CN104232121A - Organic material retorting cracking and gasifying furnace and organic material treatment method - Google Patents
Organic material retorting cracking and gasifying furnace and organic material treatment method Download PDFInfo
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- CN104232121A CN104232121A CN201410253099.6A CN201410253099A CN104232121A CN 104232121 A CN104232121 A CN 104232121A CN 201410253099 A CN201410253099 A CN 201410253099A CN 104232121 A CN104232121 A CN 104232121A
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- organic materials
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B19/00—Heating of coke ovens by electrical means
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
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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
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Processing Of Solid Wastes (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
Abstract
The invention provides an organic material retorting cracking and gasifying furnace, which comprises a cracking and gasifying furnace body, a plurality of retorting chambers and an electric heating rod, wherein a feed inlet and a gas outlet are formed in the cracking and gasifying furnace body; the plurality of retorting chambers are arranged in the cracking and gasifying furnace body side by side, and every two adjacent retorting chambers are isolated, and a material discharge outlet is formed in the bottom of each retorting chamber; the electric heating rod is vertically arranged in the plurality of retorting chambers to perform air-isolated retorting to materials in the plurality of retorting chambers so as to generate a solid carbon material and retorting gas. According to the organic material retorting cracking and gasifying furnace provided by the embodiment of the invention, the existing organic materials such as garbage and low-rank coal can be furthest utilized without pollution, and the organic materials can be utilized to the greatest extent. In addition, the invention further provides an organic material treatment method.
Description
Technical field
The present invention relates to organic materials processing technology field, especially relate to a kind of the organic materials carbonization decomposition vapourizing furnace and the treatment process that process organic materials.
Background technology
For domestic refuse, the burning disposal mode that tradition adopts all can produce dioxin and adjoint heavy metal contamination in gas and waste residue.And need oil spout combustion-supporting in burning disposal process, directly cause processing cost too high.
In addition, how by the inflammable gas in foam coal and tar extraction out as everyone knows, the utilization ratio of foam coal is much lower relative to lump coal, low order low-rank coal foam becomes high-quality smokeless fuel is simultaneously China and even a great problem in the world, the in addition resinous shale foam similar with foam coal facies.
For above-mentioned organic materials, how pollution-free and carry out processing to reach organic materials at low cost and make full use of, be the technical barrier that this area faces.
Summary of the invention
The present invention is intended at least to solve one of technical problem existed in prior art.
The present invention needs to provide a kind of organic materials carbonization decomposition vapourizing furnace, and described organic materials carbonization decomposition vapourizing furnace can at utmost contamination-freely utilize conventional example as the organic materials of rubbish, low-rank coal foam etc., farthest to utilize this organic materials.
In addition, the present invention needs to provide a kind of organic materials treatment process, and described organic materials treatment process can make the impact of organic materials on environment minimum, and organic materials utility value can be made to maximize.
The organic materials carbonization decomposition vapourizing furnace of embodiment, comprising: pyrolysis gasification body of heater according to a first aspect of the present invention, and described pyrolysis gasification body of heater is provided with opening for feed and air outlet; Multiple destructive distillation room, described multiple destructive distillation rooms juxtaposition is in described pyrolysis gasification body of heater, and spaced apart between adjacent two destructive distillation rooms, is equipped with discharge gate bottom each described destructive distillation room; And electrically heated rod, it is indoor to carry out isolated air destructive distillation, to produce solid carbonaceous material and carbonization gas to the material of described multiple destructive distillation indoor that described electrically heated rod is located at described multiple destructive distillation vertically.
Organic materials carbonization decomposition vapourizing furnace according to an embodiment of the invention, can effectively contamination-freely processing example as domestic refuse, low-rank coal foam or resinous shale foam etc., thus realize organic materials be worth utilize maximize.
The organic materials treatment process of embodiment comprises the following steps according to a second aspect of the present invention: S1, described organic materials carried out isolated air and lower than the low temperature pyrogenation destructive distillation of 650 degrees Celsius, to produce solid materials, carbonization gas and tar; S2, washing, purifying is carried out to remove tar to described carbonization gas; S3, the described carbonization gas after washing, purifying in step S2 carried out to elementary de-oiling, dehydration, desulfurization, de-naphthalene, to obtain clean gas.
By adopting according to organic materials treatment process of the present invention, by magazins' layout such as the tar in organic materials, dusts out, and de-oiling, dehydration, desulfurization, de-naphthalene can be carried out, and obtain clean gas, finally can obtain clean gas, industry and civilian combustible gas use standard can be reached.
Additional aspect of the present invention and advantage will part provide in the following description, and part will become obvious from the following description, or be recognized by practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or additional aspect of the present invention and advantage will become obvious and easy understand from accompanying drawing below combining to the description of embodiment, wherein:
Fig. 1 is the schematic diagram of organic materials carbonization decomposition vapourizing furnace according to an embodiment of the invention;
Fig. 2 is the schematic diagram of the distribution device of organic materials carbonization decomposition vapourizing furnace according to an embodiment of the invention;
Fig. 3 is the schematic diagram of elementary according to an embodiment of the invention carbonization gas washing tower;
Fig. 4 is the schematic diagram of secondary carbonization gas washing tower according to an embodiment of the invention;
Fig. 5 is the schematic diagram of self-cleaning according to an embodiment of the invention heat-exchange equipment; And
Fig. 6 is the schema of organic materials treatment process according to an embodiment of the invention.
Embodiment
Be described below in detail embodiments of the invention, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has element that is identical or similar functions from start to finish.Being exemplary below by the embodiment be described with reference to the drawings, only for explaining the present invention, and can not limitation of the present invention being interpreted as.
In describing the invention, it will be appreciated that, term " on ", D score " vertically ", " level ", " top ", " end ", " interior ", the orientation of the instruction such as " outward " or position relationship be based on orientation shown in the drawings or position relationship, only the present invention for convenience of description and simplified characterization, instead of indicate or imply that the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore can not be interpreted as limitation of the present invention.In addition, term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance or imply the quantity indicating indicated technical characteristic.Thus, be limited with " first ", the feature of " second " can express or impliedly comprise one or more these features.In describing the invention, except as otherwise noted, the implication of " multiple " is two or more.
In describing the invention, it should be noted that, unless otherwise clearly defined and limited, term " installation ", " being connected ", " connection " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or connect integratedly; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals.For the ordinary skill in the art, particular case above-mentioned term concrete meaning in the present invention can be understood.
As shown in figs 1 to 6, organic materials carbonization decomposition vapourizing furnace 100, carbonization gas washing plant and self-cleaning heat-exchange equipment 300 is comprised according to the organic materials treatment system of the embodiment of the present invention.
First it should be noted that, in the description of embodiments of the invention: shown in the arrow in " above-below direction " such as Fig. 1, Fig. 3-Fig. 5.But also it should be noted that, the instruction in this direction is for exemplary purposes, instead of in order to limit the scope of the invention.
