CN110835221A - Method for recovering energy of hydrothermal liquefied water phase component - Google Patents

Method for recovering energy of hydrothermal liquefied water phase component Download PDF

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CN110835221A
CN110835221A CN201911215841.3A CN201911215841A CN110835221A CN 110835221 A CN110835221 A CN 110835221A CN 201911215841 A CN201911215841 A CN 201911215841A CN 110835221 A CN110835221 A CN 110835221A
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sludge
cod
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CN110835221B (en
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李岩
华栋梁
范庆文
许海朋
赵玉晓
陈雷
赵保峰
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Energy Research Institute of Shandong Academy of Sciences
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/18—Treatment of sludge; Devices therefor by thermal conditioning
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/006—Electrochemical treatment, e.g. electro-oxidation or electro-osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
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    • C02F11/04—Anaerobic treatment; Production of methane by such processes

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Abstract

A method for recovering energy of hydrothermal liquefied water phase components is characterized by comprising the following steps: (1) carrying out hydrothermal liquefaction treatment on the sludge; placing the residual sludge of a secondary sedimentation tank of a municipal sewage treatment plant with the water content of 80% in a high-pressure reaction kettle, sealing, heating to 300 ℃, keeping for 30min, cooling, taking out, standing, and taking a water phase, namely hydrothermal liquefaction wastewater for later use; (2) diluted to 2625 mg COD/L and 5250 mg COD/L; (3) three-dimensional iron-carbon electrolysis technology; after pretreatment of an electrolysis system, standing to remove active carbon and residual iron powder, and taking upper-layer liquid for later use; (4) methane production: a, acclimating anaerobic granular sludge; b, adopting an upflow anaerobic sludge bed as a methanogenesis reaction device, placing the domesticated anaerobic granular sludge in the methanogenesis reaction device, generating acetic acid, hydrogen and carbon dioxide under the action of acid-producing bacteria, and then carrying out methanogenesis reaction.

Description

Method for recovering energy of hydrothermal liquefied water phase component
Technical Field
The invention relates to a comprehensive utilization method of a hydrothermal liquefied aqueous phase component, in particular to a method for recovering energy of the hydrothermal liquefied aqueous phase component.
Background
Sludge is often overlooked as a "by-product" of sewage treatment, and if not properly disposed of, secondary environmental pollution can result. Thus. How to effectively treat, dispose and utilize the sludge is an urgent problem to be solved in the current sewage treatment plant. The water content of the sludge can reach more than 80 percent. The components are complex, the pollutants are various, and the content of organic matters is high (accounting for 60-70% of dry matters).
In recent years, hydrothermal liquefaction has received widespread attention as one of the most promising green and environmentally friendly technologies and has become a research hotspot. The hydrothermal liquefaction refers to a process of converting biomass into liquid bio-oil at a certain temperature and pressure in subcritical/supercritical water, and the technology has many advantages, such as no need of drying raw materials, omission of a pretreatment link of sludge dehydration and reduction of liquefaction cost; the boiling point of water can be increased under the pressure of the external gas, which is beneficial to the hydrolysis of the biomass macromolecular organic matters and further saves heat energy; the product is convenient to separate. The direct discharge of the water phase part generated in the hydrothermal liquefaction process can cause secondary pollution to the environment, and no patent on the aspect of energy utilization of the hydrothermal liquefaction water phase components is found.
Disclosure of Invention
The invention mainly aims to provide a method for recovering energy of hydrothermal liquefied water phase components, so as to improve organic load, gas production stability and energy recovery and realize energy utilization of the hydrothermal liquefied water phase.
In order to realize the purpose, the invention is realized by the following technical scheme: a method for recovering energy of hydrothermal liquefied water phase components comprises the following steps:
(1) hydrothermal liquefaction treatment of sludge
Placing the residual sludge of the secondary sedimentation tank of the municipal sewage treatment plant with the water content of 80% in a high-pressure reaction kettle, sealing, heating to 300 ℃, keeping for 30min, cooling, taking out, and standing to obtain a water phase (hydrothermal liquefaction wastewater) for later use.
