CN212560232U - Plug-flow type micro-aerobic hydrolysis device - Google Patents
Plug-flow type micro-aerobic hydrolysis device Download PDFInfo
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- CN212560232U CN212560232U CN202020904720.1U CN202020904720U CN212560232U CN 212560232 U CN212560232 U CN 212560232U CN 202020904720 U CN202020904720 U CN 202020904720U CN 212560232 U CN212560232 U CN 212560232U
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Abstract
The utility model discloses a plug flow type micro aerobic hydrolysis device, which comprises an equipment shell (1), a stirrer (4), an air source (7), a microporous aeration pipe (8), a solid-liquid separator (13), a digestive juice reflux component and a temperature control component; a plurality of stirrer blades (24) are arranged on a central rotating shaft of the stirrer and are stirred in the equipment shell; the microporous aeration pipe is arranged at the bottom of the shell of the equipment shell and is externally connected with an air source; the solid-liquid separator is connected with a discharge hole (12) of the equipment shell and the digestive juice reflux assembly, and the discharge hole of the digestive juice reflux assembly is connected with a feed hole (2) of the equipment shell; the temperature control component heats the organic materials in a contact manner. The utility model discloses a first link for anaerobic fermentation is the section of hydrolysising promptly, can make organic material fully degrade to the liquid phase through heating temperature, digestive juice backward flow and the control of little aeration, and the material that will not degrade or difficult degradation simultaneously in time discharges, reduces follow-up anaerobic fermentation equipment scale, guarantees marsh gas output, reduces the engineering investment.
Description
Technical Field
The utility model relates to a device for handling organic waste especially relates to a plug flow formula is little good oxygen hydrolysis unit.
Background
The anaerobic fermentation technology is widely used in the field of organic waste disposal, can generate biogas which is a renewable clean energy source when being biologically treated, can perform composting or be used for producing soil conditioners on generated biogas residues, and has the advantages of high efficiency, high economy and the like. Hydrolysis acidification is the first fermentation link of anaerobic fermentation, and proper aeration and auxiliary stirring in the hydrolysis section can obviously improve the degradation efficiency of lignocellulose in organic materials, accelerate the decomposition of the organic materials and simultaneously improve the biogas yield of subsequent anaerobic fermentation.
The chinese utility model patent application CN201810105216.2 discloses a high-efficiency hydrolysis acidification method and a fermentation device thereof suitable for treating high solid content agricultural wastes, wherein the device comprises a hydrolysis acidification reactor, a hot water circulation system, percolate, a biogas slurry spraying regulation system and an aeration system. The hydrolysis acidification reactor can treat high solid content agricultural wastes, adopts a forklift to directly feed and discharge materials, continuously provides a heat source for the reactor through a hot water circulating system, and performs medium temperature fermentation; the leachate and biogas slurry spraying adjusting system is used for spraying leachate (acidizing fluid) and biogas slurry in a backflow mode, the continuous hydrolysis acidification capability of materials is enhanced, and the aeration system provides a micro aerobic hydrolysis acidification environment for hydrolysis acidification reaction and strengthens hydrolysis. The patent application has the following disadvantages:
1. the fermentation device belongs to a sequencing batch production device, and a forklift is used for feeding and discharging materials in a fermentation period, so that continuous production cannot be realized.
2. After fermentation, the fermented material is discharged through a forklift, and after the fermented material is discharged, the fermented material needs to be additionally treated, so that the operation is inconvenient, the operation efficiency is low, and pollution possibly exists.
3. The materials are in static stacking during hydrolytic acidification, stirring is not needed, the materials need longer retention time in the fermentation device, the fermentation efficiency is low, and the capacity of the fermentation device is small.
4. The biogas slurry spraying adjusting system utilizes the backflow percolate to spray, the required percolate amount is large in spraying, the energy consumption is high, and the control difficulty is large.