According to the organic materials treatment system of the embodiment of the present invention, this organic materials treatment system can be used for the organic materialss such as process domestic refuse, straw, low-rank coal foam and/or resinous shale foam.And in description below the disclosure, be described for the treatment of low-rank coal foam and/or resinous shale foam for organic materials treatment system.Need to further illustrate, low order low-rank coal foam refers to all not adhesive brown coal, bituminous coal and hard coal herein.
Certainly, those skilled in the art are appreciated that, this organic materials treatment system is only exemplarily described for the treatment of low-rank coal foam and/or resinous shale foam, and be not limited thereto, organic materials treatment system according to the present invention also can be used for the pending material processing other types, the organic materials mixtures such as the byproduct schlempe of such as agricultural byproducts stalk, cotton stalk, wine brewing and vinasse, plant leaves, industrial refuse and medical waste.
As depicted in figs. 1 and 2, the top of organic materials carbonization decomposition vapourizing furnace 100 has opening for feed and air outlet and the bottom of organic materials carbonization decomposition vapourizing furnace 100 has discharge gate, wherein organic materials enters in organic materials carbonization decomposition vapourizing furnace 100 from opening for feed and carries out isolated air destructive distillation and organic materials is discharged from discharge gate, and the carbonization gas of generation is discharged from air outlet.Wherein, the composition of carbonizing gas comprises other mixing of methane, hydrogen, hydrocarbon polymer, carbon monoxide and the Multiple components such as trace nitrogen, oxygen.
As shown in Figure 3 and Figure 4, carbonization gas washing plant is connected to the downstream of organic materials carbonization decomposition vapourizing furnace 100 and carries out reception and washing, purifying to the carbonization gas of discharging from air outlet.
As shown in Figure 5, self-cleaning heat-exchange equipment 300 is connected to the downstream of carbonization gas washing plant to process the carbonization gas after washing, purifying to obtain clean flammable carbonizing gas, and this is flammable, and carbonizing gas can supply industry and gas by Some substitute Sweet natural gas.
According to the organic materials treatment system of the embodiment of the present invention, carry out destructive distillation by first organic materials being passed into organic materials carbonization decomposition vapourizing furnace 100 and producing carbonization gas, again carbonization gas is passed into successively in carbonization gas washing plant and self-cleaning heat-exchange equipment 300, carry out washing, purifying and process, finally can obtain clean flammable carbonizing gas, the impact of organic materials on environment can be reduced thus, and by the above-mentioned treating processes to organic materials, the flammable energy can also be obtained, thus the maximization of organic materials utility value can be made.
Referring to Fig. 1, describe the organic materials carbonization decomposition vapourizing furnace 100 according to the embodiment of the present invention in detail, as shown in Figure 1, this organic materials carbonization decomposition vapourizing furnace 100 comprises pyrolysis gasification body of heater 110, multiple destructive distillation room 120 and electric heater unit.In one embodiment of the invention, this electric heater unit can be electrically heated rod 130.
Opening for feed and air outlet are formed in the top of pyrolysis gasification body of heater 110.With reference to Fig. 1, the spatial accommodation holding and treat destructive distillation material is limited in pyrolysis gasification body of heater 110, the top of pyrolysis gasification body of heater 110 has opening for feed to feed the material treating destructive distillation in spatial accommodation, and the top of pyrolysis gasification body of heater 110 is had air outlet and discharged by this air outlet with gas destructive distillation obtained.
Multiple destructive distillation room 120 is located in pyrolysis gasification body of heater 110 side by side, and spaced apart by partition wall 121 between adjacent two destructive distillation rooms 120, is equipped with discharge gate 122 bottom each destructive distillation room 120.In the example of fig. 1, multiple destructive distillation rooms 120 are located at the bottom of pyrolysis gasification body of heater 110 in parallel with each other, spaced apart by partition wall 121 between adjacent destructive distillation room 120, the top of destructive distillation room 120 is opened wide to receive the material fallen from top, and the bottom of each destructive distillation room 120 all has powder that discharge gate 122 uses with solid matter destructive distillation obtained such as smokeless fuel or building trade and the additive etc. that cement industry uses is discharged from this discharge gate 122.It is to be appreciated that the quantity of destructive distillation room 120 can be arranged according to actual requirement, to have better destructive distillation effect.
Electrically heated rod 130 is located in multiple destructive distillation room 120 vertically to carry out isolated air destructive distillation to produce solid carbonaceous material, carbonization gas and tar to the material in multiple destructive distillation room 120.Such as in the example of fig. 1, electrically heated rod 130 is provided with all vertically in each destructive distillation room 120, electrically heated rod 130 is respectively to treating that destructive distillation material carries out isolated air destructive distillation in each destructive distillation room 120, that is, treat the such as organic materials completely isolated air destructive distillation in retort process of destructive distillation material, obtain solid carbonaceous material, carbonization gas and tar.It is to be appreciated that the temperature of destructive distillation indoor can arbitrarily regulate with organic materials different in kind.And electrically heated rod 130 is located in multiple destructive distillation room 120 vertically, than the horizontally disposed situation of electrically heated rod 130, can prevents material from falling and make electrically heated rod 130 flexural deformation.It should be noted that, in one embodiment of the invention, electrically heated rod 130 also can flatly be arranged, fully to heat organic materials.
Specifically, electrically heated rod 130 can use interchange or DC voltage power supply to carry out isolated air destructive distillation to produce high-temperature hot gas with the material treating destructive distillation.Particularly, electrically heated rod 130 comprises electrical heating wire and is set in its outer insulation layer.Because which output gas heating value is higher, such as low-rank coal foam and/or resinous shale foam every side's gas calorific value are more than 4000 kilocalories, tolerance is larger, such as aerogenesis per ton more than 400 cubes, often process one ton of low-rank coal foam and/or resinous shale foam, electrically heated rod consume electric energy and only account for gas production rate per ton and produce the sub-fraction of calorific value, therefore running cost is lower.For the organic materials of such as domestic refuse, by the gas of which output every side's gas calorific value more than 6000 kilocalories, tolerance is larger, such as aerogenesis per ton more than 800 cubes, often process one ton of domestic refuse, electric heater such as electrically heated rod consume electric energy and only account for gas production rate per ton and produce the sub-fraction of calorific value, therefore running cost is lower.
Treat that the organic materials of destructive distillation enters organic materials carbonization decomposition vapourizing furnace 100 and carries out destructive distillation, discharge the powder of smokeless fuel product or building trade use and the additive of cement industry use, produce carbonizing gas and tar products continuously simultaneously, the carbonizing gas wherein produced can be inflammable gas, this inflammable gas can be used for the generating of internal combustion generator group, also can replace town gas or Sweet natural gas for user directly.