(2) Dilution of
The experimental sludge hydrothermal liquefaction wastewater is a product obtained by subjecting excess sludge to hydrothermal liquefaction treatment, wherein the concentration of organic acid is 3256 mg/L, the organic acid mainly contains acetic acid, propionic acid, butyric acid, valeric acid and the like, and the COD in the water phase is 10500 mg COD/L.
Diluting the hydrothermal liquefaction wastewater to different concentrations (2625 mg COD/L and 5250 mg COD/L), observing the methane production condition of the hydrothermal liquefaction wastewater with different concentrations, determining the gas production inhibition effect and the corresponding concentration according to the fermentation result, and taking the concentration as the research object of the electrolysis experiment.
(3) Three-dimensional iron carbon electrolysis technology.
The three-dimensional electrolytic system selects a stainless steel electrode as an anode material, a graphite electrode as a cathode material and columnar activated carbon and iron powder as diffusion electrodes. The direct current voltage stabilizer provides a stable direct current power supply for the electrolysis system. Adding the hydrothermal liquefied wastewater with the concentration generating the inhibiting effect in the step (1) into a reaction tank, controlling the electrolysis degree by controlling parameters such as voltage, electrolysis time, iron-carbon ratio and the like, wherein the voltage range is 0-20V, the treatment time is 30-120 min, the iron-carbon addition amount is 20-60 g/L, and the iron-carbon ratio is 1:2 to 2: 1. after the pretreatment of the electrolysis system, standing to remove the active carbon and the residual iron powder, and taking the upper liquid for later use.
(4) Methane production
a, anaerobic granular sludge domestication: the inoculum adopts granular sludge, the total solid matter content of which is 9.92 percent, and the volatile solid matter content of which is 72.5 percent; the granular sludge is taken from a great water-supply anaerobic fermentation tank in the Minnan province and is used as an anaerobic fermentation inoculum.
b, adopting an up-flow anaerobic sludge bed (UASB) as a methanogenesis reaction device, placing the domesticated anaerobic granular sludge into the methanogenesis reaction device, and standing the domesticated anaerobic granular sludge to be about half of the total volume of the methanogenesis reaction device. Taking out the treatment liquid obtained in the step (2), standing and layering to remove active carbon and residual iron, wherein the liquid part mainly comprises short carbon chain organic acids such as acetic acid, propionic acid and butyric acid and micromolecule organic matters generated after electrolysis, adjusting the pH value, then feeding the short carbon chain organic acids into UASB (upflow anaerobic sludge blanket), generating acetic acid, hydrogen and carbon dioxide under the action of acid-producing bacteria by the organic acids such as acetic acid, propionic acid and butyric acid in a methanogenesis reaction device, and then carrying out methanogenesis reaction. The pH value of the liquid phase after three-dimensional iron carbon electrolysis needs to be adjusted to 7.0 before entering UASB, and the requirement of pH value can be basically met.
The scheme is characterized in that the effluent in the UASB reactor is used for adjusting and diluting the hydrothermal liquefaction wastewater. The concentration of organic matters in the hydrothermal liquefaction wastewater is changed through dilution, so that the feed load of the UASB is adjusted.
The diameter of the columnar active carbon is 1.5 mm, the packing density is less than or equal to 550 g/L, and the iodine value is more than or equal to 600 mg/g. The grain sizes of the high-purity iron powder with different specifications are respectively 40 meshes, 100 meshes and 200 meshes.
In order to better improve the utilization capacity of the granular sludge on organic matters, the granular sludge is domesticated by adopting a prepared acetic acid solution, and the formula is as follows: sodium acetate is used as carbon source (2000 mg COD/L), and NH is respectively used as nitrogen source and phosphorus source4Cl and KH2PO4Provided that the COD is N: P =200:5:1, and the other trace element formulations are as shown in the table below.
