CN220788576U - Anaerobic fermentation device taking ethanol as intermediate product of kitchen waste - Google Patents
Anaerobic fermentation device taking ethanol as intermediate product of kitchen waste Download PDFInfo
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- CN220788576U CN220788576U CN202322221597.XU CN202322221597U CN220788576U CN 220788576 U CN220788576 U CN 220788576U CN 202322221597 U CN202322221597 U CN 202322221597U CN 220788576 U CN220788576 U CN 220788576U
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 75
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- 239000010806 kitchen waste Substances 0.000 title claims abstract description 34
- 239000013067 intermediate product Substances 0.000 title claims abstract description 19
- 230000020477 pH reduction Effects 0.000 claims abstract description 83
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- 238000006460 hydrolysis reaction Methods 0.000 claims description 74
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- 230000004151 fermentation Effects 0.000 claims description 16
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- 238000000034 method Methods 0.000 abstract description 23
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- 239000007789 gas Substances 0.000 description 33
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 26
- 235000011054 acetic acid Nutrition 0.000 description 16
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- 239000000047 product Substances 0.000 description 14
- 239000002207 metabolite Substances 0.000 description 13
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 12
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- NQPDZGIKBAWPEJ-UHFFFAOYSA-N valeric acid Chemical compound CCCCC(O)=O NQPDZGIKBAWPEJ-UHFFFAOYSA-N 0.000 description 6
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- 102000004169 proteins and genes Human genes 0.000 description 5
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- Treatment Of Sludge (AREA)
Abstract
The utility model belongs to the technical field of kitchen waste treatment, and particularly relates to an anaerobic fermentation device using ethanol as an intermediate product of kitchen waste. The device comprises a hydrolytic acidification tank, wherein the hydrolytic acidification tank is connected with a centrifugal dehydrator through a buffer tank, and the centrifugal dehydrator is connected with an anaerobic tank through a buffer tank II. The utility model can reduce the hydraulic retention time, improve the organic load and reduce the process difficulty.
Description
Technical Field
The utility model belongs to the technical field of kitchen waste treatment, and particularly relates to an anaerobic fermentation device using ethanol as an intermediate product of kitchen waste.
Background
Anaerobic digestion technology is a main way of recycling kitchen waste, and the occupied energy in the established recycling project reaches 66%. Wherein wet anaerobic is the main material. The prior wet anaerobic process mainly adopts the traditional four-step reaction: four stages of hydrolysis, acidification, acetic acid production and methane production.
In the hydrolysis stage, suspended particle organic matters such as carbohydrate, protein, fat and the like in the kitchen waste are hydrolyzed into soluble organic matters such as polysaccharide, polypeptide, organic acid and the like by microorganisms; the short chain organic matter is degraded into glucose, amino acid, VFAs (volatile fatty acids) and NH by acidogenic bacteria 3 And H 2 S, etc.; glucose and amino acids are utilized by acetogenic bacteria to produce acetic acid, H 2 And CO 2 The method comprises the steps of carrying out a first treatment on the surface of the Methanogen in methanation stage drives acetic acid and H 2 Conversion to CH 4 And CO 2 。
By the principle, two-phase anaerobic digestion is commonly adopted in engineering, and by separating acidogenic bacteria from methanogenic bacteria, the inhibition of the bacteria activity by the environment is avoided under the optimal environmental conditions.
But the following disadvantages exist:
(1) In the prior art of two-phase anaerobic digestion, the pH of the acid-producing phase is generally controlled to be 5.0-6.5, so that the acid-producing phase products mainly comprise butyric acid, propionic acid, acetic acid and valeric acid, and the subsequent methanation of the products needs long time.
(2) The two steps of hydrolysis acidification and methane production have long residence time, and the addition time can reach 22-43 d. Correspondingly, the required hydrolysis tank and fermentation tank have large volume, large occupied area and high investment cost, and meanwhile, large-scale stirring facilities are required to be arranged, so that the operation cost is high.
