CN113717833A - Plug flow type micro aerobic hydrolysis device and method - Google Patents
Plug flow type micro aerobic hydrolysis device and method Download PDFInfo
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- CN113717833A CN113717833A CN202010454389.2A CN202010454389A CN113717833A CN 113717833 A CN113717833 A CN 113717833A CN 202010454389 A CN202010454389 A CN 202010454389A CN 113717833 A CN113717833 A CN 113717833A
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- 230000007062 hydrolysis Effects 0.000 title claims abstract description 58
- 238000006460 hydrolysis reaction Methods 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 98
- 239000011368 organic material Substances 0.000 claims abstract description 70
- 238000000855 fermentation Methods 0.000 claims abstract description 55
- 230000001079 digestive effect Effects 0.000 claims abstract description 49
- 235000011389 fruit/vegetable juice Nutrition 0.000 claims abstract description 47
- 238000010992 reflux Methods 0.000 claims abstract description 40
- 239000000463 material Substances 0.000 claims abstract description 30
- 238000005273 aeration Methods 0.000 claims abstract description 26
- 238000010438 heat treatment Methods 0.000 claims abstract description 26
- 239000007791 liquid phase Substances 0.000 claims abstract description 6
- 230000004151 fermentation Effects 0.000 claims description 35
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 22
- 230000029087 digestion Effects 0.000 claims description 22
- 239000001301 oxygen Substances 0.000 claims description 22
- 229910052760 oxygen Inorganic materials 0.000 claims description 22
- 238000012544 monitoring process Methods 0.000 claims description 15
- 238000003756 stirring Methods 0.000 claims description 15
- 230000003301 hydrolyzing effect Effects 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 238000001514 detection method Methods 0.000 claims description 6
- 238000009264 composting Methods 0.000 claims description 4
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- 239000000523 sample Substances 0.000 claims description 4
- 239000007789 gas Substances 0.000 claims description 3
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 26
- 230000020477 pH reduction Effects 0.000 description 23
- 238000007599 discharging Methods 0.000 description 11
- 239000007787 solid Substances 0.000 description 9
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- 229910000831 Steel Inorganic materials 0.000 description 1
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Abstract
The invention discloses a plug flow type microaerophilic hydrolysis device and a method, wherein the 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 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 invention is used for the first link of anaerobic fermentation, namely the hydrolysis section, can fully degrade organic materials to a liquid phase through the control of heating temperature, digestive juice reflux and micro aeration, and simultaneously discharge undegraded or difficultly degraded materials in time, thereby reducing the scale of subsequent anaerobic fermentation equipment, ensuring the yield of methane and reducing the engineering investment.
Description
Technical Field
The invention relates to a device and a method for treating organic waste, in particular to a plug flow type micro aerobic hydrolysis device and a method.
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 patent application CN201810105216.2 discloses a high-efficiency hydrolysis acidification method suitable for treating high solid content agricultural wastes and a fermentation device thereof. 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.
The Chinese 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 to realize 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
One of the purposes of the invention is to provide a plug-flow type microaerobic hydrolysis device, which can ensure continuous and stable operation when organic materials with higher solid content are treated, and effectively improve the degradation rate of the organic materials; meanwhile, the scale of subsequent anaerobic treatment can be reduced, and the engineering investment is saved.
The second purpose of the invention is to provide a plug-flow microaerobic hydrolysis method, which can provide a slightly dissolved oxygen environment for a hydrolysis section, and simultaneously, by means of temperature control, digestive juice reflux, stirring and other measures, the strain inoculation effect and fermentation uniformity are ensured to be improved under the condition of proper fermentation temperature, so that the organic materials are hydrolyzed more fully.
The invention is realized by the following steps:
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.