According to the organic materials carbonization decomposition vapourizing furnace 100 of the embodiment of the present invention, isolated air destructive distillation process can be carried out to organic materials, not only environmental friendliness and also cost low, can existing resource be made full use of.See for the industrial experiment result of low order matter coal foam and resinous shale foam, combustiblecomponents in these two kinds of materials all can be decomposed out according to organic materials treatment system of the present invention, for Hami mire hair lake brown coal, inflammable gas can all be separated out and part precipitation does not have foeign element to produce new ash content.Raw coal enters stove and smokeless fuel comes out of the stove material ratio by (being referred to air dried basis coal foam) about 1.6:1 ton, and discharge device is for doing material system device, and without any water content consumption, the smokeless fuel of discharge is low temperature siccative.The light-end products rate of recovery is that raw material oil product content reaches 98%, and is all light-end products, and proportion is about 0.9.Brown coal inflammable gas productive rate is at 400m
3/ t raw coal, calorific value is at 17-33MJ/m
3left and right.
When carrying out isolated air destructive distillation process to the organic materials of such as domestic refuse, dioxin can not be produced in the gas that destructive distillation obtains and polity's ejecta, and heavy metal free pollutes, the solid ejecta of output can as smokeless fuel, combustion-supporting without the need to oil spout, not only environmental friendliness but also with low cost, thus make full use of existing resource.
In addition, this organic materials carbonization decomposition vapourizing furnace 100 is easy to use, starts to produce and stop production process simple, and technique whole process can realize Automated condtrol.
In one embodiment of the invention, multiple destructive distillation room 120 is arranged side by side in the horizontal direction, and each destructive distillation room 120 extends along the vertical direction, as shown in Figure 1.
In one embodiment of the invention, organic materials carbonization decomposition vapourizing furnace 100 also comprises: top feed bin 141 and automatic feeding device 142.
The top of top feed bin 141 is opened wide, and the bottom of top feed bin 141 is communicated with the opening for feed of pyrolysis gasification body of heater 110.Such as in the example of fig. 1, top feed bin 141 is located at the top of pyrolysis gasification body of heater 110, the top of top feed bin 141 opens wide to treat that the top of the material of destructive distillation from top feed bin 141 feeds, the bottom of top feed bin 141 is connected with the opening for feed of pyrolysis gasification body of heater 110, to be fed in pyrolysis gasification body of heater 110 by this opening for feed by the material in top feed bin 141, such as top feed bin 141 is formed as doline.Certainly, the present invention is not limited thereto, in other example of the present invention, top feed bin 141 also can be formed as cylindrical, the cylindroid bodily form, the long cylinder bodily form or the prism bodily form etc.
With reference to Fig. 1, automatic feeding device 142 is located between the bottom of top feed bin 141 and the opening for feed of pyrolysis gasification body of heater 110 and feeds in pyrolysis gasification body of heater 110 with the material controlled in top feed bin 141.In the example of fig. 1, automatic feeding device 142 is for being located at the valve on the pipeline between the bottom of top feed bin 141 and the opening for feed of pyrolysis gasification body of heater 110.Further, automatic feeding device 142 is motorized valve.
Further, the opening for feed place of pyrolysis gasification body of heater 110 is provided with the distribution passage 150 for distributing material further.With reference to Fig. 1, between the bottom that distribution passage 150 is located at top feed bin 141 and the top of body of heater, to distribute the material fed in body of heater.
Particularly, distribute passage 150 and be formed as down Y shape, and distribution passage 150 comprises upper channel 151, first lower channel 153 and the second lower channel 152 that communicate with each other.Wherein the top of upper channel 151 is communicated with the bottom of top feed bin 141, and the bottom of the first lower channel 153 and the second lower channel 152 is led in pyrolysis gasification body of heater 110 respectively.
Such as in the example of fig. 1, upper channel 151 extends along the vertical direction, and the top of upper channel 151 is connected with the bottom of top feed bin 141, the bottom of upper channel 151 is connected with the top of the second lower channel 152 with the top of the first lower channel 153 respectively, particularly, first lower channel 153 is oblique left-hand downward-extension first, extend straight down again, under the first oblique dextrad of second lower channel 152, extend straight down again, first lower channel 153 is connected with the top of pyrolysis gasification body of heater 110 respectively with the bottom of the second lower channel 152 and communicates with the spatial accommodation of pyrolysis gasification body of heater 110, will treat that destructive distillation material passes in pyrolysis gasification body of heater 110 in top feed bin 141.
In one embodiment of the invention, organic materials carbonization decomposition vapourizing furnace 100 comprises further: distribution device 160, and distribution device 160 is located at below opening for feed and distributes with the material fed opening for feed.See figures.1.and.2, in the spatial accommodation that distribution device 160 is located at pyrolysis gasification body of heater 110, be positioned at the top of spatial accommodation, to be distributed to equably by the material fed from top feed bin 141 in multiple destructive distillation rooms 120 of below.
Further, as depicted in figs. 1 and 2, distribution device 160 comprises strut member 161 and multiple backgauge part 162.Strut member 161 extends along the longitudinal direction (left and right directions as shown in Figure 1) of pyrolysis gasification body of heater 110.
One end of each backgauge part 162 is connected on strut member 161, and the other end of each backgauge part 162 extends to the inwall place of contiguous pyrolysis gasification body of heater 110.See figures.1.and.2, multiple backgauge part 162 is spaced apart from each other setting, and each backgauge part 162 all extends from a side wall surface of strut member 161 towards the direction of the inwall of pyrolysis gasification body of heater 110, it will be appreciated that, one end away from strut member 161 of backgauge part 162 can be tried one's best near the inwall of pyrolysis gasification body of heater 110, to have good cloth effect.
Further, multiple backgauge part 162 comprises multiple first gear materials and parts and multiple second gear materials and parts, multiple first gear materials and parts and multiple second gear materials and parts are spaced apart from each other along the length direction of strut member 161 respectively, and multiple first gear materials and parts and multiple second gear materials and parts spaced apart predetermined distance on the width of strut member 161.
In one of them example of the present invention, multiple first gear materials and parts and multiple second gear materials and parts are difference one_to_one corresponding on the length direction of strut member 161, as shown in Figure 2.Certainly, the present invention is not limited thereto, in other examples of the present invention, multiple first gear materials and parts and multiple second gear materials and parts also can on the length direction of strut member 161 staggered arrangement (scheming not shown).
Further, such as in the example of fig. 1 and 2, backgauge part 162 transversely (fore-and-aft direction as shown in Figure 1) extends, and now backgauge part 162 is substantially vertical with strut member 161, that is, the angle between strut member 161 and each backgauge part 162 is roughly in 90 °.But, in other examples of the present invention, backgauge part 162 is also tiltably connected on strut member 161, angle now between strut member 161 and each backgauge part 162 is roughly between 0 ° ~ 90 ° or 90 ° ~ 180 °, here, it should be noted that, the angle between strut member 161 and each backgauge part 162 does not comprise 90 °.
