined
The phase body refuse of discharge is discharged into second pond, is recycled into system, the filter residue outward transport compost disposal of plate and frame filter press, is finally reached dirt
The purpose of mud volume reduction loss of weight.
By experiment, the system is under 80% water content sludge 30t/d continuous processing scales, after integrated system is handled,
Produce 7t/d (solid content 50%) filter cake, 1315.4m3/ d biogas and 92.1t/d waste water, sludge can reach 76.7% and subtract
Quantify, system can realize energy self-balancing.
Case study on implementation 3
Urban life kitchen garbage：
Kitchen garbage is organic solid, liquid waste that resident is formed during personal consumption, including cities and towns food market garbage, meal
Shop catering trade rubbish, family kitchen and dining table garbage, various melon and fruit peels etc..The control of environment system of Tsing-Hua University solid waste pollution and
Resource analysis statistics show that China city produces kitchen garbage not less than 6 000 ten thousand tons every year.Kitchen garbage
It is abundant, perishable to be mainly characterized by moisture height, content of organics, leakage water meeting polluted-water, air, influences the city appearance of the city
And human settlement.
The technology of present invention processing kitchen garbage and the designed capacity index of equipment：
Technology：Kitchen garbage first is delivered into disintegrating apparatus by spiral conveyer to be crushed, the meal after crushing
Kitchen granulated garbage diameter is less than 20cm, is added in 8-12% solid contents mixed liquor supplement process water ratio in homogenate pond, stirring
200-300r/min, the 30min/ cycles are stirred, the material after homogenate is entered in subcritical hydrolysis system and hydrolyzed, and sets hydrolysis anti-
The temperature control of device is answered in the range of 180 DEG C -200 DEG C, Stress control makes the material after homogenate keep liquid in 1-2MPa, protects
Warm pressurize 30min, hydro-thermal reaction occurs, the organic matter in kitchen garbage is fully liquefied, improves the utilization rate of kitchen garbage.
Material after hydrolysis enters solid-liquid separation system, and the pressure for setting super-pressure filter press is 4-5MPa.Filter residue after separation is carried out
Outward transport disposal, filtrate enter anaerobic reaction system, and caused anaerobic sludge is periodically outer to be arranged, and caused IC discharges water to wastewater deepening
Processing system, national grade one discharge standard discharge is reached after wastewater treatment.
By experiment, the system kitchen garbage day output can reach 30t, can produce biogas 2400m3/d。
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all essences in the present invention
God any modification, equivalent substitution and improvements made etc., should be included in the scope of the protection with principle.
Claims (8)
1. the organic solid castoff processing system based on subcritical hydrolysis, it is characterised in that：Including being sequentially connected the even of setting
Slurry system, external heat subcritical hydrolysis system, solid-liquid separation system, anaerobic reaction system with waste heat recovery；
Described homogenization system includes homogenate pond (2)；
The described external heat subcritical hydrolysis system with waste heat recovery, includes first-class heat exchanger (4), the two level being sequentially connected
Heat exchanger (5) and hydrolysis reactor (6), described hydrolysis reactor (6) are used for anti-to material progress subcritical hydrolysis after homogenate
Should, described first-class heat exchanger (4) and secondary heat exchanger (5) by be separately recovered hydrolyze after material waste heat, realize hydrolysis
Device (6) external heat hydrolyzes material；
Described solid-liquid separation system is provided with super-pressure filter press (11), and described super-pressure filter press (11) passes through machinery
Mode carries out deep dehydration to the material after hydrolysis and reduces volume；
Described anaerobic reaction system, include the IC reactors (14) being sequentially connected, marsh gas purifying tower (15), reservoir hag (16)
With heat-conducting oil furnace (18), described IC reactors (14) produce natural pond by carrying out highly effective anaerobic reaction to filtrate after separation of solid and liquid
Gas, caused biogas are stored in the reservoir hag (16), the reservoir hag after the marsh gas purifying tower (15) purifies
(16) biogas in, which is delivered in the heat-conducting oil furnace (18), to burn, and is the external heat subcritical hydrolysis system with waste heat recovery
Thermal source is provided.
2. the organic solid castoff processing system according to claim 1 based on subcritical hydrolysis, it is characterised in that institute
The hydrolysis reactor (6) for the external heat subcritical hydrolysis system with waste heat recovery stated is connected with pipe circle pump (7), and described two
The output end of level heat exchanger (5) is connected with hydrolysis reactor (6) input, and the output end of hydrolysis reactor (6) is changed by one-level
Hot device (4) is connected with pressure retaining valve (8).
