CN102515454A - Device and method for realizing thermal-hydrolysis fermentation treatment in rotation way - Google Patents
Device and method for realizing thermal-hydrolysis fermentation treatment in rotation way Download PDFInfo
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- 238000009283 thermal hydrolysis Methods 0.000 title claims abstract description 119
- 238000000855 fermentation Methods 0.000 title claims abstract description 47
- 230000004151 fermentation Effects 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 40
- 239000002028 Biomass Substances 0.000 claims abstract description 106
- 239000002994 raw material Substances 0.000 claims abstract description 52
- 230000001079 digestive effect Effects 0.000 claims abstract description 26
- 235000011389 fruit/vegetable juice Nutrition 0.000 claims abstract description 23
- 238000001704 evaporation Methods 0.000 claims abstract description 20
- 230000008020 evaporation Effects 0.000 claims abstract description 20
- 239000000203 mixture Substances 0.000 claims abstract description 19
- 238000002156 mixing Methods 0.000 claims abstract description 12
- 239000002893 slag Substances 0.000 claims abstract description 5
- 239000000463 material Substances 0.000 claims description 49
- 230000029087 digestion Effects 0.000 claims description 27
- 238000006243 chemical reaction Methods 0.000 claims description 26
- 238000001816 cooling Methods 0.000 claims description 17
- 238000007599 discharging Methods 0.000 claims description 16
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 14
- 239000000498 cooling water Substances 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 5
- 230000007062 hydrolysis Effects 0.000 claims description 5
- 238000006460 hydrolysis reaction Methods 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 5
- 230000003301 hydrolyzing effect Effects 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000010586 diagram Methods 0.000 description 10
- 239000010802 sludge Substances 0.000 description 10
- 230000008569 process Effects 0.000 description 9
- 239000000243 solution Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000008676 import Effects 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 244000052616 bacterial pathogen Species 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
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- 238000004134 energy conservation Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000383 hazardous chemical Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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Abstract
The invention provides a device and a method for realizing thermal-hydrolysis fermentation treatment in a rotation way. The device provided by the invention comprises a preheating unit, a rotary thermal-hydrolysis unit and a mixing fermentation unit. The method provided by the invention comprises the following steps that 1, an organic biomass raw material is preheated by flash-off steam in a preheating tank until a temperature of the organic biomass raw material is less than or equal to 105 DEG C, and then is orderly fed into all rotary thermal-hydrolysis reactors; 2, orderly through all the rotary thermal-hydrolysis reactors, the preheated organic biomass raw material is mixed with high pressure steam in a rotation way and is subjected to thermal hydrolysis; 3, organic biomass obtained by the thermal hydrolysis is subjected to flash evaporation in a flash evaporation tank; and 4, a digestive juice and the organic biomass subjected to flash evaporation are mixed and cooled and the cooled mixture is further cooled by a heat exchanger, wherein the organic biomass subjected to flash evaporation is digested by the digestive juice and produces biogas and slag. The device and the method provided by the invention have the characteristics of high heat exchange efficiency, short thermal-hydrolysis period and low energy consumption, and can be widely utilized for the field of organic biomass treatment.
Description
Technical Field
The invention relates to a pyrohydrolysis technology, in particular to a device and a method for realizing pyrohydrolysis fermentation treatment by adopting a rotation mode.
Background
At present, the dry weight of sludge discharged by sewage treatment plants in China per year is about 140 ten thousand tons, and the dry weight is increased by more than 10% per year; moreover, the sludge contains a large amount of harmful substances such as heavy metals, pathogenic bacteria and the like, so that the sludge has great harm to the environment; therefore, the problem of environmental pollution caused by sludge is increasingly prominent, and great potential safety hazards, environmental hazards and economic burden are caused to the society. The thermal hydrolysis digestion treatment process is a treatment technology for reducing, recycling, stabilizing and safening sludge. The thermal hydrolysis reactor is the core and key equipment of the sludge thermal hydrolysis-anaerobic digestion system, and determines the effect of the produced methane and the energy consumption of the whole sludge treatment device. At present, the existing pyrohydrolysis reactors in China can be generally classified into two types: one is a high-pressure reaction kettle adopting a stirring mode, which comprises a reaction vessel, a stirrer, a transmission device, a cooling device, a safety device, a heating furnace and the like; the other is that the tubular continuous thermal hydrolysis reactor comprises feeding equipment, modification equipment, dehydration equipment, heat exchange equipment and purification equipment, adopts a catalyst injection mode, adopts medium-pressure steam to directly heat the sludge, and carries out thermal hydrolysis under the medium-temperature condition.
