CN113088303A - Heat carrier direct heat supply type multistage series turbulent bed pyrolysis stripping reactor - Google Patents
Heat carrier direct heat supply type multistage series turbulent bed pyrolysis stripping reactor Download PDFInfo
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Abstract
The application relates to the field of solid waste treatment, in particular to a direct heat supply type multistage series turbulent bed pyrolysis stripping reactor with a heat carrier, which comprises a shell, wherein the shell comprises a reaction upper section, a reaction middle section and a reaction lower section which are communicated with each other; the reaction upper section is provided with a solid waste inlet and a product outlet, the reaction middle section is provided with a plurality of groups of turbulent micro-reaction beds which are connected in series, and the reaction lower section is provided with a heat carrier inlet and a residue outlet. This application has the effect that improves reactor pyrolysis efficiency.
Description
Technical Field
The application relates to the field of solid waste treatment, in particular to a direct heat supply type multistage series turbulent bed pyrolysis stripping reactor for a heat carrier.
Background
With the acceleration of economic development and urbanization in China, the resource consumption is increasingly enlarged, the problems of increased yield of various wastes, diversified waste forms, pollution of soil and underground water and the like become more severe. The national environmental protection regulations require that the solid waste materials containing organic matters (namely organic solid wastes, most of which belong to dangerous wastes) are subjected to reduction and harmless treatment to meet the requirement of environmental protection discharge, the resource recycling can be realized by adopting a proper technology, and the polluted soil needs to be repaired and treated to meet the requirement of agricultural or urban commercial soil quality.
The organic solid waste materials (organic solid waste) mainly comprise three main types, namely organic solid waste produced in an industrial production process, such as oil field oily sludge and oily solid waste produced in the processes of petroleum and natural gas exploitation, gathering and transportation and the like, petrochemical oily sludge and organic solid waste produced in a petrochemical production process, biochemical sludge produced in municipal public works such as a water treatment plant and organic solid waste produced in the production processes of light industrial industries such as papermaking, textile, printing and dyeing and the like; organic solid wastes generated in agriculture and forestry, such as crop straws, rice (millet) shells, fruit shells, branches, firewood, leaves, wood chips and the like; and thirdly, organic solid waste of the municipal solid waste, such as toxic and harmful waste of paper, fabric, plastic rubber, wood, bamboo and the like and mixed waste.
At present, the technologies for reducing and harmlessly treating solid waste materials (organic solid waste) containing organic substances mainly comprise a single treatment method or a combination of a plurality of methods, such as a landfill method, an incineration method, a biological method, a mechanical dehydration method, a drying method, a chemical hot washing method, an extraction method, a pyrolysis method and the like. The landfill method is forbidden, and other methods have the problems of high energy consumption, long treatment process, high treatment cost, secondary pollution, incomplete treatment, small treatment scale, low treatment efficiency, low organic matter conversion recovery rate and resource waste.
The pyrolysis method can perform harmless treatment on all organic matters in the organic-containing solid waste material (organic solid waste), can also recover oil gas or convert the organic matters to realize resource utilization, and is the technology with the most development potential at present.
The pyrolysis stripping reactor is the core of the overall pyrolysis process in which the pyrolysis process takes place, the type of which determines the pyrolysis reaction regime and the composition of the pyrolysis products. Currently, pyrolysis stripping reactors are classified into fixed bed reactors, fluidized beds, rotary furnaces (kilns) and double-tower circulating pyrolysis reactors according to the difference of the structure. The fixed fluidized bed is in a counter-flow material flow direction, has long retention time and ensures that the waste is converted into fuel to the maximum extent; because the gas flow velocity is lower, the particle matters carried in the generated gas are less, and the potential influence on air pollution is reduced. The gas flow velocity in the fluidized bed reactor is high enough to enable particles to be suspended, so that organic solid waste particles are dispersed, the reaction performance is better, but the heat loss is large, and a large amount of heat is taken away in the gas and more unreacted solid fuel powder is obtained. The rotary furnace (kiln) is an indirect heating pyrolysis reactor, and the heat transfer efficiency is not high. The double-tower circulating type pyrolysis reactor separates pyrolysis and combustion reaction in two towers, so that the equipment investment is large and the occupied area is large.
The pyrolysis method has larger difference of different treatment effects along with different pyrolysis reactors, and the batch pyrolysis furnace has the advantages of one-time feeding and one-time deslagging, can not realize continuous production and has small treatment scale; the continuous pyrolyzing furnace has small treatment scale and low continuous operability influenced by various factors, and at present, no matter the intermittent pyrolyzing furnace or the continuous pyrolyzing furnace adopts an indirect heat supplying pyrolyzing method that organic solid waste is in a hearth, a heat carrier (external heat supply) is outside the hearth, and the organic solid waste in a jacket is not in direct contact with heat, so that the problems of low heat utilization efficiency caused by low heat transfer efficiency and low heat absorption efficiency, low pyrolyzing reaction speed, long reaction time, high energy consumption, incapability of meeting the requirement of ultra-clean emission environmental protection index by solid residue pyrolysis and the like exist.