3. the organic solid castoff processing system according to claim 1 based on subcritical hydrolysis, it is characterised in that institute
Stating solid-liquid separation system includes also including the hydrolysis surge tank (9) and press filtration feed pump (10) being sequentially connected, described hydrolysis
The input of surge tank (9) and the pressure retaining valve (8) of upper level are connected, and organic waste is provided with the top of described hydrolysis surge tank (9)
Gas output end, described organic exhaust gas output end are connected with spraying purification system, and described super-pressure filter press (11) is provided with
Filter residue output end and filtrate output end, described filter residue output end are connected with plasma gasification and melt follow-up disposal plant.
4. the organic solid castoff processing system according to claim 1 based on subcritical hydrolysis, it is characterised in that institute
State IC charging regulation tanks (12) and IC feed pumps (13) that anaerobic reaction system also includes being sequentially connected, described IC charging regulations
The input of tank (12) is connected with the filtrate output end of described super-pressure filter press (11), and is set in IC charging regulation tanks (12)
There is vertical stirrer.
5. the organic solid castoff processing system according to claim 1 based on subcritical hydrolysis, it is characterised in that institute
The tank wall upper end for the IC reactors (14) stated is provided with IC water sides, and described IC water sides are connected with wastewater deepening processing
System；Biogas is delivered in heat-conducting oil furnace (18) by the reservoir hag (16) by biogas conveying fan (17) to burn；Described
The conduction oil output end of heat-conducting oil furnace (18) is connected with the input of secondary heat exchanger (5), described heat-conducting oil furnace (18) output
Heat conduction oil carrier provides thermal source for external heat subcritical hydrolysis system.
6. the organic solid castoff processing system based on subcritical hydrolysis, its feature exist according to claim 1 or 5
In described reservoir hag (16) is interior to be provided with pressure sensor and flow sensor, when the internal biogas of reservoir hag (16) exceedes
Level of security, unnecessary biogas draw emergent burning through reservoir hag (16) output end.
7. the method for disposal of the organic solid castoff processing based on subcritical hydrolysis, it is characterised in that comprise the following steps：
Step (1)：Homogenate, pending organic solid castoff is added to homogenization system, by organic solid castoff and work
Skill water is added in homogenate pond (2), and the agitating device by being homogenized pond (2) stirs to form the material for possessing mobility, after homogenate
Material pass through plunger pump (3) toward with waste heat recovery external heat subcritical hydrolysis system convey；
Step (2)：Subcritical hydrolysis, the material after homogenate complete water by first-class heat exchanger (4), secondary heat exchanger (5) successively
Tank external heat is solved, is entered after external heat in hydrolysis reactor (6), subcritical hydrolysis is carried out to material after homogenate by HTHP
Reaction, beneficial to follow-up separation of solid and liquid and anaerobic digestion, while eliminates residual antibiotic, thalline or pathogenic microorganism；
Step (3)：Separation of solid and liquid, the material after hydrolysis first pass through surge tank, and caused organic exhaust gas delivers to spraying purification system,
Followed by super-pressure filter press (11), deep dehydration mechanically is carried out to material, further reduces volume, produced
Filtrate enter anaerobic reaction system, caused filter residue outward transport landfill or deliver to plasma gasification melting disposal system；
Step (4)：Anaerobic reaction, Anaerobic Digestion only is carried out to filtrate caused by solid-liquid separation system, after separation of solid and liquid
Filtrate first passes through IC charging regulation tanks (12), it is quenched after filtrate by IC feed pumps (13) to be delivered to IC reactors (14) interior,
Biogas is produced by carrying out highly effective anaerobic reaction in IC reactors (14), it is net that caused biogas first passes through marsh gas purifying tower (15)
It is stored to after change in reservoir hag (16), the biogas in reservoir hag (16) passes through biogas conveying fan (17) methane conveying to conduction oil
Burnt in stove (18), thermal source is provided for the external heat subcritical hydrolysis system with waste heat recovery；Waste water is delivered in caused IC water outlets
Deepen processing system, handle rear discharge up to standard；Caused anaerobic activated sludge is periodically outer to be arranged.