Chinese utility model patent ZL201210180850.5 discloses a method for producing biogas by anaerobic digestion of fruit and vegetable waste, which comprises the steps of firstly acidifying the fruit and vegetable waste and carrying out high-efficiency extrusion process, realizing solid-liquid separation, and then respectively treating solid and liquid products. The solid residue and the liquid acidification product enter a high-efficiency anaerobic digestion methane production reactor after secondary strengthening acidification, and meanwhile, the effluent of the methane reactor is used as reflux to circulate in the solid residue secondary strengthening hydrolysis acidification reactor to accelerate hydrolysis acidification reaction. The method adopts reflux liquid to circulate in a hydrolysis acidification reactor, the effluent of a methane reactor is used as supplement, and the purposes of strain inoculation and zero discharge of waste water are achieved, but because the water content of fruit and vegetable garbage is up to more than 80 percent, and the consideration of material balance in the anaerobic fermentation process is lacked, the patent can not achieve the purpose of zero discharge of waste water actually; in addition, the reflux liquid is hydrolytic acidification liquid, strains (hydrogen-producing acetogenic bacteria) required by hydrolytic acidification are enriched, the effluent of the methane reactor is biogas slurry, the enriched strains (methane-producing bacteria) required by hydrolytic acidification are enriched, the two strains have different growth conditions and adaptive capacities, the two strains can inhibit the hydrolytic acidification strains when put together, and the hydrolytic acidification does not need to carry out full-scale reflux inoculation on a large number of strains, so that the strain inoculation effect is poor.
Disclosure of Invention
The utility model aims to provide a plug-flow type microaerobic hydrolysis device, which can ensure continuous and stable operation when processing organic materials with higher solid content, provide a slightly dissolved oxygen environment for a hydrolysis section, and simultaneously, is assisted with measures such as temperature control, digestive juice reflux, stirring and the like, ensure that the inoculation effect and the fermentation uniformity of strains are improved under the condition of proper fermentation temperature, so that the hydrolysis of the organic materials is more sufficient, and the degradation rate of the organic materials is effectively improved; meanwhile, the scale of subsequent anaerobic treatment can be reduced, and the engineering investment is saved.
The utility model discloses a realize like this:
a plug flow type micro aerobic hydrolysis device comprises an equipment shell, a stirrer, an air source, a microporous aeration pipe, a solid-liquid separator, a digestive juice reflux assembly and a temperature control assembly; a feed inlet and a discharge outlet are respectively arranged on two sides of the equipment shell, and a biogas collecting pipe is arranged at the top of the equipment shell; the stirrer is arranged in the equipment shell, a central rotating shaft of the stirrer horizontally penetrates through the equipment shell, and a plurality of stirrer blades are arranged on the central rotating shaft of the stirrer at intervals, so that the stirrer can drive the stirrer blades to rotate and stir in the equipment shell through the central rotating shaft; the microporous aeration pipe is arranged at the bottom of the shell inside the equipment shell, and one end of the microporous aeration pipe extends to the outside of the equipment shell and is connected with an air source; a feed port of the solid-liquid separator is connected to a discharge port of the equipment shell, a liquid discharge port of the solid-liquid separator is connected to a feed port of the digestive juice reflux assembly, and a discharge port of the digestive juice reflux assembly is connected to a feed port of the equipment shell; the temperature control component is arranged on the equipment shell and contacts with the equipment shell to heat the organic materials.
The digestion liquid backflow component comprises a digestion liquid collecting tank, a backflow pump, a digestion liquid pump and a backflow pipe, a liquid discharge port of the solid-liquid separator is connected to the digestion liquid collecting tank through a pipeline, the digestion liquid collecting tank is connected to a feed inlet through the backflow pipe, the backflow pump is installed on the backflow pipe, and the digestion liquid pump is installed on the pipeline between the backflow pipe and the anaerobic fermentation tank.
The temperature control assembly comprises a heat exchange coil, a heat medium inlet pipe and a heat medium outlet pipe; the heat exchange coil is positioned below the liquid level of the organic material in the equipment shell, one end of the heat medium inlet pipe and one end of the heat medium outlet pipe are respectively connected to two ends of the heat exchange coil, and the other end of the heat medium inlet pipe and the other end of the heat medium outlet pipe are externally connected to a medium circulating heating source, so that the heating medium circularly flows between the temperature control component and the medium circulating heating source and heats the organic material.