Disclosure of Invention
In order to improve pyrolysis efficiency, the application provides a direct heat supply type multistage series turbulent bed pyrolysis stripping reactor of heat carrier.
The application provides a pair of heat carrier is directly for multistage series connection turbulent bed pyrolysis stripping reactor of hot type adopts multistage series connection turbulent bed, has the advantage that fixed bed dwell time is long and fluidized bed reactivity is better concurrently, adopts the not high shortcoming of heat transfer efficiency who has directly overcome rotary furnace (kiln) for hot type heating method, specifically adopts following technical scheme:
a heat carrier direct heat supply type multistage series turbulent bed pyrolysis stripping reactor comprises a shell, wherein the shell comprises a reaction upper section, a reaction middle section and a reaction lower section which are communicated with each other; the upper reaction section is provided with a solid waste inlet and a product outlet, the middle reaction section is provided with a plurality of groups of turbulent micro-reaction beds connected in series, and the lower reaction section is provided with a heat carrier inlet and a residue outlet; the heat carrier and the solid waste are directly contacted in the shell for heat supply; the turbulent micro-reaction bed is internally provided with a main reaction zone, and a secondary reaction zone is formed between adjacent turbulent micro-reaction beds.
By adopting the technical scheme, the high-temperature heat carrier rises from the heat carrier inlet at the lower reaction section, the organic solid wastes flow downwards from the solid waste inlet at the upper reaction section, and the high-temperature heat carrier and the organic solid wastes are directly contacted with the stripping reaction zone at the middle reaction section, so that the heat supply efficiency and the heat absorption efficiency of the organic solid wastes in the pyrolysis stripping process are greatly improved, the heat utilization efficiency is improved, and the energy consumption is effectively reduced by a direct heat supply method in which the organic solid wastes are directly contacted with the high-temperature heat carrier (heat);
the method comprises the following steps of constructing multistage series-connected turbulent micro-reaction beds, so that organic solid waste materials are in a fully-mixed state of turbulent suspension and gas-solid two phases in each group of micro-reaction beds to directly contact with heat carried by a high-temperature heat carrier for efficient heat exchange, on one hand, the heat supply efficiency and the heat absorption efficiency of the organic solid waste pyrolysis stripping process are greatly improved, the heat utilization efficiency is improved, and the energy consumption is effectively reduced;
on the other hand, the turbulent suspension micro-reaction bed in multi-stage series connection effectively prolongs the retention time of the organic solid waste materials, the full gas-solid two-phase turbulent suspension mixing state greatly improves the speed of the pyrolysis reaction and the stripping reaction of the organic solid waste materials for removing toxic and harmful substances and converting the organic solid waste materials into gaseous hydrocarbon substances and/or gas-phase oil products with low molecular weight, shortens the time of the pyrolysis stripping reaction, improves the yield of organic matter conversion and recovery in the organic solid waste, achieves the aim that the organic solid waste pyrolysis solid residue meets the requirement of ultra-clean emission environmental protection index, avoids secondary pollution, and realizes the beneficial effects of environment friendliness and resource saving of thorough harmless treatment of the organic solid waste and organic matter resource conversion and recovery.
The main reaction zone and the side reaction zone can provide a multi-layer reaction zone, so that the organic solid waste can be subjected to thermal reaction in the middle reaction section more fully, and the pyrolysis efficiency is further improved.
Optionally, the turbulent micro-reaction bed comprises at least one upper baffle and at least one lower baffle, a main reaction zone is formed between the upper baffle and the lower baffle, and a secondary reaction zone is formed between the upper baffle and the inner wall of the shell and between the lower baffle and the inner wall of the shell.
By adopting the technical scheme, the main reaction zone and the side reaction zone can be formed by combining the upper guide plate and the lower guide plate, on one hand, the combination and matching of the upper guide plate and the lower guide plate can be adjusted according to the actual product requirement, so that different organic solid waste raw materials can be suitable for stripping; on the other hand, the equipment is simple to produce, and the accessories are fewer, so that the later maintenance is facilitated.
Optionally, the reaction upper section is provided with a material distribution plate for uniformly distributing the organic solid waste.
Through adopting above-mentioned technical scheme, the distributing plate can be collected organic solid waste back even whereabouts to the reaction in the little reaction bed of turbulence in the middle section to further promote reaction efficiency.
Optionally, the reaction middle section is provided with a secondary heat carrier inlet communicated with the shell.
By adopting the technical scheme, the heat carrier can be supplemented at any time, so that the heat carrier is fully contacted with the organic solid waste raw material in the turbulent micro-reaction bed, and the decomposition and stripping efficiency of the organic solid waste raw material is improved.
Optionally, the secondary heat carrier inlet is located between adjacent turbulent micro-reaction beds.
By adopting the technical scheme, the heat carrier can fully contact the side reaction zone and the main reaction zone, so that the thermal stripping efficiency is further improved.
Optionally, the reaction lower section is provided with a slag guide plate.
By adopting the technical scheme, the slag is guided and concentrated, so that the slag is convenient to collect.
Optionally, the reaction lower section is provided with a heat carrier distribution plate.