(3) The gas components generated in the hydrolysis stage are complex and CO 2 Low content of methane and hydrogen, and low content of methane and hydrogenThe use value is low, and the odor is often used as odor to enter a deodorizing system of a whole plant for treatment, so that the deodorizing investment cost and the running cost are increased.
(4) The volume load of the anaerobic tank is low and is only (2.5-3.5) kgVS/(m) 3 D), low volumetric gas production rate.
(5) The methane content of the biogas generated by anaerobic reaction is generally 55-65%, the purification cost is high, and the purification procedure is complicated.
(6) After anaerobic fermentation, the fermentation liquid is subjected to two-phase centrifugal separation, the COD content in the biogas slurry is higher, and the subsequent sewage treatment system is complex in process, longer in flow and higher in energy consumption.
From the above, it can be seen that the high residence time and low volume load directly lead to engineering complications, large occupied area and long recovery period.
Disclosure of Invention
The utility model aims to provide an anaerobic fermentation device using ethanol as an intermediate product of kitchen waste, which can reduce hydraulic retention time, improve organic load and reduce process difficulty.
An anaerobic fermentation device taking ethanol as an intermediate product of kitchen waste comprises a hydrolysis acidification tank, wherein the hydrolysis acidification tank is connected with a centrifugal dehydrator through a buffer tank, and the centrifugal dehydrator is connected with an anaerobic tank through a buffer tank II.
Preferably, the hydrolysis acidification tank is respectively provided with a liquid level meter I, a temperature sensor I and a stirrer.
Preferably, the hydrolysis acidification tank is also provided with a pressure sensor and a first gas analyzer, and the hydrolysis acidification tank is also connected with a heat exchange system.
Preferably, a first discharging pump arranged on the hydrolysis acidification tank is arranged between the hydrolysis acidification tank and the first buffer tank; a discharge pump II arranged on the buffer tank I is arranged between the buffer tank I and the centrifugal dehydrator; and a discharge pump III arranged on the second buffer tank is arranged between the second buffer tank and the connecting anaerobic tank.
Preferably, the anaerobic tank is respectively provided with a pH detector, a second liquid level meter and a second temperature sensor.
Preferably, the anaerobic tank is also provided with a second gas analyzer and an ORP analyzer, and the anaerobic tank is also provided with a reflux pump and a fourth discharge pump.
Preferably, the hydrolysis acidification tank is a CSTR fermentation tank, and the anaerobic tank is a UASB anaerobic tank.
Another object of the present application is to provide a process for using the anaerobic fermentation device using ethanol as an intermediate product of kitchen waste, comprising the following steps:
conveying kitchen waste slurry to a hydrolysis acidification tank for hydrolysis acidification to obtain hydrolysis acidification liquid and a gas product, conveying the hydrolysis acidification liquid to a buffer tank I for precipitation and buffering to obtain buffered hydrolysis acidification liquid, conveying the buffered hydrolysis acidification liquid to a centrifugal dehydrator for dehydration to obtain centrifugal liquid and solid slag, conveying the centrifugal liquid to a buffer tank II for precipitation and buffering to obtain buffered centrifugal liquid, and conveying the buffered centrifugal liquid to an anaerobic tank for granular sludge culture to obtain liquid metabolites and gas metabolites.
Preferably, a reflux pump reflux the liquid metabolite into the anaerobic tank to adjust the pH of the anaerobic tank or to administer a medicament comprising sodium hydroxide and/or sodium bicarbonate to adjust the pH of the anaerobic tank.
Preferably, the total HRT of the materials in the hydrolytic acidification tank 1 and the anaerobic tank 14 is less than or equal to 7d.
Preferably, the TS of the kitchen waste slurry is 10-12%, the grain diameter is less than 10mm, the VS/TS is 82-85%, the sand impurity content is less than 1.0%, the pH is 5.0-6.0, and the SCOD of the liquid metabolite is 3515-4250 mg/L.