The heating medium is hot water, and the heating temperature of the organic materials by the circularly flowing heating medium is medium temperature or high temperature.
The equipment shell on be equipped with a plurality of monitoring point, and a plurality of monitoring point department all installs the monitor.
The monitor comprises a liquid level monitor, a temperature monitor, a pH value monitor, a dissolved oxygen monitor and an ORP monitor, wherein a detection head of the liquid level monitor is positioned in the equipment shell, and the liquid level monitor is interlocked with the feed inlet, the digestive juice reflux assembly and the discharge outlet; the detection heads of the temperature monitor, the PH value monitor, the dissolved oxygen monitor and the ORP monitor are all positioned below the liquid level in the equipment shell; the temperature monitor is interlocked with the temperature control component and the stirrer; the pH value monitor is interlocked with the feed inlet, the digestive juice reflux assembly, the discharge port and the stirrer; the dissolved oxygen monitor is interlocked with the microporous aeration pipe; the ORP monitor is linked to the pH monitor.
The lower part of the equipment shell is provided with a sampling port.
The bottom of the equipment shell is provided with an access hole.
Compared with the prior art, the utility model, following beneficial effect has:
1. the utility model discloses owing to adopted micropore aeration pipe and air source, can provide the required dissolved oxygen environment a little of hydrolysising at the section of hydrolysising, cooperate simultaneously in the digestive juice backward flow back equipment shell after the digestive juice backward flow subassembly with solid-liquid separation, can better inoculate the fermentation bacterial, make the hydrolysis more abundant, improve the efficiency of hydrolysising.
2. The utility model discloses owing to be equipped with agitator and agitator paddle, the accessible stirring makes organic material misce bene, keeps flowing, prevents to produce dross and crust to can be applied to the material that the high solid content was rateed, also can ensure the more stable operation of device simultaneously.
3. The utility model discloses owing to be equipped with temperature control assembly and rather than the temperature monitor of interlocking, can make organic material keep the best temperature condition of hydrolysising through heating medium, and can adapt to different organic materials to different requirements such as the medium temperature of hydrolysis temperature or high temperature.
4. The utility model discloses owing to set up solid-liquid separation machine at the discharge gate of equipment shell, can in time discharge nondegradable or difficult degradation's material, reduce follow-up anaerobic fermentation equipment's scale.
To sum up, the utility model discloses be applied to anaerobic fermentation's first link in the section of hydrolysising promptly, can make organic material fully degrade to the liquid phase through heating temperature, digestive juice backward flow and micro-aeration's control, in time discharge undegraded or difficult degradation's material simultaneously, can make follow-up anaerobic fermentation equipment's scale reduce, reduce the engineering investment when guaranteeing marsh gas output.
Drawings
FIG. 1 is a sectional view of a plug-flow microaerophilic hydrolysis apparatus of the present invention;
fig. 2 is a flow chart of the flow pushing type micro aerobic hydrolysis device of the present invention.
In the figure, 1 equipment shell, 2 feed inlets, 3 return pipes, 4 stirrers, 5 sampling ports, 6 maintenance ports, 7 air sources, 8 microporous aeration pipes, 9 digestive juice pumps, 10 return pumps, 11 digestive juice collecting tanks, 12 discharge ports, 13 solid-liquid separators, 14 biogas residues, 15 heat medium inlet pipes, 16 heat medium outlet pipes, 17 liquid level monitors, 18 biogas collecting pipes, 19 temperature monitors, 20 PH value monitors, 21 dissolved oxygen monitors, 22 ORP monitors, 23 heat exchange coil pipes, 24 stirrer blades and 25 liquid levels.
Detailed Description
The invention will be further explained with reference to the drawings and the specific embodiments.