By adopting the technical scheme, the heat carrier can be uniformly distributed.
Optionally, the reaction upper section and the reaction lower section are both provided with manholes.
Through adopting above-mentioned technical scheme, can supply the staff to get into and overhaul.
Optionally, the reaction pressure in the shell is-0.1-10 MpaG, and the reaction temperature is 300-1000 ℃; the pressure of the high-temperature heat carrier is 0.01-10MPaG, and the temperature is 300-1000 ℃.
By adopting the technical scheme, the parameters have better hot stripping effect and save energy consumption.
In summary, the present application includes at least one of the following beneficial technical effects:
1. the application discloses a medium-high temperature pyrolysis stripping process adopting an organic solid waste oxygen-poor or oxygen-free environment, through a direct heat supply method of directly contacting the organic solid waste with a high-temperature heat carrier, and constructing multistage series-connected turbulent micro-reaction beds, the organic solid waste material is in a gas-solid two-phase turbulent suspension fully-mixed state in each group of micro-reaction beds to directly contact and efficiently exchange heat with heat carried by the high-temperature heat carrier, on one hand, the heat supply efficiency and the heat absorption efficiency in the organic solid waste pyrolysis stripping process are greatly improved, the heat utilization efficiency is improved, the energy consumption is effectively reduced, on the other hand, the multistage series-connected turbulent micro-reaction beds effectively prolong the retention time of the organic solid waste material, and the sufficient gas-solid two-phase dynamic suspension mixed state greatly improves the pyrolysis reaction and stripping reaction speed of the organic solid waste material for removing toxic and harmful substances and converting the organic solid waste material into gaseous hydrocarbon substances with low molecular weight and/or gaseous oil products, The pyrolysis stripping reaction time is shortened, the organic matter conversion recovery yield in the organic solid waste is improved, the organic solid waste pyrolysis solid residue meets the requirement of ultra-clean emission environmental index, secondary pollution is avoided, and the beneficial effects of thorough harmless treatment of the organic solid waste and environment-friendly and resource-saving organic matter resource conversion recovery are realized;
2. the heat carrier used in the present application is a single component gas (excluding oxygen) or a mixture of oxygen-poor or oxygen-free multi-component gases. Such as N2Inert gas such as argon, CO2Gas, superheated steam or flue gas after combustion of fuel, pyrolysis tail gas, synthesis gas (the main chemical component is H)2CO), refinery dry gas or petrochemical waste gas or purge tail gas and the like or multi-component gas mixture of the gases have easy availability and safety and can realize the reutilization of the waste gas.
3. The multistage series turbulent bed has the advantages of long retention time of the fixed bed and better reaction performance of the fluidized bed, and overcomes the defect of low heat transfer efficiency of a rotary furnace (kiln) by adopting a direct heat supply type heating mode.
Drawings
Fig. 1 is a schematic structural diagram of embodiment 1 of the present application.
Fig. 2 is a schematic structural diagram of embodiment 2 of the present application.
FIG. 3 is a schematic structural view of a turbulent micro-reaction bed in example 3 of the present application.
FIG. 4 is a schematic structural view of a turbulent micro-reaction bed in example 4 of the present application.
Description of reference numerals: 1. a housing; 2. a refractory heat insulating lining; 11. a reaction upper section; 12. a reaction middle section; 13. a reaction lower section; 111. a solid waste inlet; 112. a product outlet; 113. a manhole; 114. a material distribution plate; 1141. a first gap is formed; 1142. a first annular gap; 121. a turbulent micro-reaction bed; 123. a secondary heat carrier inlet; 124. a slag guide plate; 1211. a primary reaction zone; 1212. a secondary reaction zone; 1214. an upper deflector; 1215. a lower deflector; 12141. a second gap; 12142. a second annular gap; 12151. a third gap; 12152. a third annular gap; 1241. a fourth gap; 1242. a fourth annular gap; 131. a heat carrier inlet; 132. a heat carrier distribution plate; 134. and (5) residue outlet.
Detailed Description
The present application is described in further detail below with reference to figures 1-4.
Example 1
The embodiment of the application discloses a direct heat supply type multistage series turbulent bed pyrolysis stripping reactor for a heat carrier. Referring to fig. 1, the heat carrier direct-heating multistage series turbulent bed pyrolysis stripping reactor comprises a shell 1, a refractory heat-insulating lining 2 is arranged between the inner wall and the outer wall of the shell 1, and three areas, namely a reaction upper section 11, a reaction middle section 12 and a reaction lower section 13, which are mutually communicated are distributed on the shell 1 from top to bottom.