The beneficial effects of the utility model are as follows:
(1) Unlike conventional anaerobic fermentation apparatus, the present application combines the hydrolysis acidification tank 1 and the anaerobic tank 14, improves the process efficiency, and also cooperates with the reflux pump 20 to adjust the pH. The utility model provides a still set up heat transfer system, in hydrolysis acidification tank 1's non-advance, the time of ejection of compact, can start ejection of compact pump 7 with hydrolysis acidification tank 1 interior material transport heat transfer system 8, the material after the heat transfer is got back to hydrolysis acidification tank 1 again, this can realize hydrolysis acidification tank 1 interior constant temperature.
(2) pH, oxidation-reduction potential (ORP) and Hydraulic Retention Time (HRT) are key factors affecting the type of fermentation. The formation of the fermentation type can be directionally regulated and controlled by controlling the pH, a higher pH (more than 5.5) is favorable for Ding Suanxing and propionic acid type fermentation, and a lower pH (4.0-4.5) is favorable for the formation of ethanol type fermentation. The method is characterized in that the hydrolysis acidification tank 1 is controlled to have a pH value range of 4.0-4.5 and a residence time of 5d, so that ethanol type fermentation dominant flora is formed, and the main fermentation products are ethanol, acetic acid and lactic acid. In addition, the method has the advantages of less alkaline reagent, no alkaline reagent added if necessary, and good economy. The metabolic products of the hydrolysis acidification tank 1 are mainly ethanol, lactic acid and acetic acid, and the products are used as matrixes for methanation, so that methanation can be rapidly realized, and the efficiency of the methane production reactor is greatly improved. The gas products in the hydrolysis acidification process mainly comprise carbon dioxide, the contents of hydrogen and methane are almost 0, the gas utilization value generated by the hydrolysis acidification tank 1 in a CSTR form is high, the gas can be prevented from entering a rear-end deodorization system, and the deodorization investment cost and the operation cost are reduced. The organic load in the hydrolytic acidification stage can reach 8-10 kgVS/(m) 3 D) the methanogenic stage volume load was 24.3 gCOD/(L.d). The treatment efficiency of the two-phase anaerobic process is remarkably improved.
(3) The anaerobic tank 14 for efficiently producing the acid granular sludge under the low pH condition has high volumetric efficiency of the reactor and high yield of VFA substances. Wherein, the ethanol is neutral substance and can not cause the pH to drop, and the acetic acid can be directly utilized by methanogen of acetic acid. The generated gas has high methane content, high heat value and high subsequent available value, and can reduce the investment and the running cost of biogas purification. In addition, the COD removal rate of the anaerobic tank 14 is high, the difficulty of a rear-end sewage treatment system is reduced, and the energy consumption of the sewage treatment system is reduced.
(4) The high organic load and the short residence time can significantly reduce the tank volumes of the hydrolytic acidification tank 1 and the anaerobic tank 14, and significantly reduce the overall investment and the occupied area of engineering. Moreover, because the volumes of the hydrolysis acidification tank 1 and the anaerobic tank 14 are smaller, the power of the devices (such as a liquid level meter I2, a temperature sensor I3, a stirrer 4, a pressure sensor 5, a gas analyzer I6, a discharge pump I7, a heat exchange system 8, a pH detector 15, a liquid level meter II 16, a temperature sensor II 17, a gas analyzer II 18, an ORP analyzer 19 and a discharge pump IV 21) which are matched with each other can be correspondingly reduced, the running power consumption can be greatly reduced, and the running cost can be saved.
In summary, by controlling the environmental parameters, the intermediate products of the anaerobic acidogenic fermentation process (in the hydrolytic acidification tank 1) are converted from conventional butyric acid, propionic acid, acetic acid, valeric acid, etc. into ethanol, lactic acid. The change of the intermediate product can greatly improve the acid-producing fermentation efficiency and promote the acid-producing fermentation. Plus the rear anaerobic tank 14, methanation is enhanced. The method can also greatly shorten the residence time of the traditional anaerobic process, improve the organic load, reduce the process difficulty, reduce the cost, save the engineering cost and shorten the investment recovery period.