Referring to the attached figure 1, the plug flow type micro aerobic hydrolysis device comprises an equipment shell 1, a stirrer 4, an air source 7, a microporous aeration pipe 8, a solid-liquid separator 13, a digestive juice reflux assembly and a temperature control assembly; a feed inlet 2 and a discharge outlet 12 are respectively arranged on two sides of the equipment shell 1, and a biogas collecting pipe 18 is arranged at the top of the equipment shell 1; the stirrer 4 is arranged in the equipment shell 1, a central rotating shaft of the stirrer 4 horizontally penetrates through the equipment shell 1, and a plurality of stirrer blades 24 are arranged on the central rotating shaft of the stirrer 4 at intervals, so that the stirrer 4 can drive the stirrer blades 24 to rotate and stir in the equipment shell 1 through the central rotating shaft, materials can be stirred and pushed, the fermentation efficiency is improved, and the retention time of the materials in the equipment shell 1 is not more than 4 days; the microporous aeration pipe 8 is arranged at the bottom of the inner part of the equipment shell 1, and one end of the microporous aeration pipe 8 extends to the outer part of the equipment shell 1 and is connected with an air source 7; a feed port of the solid-liquid separator 13 is connected to a discharge port 12 of the equipment shell 1, a liquid discharge port of the solid-liquid separator 13 is connected to a feed port of the digestive juice reflux assembly, and discharge is directly connected to the solid-liquid separator 13, so that integrated production is realized, production efficiency is improved, the load of subsequent production is effectively reduced by timely discharging solid residues, and the discharge port of the digestive juice reflux assembly is connected to a feed port 2 of the equipment shell 1; the temperature control component is arranged on the equipment shell 1 and contacts with the equipment shell to heat the organic materials.
The digestion liquid backward flow subassembly include digestion liquid collecting pit 11, backwash pump 10, digestion liquid pump 9 and back flow 3, the liquid discharge gate of solid-liquid separation machine 13 passes through pipe connection to in the digestion liquid collecting pit 11, digestion liquid collecting pit 11 is connected to feed inlet 2 through back flow 3, backwash pump 10 installs on back flow 3, digestion liquid pump 9 installs on the pipeline between back flow 3 and subsequent anaerobic fermentation pond, control material moisture content and inoculation bacterial that the mode that adopts the partial backward flow of digestion liquid can be better, the characteristics that the fermentation condition is even and the bacterial is unchangeable have, can handle the higher material of solid content rate, adaptability is wide, the hydrolysis effect is better, in addition compare current mode such as spraying and can effectively reduce the reflux of digestion liquid through the mode of backward flow, thereby reduce the energy consumption, and the reflux is adjustable, the system reliability is high. The solid-liquid separator 13 is used for solid-liquid separation of the output organic materials.
The temperature control assembly comprises a heat exchange coil 23, a heat medium inlet pipe 15 and a heat medium outlet pipe 16; the heat exchange coil 23 is located below the liquid level 25 of the organic material in the equipment shell 1, one end of the heat medium inlet pipe 15 and one end of the heat medium outlet pipe 16 are respectively connected to two ends of the heat exchange coil 23, the other end of the heat medium inlet pipe 15 and the other end of the heat medium outlet pipe 16 are externally connected to a medium circulating heating source, so that the heating medium circularly flows between the temperature control assembly and the medium circulating heating source and heats the organic material, and the medium circulating heating source realizes heating of the heating medium and circulating pumping.
The heating medium is hot water, and the heating temperature of the organic materials by the circularly flowing heating medium is medium temperature (preferably 35-37 ℃) or high temperature (preferably 52-55 ℃), so that the temperature requirements of different organic materials during fermentation are met, and the optimal hydrolysis fermentation effect is achieved.
The equipment shell 1 is provided with a plurality of monitoring points, the monitoring points are all provided with monitors, the heat exchange, stirring, micro-aeration and reflux operation of the hydrolysis section are controlled in a linkage mode according to monitoring data, closed-loop control is carried out, and the monitors can adopt a continuous or discontinuous operation mode, so that the optimal hydrolysis fermentation condition is maintained.