The high-temperature heat carrier rises from the lower reaction section 13 to the upper reaction section 11; the organic solid waste flows downwards from the reaction upper section 11 to the reaction lower section 13; in the middle reaction section 12, the descending organic solid wastes directly contact with the ascending high-temperature heat carrier for heat exchange, and the organic solid wastes absorb heat carried by the high-temperature heat carrier to generate cracking reaction and stripping reaction of organic matters to generate gaseous hydrocarbon substances with low molecular weight and/or gaseous oil products, and a gaseous mixture consisting of the high-temperature heat carrier flows from bottom to top. It should be noted that the reaction upper section 11, the reaction middle section 12 and the reaction lower section 13 may be coaxially communicated with each other with the same diameter, or communicated with each other with different diameters; the cross-sectional shapes of the upper reaction section 11, the middle reaction section 12 and the lower reaction section 13 may be cylindrical or elliptical, or rectangular or polygonal; the cross-sectional shapes of the upper reaction section 11, the middle reaction section 12 and the lower reaction section 13 may be the same cross-sectional structure, or may be a combination of different cross-sectional shapes and different structures thereof; the cross-sectional areas of the upper reaction section 11, the middle reaction section 12 and the lower reaction section 13 may be equal or different; the upper reaction section 11, the middle reaction section 12, and the lower reaction section 13 may be of an integral structure or a segmented connection structure.
In addition, the refractory heat-insulating lining 2 can be a multi-layer refractory heat-insulating castable structure, a multi-layer refractory heat-insulating brick structure, a combined structure of the refractory heat-insulating castable and the refractory heat-insulating bricks, a tubular or coil-type membrane water-cooled wall structure, a cooling jacket structure, or different combinations of the structures.
The upper reaction section 11 has a solid waste inlet 111, a product outlet 112, a manhole 113, and a material distribution plate 114 disposed in the shell 1. Specifically, the solid waste inlet 111 is arranged on the top side surface of the reaction upper section 11, and in this embodiment, 4 solid waste inlets 111 are arranged and uniformly distributed by taking the central axis of the shell 1 as an axis; the product outlets 112 are provided with 1 and are positioned at the center of the top of the shell 1 and are coaxial with the central axis of the shell 1; manhole 113 is opened in the side of casing 1 for the staff to overhaul.
The upper surface or the lower surface of the material distribution plate 114 may be a flat surface or a curved surface, and the upper surface may be straight, corrugated, or provided with a diversion trench, or different combinations thereof.
For convenience of illustration, the included angle between the upper surface of the material distribution plate 114 and the center line of the shell 1 is defined as α, and the included angle α may be any value from 0 to 180 °; when the included angle is 0 degrees < alpha < 90 degrees, the gathering point of the material distribution plate 114 is at the bottom, and when the included angle is 90 degrees < alpha < 180 degrees, the gathering point of the material distribution plate 114 is at the top.
The material distribution plate 114 is provided with a notch I1141 with the width or the diameter of a0 (a 0 is more than or equal to 0) at the bottom (when the angle is 0 degrees < alpha < 90 degrees) or the top (when the angle is 90 degrees < alpha < 180 degrees) of the central area, and correspondingly, an annular gap I1142 with the width of b01 and b02 (b 01 is more than or equal to 0, b02 is more than or equal to 0) is arranged between the bottom (when the angle is 0 degrees < beta 1< 90 degrees) or the top (when the angle is 90 degrees < beta 2 degrees < 180 degrees) and the inner wall surface of the shell 1, and the notch I1141 and the annular gap I are channels for downward movement of organic solid. In one embodiment, the material distribution plate 114 has a first gap 1141 but not a second gap 1142. In another embodiment, the material distribution plate 114 has a first annular gap 1142, but not a second annular gap 1141. In another embodiment, the material distribution plate 114 has both a first gap 1141 and a second gap 1142. In addition, the widths of the first annular gap 1142 may be the same or different, and may be partially or completely different.
The reaction middle section 12 has several groups of turbulent micro-reaction beds 121, secondary heat carrier inlets 123 and slag guide plates 124 connected in series. The turbulent micro-reaction beds 121 have a primary reaction zone 1211 therein and a secondary reaction zone 1212 is formed between adjacent turbulent micro-reaction beds 121. Specifically, the turbulent micro-reaction bed 121 comprises at least one upper baffle 1214 and at least one lower baffle 1215, a primary reaction zone 1211 is formed between the upper baffle 1214 and the lower baffle 1215, and secondary reaction zones 1212 are formed between the upper baffle 1214 and the inner wall of the housing 1 and between the lower baffle 1215 and the inner wall of the housing 1.
In this embodiment, the turbulent microreaction bed 121 includes an upper baffle 1214 and a lower baffle 1215 and is arranged symmetrically or asymmetrically in both directions about the centerline of the housing 1. In this embodiment, bidirectional symmetry is taken as an example for explanation. In addition, for convenience of illustration, an included angle β 1 between the upper surface of the upper baffle 1214 and the center line of the reactor shell 1 is defined, and the included angle β 1 is any angle between 0 ° and 180 °; the included angle beta 2 between the upper surface of the lower guide plate 1215 and the central line of the reactor shell 1 is any angle between 0 and 180 degrees; and when the angle is more than or equal to 90 degrees and less than or equal to beta 1 and less than or equal to 180 degrees, the angle is more than or equal to 0 degrees and less than or equal to beta 2 and less than or equal to 90 degrees, and correspondingly, when the angle is more than or equal to 0 degrees and less than or equal to beta 1 and less than or equal to 90 degrees, the angle is more than.