A plug flow type microaerobic hydrolysis method comprises the following steps:
step 1: organic materials enter the equipment shell through the feeding hole to be hydrolyzed and fermented;
step 2: simultaneously starting the stirrer and the air source to enable a central rotating shaft of the stirrer to drive a plurality of stirrer blades to stir the organic materials, and supplying oxygen into the equipment shell through the microporous aeration pipe by the air source to enable the organic materials to be fully degraded to a liquid phase;
and step 3: discharging the hydrolyzed and fermented materials out of the equipment shell through a discharge port, feeding the materials into a solid-liquid separator, and leading out and collecting the hydrolyzed and fermented methane or mixed gas through a methane collection pipe;
and 4, step 4: the materials are separated into digestive juice and biogas residues for aerobic composting by a solid-liquid separator, and the digestive juice enters a digestive juice reflux assembly through a liquid discharge port of the solid-liquid separator;
and 5: one part of the digestive juice in the digestive juice reflux assembly is pumped into the anaerobic fermentation tank, and the other part of the digestive juice is refluxed to the feeding hole;
step 6: the reflux digestive liquid is mixed with the organic materials in the equipment shell and continuously participates in the hydrolytic fermentation of the organic materials.
In the step 1 and the step 6, when the organic material is hydrolyzed and fermented in the equipment shell, the heat exchange coil of the temperature control assembly positioned below the liquid level of the organic material exchanges heat with the organic material, so that the temperature of the organic material is always positioned in a fermentation middle temperature area or a fermentation high temperature area.
Compared with the prior art, the invention has the following beneficial effects:
1. the invention can provide micro dissolved oxygen environment required by hydrolysis in the hydrolysis section by adopting the microporous aeration pipe and the air source, and simultaneously, the digestive juice after solid-liquid separation flows back to the shell of the equipment by matching with the digestive juice backflow component, so that zymophyte can be better inoculated, the hydrolysis is more sufficient, and the hydrolysis efficiency is improved.
2. The invention can mix the organic material evenly, keep flowing and prevent floating slag and crusting by stirring because of the stirrer and the stirrer blade, thereby being applied to the material with high solid content and ensuring the more stable operation of the device.
3. The invention can keep the best hydrolysis temperature condition of the organic material by heating medium and can adapt to different requirements of different organic materials on medium temperature or high temperature of the hydrolysis temperature and the like because of being provided with the temperature control component and the temperature monitor interlocked with the temperature control component.
4. The solid-liquid separator is arranged at the discharge port of the equipment shell, so that undegraded or difficultly degraded materials can be discharged in time, and the scale of subsequent anaerobic fermentation equipment is reduced.
In conclusion, the invention is applied to the first link of anaerobic fermentation, namely the hydrolysis section, can fully degrade organic materials to a liquid phase through the control of heating temperature, digestive juice reflux and micro aeration, and simultaneously discharge undegraded or difficultly degraded materials in time, thereby reducing the scale of subsequent anaerobic fermentation equipment, ensuring the yield of methane and simultaneously reducing the engineering investment.
Drawings
FIG. 1 is a cross-sectional view of a plug flow microaerophilic hydrolysis apparatus of the present invention;
FIG. 2 is a flow diagram of a plug-flow microaerobic hydrolysis process 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 is further described with reference to the following figures and specific examples.
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 the optimal reaction environment are 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 fig. 2, a plug-flow microaerobic hydrolysis method 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 a central rotating shaft of the stirrer 4 drives a plurality of 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 while 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 ℃.
The anaerobic fermentation is respectively carried out on kitchen garbage, pig manure, straw and straw by adopting the device and the method, and the fermentation conditions are as follows:
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 present invention is not limited to the above embodiments, and any modifications, equivalent replacements, improvements, etc. within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
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).
9. A microaerobic hydrolysis method using the plug-flow microaerobic hydrolysis apparatus of claim 1, wherein: the method comprises the following steps:
step 1: organic materials enter the equipment shell (1) through the feed inlet (2) for hydrolytic fermentation;
step 2: simultaneously starting the stirrer (4) and the air source (7) to enable a central rotating shaft of the stirrer (4) to drive a plurality of stirrer blades (24) to stir the organic materials, and supplying oxygen into the equipment shell (1) by the air source (7) through the microporous aeration pipe (8) to fully degrade the organic materials to a liquid phase;
and step 3: the hydrolyzed and fermented materials are discharged out of the equipment shell (1) through a discharge hole (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 reflux assembly through a liquid discharge port of the solid-liquid separator (13);
and 5: one part of the digestive juice in the digestive juice reflux assembly is pumped into the anaerobic fermentation tank, and the other part of the digestive juice is refluxed to the feeding hole (2);
step 6: the reflux digestive liquid is mixed with the organic materials in the equipment shell (1) and continuously participates in the hydrolytic fermentation of the organic materials.