Preferably, the monitors include a liquid level monitor 17, a temperature monitor 19, a PH monitor 20, a dissolved oxygen monitor 21, and an ORP (oxidation-reduction potential) monitor 22, and the probing tips of the liquid level monitor 17 are located below the liquid level 25 in the apparatus housing 1 in all of the temperature monitor 19, the PH monitor 20, the dissolved oxygen monitor 21, and the ORP monitor 22; and the temperature monitor 19 is electrically connected to the media circulation heating source.
The liquid level monitor 17 can use the ultrasonic wave or radar liquid level meter (such as the ultrasonic wave liquid level meter with the model of FMU30 series) in the prior art to realize the liquid level height detection of the organic materials in the equipment shell 1, and the on-off of the feed inlet 2 and the feed system thereof, the stirrer 4, the discharge outlet 12 and the discharge pump thereof is controlled in an interlocking manner, so that the entering amount or the output amount of the organic materials in the equipment shell 1 can be better controlled. The liquid level monitoring is interlocked with feeding, backflow and discharging, and the process adopts the form of continuous allocation and continuous discharging, so that materials in the device fluctuate slightly within a set range during normal operation, and the feeding system, the digestive juice backflow component, the stirrer 4 and the discharging pump operate simultaneously within a set liquid level range, so that the automation degree is high. If the actual liquid level reaches the set liquid level, automatic alarm, feeding and backflow stop can be realized; if the actual liquid level is higher than the set liquid level, reducing feeding and backflow and increasing discharging; if the actual liquid level is lower than the set liquid level, the feeding and the backflow are increased, the discharging is reduced, and the feeding system, the stirrer and the discharging pump are stopped. At first start-up, fresh water is used as the make-up water.
The temperature monitor 19 can adopt the contact temperature sensor in the prior art to realize the temperature sensing detection of the organic materials in the equipment shell 1, thereby being capable of better controlling the temperature of the heating medium and ensuring the fermentation temperature of the organic materials. The temperature monitoring is interlocked with the temperature control component and the stirrer 4, the temperature control component provides a heat source and a heat exchange medium, the stirrer 4 is responsible for stirring, so that the heat exchange between the organic material and the heat exchange medium is uniform, the temperature of the organic material is controlled to be 35-37 ℃ at the middle temperature, and the temperature is controlled to be 52-55 ℃. The temperature monitor 19 can be preferably a heat resistance thermometer of WZPK series in the prior art, three heat resistance thermometers can be arranged in the equipment shell 1 at intervals to monitor the temperature of the organic material, so that the temperature difference of the material at any two monitoring points is not more than 0.5 ℃, and the temperature difference is controlled by adjusting the stirring time of the stirrer 4 in a linkage manner.
The pH monitor 20 can be a pH value detector composed of a BPH-200 series sensor and its instrument in the prior art. The pH value monitoring is interlocked with the feeding, the refluxing, the discharging and the stirrer 4, preferably, the pH value of the organic material in the equipment shell 1 is maintained between 6 and 7, and the refluxing amount and the discharging amount are adjusted according to the feeding amount under the condition of certain stirring intensity of the stirrer 4; after a certain feeding proportion is exceeded, the stirring intensity and the discharge amount are adjusted. The pH monitor 20 may be a 2-pack split pH meter, with the transducer CM442 and the measurement electrode CPF 81D. The inside of the equipment shell 1 is provided with a hydrolytic acidification section for producing methane by anaerobic fermentation, which mainly has the function of mass propagation of acetic acid bacteria and the pH value adaptive range of 5.0-8.5, while the next methanogenesis section connected with the equipment shell 1 is mainly used for producing methane bacteria, which are sensitive to the pH value and the suitable range of pH6.5-7.8, and in order to consider two different reaction conditions and the efficiency of the hydrolytic acidification section, the pH of the hydrolytic acidification section is set to be between 6.0 and 7.0.
The dissolved oxygen monitoring is interlocked with the microporous aeration pipe 8 and an air source control system thereof, preferably, the dissolved oxygen concentration in the organic material is maintained within 1.0mg/L, the air source control system controls the microporous aeration pipe 8 to run discontinuously, and the aeration amount and the running frequency are adjusted according to the dissolved oxygen concentration. The dissolved oxygen monitor 21 can adopt a split type dissolved oxygen instrument, a transmitter CM442, a measuring electrode is COS61D series, the opening degree of an air inlet regulating valve of an air source and the frequency of a frequency converter of a fan are controlled according to the content of dissolved oxygen in the biogas slurry, and the content of the dissolved oxygen in the biogas slurry is ensured within a set range.