The other nutrient elements for domesticating the granular sludge comprise (mg/L), and the adding proportion is 1gCOD/mL trace elements.
Figure 100002_DEST_PATH_IMAGE001
The invention has the beneficial effects that: (1) the content of organic acid and the concentration of COD in the sludge hydrothermal liquefaction wastewater are much lower than those of pyroligneous liquor, and the proportion of the organic acid in the COD is about 35 percent, which shows that the content of biochemically usable substances is less, and the concentration of inhibitory substances in the pyroligneous liquor after dilution is relatively less than that of the organic acid, so that the loss of the organic acid is required to be reduced as much as possible during the electrolytic pretreatment, and in order to ensure the smooth proceeding of the anaerobic fermentation process in the hydrothermal liquefaction wastewater, the contained inhibitory substances are required to be subjected to a large degree of electrolytic treatment, so as to realize the ring opening, the fracture and the like of difficultly degraded components, so as to improve the biochemically usable property and the energy recovery rate of the materials as the final targets, the loss of the organic acid is ignored, and thus the anaerobic conversion efficiency of the components under the. Tong (Chinese character of 'tong')Through the dilution with different multiples and the control on main parameters in the three-dimensional electrolytic pretreatment process, the removal rate of COD after the treatment is 18 percent and is lower than that in the normal electrolytic operation process. (2) Fe and C are selected as micro-electrolysis electrode materials, particularly suitable for being combined with the anaerobic fermentation process, and the upper layer liquid obtained by standing after three-dimensional electrolysis treatment contains Fe2+And a small amount of suspended C powder, Fe2+The activated carbon can be used as a carrier for directly transferring electrons between inoculations to improve the conversion efficiency and the gas yield of acid, and the adsorption performance of the activated carbon can act on a small amount of residual toxic substances to reduce the negative effect on microorganisms, so that the methane yield can be improved by 326.9% at most compared with a control group without electrolysis treatment. (3) The hydrothermal liquefaction wastewater treated by UASB can be used as dilution water, so that the addition of external water sources can be reduced, meanwhile, secondary treatment is carried out on organic matters which are not completely degraded, and the degradation degree and the gas yield of substrates are improved.
Detailed Description
Example 1: the batch toxicity test of the hydrothermal liquefaction wastewater with different loads comprises the following steps:
(1) hydrothermal liquefaction treatment of sludge
Placing the residual sludge of the secondary sedimentation tank of the municipal sewage treatment plant with the water content of 80% in a high-pressure reaction kettle, sealing, heating to 300 ℃, keeping for 30min, cooling, taking out, and standing to obtain a water phase (hydrothermal liquefaction wastewater) for later use.
(2) And (5) diluting the wastewater.
Diluting the sludge hydrothermal liquefaction wastewater by 2 times and 4 times with tap water respectively to obtain fermentation raw materials with initial COD loads of 5250 mg/L and 2625 mg/L.
(3) And (5) anaerobic fermentation.
400ml of hydrothermal liquefaction wastewater with different concentrations is put into an anaerobic reaction bottle. Granular sludge is inoculated into the anaerobic bottle to ensure that the anaerobic reaction system is more than 20 gVS/L. Adding trace elements and NaHCO according to the COD concentration of the solution to be treated3. The nitrogen source and the phosphorus source are respectively composed of NH4Cl and KH2PO4The additive is added according to the mass ratio of COD to N to P =200 to 5 to 1. NaHCO 23Mainly as a pH buffer, was added at 5 g/g COD. The pH was adjusted to around 7 with HCl and NaOH. Blowing off the headspace for 3min by nitrogen, adding a rubber pad for sealing to ensure a closed anaerobic environment in the reaction bottle, fermenting at constant temperature in a 38 ℃ water bath kettle, shaking up every 5h to ensure that the substrate is uniformly contacted with the granular sludge. Biogas is collected every day and the volume and composition of the gas are measured. The pH in the batch reactor was monitored to ensure proper pH in the fermentation environment.