Like the material distribution plate 114, when the included angle of the upper deflector 1214 is 0 ° < β 1 ≦ 90 °, the convergence point of the upper deflector 1214 is at the bottom, and when the included angle is 90 ° < β 1 ≦ 180 °, the convergence point of the upper deflector 1214 is at the top; when the included angle of the lower guide plate 1215 is 0 degrees < beta 1< 90 degrees, the convergence point of the lower guide plate 1215 is at the bottom, and when the included angle is 90 degrees < beta 1< 180 degrees, the convergence point of the lower guide plate 1215 is at the top. In addition, the included angles β 1 and β 2 between the different upper baffle 1214 and the lower baffle 1215 and the center line of the reactor shell 1 may be the same value or different values.
A notch two 12141 with the width or the diameter of a1 (a 1 is more than or equal to 0) is arranged at the top (when the angle is more than or equal to 90 degrees and less than or equal to 1 and less than or equal to 180 degrees) or the bottom (when the angle is more than or equal to 0 degrees and less than or equal to 1 and less than or equal to 90 degrees) of the central area of the upper deflector 1214, correspondingly, an annular gap two 12142 with the width of b11 and b12 (b 11 is more than or equal to 0, b12 is more than or equal to 0) is arranged between the bottom (when the angle is more than or equal to 90 degrees and less than or equal to 1 degrees) or the top (when the angle is more than or equal to 0 degrees and less than or equal to 90 degrees) of the upper deflector 1214 and the. That is, in one embodiment, the upper baffle 1214 has the second opening 12141, but does not have the second annular gap 12142. In another embodiment, the upper baffle 1214 has two annular gaps 12142 but not has two notches 12141. In another embodiment, the upper baffle 1214 has both the second opening 12141 and the second annular gap 12142. In addition, the a1 and b11 and b12 of the baffles 1214 of each adjacent two sets of turbulent micro-reaction beds 121 may be the same value or different values.
A notch three 12151 with the width or the diameter of a2 (a 2 is greater than or equal to 0 mm) is arranged at the bottom (when 0 degrees < beta 2 is less than or equal to 90 degrees) or the top (when 90 degrees < beta 2 < 180 degrees) of the central area of the lower guide plate 1215, correspondingly, an annular gap three 12152 with the width of b21 and b22 (b 21 is greater than or equal to 0, b22 is greater than or equal to 0) is arranged between the top (when 0 degrees < beta 2 is less than or equal to 90 degrees) or the bottom (90 degrees < beta 2 < 180 degrees) of the lower guide plate 1215 and the inner wall surface of the shell 1, and the annular gap three 12152 are both passages for solid materials descending and gaseous materials ascending, and a2, b21 and b22 are not. That is, in one embodiment the lower baffle 1215 is notched three 12151, but not notched three 12152. In another embodiment, the lower baffle 1215 defines an annulus triple 12152, but does not define a gap triple 12151. In another embodiment, the lower baffle 1215 defines both a notch three 12151 and an annular space three 12152. In addition, the a2 and b21 and b22 values of the bottom baffle 1215 of each adjacent two sets of turbulent microreactors 121 may be the same or different values from each other.
To this end, the space region between the upper baffle 1214 and the lower baffle 1215 in each group of turbulent micro-reaction beds 121 is the main reaction region 1211, and the two space regions on two sides between the two adjacent groups of turbulent micro-reaction beds 121, i.e., between the lower baffle 1215 of the upper group of micro-reaction beds and the upper baffle 1214 of the lower group of micro-reaction beds, are the secondary reaction regions 1212. After the organic solid waste is subjected to stripping reaction in the turbulent micro-reaction bed 121, the organic solid waste residue materials descend and are collected on the slag guide plate 124.
The upper surface or the lower surface of the slag guide plate 124 may be a flush surface or a bent surface, and the upper surface may be straight, corrugated, or provided with a flow guide groove structure, or different combinations of these structures.
For convenience of description, an included angle β 3 is defined between the upper surface of the slag guide plate 124 and the center line of the shell 1, and the included angle β 3 may be any value between 0 ° and 180 °; when the included angle is 0 degrees < beta 3 degrees and is not more than 90 degrees, the gathering point of the material distribution plate 114 is at the bottom, and when the included angle is 90 degrees < beta 3 degrees and is not more than 180 degrees, the gathering point of the material distribution plate 114 is at the top.
A notch four 1241 with the width or the diameter of a3 (a 3 is more than or equal to 0) is arranged at the bottom (when the angle is more than 0 degrees and less than or equal to 90 degrees) or the top (when the angle is more than 90 degrees and less than or equal to 180 degrees) of the slag guide plate 124, correspondingly, an annular gap four 1242 with the width of b31 and b32 (b 31 is more than or equal to 0, b32 is more than or equal to 0) is arranged between the top (when the angle is more than or equal to 0 degrees and less than or equal to 90 degrees) or the bottom (when the angle is more than or equal to 90 degrees and less than or equal to 180 degrees) and the inner wall surface of the shell 1, and the solid pyrolysis residue outlet 134 and a heat carrier upward channel are. That is, in one embodiment, the slag guide plate 124 is provided with a notch four 1241, but is not provided with an annular gap four 1242. In another embodiment, the slag guide plate 124 is provided with an annular gap four 1242, but is not provided with a notch four 1241. In another embodiment, the slag guide plate 124 is provided with both a notch four 1241 and an annular gap four 1242.