Further, multiple backgauge part 162 is evenly distributed on the both lateral sides of strut member 161.In other words, as depicted in figs. 1 and 2, spaced apart from roughly equal between backgauge part 162 adjacent one another are on the length direction of strut member 161.
In an example of the present invention, strut member 161 is identical with the shape of backgauge part 162, particularly, as shown in Figure 2, each in strut member 161 and backgauge part 162 includes symmetrically arranged first plate and the second plate on cross section, and the first plate and the second plate upper end connect and form the angle of 30-180 degree between the first plate and the second plate.
Further, strut member 161 is formed with ventilating pit, ventilating pit is connected with the vertical ventpipe 163 extended, wherein air outlet is made up of ventpipe 163.Such as in the example of fig. 1 and 2, the center of top of strut member 161 is formed with the ventilating pit running through it, ventpipe 163 vertically extends, and the bottom of ventpipe 163 is connected with ventilating pit, its top is connected with the top of pyrolysis gasification body of heater 110, the carbonizing gas produced after destructive distillation is discharged via ventpipe 163, and the composition of carbonizing gas can comprise methane, hydrogen, hydrocarbon polymer, carbon monoxide, carbonic acid gas, nitrogen etc.Certainly, the present invention is not limited thereto, in other example of the present invention, strut member 161 also can be formed with multiple ventilating pit, multiple ventilating pit is connected to the ventpipe 163 (scheming not shown) of multiple vertical extension.
In one embodiment of the invention, organic materials carbonization decomposition vapourizing furnace 100 comprises further: multiple automatic-sealed discharge device 170, and the discharge gate 122 that multiple automatic-sealed discharge device 170 is located at multiple destructive distillation room 120 respectively sentences opening and closing discharge gate 122.As shown in Figure 1, multiple automatic-sealed discharge device 170 is located at the bottom of multiple destructive distillation room 120 respectively, and when automatic-sealed discharge device 170 is in open mode, the solid matter that in pyrolysis gasification body of heater 110, destructive distillation obtains can be discharged via discharge gate 122.
Further, with reference to Fig. 1, organic materials carbonization decomposition vapourizing furnace 100 also comprises sealing discharging storehouse 180 and chain type discharge device 200.Sealing discharging storehouse 180 is located at the bottom of pyrolysis gasification body of heater 110, and sealing discharging storehouse 180 is communicated with pyrolysis gasification body of heater 110 inside, wherein the bottom of multiple destructive distillation room 120 extend in sealing discharging storehouse 180, and the solid matter that destructive distillation obtains falls in sealing discharging storehouse 180 after discharging via discharge gate 122.
Chain type discharge device 200 is located in sealing discharging storehouse 180 to be received from the material of dynamic seal discharge device 170 discharge and to be discharged.
Further, organic materials carbonization decomposition vapourizing furnace 100 also comprises: support frame of furnace body 190, to support body of heater on the outer side wall that support frame of furnace body 190 is located at lower portion of furnace body.Such as in the example of fig. 1, support frame of furnace body 190 is located at the bottom of body of heater, and is positioned at the top in sealing discharging storehouse 180.
The working process of organic materials carbonization decomposition vapourizing furnace 100 is as follows: treat that the material of destructive distillation enters in organic materials carbonization decomposition vapourizing furnace 100 continuously, run into the high temperature hot gas risen by bottom and carry out reverse exchange, the moisture that removing material outside is carried, drying and destructive distillation is carried out respectively in multiple destructive distillation rooms 120 below material is advanced under continuing, continuous carbonization thermal source is provided by the electrically heated rod in destructive distillation room 120, the powder that the solid matter that destructive distillation afterwards obtains such as smokeless fuel or building trade use and the additive etc. that cement industry uses are discharged by the automatic-sealed discharge device 170 bottom pyrolysis gasification body of heater 110, the gas that destructive distillation obtains is discharged via the ventpipe 163 above pyrolysis gasification body of heater 110.
In some embodiments of the invention, organic materials treatment system also can comprise primary screen subset (scheming not shown), and primary screen subset is connected to the upstream of organic materials carbonization decomposition vapourizing furnace 100 to sieve pending organic materials.Such as, in some embodiments of the invention, for low-rank coal foam and/or resinous shale foam, the particle diameter of coal foam or resinous shale foam can be screened as being not more than 5mm, to carry out destructive distillation better.
Particularly, this primary screen subset can comprise strip-type screen (scheming not shown), and strip-type screen is for screening out a part of heavy seeds in pending organic materials.Particularly, a small amount of heavy seeds using strip-type screen can go out based on metal.
In some embodiments of the invention, organic materials treatment system also comprises the dewatering unit (scheming not shown) for dewatering to organic materials, and dewatering unit is located between primary screen subset and organic materials carbonization decomposition vapourizing furnace 100.Particularly, the impurity after primary screen subset screens out can carry out processed in dewatering unit.
In some embodiments of the invention, when organic materials is live rubbish, agricultural byproducts stalk, cotton stalk, the byproduct schlempe of wine brewing and vinasse, plant leaves, industrial refuse, medical waste, low-rank coal foam, resinous shale foam or its mixture, organic materials treatment system also comprises molding device (scheming not shown), molding device be located between dewatering unit and organic materials carbonization decomposition vapourizing furnace 100 with by dehydration after organic materials mixing moulding.
As shown in Figure 3, in some embodiments of the invention, carbonization gas washing plant can comprise elementary carbonization gas washing tower 210.Particularly, as shown in Figure 3, elementary carbonization gas washing tower 210 can comprise the first tower body 211 and flashback tank 212.
Wherein, the top of the first tower body 211 has the first carbonization gas entrance 2111, through the carbonization gas that organic materials carbonization decomposition vapourizing furnace 100 produces, after discharging from the air outlet of organic materials carbonization decomposition vapourizing furnace 100, can enter in the first tower body 211 via this first carbonization gas entrance 2111 and wash.And the top of the first tower body 211 has the first recirculated water entrance 2112, what be worth understanding is, this the first recirculated water entrance 2112 is positioned at above the first carbonization gas entrance 2111, to make the carbonization gas entered from the first carbonization gas entrance 2111, through mixing with the recirculated water that the first recirculated water entrance 2112 from the upper side flows into, thus complete washing.Elementary carbonization gas washing tower 210 can remove most of dust, heavy wet goods in carbonization gas.