ORP monitor 22 is used for monitoring and reflecting the anaerobic state of the material, the data mainly judges whether the organic material is operated under the facultative condition, since the oxidation-reduction potential is influenced by the pH value (low pH value, high oxidation-reduction potential; high pH value, low oxidation-reduction potential), ORP monitoring can be linked with pH value monitoring, the ORP value can be adjusted by adjusting the pH value, and the ORP can also be independently monitored. In the whole process of methane fermentation, the hydrolysis acidification section has the highest efficiency under the facultative condition, preferably, the oxidation-reduction potential of the organic materials is +100 to-100 mV, and the oxidation-reduction potential of the methane fermentation stage is-150 to-400 mV. ORP monitor 22 can employ a split ORP meter, transmitter CM442 with a CPF82D measuring electrode.
Each part of the chain control is controlled by an automatic control system which takes a PLC as a core controller and takes a field sensing probe as signal input, and the control mode of combining automation and manual operation in a remote centralized and on-site manner is adopted, so that the flexible adjustment of system control parameters can be realized, and the manual/automatic control undisturbed switching of all automatic control equipment can be realized. Preferably, the PLC controller is S7-200 SMART, is provided with a SIMATIC HMI 9' touch screen, is matched with upper software SIMATIC Wincc, and has about 5 control loops and about 50 detection points, and a corresponding low-voltage power distribution system monitors and controls the whole production device.
One side of equipment shell 1 be equipped with sample connection 5, sample connection 5 is located the lower part of equipment shell 1, can be used to gather organic material from equipment shell 1 in and be used for the chemical examination to know the hydrolysis state of organic material.
The bottom of the equipment shell 1 is provided with an access hole 6, so that the equipment inside the equipment shell 1 can be conveniently dismounted and overhauled.
Preferably, the equipment housing 1 is preferably a concrete structure, a steel structure or a reinforced concrete integrated structure according to the requirements of the amount, the characteristics and the like of the organic materials to be actually treated, and can also be designed and manufactured by using other materials according to the needs.
Preferably, the central rotating shaft of the stirrer 4 can be of a single-shaft type or a multi-shaft type, the number of the central rotating shafts of the multi-shaft type is determined and installed according to actual needs, and the arrangement mode and the form of the stirrer blade 24 on the central rotating shaft can be determined through numerical simulation according to the fluid state, so that the optimal hydrolysis fermentation condition and reaction environment can be always kept in the equipment shell 1.
Preferably, the air source 7 can be a blower or an air compressor of the prior art, and provides corresponding air flow into the equipment housing 1 according to the dissolved oxygen required by the hydrolysis section.
Preferably, the selection of the solid-liquid separator 13 can be determined according to the characteristics of the organic materials.
Referring to the attached fig. 2, the plug-flow microaerobic hydrolysis method using the plug-flow microaerobic hydrolysis apparatus of the present invention comprises the following steps:
step 1: organic materials enter the equipment shell 1 through the feed inlet 2 for hydrolytic fermentation.
Step 2: simultaneously, the stirrer 4 and the air source 7 are started, so that the central rotating shaft of the stirrer 4 drives the stirrer blades 24 to stir the organic materials, the organic materials are uniformly mixed and flow to the discharge port 12, scum or crusting is prevented from being generated, the air source 7 supplies oxygen into the equipment shell 1 through the microporous aeration pipe 8 when the organic materials flow, a microaerobic environment required by hydrolysis in the equipment shell 1 is maintained, and the organic materials are fully degraded to a liquid phase.
And step 3: the hydrolyzed and fermented materials are discharged out of the equipment shell 1 through a discharge port 12 and enter a solid-liquid separator 13, and the hydrolyzed and fermented biogas or mixed gas is guided out and collected through a biogas collecting pipe 18.