The secondary heat carrier inlet 123 is arranged on the side surface of the shell 1 and is positioned between two adjacent groups of turbulent micro-reaction beds 121. In addition, it should be noted that, in the actual production process, the number of the secondary heat carrier inlets 123 is determined according to the composition of the organic solid waste material, the processing scale, the temperature of the gaseous organic matter pyrolysis stripping product outlet 112, and the composition of the pyrolysis solid residue outlet 134, and the number thereof may be 0, or 1 or more.
Reaction lower section 13 has heat carrier inlet 131, heat carrier distribution plate 132, residue outlet 134 and manhole 113. Specifically, two heat carrier inlets 131 are symmetrically formed and arranged on the side surface of the housing 1; the residue outlets 134 are provided with 1 and are positioned at the center of the bottom of the shell 1 and are coaxial with the central axis of the shell 1; the heat carrier distribution plate 132 is provided with one heat carrier distribution plate, the shape of the heat carrier distribution plate is matched with the shape of the cross section of the lower end of the shell 1, for convenience of description, the included angle between the upper surface of the heat carrier distribution plate 132 and the center line of the shell 1 is defined as gamma, and the included angle gamma can be any value between 0 and 90 degrees; manhole 113 is opened at the side of housing 1, which is convenient for the subsequent maintenance of the worker.
The implementation principle of the multistage series turbulent bed pyrolysis stripping reactor with the direct heat supply type heat carrier in the embodiment of the application is as follows:
the high temperature heat carrier gets into the reactor hypomere from the heat carrier import 131 of the reaction hypomere 13 of reactor, gets into the bottommost of the little reacting bed 121 of the turbulence of series connection from reactor middle section bottom after the even distribution of heat carrier distributing plate 132, flows for the pyrolysis stripping reaction that the little reacting bed 121 of turbulence carries out provides heat from bottom to top, and the pressure of high temperature heat carrier is 0.01-10MPaG, and the temperature is 300 + 1000 ℃. The heat carrier used in the present application is a single component gas (excluding oxygen) or a mixture of oxygen-poor or oxygen-free multi-component gases. Such as N2Inert gas such as argon, CO2The single component gas or the multi-component gas mixture of the gas, such as the gas, the flue gas after the combustion of superheated steam or fuel, pyrolysis tail gas, synthesis gas, refinery dry gas or petrochemical waste gas or purge tail gas and the like, has the advantages of easy availability, safety and realization of the reutilization of the waste gas.
Meanwhile, the organic solid waste enters the shell 1 from a solid waste inlet 111 of the upper reaction section 11, moves downwards by gravity, directly contacts with a mixture of the ascending gaseous pyrolysis stripping product and a heat carrier for heat exchange, and flows downwards into a material distribution plate 114 after heat absorption and preheating, and then enters the top of the middle reaction section 12 after being collected.
The preheated organic solid wastes flow from top to bottom from the top of the reaction middle section 12 and sequentially enter each group of turbulent micro-reaction beds 121, and directly contact with a mixture of a high-temperature heat carrier flowing from bottom to top and a pyrolysis stripping gaseous product to carry out pyrolysis stripping reaction; specifically, the pyrolysis stripping reaction pressure of the reactor is-0.1-10 MPaG, and the reaction temperature is 300-1000 ℃.
The mixture of descending organic solid waste and ascending high-temperature heat carrier and pyrolysis stripping gaseous product is in a fully mixed state of gas-solid two-phase turbulent suspension inside the main reaction zone 1211 and the auxiliary reaction zone 1212 for direct contact heat exchange, the organic solid waste absorbs heat carried by the high-temperature heat carrier, the organic matter is subjected to cracking reaction and stripping reaction to generate low-molecular-weight gaseous hydrocarbon substance and/or gas-phase oil product, and the gaseous mixture and the high-temperature heat carrier with step heat release and temperature reduction flows from bottom to top. The organic solid waste residue materials after completing the pyrolysis stripping reaction in the middle reaction section 12 flow downward, are collected by the slag guide plate 124, and then flow into the lower reaction section 13.
The organic solid waste solid residue materials are further collected by a heat carrier distribution plate 132 to form a material moving bed layer with a certain thickness, and directly contact with a high-temperature heat carrier which is uniformly distributed by the heat carrier distribution plate 132 and then moves upwards to exchange heat and continue to carry out pyrolysis reaction and stripping reaction, wherein the pressure of the pyrolysis stripping reaction in the shell 1 is-0.1-10 MPaG, and the reaction temperature is 300-1000 ℃; the generated gaseous reaction products go upward along with the high-temperature heat carrier, and finally the pyrolysis solid residues flow out of the shell 1 from the pyrolysis solid residue outlet 134 and enter the subsequent residue cooling and waste heat recovery processes.