As a result, the cumulative methane yields at 2625 mg COD/L and 5250 mg COD/L of the hydrothermal liquefaction wastewater were 89.6 mL/g COD and 45.7 mL/g COD, respectively. The inhibition effect is obvious under the condition of the concentration.
Example 2: pretreatment of hydrothermal liquefaction wastewater by using three-dimensional iron-carbon electrolysis technology and using zero-valent iron with different particle sizes
A method for recovering energy of hydrothermal liquefied water phase components comprises the following steps:
(1) hydrothermal liquefaction treatment of sludge
Placing municipal sludge with the water content of 80% in a high-pressure reaction kettle, sealing, heating to 300 ℃, keeping for 30min, cooling, taking out, and standing to obtain a water phase (hydrothermal liquefaction wastewater) for later use.
(2) And (5) diluting the wastewater.
The sludge hydrothermal liquefaction wastewater diluted 2 times and having a concentration of 5250 mg COD/L was selected as a study object.
(3) Three-dimensional iron carbon electrolysis technology.
And adding uniformly mixed columnar activated carbon and iron powder into the reaction tank to serve as a granular electrode. Adding iron-carbon filler according to 40 g/L, wherein the weight ratio of Fe: c =1: 2. The particle sizes of the iron powder for experiments are 40 meshes, 100 meshes and 200 meshes respectively. The anode material is a stainless steel electrode, and the cathode material is a graphite electrode. The direct current voltage stabilizer provides a stable direct current power supply for the electrolysis system. 5250 mg of COD/L hydrothermal liquefied wastewater is added into a reaction tank, and the hydrothermal liquefied wastewater is treated under the conditions of 5V of voltage, 60min of electrolysis and stirring. After pretreatment by an electrolysis system, standing to remove the active carbon and the residual iron powder, and taking the upper liquid for later use.
(4) Methane production
a, acclimating anaerobic granular sludge.
In order to better improve the utilization capacity of the granular sludge to organic acid, the prepared acetic acid solution is adopted to acclimate the sludge, and the formula is as follows: sodium acetate is used as carbon source (2000 mg COD/L), nitrogen and phosphorus are respectively NaNO3And KH2PO4Provided that the COD is N: P =200:5:1, and the other trace element formulations are as shown in the table below.
The other nutrient elements for domesticating the granular sludge comprise (mg/L), and the adding proportion is 1g COD/mL trace elements.
b: an Upflow Anaerobic Sludge Blanket (UASB) is used as a methane production reaction device, and the domesticated anaerobic granular sludge is placed in a reactor and is added to stand to account for about half of the total volume of the reactor. And (3) taking the treatment liquid obtained in the step (2) out, standing and layering to remove activated carbon and residual iron, wherein the liquid part mainly comprises short carbon chain organic acids such as acetic acid, propionic acid and butyric acid and micromolecular organic matters generated after electrolysis, the short carbon chain organic acids are fed into UASB after pH adjustment, the organic acids such as acetic acid, propionic acid and butyric acid generate acetic acid, hydrogen and carbon dioxide under the action of acid-producing bacteria in a methanogenesis reactor, and then methanogenesis reaction is carried out. After the iron powder with different particle sizes (40 meshes, 100 meshes and 200 meshes) is pretreated by the three-dimensional electrolysis technology, the cumulative methane yield respectively reaches 124.1 mL/g COD, 147.3 mL/g COD and 173.5 mL/g COD, and is improved by 326.9 percent compared with a control group which is not subjected to electrolysis treatment and has the load of 5250 mg COD/L in example 1.