Therefore, in the prior art, the hot hydrolysis fermentation treatment technology has the problems of low heat exchange efficiency in unit time or unit energy consumption, long hot hydrolysis period, high energy consumption and the like.
Disclosure of Invention
In view of the above, the main objective of the present invention is to provide a device and a method for implementing thermal hydrolysis fermentation treatment by using a rotary method, which have the advantages of high heat exchange efficiency, short thermal hydrolysis period, energy saving and consumption reduction.
In order to achieve the purpose, the device for realizing the hot hydrolysis fermentation treatment by adopting the rotary mode comprises a preheating unit for preheating an externally input organic biomass raw material by adopting flash steam from the rotary thermal hydrolysis unit, a rotary thermal hydrolysis unit for sequentially carrying out thermal hydrolysis and flash evaporation after mixing externally input high-pressure steam with the preheated organic biomass raw material input by the preheating unit by adopting the rotary mode, and a mixed fermentation unit for sequentially carrying out cooling and digestion after mixing the organic biomass obtained by flash evaporation with a digestive juice to obtain biogas and residues; the rotary thermal hydrolysis unit comprises one or more rotary thermal hydrolysis reactors which carry out thermal hydrolysis after high-pressure steam input from the outside exchanges heat with the organic biomass raw material input from the preheating unit in a rotary mode, and one or more flash tanks which are connected in series and used for carrying out flash evaporation on the organic biomass obtained by thermal hydrolysis; the material inlet of each rotary pyrohydrolysis reactor is connected to the material outlet of the preheating unit through a pipeline, the high-pressure steam inlet of each rotary pyrohydrolysis reactor is connected to the outside through a pipeline, each rotary pyrohydrolysis reactor comprises a pressure-release steam inlet and a pressure-release steam outlet, the pressure-release steam inlet of each rotary pyrohydrolysis reactor is connected with the pressure-release steam outlets of other rotary pyrohydrolysis reactors through pipelines, the pressure-release steam outlet of each rotary pyrohydrolysis reactor is connected with the pressure-release steam inlets of other rotary pyrohydrolysis reactors through pipelines, and the material outlet of each rotary pyrohydrolysis reactor is connected to the material inlet of a first flash tank connected in series through a pipeline; in the flash tanks connected in series, the material outlet of the previous flash tank is connected with the material inlet of the next flash tank, and the material outlet of the last flash tank is connected with the material inlet of the mixed fermentation unit; the flash steam outlet of each flash tank is connected by a conduit to the flash steam inlet of the preheating unit.
In order to achieve the purpose, the method for realizing the thermal hydrolysis fermentation treatment by adopting the rotation mode comprises the following steps:
step 1, preheating an externally input organic biomass raw material to a temperature of less than or equal to 105 ℃ by flash steam from a preheating tank, and then sequentially inputting the organic biomass raw material into each rotary thermal hydrolysis reactor.
Step 2, the rotary pyrohydrolysis reactor which just completes pyrohydrolysis outputs the pressure relief steam generated by pyrohydrolysis to the rotary pyrohydrolysis reactor which is used for inputting the preheated organic biomass raw material; after the rotary thermal hydrolysis reactors complete feeding, the preheated organic biomass raw material and high-pressure steam from the outside are mixed in a rotary mode in sequence and then subjected to thermal hydrolysis.
Step 3, carrying out flash evaporation on the organic biomass obtained after thermal hydrolysis by using a flash evaporation tank; if the pressure of the flash steam generated by flashing is less than the internal pressure of the preheating tank, the pressure of the flash steam is pressurized to be greater than the internal pressure of the preheating tank by a jet pump, and the pressurized flash steam is returned to the step 1; if the pressure of the flash steam generated by flashing is larger than the internal pressure of the preheating tank, directly returning the flash steam to the step 1; step 4 is performed on the flashed organic biomass.
Step 4, mixing and cooling the digestive juice and the organic biomass subjected to flash evaporation to obtain a cooled mixture; and further cooling the cooled mixture by adopting a heat exchanger, then digesting the organic biomass mixed with the cooled mixture by using a digestive liquid, and respectively outputting the digested methane and the digested slag to the outside.
And 4, the digestive juice is a fermented material after anaerobic fermentation in the digestion tank.
In summary, in the device and method for implementing the thermal hydrolysis fermentation treatment by using the rotary method, the preheating unit preheats the organic biomass raw material inputted from the outside, and the rotary thermal hydrolysis unit adopts the internal rotary method to fully perform heat exchange between the preheated organic biomass raw material and the high-pressure steam, so that the organic biomass raw material is further heated, and the thermal hydrolysis process is accelerated; therefore, the device and the method have high heat exchange efficiency and short thermal hydrolysis period. In addition, the device and the method of the invention utilize flash steam generated in the thermal hydrolysis process to heat the externally input organic biomass raw material, and the thermal hydrolysis period is short, so the device and the method of the invention also have the characteristics of energy saving and consumption reduction.