In addition, according to the analysis of the temperature of the gaseous organic matter pyrolysis stripping product outlet 112 and the composition of the pyrolysis solid residue outlet 134, if the content of residual organic matter in the pyrolysis solid residue exceeds the standard, the organic solid waste pyrolysis reaction is not complete, or the temperature of the gaseous organic matter pyrolysis stripping product outlet 112 is low, the flow rate of the heat carrier can be increased from the heat carrier inlet 131 of the reaction lower section 13, the heat carrier with a certain flow rate can be added into the secondary heat carrier inlet 123, or the flow rate of the heat carrier can be increased from the heat carrier inlet 131 of the reaction lower section 13 and the heat carrier with a certain flow rate can be added into one or more of the secondary heat carrier inlets 123 at the same time.
And finally, the mixture consisting of the gaseous hydrocarbons, the gas-phase oil products and the heat carrier with stepped heat release and temperature reduction flows out of the reactor through a gaseous organic matter pyrolysis stripping product and heat carrier mixture outlet at the upper section of the reactor, and enters a subsequent working procedure of waste heat recovery and organic matter separation and recovery of the pyrolysis stripping product.
Example 2
The present embodiment is different from embodiment 1 in that the material distribution plate 114 is not disposed in the upper reaction section 11, and the organic solid waste directly falls into the upper baffle 1214 at the top of the middle reaction section 12.
Example 3
Referring to fig. 3, this embodiment is different from embodiment 1 in the structure of the turbulent micro-reaction bed 121. Each group of turbulent micro-reaction beds 121 consists of 3 upper baffles 1214 and 3 lower baffles 1215, which are bilaterally symmetrical and arranged in a step shape by taking the central line of the shell 1 as a central axis; the 3 upper deflectors 1214 can be arranged at unequal intervals or equal intervals.
The central region between the first upper baffle 1214 and the first lower baffle 1215 of each set constitutes the primary reaction zone 1211 of the set of turbulent micro-reaction beds 121; the annular space area between the 3 upper baffles 1214 and the inner wall surface of the shell 1 forms 3 secondary reaction areas 1212; the central area of the 3 upper baffles 1214 forms 3 secondary reaction zones 1212; the annular space between the second and third bottom baffles 1215 and the inside wall of the housing 1 forms 2 secondary reaction zones 1212.
Example 4
Referring to fig. 4, this embodiment is different from embodiment 1 in that the turbulent micro-reaction bed 121 has a different structure. Each group of turbulent micro-reaction beds 121 comprises a plurality of upper baffles 1214 and a plurality of lower baffles 1215, the upper baffles 1214 and the lower baffles 1215 are arranged in a unidirectional manner with respect to the inner wall surface of the shell 1, and the orientation of the upper baffles 1214 and the lower baffles 1215 is opposite. This example 4 is illustrated by using 6 series of turbulent micro-reactor beds 121 from top to bottom.
The first group of turbulent micro-reaction beds 121 consists of 1 upper baffle 1214 and 1 lower baffle 1215, and a main reaction zone 1211 is formed between the upper baffle 1214 and the lower baffle 1215 and the inner wall surface of the shell 1.
The second group of turbulent micro-reaction beds 121 consists of 2 upper baffles 1214 and 2 lower baffles 1215, and the primary reaction zone 1211 is defined by the first upper baffles 1214 and the second lower baffles 1215 and the area between the inner wall of the housing 1. Similarly, the main reaction zone 1211 is also defined by the second upper baffle 1214 and the first group of lower baffles 1215 as well as the area between the inner wall of the reactor shell 1. Meanwhile, the first upper baffle 1214 and the second lower baffle 1215 respectively constitute two secondary reaction zones 1212 with the respective ceiling regions between the inner wall surfaces of the casing 1.
The third to sixth groups of turbulent micro-reaction beds 121 (two groups are shown in the figure) are each composed of 3 upper baffles 1214 and 3 lower baffles 1215, the region between the first upper baffle 1214 and the third lower baffle 1215 of each group and the inner wall surface of the housing 1 constitutes a main reaction zone 1211, and similarly, the third upper baffle 1214 of each group and the region between the first lower baffle 1215 of the adjacent group and the inner wall surface of the housing 1 also constitute the main reaction zone 1211, and at the same time, the first and second upper baffles 1214 of each group and the first and second lower baffles 1215 of each group respectively constitute four secondary reaction zones 1212 with the respective top regions between the inner wall surface of the housing 1.
In addition, the distance between the 3 upper baffles 1214 may be the same or different, and the distance between the 3 lower baffles 1215 may be the same or different; the distance between the upper baffle 1214 and the lower baffle 1215 may be the same or different.
The above embodiments are preferred embodiments of the present application, and the protection scope of the present application is not limited by the above embodiments, so: all equivalent changes made according to the structure, shape and principle of the present application shall be covered by the protection scope of the present application.