Example 3: the same parts of this embodiment as embodiment 2 will not be described again, but the differences are: comparison of gas evolution under different Filler amount electrolytic conditions
The operating conditions of micro-electrolysis in example 2 were changed to 20 g/L filler addition and 100 mesh iron powder particle size. The electrolysis and fermentation conditions were the same as in example 2, and the anaerobic fermentation results showed a lower methane yield of 113.5 mL/g COD compared to a 40 g/L filler ratio.
Example 4: the same parts of this embodiment as embodiment 2 will not be described again, but the differences are: comparison of gas evolution under different Filler amount electrolytic conditions
The operating conditions of micro-electrolysis in the embodiment 2 are changed into that the adding amount of the filler is 60 g/L, and the particle size of the iron powder is 100 meshes. The electrolysis and fermentation conditions were the same as in example 2, and the anaerobic fermentation results showed a lower methane yield of 113.5 mL/g COD compared to a 40 g/L filler ratio.
Example 5: the same parts of this embodiment as embodiment 2 will not be described again, but the differences are: comparison of gas evolution under different Fe/C ratio electrolysis conditions
The operating conditions for the microelectrolysis in example 2 were changed to Fe: c =1:1, and the particle size of the iron powder is 100 meshes. The rest of the operation is the same as that of the example 2, and the gas production result shows that the ratio of Fe: the yield of C at 1:2 was low compared to methane and was 117.2 mL/g COD.
Example 6: the same parts of this embodiment as embodiment 2 will not be described again, but the differences are: comparison of gas evolution under different Fe/C ratio electrolysis conditions
The operating conditions for the microelectrolysis in example 2 were changed to Fe: c =2:1, and the particle size of the iron powder is 100 meshes. The rest of the operation is the same as that of the example 2, and the gas production result shows that the ratio of Fe: the yield of C at 1:2 was lower than that of methane, 96.9 mL/g COD.
Example 7: the same parts of this embodiment as embodiment 2 will not be described again, but the differences are: comparison of gas evolution under different Voltage Electrolysis conditions
The operating conditions of the micro-electrolysis in example 2 were changed to a voltage of 3V, and the particle size of the iron powder was 100 mesh. The remaining operating conditions were the same as in example 2. The gas production results showed that the methane yield was lower than that at a voltage of 5v, 88.2 mL/g COD.
Example 8: the same parts of this embodiment as embodiment 2 will not be described again, but the differences are: comparison of gas evolution under different Voltage Electrolysis conditions
The operating conditions of the micro-electrolysis in example 2 were changed to a voltage of 10V, and the particle size of the iron powder was 100 mesh. The remaining operating conditions were the same as in example 2. The gas production results showed that the methane yield was lower than that at a voltage of 5v, and was 136.3 mL/g COD.
Example 9: the same parts of this embodiment as embodiment 2 will not be described again, but the differences are: comparison of gas evolution under different Voltage Electrolysis conditions
The operating conditions of the micro-electrolysis in example 2 were changed to a voltage of 20V, and the particle size of the iron powder was 100 mesh. The remaining operating conditions were the same as in example 2, and the gas evolution results showed a lower methane yield of 80.7 mL/g COD than at a voltage of 5 v.
Example 10: the same parts of this embodiment as embodiment 2 will not be described again, but the differences are: comparison of gas evolution at different electrolysis times
The micro-electrolysis operation condition in the example 2 is changed into micro-electrolysis treatment time of 30min, and the particle size of the iron powder is 100 meshes. The rest of the operation was the same as that of example 2, and the gas production result showed that the methane yield was 127.9 mL/gCOD, which was lower than that at an electrolysis time of 60 min.
Example 11: the same parts of this embodiment as embodiment 2 will not be described again, but the differences are: comparison of gas evolution at different electrolysis times
The micro-electrolysis operation condition in the embodiment 2 is changed into micro-electrolysis treatment time of 90min, and the particle size of the iron powder is 100 meshes. The rest of the operation was the same as that of example 2, and the gas production result showed that the methane yield was 195.1 mL/gCOD, which was higher than that at an electrolysis time of 60 min.