Drawings
The accompanying drawings are included to provide a further understanding of the utility model and are incorporated in and constitute a part of this specification, illustrate the utility model and together with the embodiments of the utility model, serve to explain the utility model. In the drawings:
FIG. 1 is a schematic view of the overall structure of the present utility model;
marked in the figure as: 1. a hydrolytic acidification tank; 2. a liquid level meter I; 3. a first temperature sensor; 4. a stirrer; 5. a pressure sensor; 6. a first gas analyzer; 7. a discharge pump I; 8. a heat exchange system; 9. a buffer pool I; 10. a second discharging pump; 11. a centrifugal dehydrator; 12. a buffer pool II; 13. a discharge pump III; 14. an anaerobic tank; a ph detector; 16. a second liquid level meter; 17. a second temperature sensor; 18. a second gas analyzer; orp analyzer; 20. a reflux pump; 21. and a discharging pump IV.
Detailed Description
The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
The equipment or materials used in the examples are readily available from commercial companies unless otherwise indicated. In water treatment, the following abbreviations are generic abbreviations, the specific meanings of which are not repeated herein:
TS: the total solids content of the product is,
VS: the volatile solid(s) present in the composition,
VFA(s) is a volatile fatty acid,
COD: the Chemical Oxygen Demand (COD) of the waste water,
HRT: hydraulic retention time.
The working principles of CSTR fermenters, settling tanks, UASB anaerobic tanks mentioned below are well known and will not be described in detail here.
Example 1
Referring to FIG. 1, an anaerobic fermentation apparatus using ethanol as intermediate of kitchen waste comprises a hydrolysis acidification tank 1, wherein the hydrolysis acidification tank 1 is preferably a CSTR fermentation tank, and the preferable volume of the CSTR fermentation tank is 1000m 3 The CSTR fermentation tank (1) is provided with an on-line instrument and an automatic control system, the top end of the hydrolysis acidification tank (1) is provided with a stirrer (4), the stirrer (4) penetrates into the hydrolysis acidification tank (1), the top end of the hydrolysis acidification tank (1) is also provided with a pressure sensor (5) and a gas analyzer (6) respectively, and the gas analyzer (6) is used for analyzing gas components obtained by hydrolysis acidification in the hydrolysis acidification tank (1). The pressure sensor 5 is used to detect the pressure in the hydrolytic acidification tank 1. The side of the hydrolysis acidification tank 1 is also provided with a liquid level meter I2 and a temperature sensor I3 respectively, wherein the liquid level meter I2 is used for monitoring the liquid level height in the hydrolysis acidification tank 1, and the temperature sensor I3 is used for monitoring the temperature in the hydrolysis acidification tank 1. The side of the hydrolysis acidification tank 1 is also connected with a first discharge pump 7, the first discharge pump 7 is connected with a first buffer tank 9, a pipeline between the first discharge pump 7 and the first buffer tank 9 is connected with one end of a heat exchange system 8, the other end of the heat exchange system 8 is connected with the hydrolysis acidification tank 1, the heat exchange system 8 is preferably a heat exchanger, the heat exchanger is preferably a double-pipe heat exchanger, and the cold source and the heat source of the heat exchanger are preferably external boiler hot water and cooling tower tap water respectively.
The buffer tank I9 is provided withThe stirring device is arranged, the buffer tank I9 is connected with the centrifugal dehydrator 11 through the discharge pump II 10, the centrifugal dehydrator 11 is preferably a two-phase centrifugal dehydrator, the centrifugal dehydrator 11 is connected with the buffer tank II 12, the height of the buffer tank II 12 is equal to that of the centrifugal dehydrator 11, the buffer tank II 12 is connected with the anaerobic tank 14 through the discharge pump III 13, the anaerobic tank 14 is preferably a UASB anaerobic tank, and the preferable volume of the UASB anaerobic tank is 400m 3 The UASB anaerobic tank of (1) is characterized in that a pH detector 15, a second liquid level meter 16 and a second temperature sensor 17 are respectively arranged on one side surface of the anaerobic tank 14, a second gas analyzer 18 is arranged at the top of the anaerobic tank 14, an ORP analyzer 19 and a reflux pump 20 connected with the ORP analyzer are respectively arranged on the other side surface of the anaerobic tank 14, and a fourth discharge pump 21 is also connected with the anaerobic tank 14.