Drawings
FIG. 1 is a schematic diagram of the structure of the apparatus for implementing thermal hydrolysis fermentation treatment by rotation according to the present invention.
Fig. 2 is a schematic view of the structure of the rotary thermal hydrolysis unit according to the present invention.
FIG. 3 is a schematic diagram of the structure of the rotary thermal hydrolysis reactor according to the present invention.
FIG. 4 is a schematic diagram of the structure of the preheating unit according to the present invention.
FIG. 5 is a schematic diagram of the structure of the mixed fermentation unit according to the present invention.
FIG. 6 is a flow chart of the thermal hydrolysis fermentation treatment method of the present invention.
FIG. 7 is a schematic structural diagram of an embodiment of the apparatus and method for implementing thermal hydrolysis fermentation treatment by rotation according to the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
FIG. 1 is a schematic diagram of the structure of the apparatus for implementing thermal hydrolysis fermentation treatment by rotation according to the present invention. As shown in fig. 1, the apparatus for implementing the thermal hydrolysis fermentation treatment by using the rotation method according to the present invention includes a preheating unit 1 for preheating an organic biomass raw material inputted from an external by using flash steam from a rotary thermal hydrolysis unit 2, a rotary thermal hydrolysis unit 2 for mixing high-pressure steam inputted from an external by using the rotation method with the preheated organic biomass raw material inputted from the preheating unit 1 and then sequentially performing thermal hydrolysis and flash evaporation, and a mixed fermentation unit 3 for mixing an organic biomass obtained by flash evaporation with a digestive juice and then sequentially performing cooling and digestion to obtain biogas and residue; wherein, preheat unit 1's material entry and be connected to the outside, preheat unit 1's flash steam entry connection rotatory thermal hydrolysis unit 2's flash steam delivery outlet, preheat unit 1's material exit linkage rotatory thermal hydrolysis unit 2's material import, rotatory thermal hydrolysis unit 2's high-pressure steam import is connected with the external equipment who carries high-pressure steam, rotatory thermal hydrolysis unit 2's material exit linkage mixed fermentation unit 3's material entry, mixed fermentation unit 3's marsh gas export and thing sediment export are connected to the outside respectively, mixed fermentation unit still is provided with a cooling water import and a cooling water export.
Fig. 2 is a schematic view of the structure of the rotary thermal hydrolysis unit according to the present invention. As shown in fig. 2, the rotary thermal hydrolysis unit 2 includes one or more rotary thermal hydrolysis reactors 211, …, 21i, …, 21n for performing thermal hydrolysis after the externally input high-pressure steam exchanges heat with the organic biomass raw material input by the preheating unit 1 in a rotary manner, and one or more flash tanks 221, 222, …, 22m connected in series for performing flash evaporation on the organic biomass obtained through thermal hydrolysis; wherein, m and n are selected from the group consisting of, i is a natural number greater than or equal to 1, i is greater than or equal to 1 and less than or equal to n, a material inlet of any rotary pyrohydrolysis reactor 21i is connected to a material outlet of the preheating unit 1 through a pipeline, a high-pressure steam inlet of any rotary pyrohydrolysis reactor 21i is connected to the outside through a pipeline, any rotary pyrohydrolysis reactor 21i comprises a pressure-relief steam inlet and a pressure-relief steam outlet, a pressure-relief steam inlet of any rotary pyrohydrolysis reactor 21i is connected with pressure-relief steam outlets of other rotary pyrohydrolysis reactors through a pipeline, a pressure-relief steam outlet of any rotary pyrohydrolysis reactor 21i is connected with pressure-relief steam inlets of other rotary pyrohydrolysis reactors through a pipeline, and a material outlet of any rotary pyrohydrolysis reactor 21i is connected to a material inlet of a first flash tank 221 connected in series through a pipeline; in the flash tanks connected in series, the material outlet of the former flash tank is connected with the material inlet of the latter flash tank, and the material outlet of the last flash tank 22m is connected with the material inlet of the mixed fermentation unit 3; and flash steam outlets of 221-22 m of each flash tank are connected to a flash steam inlet of the preheating unit 1 through a pipeline.