As shown in Figure 3, the middle part of the first tower body 211 can be provided with the first carbonization gas outlet 2113, through the carbonization gas of washing in the first tower body 211, can discharge from this first carbonization gas outlet 2113 and proceed the operation in downstream.The bottom of the first tower body 211 is provided with water oil-in 2114, through organic materials carbonization decomposition vapourizing furnace 100 produce carbonization gas the first tower body 211 in wash after, water-oil mixture body can be produced, this mixed solution can enter into the flashback tank 212 being arranged in the first tower body 211 bottom from this water oil-in 2114, namely flashback tank 212 is communicated with by this water oil-in 2114 with the first tower body 211, wherein, the top of flashback tank 212 is formed with the first tar overflow port 2121, when water-oil mixture body flow in flashback tank 212, and when liquid level slowly rises to the first tar overflow port 2121, water-oil mixture can overflow from this first tar overflow port 2121 and can collect it, in order to avoid too much water-oil mixture stores too much and is guided in the first tower body 211 from water oil-in 2114 in this flashback tank 212.
Preferably, as shown in Figure 3, elementary carbonization gas washing tower 210 can also be provided with water dispenser box 213.This water dispenser box 213 can be located at the top of the first tower body 211, and the first recirculated water entrance 2112 is located on water dispenser box 213.Particularly, this the first recirculated water entrance 2112 can be located at the top of water dispenser box 213, the diapire of water dispenser box 213 or sidewall can be provided with multiple water dispenser mouth, from the recirculated water that the first recirculated water entrance 2112 flows into, can flow out from multiple water dispenser mouth, thus, recirculated water can flow to the first tower body 211 inside from multiple directions and clean carbonization gas, in other words, at the top of the first tower body 211, water dispenser box 213 is set, thus can distribute equably recirculated water, improve the contact area of recirculated water and carbonization gas, clean more even.
In embodiment more of the present invention, elementary carbonization gas washing tower 210 can also comprise multiple first Venturi meter 214, multiple first water spray pipe 215 and the second Venturi meter 216.Particularly, multiple first Venturi meter 214, multiple first water spray pipe 215 and the second Venturi meter 216 can all be located in the first tower body 211.
Wherein, as shown in Figure 3, multiple first Venturi meter 214 can be arranged side by side and each first Venturi meter 214 vertically extends in direction, and the top of multiple first Venturi meter 214 can lower than the first carbonization gas entrance 2111.Further, one end (upper end such as shown in Fig. 3) of each first water spray pipe 215 is connected with water dispenser box 213, particularly, each first water spray pipe 215 upper end can be connected on the multiple water dispenser mouths on water dispenser box 213, and each first water spray pipe 215 the other end (lower end such as shown in Fig. 3) can stretch in corresponding first Venturi meter 214 to rinse the carbonization gas entered from the first carbonization gas entrance 2111.That is, multiple first water spray pipe 215 is arranged one to one with multiple first Venturi meter 214, like this, from the carbonization gas that the first carbonization gas entrance 2111 enters, can enter into respectively in multiple the first Venturi meter 214 be arranged side by side, and rinse under the sprinkling of the first water spray pipe 215 in each first Venturi meter 214.
Wherein, the second Venturi meter 216 can be positioned at below multiple first Venturi meter 214, the carbonization gas after rinsing respectively from multiple first Venturi meter 214, can carry out collecting in the second Venturi meter 216 and to the lower flow of the first tower body 211.
In some embodiments of the invention, carbonization gas washing plant can also comprise secondary carbonization gas washing tower 220.Secondary carbonization gas washing tower 220 can be located at the downstream of elementary carbonization gas washing tower 210.
Particularly as shown in Figure 4, secondary carbonization gas washing tower 220 comprises the second tower body 221, second water spray pipe 222 and multiple distribution heat exchange tower tray 223.The bottom of the second tower body 221 has the second carbonization gas entrance 2211, can enter in secondary carbonization gas washing tower 220 carry out secondary washing from the carbonization gas of the first carbonization gas outlet 2113 discharge of elementary carbonization gas washing tower 210 from the second carbonization gas entrance 2211.The top of the second tower body 221 can be provided with the second carbonization gas outlet 2212, and the carbonization gas after the washing of secondary carbonization gas washing tower 220 can be discharged from this second carbonization gas outlet 2212, and proceeds the operation in downstream.Wherein, secondary carbonization gas washing tower 220 can from the lightweight oil removing carbonization gas and the washing liq being unfavorable for burning.
Alternatively, as shown in Figure 4, the second carbonization gas entrance 2211 is connected with dry main 226, and the other end of dry main 226 extends upwardly to the top exceeding the second tower body 221.Like this, carbonization gas can flow in the second tower body 221 from dry main 226, the carbonization gas entered in the second tower can be made thus first to flow through one section of pipeline and cool after discharging from elementary carbonization gas washing tower 210, improves cleaning performance.
Wherein, the second water spray pipe 222 can be provided with from the middle part of the second tower body 221 and insert into the inner, and recirculated water can flow into from this second water spray pipe 222 and be sprayed onto the second his tower body.Advantageously, second water spray pipe 222 can be multiple and interval is arranged, and each second water spray pipe 222 can be provided with multiple isolated water and spray mouth, can make thus recirculated water more all be sprayed onto in the second tower, and then the homogeneity of the flushing to carbonization gas can be improved.
As shown in Figure 4, multiple distribution heat exchange tower tray 223 can arrange along the radial direction of the second tower body 221 and be spaced apart from each other along the vertical direction.In other words, each distribution heat exchange tower tray 223 can be arranged along the radial direction of the second tower body 221, and multiple distribution heat exchange tower tray 223 can be spaced apart from each other respectively along the vertical direction.Here what deserves to be explained is, the complicated component of carbonization gas is various, the density of the gas of each composition is different, can cause thus in the second tower body 221, the gaseous constituent that density is little can rise to the second tower body 221 top rapidly, and the speed that the large gaseous constituent of density rises relatively is slower, the second tower body 221 is discharged with mixing in order to enable multicomponent gas, can arrange along the radial direction of the second tower body 221 thus and distribute heat exchange tower tray 223, distribute heat exchange tower tray 223 thus and can play to zooming gas the effect kept out, multi-component gas continues to rise after can mixing in the below distributing heat exchange tower tray 223 again.Further, by arranging multiple multiple distribution heat exchange tower tray 223 is set along the vertical direction, thus can multi-component gas through repeatedly mixing, finally discharge from the second carbonization gas outlet 2212 again.
Alternatively, secondary carbonization gas washing tower 220 can also comprise water seal cylinder 224 and washings liquid discharge pipe 225.As shown in Figure 4, the top of water seal cylinder 224 has the second tar overflow port 2241, one end (upper end in such as Fig. 4) of washings liquid discharge pipe 225 is communicated with the bottom of the second tower body 221, and the second end of washings liquid discharge pipe 225 (lower end in such as Fig. 4) extend into the bottom in water seal cylinder 224, the lower end of water seal cylinder 224 lower than the lower end of the second tower body 221 so that the water of condensation in the second tower body 221 is discharged in water seal cylinder 224.And by arranging the second tar overflow port 2241, thus can to make to be pooled in water seal cylinder 224 to a certain degree, namely when liquid level is more than the second tar overflow port 2241, washings can be discharged from this second tar overflow port 2241 and can collect it, in order to avoid washings is got back in the second tower body 221 from washings liquid discharge pipe 225 adverse current.