Anaerobic tank 14 is also connected to an external three-phase separator.
The connection means pipeline connection, and pipeline connection is also adopted between the buffer tank I9 and the discharge pump II 10, and pipeline connection is also adopted between the buffer tank II 12 and the discharge pump III 13. The device without written effect is specifically elucidated in the following process and working principle.
The process performed by using the anaerobic fermentation device using ethanol as the intermediate product of the kitchen waste comprises the following steps:
s1, conveying kitchen waste slurry to a hydrolysis acidification tank 1 by an external conveying device (preferably a pump) for hydrolysis acidification, wherein the temperature value is detected by a first temperature sensor 3, the pressure in the hydrolysis acidification tank 1 is detected by a pressure sensor 5, the components of a gas product are detected and analyzed by a first gas analyzer 6, and the liquid level change in the hydrolysis acidification tank 1 is detected by a first liquid level meter 2.
The feeding conditions of the kitchen waste slurry are as follows: TS is 10-12%, grain diameter is less than 10mm, VS/TS is 82-85%, sand impurity content is less than 1.0%, pH is 5.0-6.0.
In addition, the carbohydrate, the protein and the fat are three organic components in the kitchen waste, after the kitchen waste is subjected to front-end sorting, crushing, impurity removal, sand removal and three-phase oil extraction, the rest components in the kitchen waste slurry entering the hydrolysis acidification tank 1 comprise at least one of the carbohydrate, the protein, the fat, the cellulose and the impurity, the main components are the carbohydrate and the protein, the carbohydrate (expressed by sugar in measurement) accounts for 47.2 percent, the protein accounts for 30.1 percent and the fat accounts for 3.2 percent based on dry weight.
The TCOD in the kitchen waste slurry is 160+/-3.0 g/kg, and the SCOD is 136+/-3.0 g/kg. The front-end pretreatment process comprises heating and oil extraction, so that the temperature of the fed kitchen waste slurry is 45 ℃.
The operator regulates and controls the parameters in the hydrolytic acidification tank 1 through the on-line instrument and the automatic control system of the hydrolytic acidification tank 1 to be: pH is 4.0-4.6, and the organic load is 8-10 kgVS/(m) 3 D), wherein the HRT is 5d on average, the temperature is constant at 35+/-1 ℃, and the kitchen waste slurry is stirred by adopting a mechanical stirring mode, specifically a stirrer 4.
After the kitchen waste slurry reacts in the hydrolysis acidification tank 1, hydrolysis acidification liquid and gas products are obtained, wherein the components of the hydrolysis acidification liquid comprise at least one of ethanol, acetic acid and lactic acid, the lactic acid is the most main metabolite, and the concentration is 8.1-15.5g/L; acetic acid concentration is 2.8+/-1.0 g/L; the concentration of ethanol is 1.2+/-0.6 g/L. The gaseous product comprising CO 2 、H 2 、CH 4 The content of carbon dioxide accounts for 98% of the total content of the gas, the gas can enter an external gas storage system from the side surface of the upper end of the hydrolysis acidification tank 1, and in addition, the gas collected by the external gas storage system can be used later only through a simpler purification process.
The number of times of the hydrolysis acidification tank 1 for evenly feeding and discharging every day is determined according to actual requirements, and preferably 8 times are selected.
The daily test hydrolysis acidification tank 1 index is as follows:
feeding: feed amount, TS, VS, pH.
In-can index: organic load, VFA, and component analysis, pH.
Gas index: CO 2 、H 2 、CH 4 The content is as follows.
The hydrolysis acidification tank 1 index was tested weekly as follows:
in-can index: TS, VS, COD.
And after the reaction of the kitchen waste slurry in the hydrolysis acidification tank 1 is finished, discharging is started, wherein TCOD and SCOD in the discharging are respectively 41.1+/-3.0 g/L and 27.2+/-3.0 g/L. And starting a discharge pump I7, and pumping the hydrolysis acidification liquid (namely discharging) in the hydrolysis acidification tank 1 into a buffer tank I9 by the discharge pump I7, and depositing and buffering the hydrolysis acidification liquid in the buffer tank I9 to obtain buffered hydrolysis acidification liquid.