In practical application, the preheating unit 1 sequentially inputs preheated organic biomass raw materials into the rotary pyrohydrolysis reactors 211-21 n in the rotary pyrohydrolysis unit 2, that is, the preheating unit 1 firstly feeds the first rotary pyrohydrolysis reactor 211, and after the feeding of the first rotary pyrohydrolysis reactor 211 is completed, the preheating unit feeds the second rotary pyrohydrolysis reactors 212 and … in sequence until the nth rotary pyrohydrolysis reactor 21n is completed, so that continuous pyrohydrolysis of the organic biomass can be realized by rotating the plurality of rotary pyrohydrolysis reactors 211-21 n.
In practical application, each rotary thermal hydrolysis reactor 211-21 n does not need to rotate continuously when the organic biomass raw material is subjected to thermal hydrolysis, and only needs to rotate in the process of heat exchange between high-pressure steam and the preheated organic biomass raw material, so that the high-pressure steam and the preheated organic biomass raw material are fully mixed, and the thermal hydrolysis of the organic biomass raw material is accelerated.
In practical application, according to different pressures of different stages of the thermal hydrolysis of the rotary thermal hydrolysis reactor, in a thermal hydrolysis period, the rotary thermal hydrolysis reactor which completes the thermal hydrolysis does not need higher pressure, in order to fully utilize energy generated in the thermal hydrolysis process, the rotary thermal hydrolysis reactor which completes the thermal hydrolysis also releases pressure-released steam to the rotary thermal hydrolysis reactor which is feeding, the heat loss of the pressure-released steam generated in pipeline conveying is reduced, and meanwhile, the consumption of the rotary thermal hydrolysis reactor which is feeding to high-pressure steam can be reduced.
In practical application, when the pressure of the flash steam discharged from each flash tank 221-22 m is too low, so that the flash steam cannot enter the preheating unit 1 by itself, the flash steam can be pressurized to a required pressure by using an ejector or a steam compressor, for example, a water-steam ejector, a steam-steam ejector and the like, so as to ensure that the flash steam enters the preheating unit 1.
In practical application, the internal pressure of each flash tank 221-22 m is slightly higher than the normal pressure.
In a word, in the device for realizing the thermal hydrolysis fermentation treatment by adopting the rotary mode, the preheating unit preheats the organic biomass raw material input from the outside and then enters the rotary thermal hydrolysis unit; the rotary thermal hydrolysis reactors in the rotary thermal hydrolysis unit fully exchange heat between the preheated organic biomass raw material and high-pressure steam in a rotary mode, so that the organic biomass raw material is further heated, the thermal hydrolysis process is accelerated, and large-particle organic organisms are rapidly degraded; therefore, the device has high heat exchange efficiency and short thermal hydrolysis period, and compared with the prior art, the thermal hydrolysis period can be shortened by 1/3-1/2 under the condition that the quality of the organic biomass is the same. In addition, under the condition of normal operation of the device, the flash steam generated by each flash tank is used for preheating the organic biomass raw material input from the outside, and the decompression steam generated by the rotary pyrohydrolysis reactor which just completes pyrohydrolysis is output to the rotary pyrohydrolysis reactor which is feeding.
FIG. 3 is a schematic diagram of the structure of the rotary thermal hydrolysis reactor according to the present invention. As shown in fig. 3, each rotary pyrohydrolysis reactor 2i includes a rotary reaction tank 2i1, a feed pipe 2i2, a feed valve 2i3, one or more first guide pipes 2i4, a pressure-relief steam inlet pipe 2i5, a pressure-relief steam inlet valve 2i6, a discharge pipe 2i7, a first discharge valve 2i8, a second discharge valve 2i9, a high-pressure steam inlet pipe 2i10, a high-pressure steam inlet valve 2i11, one or more second guide pipes 2i12, a pressure-relief steam outlet pipe 2i13, a pressure-relief steam outlet valve 2i 14; the feeding pipe 2i2 of the rotary reaction tank 2i1 is used for communicating a first guide pipe 2i4 arranged at the feeding hole of the rotary reaction tank 2i1 with the discharging hole of the preheating unit 1 through a feeding valve 2i3, the pressure relief steam inlet pipe 2i5 is communicated with the first guide pipe 2i4 through a pressure relief steam inlet valve 2i6, and the discharging pipe 2i7 is communicated with the first guide pipe 2i4 through a first discharging valve 2i8 and a second discharging valve 2i9 in sequence; the high pressure steam inlet pipe 2i10 of the rotary reaction tank 2i1 communicates the second guide pipe 2i12 installed at the high pressure steam inlet of the rotary reaction tank 2i1 with an external device outputting high pressure steam through the high pressure steam inlet valve 2i11, and the pressure relief steam outlet pipe 2i13 communicates with the second guide pipe 2i12 through the pressure relief steam outlet valve 2i 14.