And 4, step 4: the materials are separated into digestive juice and biogas residue 14 for aerobic composting by a solid-liquid separator 13, and the digestive juice enters a digestive juice collecting tank 11 of a digestive juice reflux assembly through a liquid discharge port of the solid-liquid separator 13. The solid discharge port of the solid-liquid separator 13 discharges undegraded and difficultly degraded materials in time, so that the scale of subsequent anaerobic fermentation is reduced, and the engineering investment is reduced.
And 5: one part of the digestive juice in the digestive juice collecting tank 11 is pumped into the anaerobic fermentation tank, the other part of the digestive juice flows back to the feed inlet 2 through the reflux pipe 3 by the reflux pump 10 of the digestive juice reflux assembly, and the yield of the biogas can be ensured by the reflux of the liquid phase digestive juice.
Step 6: the refluxed digestive juice is mixed with the organic materials in the equipment shell 1 and continuously participates in the hydrolytic fermentation of the organic materials. The reflux digestive juice can be better inoculated with fermentation strains, and the hydrolysis efficiency is improved.
In the step 1 and the step 6, when the organic material is hydrolyzed and fermented in the equipment shell 1, the heat exchange coil 23 of the temperature control component positioned below the liquid level 25 of the organic material exchanges heat with the organic material, so that the temperature of the organic material is always positioned in a fermentation temperature range. According to the fermentation requirement of the organic materials, the fermentation temperature interval can be 35-37 ℃ or 52-55 ℃.
Adopt the utility model discloses the device carries out anaerobic fermentation to rubbish from cooking, pig manure with straw, straw respectively, and the fermentation condition is:
in example 1, the anaerobic fermentation retention time of the kitchen waste is only 1 day; in the embodiment 2, the retention time of the anaerobic fermentation of the pig manure and the straws is only 2 to 3 days; in example 3, the anaerobic fermentation retention time of the straw is only 4 days; the hydrolysis efficiency is high. Meanwhile, in the examples 1-3, the change difference of volatile organic acid (VFA) in the materials in the water inlet and the water outlet is large, the hydrolysis acidification degree is high, after kitchen garbage, pig manure and straw are added, and the straw is subjected to hydrolysis acidification, non-soluble organic matters and organic matters which are difficult to biodegrade are converted into soluble substances which are easy to biodegrade, so that the BOD of the water outlet of the hydrolysis device in a dissolved state is generated5The value tends to increase, and the oxygen consumption rate of the waste water is obviously improved, so that the obtained hydrolysis effect is better.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and should not be taken as limiting the scope of the present invention, therefore, any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention should be included in the scope of the present invention.
Claims (8)
1. A plug flow type micro aerobic hydrolysis device is characterized in that: comprises an equipment shell (1), a stirrer (4), an air source (7), a microporous aeration pipe (8), a solid-liquid separator (13), a digestive juice reflux assembly and a temperature control assembly; a feed inlet (2) and a discharge outlet (12) are respectively arranged on two sides of the equipment shell (1), and a biogas collecting pipe (18) is arranged at the top of the equipment shell (1); the stirrer (4) is arranged in the equipment shell (1), a central rotating shaft of the stirrer (4) horizontally penetrates through the equipment shell (1), and a plurality of stirrer blades (24) are arranged on the central rotating shaft of the stirrer (4) at intervals, so that the stirrer (4) can drive the stirrer blades (24) to rotate and stir in the equipment shell (1) through the central rotating shaft; the microporous aeration pipe (8) is arranged at the bottom of the inner part of the equipment shell (1), and one end of the microporous aeration pipe (8) extends to the outside of the equipment shell (1) and is connected with an air source (7); a feed port of the solid-liquid separator (13) is connected to a discharge port (12) of the equipment shell (1), a liquid discharge port of the solid-liquid separator (13) is connected to a feed port of the digestive juice reflux assembly, and a discharge port of the digestive juice reflux assembly is connected to a feed port (2) of the equipment shell (1); the temperature control component is arranged on the equipment shell (1) and contacts with the equipment shell to heat the organic materials.