As shown in Figure 4, in a preferred exemplary of the present invention, the bottom of the second tower body 221 can also be provided with cleanout opening 2213, and cleanout opening 2213 is lower than one end of washings liquid discharge pipe 225.By arranging this cleanout opening 2213, thus operator can carry out the cleaning of impurity from this cleanout opening 2213, facilitate bottom impurity or pollutant sediment to the second tower body 221, even block washings liquid discharge pipe 225.
As shown in Figure 5, self-cleaning heat-exchange equipment 300 can be located at the downstream of secondary carbonization gas washing tower 220, self-cleaning heat-exchange equipment 300 comprises the self-cleaning interchanger 310 of at least one-level, and each self-cleaning interchanger 310 comprises housing 311, multiple heat transfer tube 312, gas filter 313 and multiple self-cleaning heat exchange tower tray 314.
Square tube shape gas compartment directed along the vertical direction can be had in housing 311, the top of housing 311 has pneumatic outlet 3111, carbonization gas after clean in self-cleaning heat-exchange equipment 300 can be discharged from this pneumatic outlet 3111, the bottom of housing 311 has gas inlet 3112, like this, the carbonization gas of discharging from secondary carbonization gas washing tower 220 can flow into self-cleaning heat-exchange equipment 300 from this gas inlet 3112 and clean.
Multiple heat transfer tube 312 is distributed as the multilayer be spaced apart from each other in the vertical direction, and each heat transfer tube 312 can be configured to transversely (direction perpendicular with above-below direction in such as Fig. 5) and be configured to plum blossom-shaped.Be connected with water coolant in each heat transfer tube 312, thus, from gas inlet 3112 flow out carbonization gas upwards flow, and with each heat exchange after carry out heat exchange, cooled.Gas filter 313 is located at bottom in housing 311 and higher than gas inlet 3112 with to the gas filtration entered in housing 311, multiple self-cleaning heat exchange tower tray 314 arranges along the radial direction of housing 311 and is spaced apart from each other along the vertical direction, and wherein each self-cleaning heat exchange tower tray 314 can be arranged on wherein between two-layer heat transfer tube 312.Similar with the distribution heat exchange tower tray 223 in secondary carbonization gas washing tower 220, by arranging self-cleaning heat exchange tower tray 314, thus the multi-component gas of rising can be made to mix rear discharge.
Wherein, the bottom of housing 311 is provided with washings relief outlet 3113, and wherein gas inlet 3112 is higher than washings relief outlet 3113, thus, can discharge washings from this washings relief outlet 3113.
In a concrete example of the present invention, as shown in Figure 4, self-cleaning heat exchange tower tray 314 comprises three.Under other prerequisites mixed of guarantee multicomponent, equipment investment can be reduced, reduces costs thus.
As shown in Figure 5, in an alternate exemplary of the present invention, housing 311 can have cooling water connector 3114, cooling water connector 3114 is communicated with to feed water coolant with multiple heat transfer tube 312.
The outer wall of housing 311 is also provided with water wall 315.Can water coolant be passed into this on this water wall 315, to carry out heat exchange with the carbonization gas in self-cleaning heat-exchange equipment 300 further, make it cool.
In some embodiments of the invention, each self-cleaning interchanger 310 can also comprise outlet and flutters day with fog 316, self-cleaning uniform divider 317 and desulfurizing scrubber 318.
Outlet is flutterred day with fog 316 and to be located in housing 311 and to be arranged in below pneumatic outlet 3111 and be separated with the drop be mingled with gas, self-cleaning uniform divider 317 is located at above multiple heat transfer tube 312 to carry out uniformly distributing to the gas in housing 311, desulfurizing scrubber 318 to be located in housing 311 and to flutter between day with fog 316 and self-cleaning uniform divider 317, to carry out desulfurization to gas in outlet.
That is, pneumatic outlet 3111, outlet are flutterred day with fog 316, desulfurizing scrubber 318, self-cleaning uniform divider 317 and self-cleaning heat exchange tower tray 314 and are arranged in order from top to bottom.
Gas inlet 3112 is connected with dry main 226, and the other end of dry main 226 extends upwardly to the top exceeding housing 311.Thus, from the carbonization gas that secondary carbonization gas washing tower 220 is discharged, can first lower the temperature from the flowing of this dry main 226, then in self-cleaning heat-exchange equipment 300.
To sum up, after washing, gas carries out de-oiling, dehydration, cooling through self-cleaning heat-exchange equipment 300, and the lightweight oil that self-cleaning heat-exchange equipment 300 produces and weakly alkaline liquid can carry out desulfurization, de-naphthalene to gas.
In some embodiments of the invention, organic materials treatment system can also comprise washings circulation vessel (scheming not shown).Washings circulation vessel is communicated with the second water spray pipe 222 with the second tar overflow port 2241 of the first recirculated water entrance 2112, secondary carbonization gas washing tower 220 with the first tar overflow port 2121 of elementary carbonization gas washing tower 210 respectively, the first washings wherein produced after initial wash in elementary carbonization gas washing tower 210 is discharged in washings circulation vessel from the first tar overflow port 2121 and isolates tar, dust and the first water of condensation, and the first water of condensation gets back to the first recirculated water entrance 2112; The second washings produced after secondary washing in secondary carbonization gas washing tower 220 is discharged to state in washings circulation vessel from the second tar overflow port 2241 isolates tar, dust and the second water of condensation, and the first water of condensation gets back to the second water spray pipe 222.
That is, by arranging this washings circulation vessel, thus the impurity such as tar, dust that elementary carbonization gas washing tower 210 can be entered washing generation interior with secondary carbonization gas washing tower 220 is separated with water of condensation, and water of condensation is sent back to elementary carbonization gas washing tower 210 and enter with in secondary carbonization gas washing tower 220, carry out recycle.Tar after sedimentation regularly can be drawn to oil tank China and foreign countries and sell.
Further, this washings circulation vessel can also be connected to receive the washings of discharging with at least self-cleaning interchanger 310 of one-level, and be separated with the 3rd water of condensation by the impurity such as the tar in this washings, dust, and the 3rd water of condensation is sent back to cooling water connector 3114.
According to the organic materials treatment system of the embodiment of the present invention, carry out destructive distillation by first organic materials being passed into organic materials carbonization decomposition vapourizing furnace 100 and producing carbonization gas, again carbonization gas is passed into successively in carbonization gas washing plant and self-cleaning heat-exchange equipment 300, carry out washing, purifying and process, finally can obtain clean flammable carbonizing gas, the impact of organic materials on environment can be reduced thus, and by the above-mentioned treating processes to organic materials, the flammable energy can also be obtained, thus the maximization of organic materials utility value can be made.