In practical application, the rotary pyrohydrolysis reactor 2i is used for pyrohydrolysis, a feeding valve 2i3 of a rotary reaction tank 2i1 is opened, a high-pressure steam inlet valve 2i11, a pressure-relief steam outlet valve 2i14, a pressure-relief steam inlet valve 2i6, a first discharging valve 2i8 and a second discharging valve 2i9 are closed at the same time, the feeding pipe 2i2 starts to be fed by the preheating unit 1, an organic biomass raw material flow enters the rotary reaction tank 2i1 through a first guide pipe 2i4, and when the accumulated flow of the input organic biomass raw material reaches a preset value, the feeding valve 2i3 is closed to finish feeding. At the same time or after a period of time, opening a pressure relief steam valve inlet valve 2i6 of the rotary reaction tank 2i 1; and opening a pressure relief steam outlet valve of the other rotary pyrohydrolysis reactor which just completes pyrohydrolysis, and closing the pressure relief steam outlet valve of the other rotary pyrohydrolysis reactor which just completes pyrohydrolysis when the internal pressure of the other rotary pyrohydrolysis reactor which just completes pyrohydrolysis is less than the preset pressure of 0.1-0.5 MPa. Delaying for a certain time, opening a high-pressure steam inlet valve 2i11, allowing external high-pressure steam to enter from a high-pressure steam inlet pipe 2i10, rotating a rotary reaction tank 2i1 to promote heat exchange and accelerate a thermal hydrolysis process, closing the high-pressure steam inlet valve 2i11 when the internal pressure of the rotary reaction tank 2i1 reaches 0.5-1.0 MPa and the internal organic biomass raw material is in a non-boiling state, and keeping the rotary reaction tank 2i1 in the state for 15-90 minutes; and after 15-90 minutes, opening a pressure relief steam outlet valve 2i14 of the rotary pyrohydrolysis reactor 2i, releasing pressure relief steam from the rotary pyrohydrolysis reactor 2i to another rotary pyrohydrolysis reactor which is feeding, and closing the pressure relief steam outlet valve 2i14 when the internal pressure of a rotary reaction tank 2i1 of the rotary pyrohydrolysis reactor 2i is reduced to 0.1-0.7 MPa. After the pressure relief steam outlet valve 2i14 is closed, the first guide pipe 2i4 is screwed to the bottom of the rotary reaction tank 2i1, the first discharge valve 2i8 and the second discharge valve 2i9 are opened in a delayed mode, and organic biomass obtained after thermal hydrolysis reaction is output to the first flash tank 221 through the discharge pipe 2i 7. After the discharging is finished, the first discharging valve 2i8 and the second discharging valve 2i9 are closed, and the thermal hydrolysis reactor 2i is rotated to finish a thermal hydrolysis cycle.
In practical application, the rotary reaction tank 2i1 is driven by a motor or other power devices to rotate, so that the power consumption is low; for example, when the rotary reaction tank 2i1 drives 25-30 tons of organic biomass, the power consumption of the motor is 5-7.5 kW; the rotation time of the rotary reaction tank 2i1 accounts for 1/4-1/5 of the whole pyrohydrolysis period, and the pyrohydrolysis power consumption of the organic biomass in unit mass is 0.05-0.0625 kW/t.
In practical application, when the rotary pyrohydrolysis reactor 2i discharges, the internal pressure of the rotary pyrohydrolysis reactor 2i is greater than the internal pressure of the first flash tank 221, and the pressure difference is large, so that all organic biomass obtained by pyrohydrolysis of the rotary pyrohydrolysis reactor 2i is emptied.
In practical applications, the rotary reaction tank 2i1 performs horizontal rotation, vertical rotation, or oblique rotation.
FIG. 4 is a schematic diagram of the structure of the preheating unit according to the present invention. As shown in fig. 4, the preheating unit 1 includes a preheating tank 11 for sequentially outputting the preheated organic biomass raw materials to each of the rotary pyrohydrolysis reactors 211 to 21n, and recovering the preheated organic biomass raw materials output by the preheating unit 1 when each of the rotary pyrohydrolysis reactors 211 to 21n is subjected to pyrohydrolysis; wherein a material inlet of the preheating tank 11 is connected to the outside, a flash steam inlet of the preheating tank 11 is communicated with flash steam outlets 221-22 m of the flash tanks through pipelines, and a material outlet of the preheating tank 11 is connected to material inlets of the rotary pyrohydrolysis reactors 211-21 n through third discharge valves; the preheating tank 11 is also provided with a return inlet which is connected to the material outlet of the preheating tank 11 via a return valve.