8. the method for disposal of the organic solid castoff processing according to claim 7 based on subcritical hydrolysis, its feature
It is, the parameter of described step (2) subcritical hydrolysis is as follows：The external heat subcritical hydrolysis system with waste heat recovery of control
Pressure is maintained at 0.8-1.5MPa, the temperature control of hydrolysis reactor (6) is set in the range of 150 DEG C -200 DEG C, after making homogenate
Material keep liquid, heat-insulation pressure keeping 30-60min；First-class heat exchanger (4) in described step (2) to material after hydrolysis and
Material is exchanged heat after homogenate, and waste heat recovery is carried out to material after hydrolysis；Secondary heat exchanger (5) in described step (2) is used
Material before heat transfer oil heat carrier heating hydrolysis.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108424936A (en) * | 2018-03-30 | 2018-08-21 | 中冶华天工程技术有限公司 | A kind of method and system of Chinese medicine slag hydro-thermal process combined anaerobic digestion methane phase |
| CN108585407A (en) * | 2018-06-20 | 2018-09-28 | 西安交通大学 | A kind of more technologies coupling bio-toilet fecaluria processing system and method turning to core with subcritical water hydrothermal solution |
| CN109054079A (en) * | 2018-09-10 | 2018-12-21 | 遵义师范学院 | A kind of waste plastic two-stage hydrolysis device and method |
| CN109231793A (en) * | 2018-09-13 | 2019-01-18 | 西安交通大学 | A kind of ecological toilet system and processing fecaluria method turning to core with subcritical water hydrothermal solution |
| CN109628497A (en) * | 2018-12-10 | 2019-04-16 | 河北科技大学 | A kind of antibiotic bacterium dregs recycling processing method |
| CN112280582A (en) * | 2019-07-24 | 2021-01-29 | 中国石油天然气集团有限公司 | Deep resource treatment system and method for oil-containing scum |
| CN114591106A (en) * | 2022-03-16 | 2022-06-07 | 金锋馥(滁州)科技股份有限公司 | Production method for comprehensively treating solid-liquid organic fertilizer through subcritical hydrolysis of organic waste |
| CN114985434A (en) * | 2022-06-06 | 2022-09-02 | 杭州坤灵环境技术有限公司 | Subsequent substance and energy comprehensive utilization process of organic residue hydrolysis treatment device |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2641270A1 (en) * | 2008-06-25 | 2009-12-25 | Gemini Corporation | Apparatus and process for production of biogas |
| CN104030537A (en) * | 2014-06-09 | 2014-09-10 | 王胜初 | Sludge treatment system and sludge treatment method |
| CN104355512A (en) * | 2014-10-29 | 2015-02-18 | 同济大学 | Subcritical hydrothermal treatment-based efficient recycling treatment process for sludge |
| CN105396862A (en) * | 2015-11-09 | 2016-03-16 | 天津市裕川环境科技有限公司 | Energy regeneration method for solid organic waste alkaline thermal hydrolysis supernate |
| US20170050892A1 (en) * | 2015-08-19 | 2017-02-23 | Council Of Scientific & Industrial Research | Anaerobic column reactor for biodegradation of wastes and the process thereof |
-
2017
- 2017-09-25 CN CN201710875165.7A patent/CN107460111A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2641270A1 (en) * | 2008-06-25 | 2009-12-25 | Gemini Corporation | Apparatus and process for production of biogas |
| CN104030537A (en) * | 2014-06-09 | 2014-09-10 | 王胜初 | Sludge treatment system and sludge treatment method |
| CN104355512A (en) * | 2014-10-29 | 2015-02-18 | 同济大学 | Subcritical hydrothermal treatment-based efficient recycling treatment process for sludge |
| US20170050892A1 (en) * | 2015-08-19 | 2017-02-23 | Council Of Scientific & Industrial Research | Anaerobic column reactor for biodegradation of wastes and the process thereof |
| CN105396862A (en) * | 2015-11-09 | 2016-03-16 | 天津市裕川环境科技有限公司 | Energy regeneration method for solid organic waste alkaline thermal hydrolysis supernate |
Non-Patent Citations (2)
| Title |
|---|
| 胡亨魁: "水污染治理技术", 武汉：武汉理工大学出版社 * |
| 许美芝: "亚临界水热法处理市政污泥技术及应用研究", 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》 * |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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| CN114591106A (en) * | 2022-03-16 | 2022-06-07 | 金锋馥(滁州)科技股份有限公司 | Production method for comprehensively treating solid-liquid organic fertilizer through subcritical hydrolysis of organic waste |
| CN114985434A (en) * | 2022-06-06 | 2022-09-02 | 杭州坤灵环境技术有限公司 | Subsequent substance and energy comprehensive utilization process of organic residue hydrolysis treatment device |
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