Example 12: the same parts of this embodiment as embodiment 2 will not be described again, but the differences are: comparison of gas evolution at different electrolysis times
The three-dimensional electrolysis operation condition in example 2 was changed to 120min, and the particle size of the iron powder was 100 mesh. The rest of the operation was the same as that of example 2, and the gas production result showed a lower methane yield of 112.7 mL/gCOD than that obtained when the electrolysis time was 60 min.
Example 13: the same parts of this embodiment as embodiment 2 will not be described again, but the differences are: experiment of promoting effect of Fe and C on anaerobic fermentation
The particle size of the iron powder is selected to be 100 meshes, and the rest of the electrolysis and fermentation operation steps are the same as those of the example 2, and the difference is that: the liquid obtained after the three-dimensional electrolytic pretreatment in the embodiment 2 is subjected to carbon removal and iron removal treatment, and the method comprises the following specific steps: (1) the insoluble carbon was removed by centrifugation at 10000 rpm. (2) The precipitate was removed by centrifugation after adjusting the pH to 10. The fermentation gas production result shows that the yield of the accumulated methane after carbon removal and iron removal is 121.3 mL/g COD, and compared with the 100-mesh iron powder electrolytic treatment in the example 2, the yield of the methane is reduced by 17.6 percent.
Example 14: comparison of three-dimensional iron-carbon Electrolysis techniques
Through literature research, under the optimal condition, the COD removal rate reaches 72.3 percent and most of COD is removed in the berberine waste water treated by the three-dimensional electrode-iron carbon micro-electrolysis combined process. If macromolecular compounds in the hydrothermal liquefaction wastewater are completely degraded, the final product is CO2And H2O and COD can be obviously changed, the COD removal rate before and after electrolysis is 15% under the conditions that the voltage is 5V, the filler is 40 g/L, Fe/C is 1:2 and the electrolysis is carried out for 90min through the implementation of controllable three-dimensional electrolysis, the treatment effect is greatly different from that in the literature, the removal rate can indicate that macromolecular substances are not fully degraded, the degradation degree is effectively controlled, and the methane yield can reach 147.3 mL/g COD at most from the aspect of gas production rate.

Claims (4)

1. A method for recovering energy of hydrothermal liquefied water phase components is characterized by comprising the following steps:
(1) hydrothermal liquefaction treatment of sludge
Placing the residual sludge of a secondary sedimentation tank of a municipal sewage treatment plant with the water content of 80% in a high-pressure reaction kettle, sealing, heating to 300 ℃, keeping for 30min, cooling, taking out, standing, and taking a water phase, namely hydrothermal liquefaction wastewater for later use;
(2) dilution of
Diluting the hydrothermal liquefaction wastewater to different concentrations, namely 2625 mg COD/L and 5250 mg COD/L;
(3) three-dimensional iron-carbon electrolysis technology;
the three-dimensional electrolytic system selects a stainless steel electrode as an anode material, a graphite electrode as a cathode material, and columnar activated carbon and iron powder as diffusion electrodes; the direct current voltage stabilizer provides a stable direct current power supply for the electrolysis system; adding the hydrothermal liquefaction wastewater with the concentration generating the inhibiting effect in the step (1) into a reaction tank, controlling the electrolysis degree by controlling the voltage, the electrolysis time and the iron-carbon ratio, wherein the voltage range is 0-20V, the treatment time is 30-120 min, the iron-carbon addition amount is 20-60 g/L, and the iron-carbon ratio is 1:2 to 2: 1; after pretreatment of an electrolysis system, standing to remove active carbon and residual iron powder, and taking upper-layer liquid for later use;
(4) methane production
a, anaerobic granular sludge domestication: the inoculum adopts granular sludge, the total solid matter content of which is 9.92 percent, and the volatile solid matter content of which is 72.5 percent;
b, taking an upflow anaerobic sludge blanket as a methanogenesis reaction device, placing the domesticated anaerobic granular sludge into the methanogenesis reaction device, and standing the domesticated anaerobic granular sludge to be about half of the total volume of the methanogenesis reaction device; taking out the treatment liquid obtained in the step (2), standing and layering to remove activated carbon and residual iron, adjusting the pH value, then feeding into an upflow anaerobic sludge blanket, generating acetic acid, hydrogen and carbon dioxide by organic acid in a methane-generating reaction device under the action of acid-producing bacteria, and then carrying out methane-generating reaction; the pH value of the liquid phase after three-dimensional iron carbon electrolysis before entering an upflow anaerobic sludge blanket needs to be adjusted to 7.0.