In practical application, the preheating tank 11 adopts the flash steam from each flash tank 221-22 m to heat the organic biomass raw material input from the outside to be less than or equal to 105 ℃, and the preheated organic biomass raw material is sequentially pumped into each rotary pyrohydrolysis reactor 211-21 n by a pump.
FIG. 5 is a schematic diagram of the structure of the mixed fermentation unit according to the present invention. As shown in fig. 5, the mixed fermentation unit 3 includes a heat exchanger 31 for cooling a mixture of the organic biomass output from the rotary thermal hydrolysis unit 2 and the digestion solution output from the digestion tank 32 by external cooling water, the digestion tank 32 for digesting the cooled organic biomass by the digestion solution; wherein, the material inlet of the heat exchanger 31 is simultaneously communicated with the material outlet of the latter flash tank and the digestion liquid outlet of the digestion tank 32, the material outlet of the heat exchanger 31 is connected with the material inlet of the digestion tank 32, and the methane outlet and the material slag outlet of the digestion tank 32 are respectively connected to the outside.
In practical applications, the cooling water after heat exchange in the heat exchanger 31 can be used for the requirement of the device for performing the thermal hydrolysis fermentation treatment in a rotating manner for low-temperature hot water, for example, the cooling water can be input into the preheating tank 11 to dilute the organic biomass raw material.
In the present invention, the organic biomass output from the last flash tank 22m of the rotary thermal hydrolysis unit 2 is mixed with the digestion solution output from the digestion tank 32 in a pipeline via a booster pump. Before the organic biomass is mixed with the digestive juice, the temperature of the digestive juice is 35-60 ℃; after the organic biomass is mixed with the digestive juice, the temperature of the obtained cooling mixture is 35-90 ℃. The mixing ratio value of the digestive juice and the flashed organic biomass is more than or equal to 1.
In practical application, the organic biomass subjected to flash evaporation is mixed with the digestive juice for cooling, and then is further cooled by the heat exchanger 31, so that the phenomenon that the temperature of the organic biomass is too high and the activity of strains in the digestive juice is damaged is avoided. After the flashed organic biomass is mixed with the digestive juice for cooling, if the temperature of the cooled mixture is lower than a set standard, the cooled mixture directly enters the digestion tank 32 for digestion without further heat exchange.
In the device, the digestion solution digests the cooled organic biomass into anaerobic fermentation.
FIG. 6 is a flow chart of the method for implementing the thermal hydrolysis fermentation treatment by using a rotary mode according to the invention. As shown in FIG. 6, the method for implementing thermal hydrolysis fermentation treatment by rotation according to the present invention comprises the following steps:
step 1, preheating an externally input organic biomass raw material to a temperature of less than or equal to 105 ℃ by flash steam from a preheating tank, and then sequentially inputting the organic biomass raw material into each rotary thermal hydrolysis reactor.
Step 2, the rotary pyrohydrolysis reactor which just completes pyrohydrolysis outputs the pressure relief steam generated by pyrohydrolysis to the rotary pyrohydrolysis reactor which is used for inputting the preheated organic biomass raw material; after the rotary thermal hydrolysis reactors complete feeding, the preheated organic biomass raw material and high-pressure steam from the outside are mixed in a rotary mode in sequence and then subjected to thermal hydrolysis.
Step 3, carrying out flash evaporation on the organic biomass obtained after thermal hydrolysis by using a flash evaporation tank; if the pressure of the flash steam generated by flashing is less than the internal pressure of the preheating tank, the pressure of the flash steam is pressurized to be greater than the internal pressure of the preheating tank by a jet pump, and the pressurized flash steam is returned to the step 1; if the pressure of the flash steam generated by flashing is larger than the internal pressure of the preheating tank, directly returning the flash steam to the step 1; step 4 is performed on the flashed organic biomass.
Step 4, mixing the flash-evaporated organic biomass with the digestive juice, and cooling to obtain a cooled mixture; and further cooling the cooled mixture by adopting a heat exchanger, then digesting the organic biomass mixed with the cooled mixture by using a digestive liquid, and respectively outputting the digested methane and the digested slag to the outside.
In the method, before the organic biomass is mixed with the digestive juice, the temperature of the digestive juice is 35-60 ℃; and after mixing the organic biomass and the digestive juice, cooling the mixture to 35-90 ℃. The mass ratio of the mixture of the flashed digestive juice and the organic biomass is greater than or equal to 1.
In practical application, the organic biomass subjected to flash evaporation is mixed with the digestive juice for cooling, and then is further cooled by a heat exchanger, so that the phenomenon that the temperature of the organic biomass is too high and the strain activity in the digestive juice is damaged is avoided. After the flash-evaporated organic biomass is mixed with the digestive juice for cooling, if the temperature of the cooled mixture is lower than a set standard, the cooled mixture is directly digested without further heat exchange.