2. A plug flow microaerobic hydrolysis unit as claimed in claim 1, wherein: the digestion liquid backflow component comprises a digestion liquid collecting pool (11), a backflow pump (10), a digestion liquid pump (9) and a backflow pipe (3), a liquid discharge port of a solid-liquid separator (13) is connected into the digestion liquid collecting pool (11) through a pipeline, the digestion liquid collecting pool (11) is connected to a feed port (2) through the backflow pipe (3), the backflow pump (10) is installed on the backflow pipe (3), and the digestion liquid pump (9) is installed on the pipeline between the backflow pipe (3) and an anaerobic fermentation pool.
3. A plug flow microaerobic hydrolysis unit as claimed in claim 1, wherein: the temperature control assembly comprises a heat exchange coil (23), a heat medium inlet pipe (15) and a heat medium outlet pipe (16); the heat exchange coil (23) is positioned below the liquid level (25) of the organic material in the equipment shell (1), one end of the heat medium inlet pipe (15) and one end of the heat medium outlet pipe (16) are respectively connected to two ends of the heat exchange coil (23), the other end of the heat medium inlet pipe (15) and the other end of the heat medium outlet pipe (16) are externally connected to a medium circulating heating source, and the heating medium circularly flows between the temperature control assembly and the medium circulating heating source and heats the organic material.
4. A plug flow microaerobic hydrolysis unit as claimed in claim 3, wherein: the heating medium is hot water, and the heating temperature of the organic materials by the circularly flowing heating medium is medium temperature or high temperature.
5. A plug flow microaerobic hydrolysis unit as claimed in claim 1, wherein: the equipment shell (1) on be equipped with a plurality of monitoring point, and a plurality of monitoring point department all installs the monitor.
6. The plug-flow microaerobic hydrolysis unit of claim 5, further comprising: the monitor comprises a liquid level monitor (17), a temperature monitor (19), a PH value monitor (20), a dissolved oxygen monitor (21) and an ORP monitor (22), a probe of the liquid level monitor (17) is positioned in the equipment shell (1), and the liquid level monitor (17) is interlocked with the feed inlet (2), the digestive juice reflux assembly and the discharge outlet (12); the detection heads of the temperature monitor (19), the PH value monitor (20), the dissolved oxygen monitor (21) and the ORP monitor (22) are all positioned below the liquid level (25) in the equipment shell (1); the temperature monitor (19) is interlocked with the temperature control component and the stirrer (4); the PH value monitor (20) is interlocked with the feed inlet (2), the digestive juice reflux assembly, the discharge outlet (12) and the stirrer (4); the dissolved oxygen monitor (21) is interlocked with the microporous aeration pipe (8); the ORP monitor (22) is linked to the pH monitor (20).
7. A plug flow microaerobic hydrolysis unit as claimed in claim 1, wherein: the lower part of the equipment shell (1) is provided with a sampling port (5).
8. The plug-flow microaerobic hydrolysis unit of claim 1 or 7, wherein: the bottom of the equipment shell (1) is provided with an access hole (6).
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| CN202020904720.1U CN212560232U (en) | 2020-05-26 | 2020-05-26 | Plug-flow type micro-aerobic hydrolysis device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113717833A (en) * | 2020-05-26 | 2021-11-30 | 上海市机电设计研究院有限公司 | Plug flow type micro aerobic hydrolysis device and method |
| CN116082138A (en) * | 2022-12-28 | 2023-05-09 | 中国农业大学 | Method and device for directionally regulating and controlling anaerobic continuous production of volatile fatty acid by corn straw |
-
2020
- 2020-05-26 CN CN202020904720.1U patent/CN212560232U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113717833A (en) * | 2020-05-26 | 2021-11-30 | 上海市机电设计研究院有限公司 | Plug flow type micro aerobic hydrolysis device and method |
| CN116082138A (en) * | 2022-12-28 | 2023-05-09 | 中国农业大学 | Method and device for directionally regulating and controlling anaerobic continuous production of volatile fatty acid by corn straw |
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