As mentioned above, for the organic materials of such as domestic refuse, compared with the existing processing mode of burning away the refuse generally adopted, the gas produced according to the organic materials treatment system of the embodiment of the present invention and solid emission all do not produce dioxin and heavy metal contamination, without waste residue after process, the solid of output can be used as smokeless fuel, its calorific value is more than per kilogram 5000 kilocalorie, certainly also can follow according to actual needs, allow the complete destructive distillation of material, the powder that output building trade uses and the additive that cement industry uses.Simultaneously output is used for the carbonizing gas that generates electricity, for domestic refuse: calorific value is more than every cubic metre of 6000 kilocalories.For the lignitoid coal foam of example, according to organic materials treatment system of the present invention, not only can obtain the recovering of vaporized hydrocarbons rate up to 98%, and the gas yield of routine lignitoid low-rank coal foam can reach 400m
3/ t raw coal, calorific value is at 17-33MJ/m
3left and right.
In process of production, the temperature of organic materials carbonization decomposition vapourizing furnace 100 inside can arbitrarily regulate, start to produce and stop production process simple, technique whole process can realize Automated condtrol, the inflammable gas produced both can generate electricity by internal combustion generator group, also can replace town gas or Sweet natural gas for user directly.This technique can also be applicable to following material further: the organic materials mixtures such as the byproduct schlempe of agricultural byproducts stalk, cotton stalk wine brewing and vinasse, plant leaves, industrial refuse, medical waste, domestic refuse.
When organic materials treatment system according to the present invention is used for cracking low-rank coal foam and resinous shale foam, production process is safe and reliable, operation is full-automatic, without three wastes mass emissions, make at a low price coal become smokeless fuel, reduce the pollution to environment, the Application Areas of coal more extensively, environmental protection.
Below with reference to Fig. 6, the organic materials treatment process according to the embodiment of the present invention is described.
As shown in Figure 6, this treatment process comprises the following steps.Organic materials is carried out isolated air destructive distillation and produces solid materials, carbonization gas and tar (step S1).Step S1 can complete in organic materials carbonization decomposition vapourizing furnace 100.
Washing, purifying is carried out to remove tar (step S2) to carbonization gas.This step S2 can complete in carbonization gas washing plant, and particularly, this step S2 can complete in elementary carbonization gas washing tower 210 and secondary carbonization gas washing tower 220.
Elementary de-oiling, dehydration, desulfurization, de-naphthalene are carried out to the carbonization gas after washing, purifying in step S2, and obtains clean gas (step S3).By this step S3, by magazins' layout such as the tar in organic materials, dusts out, and de-oiling, dehydration, desulfurization, de-naphthalene can be carried out, and obtain clean gas, finally can obtain clean gas, industry and civilian combustible gas use standard can be reached.
Further, step S2 can comprise the steps:
S21, initial wash is carried out to remove dust and heavy tar to carbonization gas.Particularly, in this step, washing can be sprayed for the first time by the recirculated cooling water of 60-65 degree.
S22, secondary washing is carried out to remove tar light oil to carbonization gas.Particularly, in this step, secondary washing can be carried out by the cold cycle water coolant of 40-60 degree.
Further, this organic materials treatment process also comprises the steps: to reclaim the washings obtained after process in step S2 and S3, sedimentation be separated to obtain dust, tar and water coolant, cooling water circulationly gets back to (step S4) in the treating processes of step S2.Particularly, in this step S4, also comprise and 60-65 degree is heated to washings isolates tar with natural sedimentation.
Further, as shown in Figure 6, this organic materials treatment process can also comprise the step (step S5) reclaimed the solid materials produced in step S1.
In embodiment more of the present invention, when such as processing the organic materialss such as domestic refuse, further comprising the steps of before step S1: S01: elementary screening is carried out to organic materials.This step can be carried out in primary screen subset.Particularly, this light material is crushed to less than 5 millimeters.S02: the organic materials that step S01 obtains is carried out processed and pulverized light material fragmentation wherein.This step can complete in dewatering unit.S03: mixing moulding process is carried out to the organic materials through step S02 process.
And for the organic materials of such as low-rank coal foam and/or resinous shale foam, further comprising the steps of before step S1: S01: to carry out elementary screening to described organic materials, the particle diameter of wherein said organic materials is not more than 5mm; S02: the organic materials that step S01 obtains is carried out processed and pulverized light material fragmentation wherein.
By adopting according to organic materials treatment process of the present invention, by magazins' layout such as the tar in organic materials, dusts out, and de-oiling, dehydration, desulfurization, de-naphthalene can be carried out, and obtain clean gas, finally can obtain clean gas, industry and civilian combustible gas use standard can be reached.In above-mentioned organic materials treatment system of the present invention and method, can at utmost contamination-freely utilize conventional example as the organic materials of rubbish, low-rank coal foam etc., farthest to make full use of this organic materials.
In the description of this specification sheets, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " illustrative examples ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present invention or example.In this manual, identical embodiment or example are not necessarily referred to the schematic representation of above-mentioned term.And the specific features of description, structure, material or feature can combine in an appropriate manner in any one or more embodiment or example.
Although illustrate and describe embodiments of the invention, those having ordinary skill in the art will appreciate that: can carry out multiple change, amendment, replacement and modification to these embodiments when not departing from principle of the present invention and aim, scope of the present invention is by claim and equivalents thereof.
Claims (22)
1. an organic materials carbonization decomposition vapourizing furnace, is characterized in that, comprising:
Pyrolysis gasification body of heater, described pyrolysis gasification body of heater is provided with opening for feed and air outlet;
Multiple destructive distillation room, described multiple destructive distillation rooms juxtaposition is in described pyrolysis gasification body of heater, and spaced apart between adjacent two destructive distillation rooms, is equipped with discharge gate bottom each described destructive distillation room; And
Electrically heated rod, it is indoor to carry out isolated air destructive distillation, to produce solid carbonaceous material and carbonization gas to the material of described multiple destructive distillation indoor that described electrically heated rod is located at described multiple destructive distillation vertically.
2. organic materials carbonization decomposition vapourizing furnace according to claim 1, it is characterized in that, described multiple destructive distillation rooms juxtaposition is in described pyrolysis gasification body of heater, and adjacent two described destructive distillation rooms are spaced apart from each other, and described discharge gate is located at the bottom of each described destructive distillation room respectively.
3. organic materials carbonization decomposition vapourizing furnace according to claim 1, is characterized in that, also comprise:
Top feed bin, the top of described top feed bin is opened wide, and the bottom of described top feed bin is communicated with the opening for feed of described pyrolysis gasification body of heater; And
Sealed automatic feeding device, described sealed automatic feeding device be located between the bottom of described top feed bin and the opening for feed of described pyrolysis gasification body of heater with isolated air the material controlled in the feed bin of top be supplied in described pyrolysis gasification body of heater.