In a word, in the method for realizing the thermal hydrolysis fermentation treatment by adopting the rotary mode, the preheating tank preheats the organic biomass raw material input from the outside by adopting the pressure relief steam generated in the thermal hydrolysis process; the rotary thermal hydrolysis device adopts a rotary mode to ensure that the preheated organic biomass raw material and high-pressure steam fully carry out heat exchange, so that the organic biomass raw material is further heated, the thermal hydrolysis process is accelerated, and large-particle organic organisms are rapidly degraded; therefore, the method has higher heat exchange efficiency and shorter thermal hydrolysis period, and compared with the prior art, the thermal hydrolysis period can be shortened by 1/3-1/2 under the condition of the same organic biomass; meanwhile, the method has the characteristics of energy conservation and consumption reduction.
In step 2, the preheated organic biomass raw material is mixed with high-pressure steam from the outside as follows: and carrying out heat exchange on the high-pressure steam and the preheated organic biomass raw material, so that the organic biomass obtained after heat exchange is heated to 0.5-1.0 Mpa and is in a non-boiling state.
In practical application, the organic biomass obtained after heat exchange is heated to 0.5-1.0 Mpa and is in a non-boiling state for 15-90 minutes.
In practical application, different thermal hydrolysis durations are adopted according to different organic biomass raw materials.
Examples
FIG. 7 is a schematic structural diagram of an embodiment of the apparatus and method for implementing thermal hydrolysis fermentation treatment by rotation according to the present invention. As shown in fig. 7, the apparatus for implementing thermal hydrolysis fermentation treatment by rotation in this embodiment includes a preheating tank, a rotary thermal hydrolysis reactor a, a rotary thermal hydrolysis reactor b, a flash tank, a heat exchanger, and a digestion tank. The organic biomass feedstock in this example is a sludge, such as a municipal sludge. The method for implementing the thermal hydrolysis fermentation treatment by adopting the rotation mode in the embodiment is as described above.
In summary, the above description is only a preferred embodiment of the present invention, and is not intended to limit the scope of the present invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (9)
1. The device for realizing the thermal hydrolysis and fermentation treatment by adopting the rotation mode is characterized by comprising a preheating unit, a rotary thermal hydrolysis unit and a mixed fermentation unit, wherein the preheating unit is used for preheating an externally input organic biomass raw material by adopting flash steam from the rotary thermal hydrolysis unit; the rotary thermal hydrolysis unit comprises one or more rotary thermal hydrolysis reactors which carry out thermal hydrolysis after high-pressure steam input from the outside exchanges heat with the organic biomass raw material input from the preheating unit in a rotary mode, and one or more flash tanks which are connected in series and used for carrying out flash evaporation on the organic biomass obtained by thermal hydrolysis; wherein,
the material inlet of each rotary pyrohydrolysis reactor is connected to the material outlet of the preheating unit through a pipeline, the high-pressure steam inlet of each rotary pyrohydrolysis reactor is connected to the outside through a pipeline, each rotary pyrohydrolysis reactor comprises a pressure-release steam inlet and a pressure-release steam outlet, the pressure-release steam inlet of each rotary pyrohydrolysis reactor is connected with the pressure-release steam outlets of other rotary pyrohydrolysis reactors through pipelines, the pressure-release steam outlet of each rotary pyrohydrolysis reactor is connected with the pressure-release steam inlets of other rotary pyrohydrolysis reactors through pipelines, and the material outlet of each rotary pyrohydrolysis reactor is connected to the material inlet of a first flash tank connected in series through a pipeline; in the flash tanks connected in series, the material outlet of the previous flash tank is connected with the material inlet of the next flash tank, and the material outlet of the last flash tank is connected with the material inlet of the mixed fermentation unit; the flash steam outlet of each flash tank is connected by a conduit to the flash steam inlet of the preheating unit.
2. The device for realizing the thermal hydrolysis fermentation treatment in a rotating mode according to claim 1, wherein each rotary thermal hydrolysis reactor comprises a rotary reaction tank, a feeding pipe, a feeding valve, one or more first guide pipes, a pressure relief steam inlet pipe, a pressure relief steam inlet valve, a discharging pipe, a first discharging valve, a second discharging valve, a high-pressure steam inlet pipe, a high-pressure steam inlet valve, one or more second guide pipes, a pressure relief steam outlet pipe and a pressure relief steam outlet valve; wherein,
a feeding pipe of the rotary reaction tank is used for communicating a first guide pipe arranged at a feeding hole of the rotary reaction tank with a discharging hole of the preheating unit through a feeding valve, a pressure relief steam inlet pipe is communicated with the first guide pipe through a pressure relief steam inlet valve, and the discharging pipe is communicated with the first guide pipe through a first discharging valve and a second discharging valve in sequence; a high-pressure steam inlet pipe of the rotary reaction tank is communicated with a second guide pipe arranged at a high-pressure steam inlet of the rotary reaction tank and external equipment for outputting high-pressure steam through a high-pressure steam inlet valve, and a pressure-relief steam outlet pipe is communicated with the second guide pipe through a pressure-relief steam outlet valve.