10. The microaerobic hydrolysis process of claim 9, wherein: in the step 1 and the step 6, when the organic materials are hydrolyzed and fermented in the equipment shell (1), the heat exchange coil (23) of the temperature control assembly below the liquid level (25) of the organic materials exchanges heat with the organic materials, so that the temperature of the organic materials is always in a fermentation middle temperature area or a fermentation high temperature area.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN118064266A (en) * | 2024-04-22 | 2024-05-24 | 中国农业科学院农业环境与可持续发展研究所 | Microaerobic fermentation methane potential test device |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202089979U (en) * | 2011-06-01 | 2011-12-28 | 上海亚舟环保科技事务所（普通合伙） | Plug flow type garbage anaerobic digestor |
| CN102321675A (en) * | 2011-08-26 | 2012-01-18 | 中国农业机械化科学研究院 | Method and device for producing bio-gas by organic waste |
| CN204470272U (en) * | 2015-02-16 | 2015-07-15 | 江苏维尔利环保科技股份有限公司 | For changing food waste heating hydrolysis equipment |
| KR20170030404A (en) * | 2015-09-09 | 2017-03-17 | 이동주 | Method for reduction and high temperature digestion of excess sludge and high density organic waste water by aerobic and anaerobic, complex digestion tank and its system thereof |
| CN107460120A (en) * | 2017-10-10 | 2017-12-12 | 英普（北京）环境科技有限公司 | A kind of cellulose, micro- oxygen pretreatment unit of lignin fermentation methane production and method |
| CN108165478A (en) * | 2018-02-01 | 2018-06-15 | 农业部规划设计研究院 | A kind of the effectively hydrolyzing acidization tool and its installation for fermenting of the suitable high solid content agricultural wastes of processing |
| CN110643491A (en) * | 2019-09-20 | 2020-01-03 | 同济大学 | Anti-feeding impact load plug-flow anaerobic digestion reactor |
| CN212560232U (en) * | 2020-05-26 | 2021-02-19 | 上海市机电设计研究院有限公司 | Plug-flow type micro-aerobic hydrolysis device |
-
2020
- 2020-05-26 CN CN202010454389.2A patent/CN113717833A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202089979U (en) * | 2011-06-01 | 2011-12-28 | 上海亚舟环保科技事务所（普通合伙） | Plug flow type garbage anaerobic digestor |
| CN102321675A (en) * | 2011-08-26 | 2012-01-18 | 中国农业机械化科学研究院 | Method and device for producing bio-gas by organic waste |
| CN204470272U (en) * | 2015-02-16 | 2015-07-15 | 江苏维尔利环保科技股份有限公司 | For changing food waste heating hydrolysis equipment |
| KR20170030404A (en) * | 2015-09-09 | 2017-03-17 | 이동주 | Method for reduction and high temperature digestion of excess sludge and high density organic waste water by aerobic and anaerobic, complex digestion tank and its system thereof |
| CN107460120A (en) * | 2017-10-10 | 2017-12-12 | 英普（北京）环境科技有限公司 | A kind of cellulose, micro- oxygen pretreatment unit of lignin fermentation methane production and method |
| CN108165478A (en) * | 2018-02-01 | 2018-06-15 | 农业部规划设计研究院 | A kind of the effectively hydrolyzing acidization tool and its installation for fermenting of the suitable high solid content agricultural wastes of processing |
| CN110643491A (en) * | 2019-09-20 | 2020-01-03 | 同济大学 | Anti-feeding impact load plug-flow anaerobic digestion reactor |
| CN212560232U (en) * | 2020-05-26 | 2021-02-19 | 上海市机电设计研究院有限公司 | Plug-flow type micro-aerobic hydrolysis device |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN118064266A (en) * | 2024-04-22 | 2024-05-24 | 中国农业科学院农业环境与可持续发展研究所 | Microaerobic fermentation methane potential test device |
| CN118064266B (en) * | 2024-04-22 | 2024-07-19 | 中国农业科学院农业环境与可持续发展研究所 | Microaerobic fermentation methane potential test device |
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