Claims (9)
1. A heat carrier direct heat supply type multistage series turbulent bed pyrolysis stripping reactor is characterized in that: the device comprises a shell (1), wherein the shell (1) comprises a reaction upper section (11), a reaction middle section (12) and a reaction lower section (13) which are communicated with each other;
the upper reaction section (11) is provided with a solid waste inlet (111) and a product outlet (112), and the middle reaction section (12) is provided with a plurality of groups of turbulent micro-reaction beds (121) connected in series; the reaction lower section (13) is provided with a heat carrier inlet (131) and a residue outlet (134); the heat carrier and the solid waste are directly contacted in the shell (1) for heat supply;
the turbulent micro-reaction bed (121) has a main reaction zone (1211) therein, and a side reaction zone (1212) is formed between adjacent turbulent micro-reaction beds (121).
2. The heat carrier direct-heat-feeding multistage series-connection turbulent bed pyrolysis stripping reactor according to claim 1, characterized in that: the turbulent micro-reaction bed (121) comprises at least one upper baffle (1214) and at least one lower baffle (1215), a primary reaction zone (1211) is formed between the upper baffle (1214) and the lower baffle (1215), and secondary reaction zones (1212) are formed between the upper baffle (1214) and the inner wall of the shell (1) and between the lower baffle (1215) and the inner wall of the shell (1).
3. The heat carrier direct-heat-feeding multistage series-connection turbulent bed pyrolysis stripping reactor according to claim 1, characterized in that: the reaction upper section (11) is provided with a material distribution plate (114) for uniformly distributing organic solid wastes.
4. The heat carrier direct-heat-feeding multistage series-connection turbulent bed pyrolysis stripping reactor according to claim 1, characterized in that: the reaction middle section (12) is provided with a secondary heat carrier inlet (123) communicated with the inside of the shell (1).
5. The heat carrier direct-heat-feeding multistage series-connection turbulent bed pyrolysis stripping reactor according to claim 4, characterized in that: the secondary heat carrier inlet (123) is located between adjacent turbulent micro-reaction beds (121).
6. The heat carrier direct-heat-feeding multistage series-connection turbulent bed pyrolysis stripping reactor according to claim 1, characterized in that: the reaction lower section (13) is provided with a slag guide plate (124).
7. The heat carrier direct-heat-feeding multistage series-connection turbulent bed pyrolysis stripping reactor according to claim 1, characterized in that: the reaction lower section (13) is provided with a heat carrier distribution plate (132).
8. The heat carrier direct-heat-feeding multistage series-connection turbulent bed pyrolysis stripping reactor according to claim 1, characterized in that: the reaction upper section (11) and the reaction lower section (13) are both provided with manholes (113).
9. The heat carrier direct-heat-feeding multistage series-connection turbulent bed pyrolysis stripping reactor according to claim 1, characterized in that: the reaction pressure in the shell (12) is-0.1-10 MpaG, and the reaction temperature is 300-1000 ℃; the pressure of the high-temperature heat carrier is 0.01-10MPaG, and the temperature is 300-1000 ℃.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102102022A (en) * | 2010-12-31 | 2011-06-22 | 清华大学 | Moving bed reactor for medium temperature dry distillation |
| CN202465596U (en) * | 2012-03-27 | 2012-10-03 | 大庆华凯石油化工设计工程有限公司 | Multi-section type oil shale retort |
| WO2013030027A1 (en) * | 2011-08-26 | 2013-03-07 | Harinck John | A reaction apparatus and a process for the gasification of wet biomass |
| CN103119135A (en) * | 2010-07-27 | 2013-05-22 | 科廷科技大学 | A method of gasifying carbonaceous material and a gasification system |
| CN103160291A (en) * | 2011-12-09 | 2013-06-19 | 新疆美特镁业有限公司 | Powdered coal coking device and powdered coal coking method |
| CN207793166U (en) * | 2017-12-13 | 2018-08-31 | 神雾科技集团股份有限公司 | A kind of air blowing destructive distillation device |
-
2021
- 2021-03-23 CN CN202110310334.9A patent/CN113088303A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103119135A (en) * | 2010-07-27 | 2013-05-22 | 科廷科技大学 | A method of gasifying carbonaceous material and a gasification system |
| CN102102022A (en) * | 2010-12-31 | 2011-06-22 | 清华大学 | Moving bed reactor for medium temperature dry distillation |
| WO2013030027A1 (en) * | 2011-08-26 | 2013-03-07 | Harinck John | A reaction apparatus and a process for the gasification of wet biomass |
| CN103160291A (en) * | 2011-12-09 | 2013-06-19 | 新疆美特镁业有限公司 | Powdered coal coking device and powdered coal coking method |
| CN202465596U (en) * | 2012-03-27 | 2012-10-03 | 大庆华凯石油化工设计工程有限公司 | Multi-section type oil shale retort |
| CN207793166U (en) * | 2017-12-13 | 2018-08-31 | 神雾科技集团股份有限公司 | A kind of air blowing destructive distillation device |
Non-Patent Citations (2)
| Title |
|---|
| 林世雄主编: "《石油炼制工程 第3版》", 31 July 2000, 北京：石油工业出版社 * |
| 贾冬梅等主编: "《化工原理》", 31 October 2020, 北京：冶金工业出版社 * |
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