3. The apparatus for implementing thermal hydrolysis fermentation treatment by rotation according to claim 2, wherein the rotary reaction tank rotates horizontally or vertically or obliquely.
4. The apparatus for rotary realization of a thermal hydrolysis fermentation process according to claim 1, wherein the preheating unit comprises a preheating tank for sequentially outputting the preheated organic biomass material to each of the rotary thermal hydrolysis reactors, and recovering the preheated organic biomass material output by the preheating unit when each of the rotary thermal hydrolysis reactors is thermally hydrolyzed; wherein,
a material inlet of the preheating tank is connected to the outside, a flash steam inlet of the preheating tank is communicated with a flash steam outlet of each flash tank through a pipeline, and a material outlet of the preheating tank is connected to a material inlet of each rotary thermal hydrolysis reactor through a third discharge valve; the preheating tank is also provided with a feed back inlet which is connected to the material outlet of the preheating tank through a feed back valve.
5. The apparatus for rotary realization of a thermal hydrolysis and fermentation process according to claim 1, wherein the mixed fermentation unit comprises a heat exchanger for cooling the mixture of the organic biomass output from the rotary thermal hydrolysis unit and the digestion solution output from the digestion tank 32 by external cooling water, and a digestion tank for digesting the cooled organic biomass by the digestion solution; wherein,
and a material inlet of the heat exchanger is simultaneously communicated with a material outlet of the last flash tank and a digestion liquid outlet of the digestion tank, the material outlet of the heat exchanger is connected with the material inlet of the digestion tank, and a methane outlet and a residue outlet of the digestion tank are respectively connected to the outside.
6. A method for realizing the thermal hydrolysis fermentation treatment by adopting a rotating mode is characterized by comprising the following steps:
step 1, preheating an externally input organic biomass raw material to a temperature of less than or equal to 105 ℃ by flash steam from a preheating tank, and then sequentially inputting the organic biomass raw material into each rotary thermal hydrolysis reactor;
step 2, the rotary pyrohydrolysis reactor which just completes pyrohydrolysis outputs the pressure relief steam generated by pyrohydrolysis to the rotary pyrohydrolysis reactor which is used for inputting the preheated organic biomass raw material; after the rotary thermal hydrolysis reactors finish feeding, mixing the preheated organic biomass raw material with high-pressure steam from the outside in a rotary mode in sequence and then performing thermal hydrolysis;
step 3, carrying out flash evaporation on the organic biomass obtained after thermal hydrolysis by using a flash evaporation tank; if the pressure of the flash steam generated by flashing is less than the internal pressure of the preheating tank, the pressure of the flash steam is pressurized to be greater than the internal pressure of the preheating tank by a jet pump, and the pressurized flash steam is returned to the step 1; if the pressure of the flash steam generated by flashing is larger than the internal pressure of the preheating tank, directly returning the flash steam to the step 1; performing step 4 on the flashed organic biomass;
step 4, mixing the flash-evaporated organic biomass with the digestive juice, and cooling to obtain a cooled mixture; and further cooling the cooled mixture by adopting a heat exchanger, then digesting the organic biomass mixed with the cooled mixture by using a digestive liquid, and respectively outputting the digested methane and the digested slag to the outside.
7. The method for realizing hot hydrolysis fermentation treatment by adopting a rotating mode according to claim 6, wherein in the step 2, the preheated organic biomass raw material is mixed with high-pressure steam from the outside to form: and carrying out heat exchange on the high-pressure steam and the preheated organic biomass raw material, so that the organic biomass obtained after heat exchange is heated to 0.5-1.0 Mpa and is in a non-boiling state.
8. The method for realizing hot hydrolysis fermentation treatment by adopting a rotating mode according to claim 7, wherein the organic biomass obtained after heat exchange is heated to 0.5-1.0 Mpa and is in a non-boiling state for 15-90 minutes.
9. The method for realizing hot hydrolytic fermentation treatment by adopting the rotating mode as claimed in claim 7, wherein the mixing mass proportion value of the digestive juice and the organic biomass in the step 4 is more than or equal to 1.
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