In addition, in the time of non-feeding and discharging of the hydrolysis acidification tank 1, a discharging pump 7 can be started to convey the materials in the hydrolysis acidification tank 1 to a heat exchange system 8, and the materials after heat exchange return to the hydrolysis acidification tank 1 again, so that the constant temperature in the hydrolysis acidification tank 1 can be realized.
And starting a second discharging pump 10, conveying the buffered hydrolysis acidification liquid to a centrifugal dehydrator 11 for dehydration, and obtaining centrifugal liquid and solid slag under the action of centrifugal force, wherein the solid content of the solid slag is 20%, and the solid slag can be conveyed to the outside to be used as nutrient soil for subsequent use. SCOD in the centrifugate is 24.1+ -2.0 g/L, the centrifugate contains soluble organic matters, the soluble organic matters comprise VFA, the VFA comprises at least one of lactic acid, acetic acid and ethanol, and the concentration of lactic acid is 6.4-12.1g/L; acetic acid concentration is 2.2+/-1.0 g/L; the concentration of ethanol is 0.9+/-0.5 g/L.
After the reaction, the centrifugate enters a buffer tank II 12 through a pipeline to carry out precipitation buffer to obtain buffered centrifugate, then a discharge pump III 13 is started, the buffered centrifugate is conveyed to an anaerobic tank 14 to carry out granular sludge culture, the shape of the larger granular sludge is elliptic and/or short rod-shaped, the shape of the smaller sludge is spherical, and the color is mainly black gray. The flora in the granular sludge comprises at least one of cocci, bacilli and longbacilli and methanogens. Wherein, in methanogenic bacteria, methanogenic trendy bacteria Methanosaeta spp which takes acetic acid as a matrix to generate methane is taken as dominant bacterial colony in granular sludge, the abundance reaches 48.65 percent, and H is taken as 2 And CO 2 Methanolic and methanospiralum (methanospiralum) are present in relatively small abundance amounts, 15.3% and 5.34%, respectively, for the substrate to produce methanolic nutrition.
The pH value in the anaerobic tank 14 is detected by a pH detector, the temperature value is detected by a second temperature sensor 17, the components of the gas product are detected and analyzed by a second gas analyzer 18, and the comprehensive index of the oxidation-reduction state in the anaerobic tank 14 is detected and fed back by an ORP analyzer 19.
The buffered centrate had an HRT of 2d and a volume load of 24.3.+ -. 2.0 gCOD/(L.d) in the anaerobic tank 14. After the reaction is finished, obtaining liquid metabolite and gas metabolite, wherein the SCOD of the liquid metabolite is 3515-4250 mg/L, and the SCOD removal rate is 81-85%. The liquid metabolite comprises VFA, the VFA comprises at least one of lactic acid, acetic acid and propionic acid, and the propionic acid content is up to 350mg/L.
The gas metabolites comprise methane, the methane proportion in the methane is 70% -80%, and the average methane yield is 256ml/gCOD. The gas metabolites are collected by an external three-phase separator and can be continuously utilized after subsequent desulfurization treatment.
In the whole process, the total HRT of the materials in the hydrolysis acidification tank 1 and the anaerobic tank 14 is 7d, and the ORP is-236 mv to-239 mv in the hydrolysis acidification stage (in the hydrolysis acidification tank 1); in the methanogenic stage (within the anaerobic tank 14), ORP is from-287 mv to-293 mv.
When discharging is needed, the discharging pump IV 21 is started to discharge the liquid metabolite in the anaerobic tank 14 out of the anaerobic tank 14.
Example 2
Referring to fig. 1, an anaerobic fermentation apparatus and process using ethanol as an intermediate product of kitchen waste is different from that of embodiment 1, further, when the pH value in the anaerobic tank 14 needs to be adjusted, the reflux pump 20 is started to reflux the liquid metabolite into the anaerobic tank 14 to adjust the pH value or to add a medicament to adjust the alkalinity, wherein the medicament comprises sodium hydroxide and/or sodium bicarbonate. This allows control of the pH in the anaerobic tank 14 to 7.2-7.5. The remaining steps were the same as in example 1.