2. The method for energy recovery of a hydrothermally liquefied aqueous phase component of claim 1, wherein the effluent from the upflow anaerobic sludge blanket is used to condition dilute the hydrothermally liquefied wastewater.
3. The method for recovering energy of the hydrothermal liquefied water phase components as claimed in claim 1, wherein the diameter of the columnar activated carbon is 1.5 mm, the packing density is less than or equal to 550 g/L, and the iodine value is more than or equal to 600 mg/g.
4. The method for recovering energy of the hydrothermal liquefied aqueous phase component as claimed in claim 1, wherein the granular sludge is acclimated by using a prepared acetic acid solution, and the formula is as follows: sodium acetate is used as carbon source (2000 mg COD/L), and NH is respectively used as nitrogen source and phosphorus source4Cl and KH2PO4Provided that the COD is N: P =200:5:1, and the other trace element formulas are shown in the table below;
the other nutrient elements for domesticating the granular sludge comprise (mg/L), and the adding proportion is 1g COD/mL trace elements.
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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103555566A (en) * 2013-11-14 2014-02-05 大连理工大学 Novel external electrolysis device for promoting anaerobic digestion to produce methane
CN104355512A (en) * 2014-10-29 2015-02-18 同济大学 Subcritical hydrothermal treatment-based efficient recycling treatment process for sludge
CN106882885A (en) * 2017-03-07 2017-06-23 南昌大学 A kind of three-diemsnional electrode couples iron-carbon micro-electrolysis sewage treatment process
CN107522375A (en) * 2017-08-22 2017-12-29 华南理工大学 A kind of method that Zero-valent Iron and activated carbon strengthen excess sludge anaerobic digestion methane phase
US20190263700A1 (en) * 2016-10-27 2019-08-29 The University Of Western Ontario Hydrothermal liquefaction co-processing of wastewater sludge and lignocellulosic biomass for co-production of bio-gas and bio-oils
CN110295201A (en) * 2019-06-26 2019-10-01 山东省科学院能源研究所 The method that ligno-cellulose hydrolysate prepares biogas

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103555566A (en) * 2013-11-14 2014-02-05 大连理工大学 Novel external electrolysis device for promoting anaerobic digestion to produce methane
CN104355512A (en) * 2014-10-29 2015-02-18 同济大学 Subcritical hydrothermal treatment-based efficient recycling treatment process for sludge
US20190263700A1 (en) * 2016-10-27 2019-08-29 The University Of Western Ontario Hydrothermal liquefaction co-processing of wastewater sludge and lignocellulosic biomass for co-production of bio-gas and bio-oils
CN106882885A (en) * 2017-03-07 2017-06-23 南昌大学 A kind of three-diemsnional electrode couples iron-carbon micro-electrolysis sewage treatment process
CN107522375A (en) * 2017-08-22 2017-12-29 华南理工大学 A kind of method that Zero-valent Iron and activated carbon strengthen excess sludge anaerobic digestion methane phase
CN110295201A (en) * 2019-06-26 2019-10-01 山东省科学院能源研究所 The method that ligno-cellulose hydrolysate prepares biogas

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