Example 3
An anaerobic fermentation device and process using ethanol as intermediate product of kitchen waste is different from the embodiment 1 and 2, further, according to the requirement, when the temperature is low, such as in winter, an operator can set a temperature supplementing device on a water inlet pipeline, preferably steam or hot water is used for supplementing the temperature, and the temperatures of the hydrolytic acidification tank 1 and the anaerobic tank 14 are maintained to be constant at 35+/-1 ℃. The remaining steps are the same as in example 1 or 2.
Comparative example 1
A traditional anaerobic fermentation device and process are basically the same as those in example 1 according to the traditional two-phase anaerobic engineering of producing acid phase products from butyric acid, propionic acid, acetic acid and valeric acid. Except that the hydrolysis stage (within hydrolytic acidification tank 1) does not artificially adjust the pH and the methanogenic stage uses a conventional CSTR process, i.e. the anaerobic tank 14 of example 1 is replaced by a CSTR anaerobic fermentation tank.
The performance of example 1 and comparative example 1 were compared, and the results are shown in table 1 below.
TABLE 1
Analysis of results: compared with the comparative example 1, namely, compared with the traditional technology, the product in the stage of the example 1 is different, the HRT time of the whole process can be shortened, the HRT of the comparative example 1 can reach 4.5 times of that of the example 1, and the organic load of the comparative example 1 is lower, so that the anaerobic fermentation efficiency is influenced, the gas production rate is reduced, and the operation cost of anaerobic fermentation is increased.
The foregoing description is only a preferred embodiment of the present utility model, and the present utility model is not limited thereto, but it is to be understood that modifications and equivalents of some of the technical features described in the foregoing embodiments may be made by those skilled in the art, although the present utility model has been described in detail with reference to the foregoing embodiments. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (7)
1. The anaerobic fermentation device taking ethanol as an intermediate product of kitchen waste is characterized by comprising a hydrolysis acidification tank (1), wherein the hydrolysis acidification tank (1) is connected with a centrifugal dehydrator (11) through a buffer tank I (9), and the centrifugal dehydrator (11) is connected with an anaerobic tank (14) through a buffer tank II (12).
2. The anaerobic fermentation device using ethanol as the intermediate product of kitchen waste according to claim 1, wherein the hydrolysis acidification tank (1) is respectively provided with a liquid level meter I (2), a temperature sensor I (3) and a stirrer (4).
3. The anaerobic fermentation device using ethanol as the intermediate product of kitchen waste according to claim 1, wherein the hydrolysis acidification tank (1) is further provided with a pressure sensor (5) and a gas analyzer I (6), and the hydrolysis acidification tank (1) is further connected with a heat exchange system (8).
4. The anaerobic fermentation device using ethanol as the intermediate product of kitchen waste according to claim 1, wherein a discharge pump I (7) arranged on the hydrolysis acidification tank (1) is arranged between the hydrolysis acidification tank (1) and the buffer tank I (9); a second discharging pump (10) arranged on the first buffering tank (9) is arranged between the first buffering tank (9) and the centrifugal dehydrator (11); a third discharging pump (13) arranged on the second buffer tank (12) is arranged between the second buffer tank (12) and the connecting anaerobic tank (14).
5. The anaerobic fermentation device using ethanol as the intermediate product of kitchen waste according to claim 1, wherein the anaerobic tank (14) is respectively provided with a pH detector (15), a second liquid level meter (16) and a second temperature sensor (17).
6. Anaerobic fermentation device with ethanol as intermediate product of kitchen waste according to claim 1, characterized in that the anaerobic tank (14) is provided with a second gas analyzer (18) and an ORP analyzer (19), respectively, and the anaerobic tank (14) is provided with a reflux pump (20) and a fourth discharge pump (21), respectively.
7. Anaerobic fermentation device with ethanol as intermediate product of kitchen waste according to claim 1, characterized in that the hydrolytic acidification tank (1) is a CSTR fermentation tank and the anaerobic tank (14) is a UASB anaerobic tank.
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