4. organic materials carbonization decomposition vapourizing furnace according to claim 3, is characterized in that, described top feed bin is formed as doline.
5. organic materials carbonization decomposition vapourizing furnace according to claim 3, is characterized in that, described sealed automatic feeding device is be located at the motorized valve on the pipeline between the bottom of described top feed bin and the opening for feed of described pyrolysis gasification body of heater.
6. organic materials carbonization decomposition vapourizing furnace according to claim 3, is characterized in that, the opening for feed place of described pyrolysis gasification body of heater is provided with further:
For distributing the distribution passage of material, described distribution channels configuration becomes to be introduced equably in described pyrolysis gasification body of heater by described material.
7. organic materials carbonization decomposition vapourizing furnace according to claim 6, it is characterized in that, described distribution passage is formed as down Y shape and comprises the upper channel, the first lower channel and the second lower channel that communicate with each other, the top of wherein said upper channel is communicated with the bottom of described top feed bin, and the bottom of the first lower channel and the second lower channel is led in described pyrolysis gasification body of heater respectively.
8. the organic materials carbonization decomposition vapourizing furnace according to any one of claim 3-7, is characterized in that, comprise further:
Distribution device, described distribution device is located at below described opening for feed, carries out uniformly distributing with the material fed described opening for feed.
9. organic materials carbonization decomposition vapourizing furnace according to claim 8, it is characterized in that, described distribution device comprises:
Strut member, described strut member is extending longitudinally along described pyrolysis gasification body of heater;
Multiple backgauge part, one end of each described backgauge part is connected on described strut member and the other end transversely extends towards the inner side-wall of described pyrolysis gasification body of heater.
10. organic materials carbonization decomposition vapourizing furnace according to claim 9, is characterized in that, described backgauge part extends transversely; And described multiple backgauge part is evenly distributed on the both lateral sides of described strut member.
11. organic materials carbonization decomposition vapourizing furnaces according to claim 9, it is characterized in that, described strut member is identical with the shape of described backgauge part, and each in described strut member and described backgauge part includes symmetrically arranged first plate and the second plate on cross section, described first plate and the second plate upper end connect and form the angle of 30-180 degree between described first plate and the second plate.
12. organic materials carbonization decomposition vapourizing furnaces according to claim 9, it is characterized in that, described strut member is fixedly installed the vertical ventpipe extended, described ventpipe is formed with the venting channels be connected with the inside of described pyrolysis gasification body of heater, and described air outlet is formed in the exit end of described venting channels.
13. organic materials carbonization decomposition vapourizing furnaces according to claim 1, is characterized in that, comprise further:
Multiple automatic-sealed discharge device, described multiple automatic-sealed discharge device is located at the described discharge gate place of described multiple destructive distillation room respectively, to carry out blowing to described destructive distillation room.
14. organic materials carbonization decomposition vapourizing furnaces according to claim 13, is characterized in that, also comprise:
Sealing discharging storehouse, described sealing discharging storehouse is located at the bottom of described pyrolysis gasification body of heater and is communicated with described pyrolysis gasification furnace interior, and the bottom of wherein said multiple destructive distillation room extend in described sealing discharging storehouse;
Chain type discharge device, described chain type discharge device is located in described sealing discharging storehouse to receive the material of described automatic-sealed discharge device discharge and to discharge.
15. organic materials carbonization decomposition vapourizing furnaces according to claim 1, is characterized in that, described organic materials is low-rank coal foam and/or resinous shale foam.
16. 1 kinds, based on the organic materials treatment process of organic materials carbonization decomposition vapourizing furnace as claimed in claim 1, is characterized in that, comprise the following steps:
S1, described organic materials carried out isolated air in described organic materials carbonization decomposition vapourizing furnace and lower than the low temperature pyrogenation destructive distillation of 650 degrees Celsius, to produce solid materials, carbonization gas and tar;
S2, washing, purifying is carried out to remove tar to described carbonization gas; And
S3, the described carbonization gas after washing, purifying in step S2 carried out to elementary de-oiling, dehydration, desulfurization, de-naphthalene, to obtain clean gas.
17. organic materials treatment processs according to claim 16, it is characterized in that, described step S2 comprises:
S21, initial wash is carried out to remove dust and heavy tar to described carbonization gas;
S22, secondary washing is carried out to remove tar light oil to described carbonization gas.
18. organic materials treatment processs according to claim 17, is characterized in that, in described step S21, carry out initial wash by the high-temperature cooling water of 60-65 degree.
19. organic materials treatment processs according to claim 17, is characterized in that, in described step S22, carry out secondary washing by the low-temperature cooling water of 40-60 degree.
20. organic materials treatment processs according to claim 17, is characterized in that, also comprise:
S4, the washings obtained after process in step S2 and S3 is reclaimed, sedimentation be separated to obtain dust, tar and water coolant, describedly cooling water circulationly to get back in the treating processes of step S2.
21. organic materials treatment processs according to claim 20, is characterized in that, in described step S4, also comprise and isolate tar to 60-65 degree with natural sedimentation to described washings temperature control.
22. organic materials treatment processs according to claim 21, is characterized in that, described organic materials is low-rank coal foam and/or resinous shale foam, wherein further comprising the steps of before step S1:
S01: elementary screening is carried out to described organic materials, the particle diameter of wherein said organic materials is not more than 5mm;
S02: the organic materials that step S01 obtains is carried out processed and pulverized light material fragmentation wherein.
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| CN105400527A (en) * | 2015-12-08 | 2016-03-16 | 北京神雾环境能源科技集团股份有限公司 | Pyrolysis reactor |
| WO2017207104A1 (en) * | 2016-06-03 | 2017-12-07 | Bernd Schottdorf | Device and method for continuous production of vegetable carbon and vegetable carbon produced by said method |
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| BR112015030168B1 (en) * | 2013-06-09 | 2021-04-27 | Shan Dong Hi-Link Electricity Co. Ltd | DRY DISTILLATION AND GASIFICATION OVEN FOR ORGANIC MATERIALS, AND SYSTEM FOR ORGANIC MATERIALS PROCESSING |
| CN107325834B (en) * | 2017-07-24 | 2018-05-25 | 辽宁清道夫环保工程有限公司 | Greasy dirt solid waste processing system and greasy dirt solid waste substance treating method |
| CN109666512A (en) * | 2019-02-18 | 2019-04-23 | 中国华能集团清洁能源技术研究院有限公司 | A kind of downlink Quench furnace moves the dry coal powder pressure gasifying device of heat outside |
| HUE063888T2 (en) * | 2020-06-04 | 2024-02-28 | Reimund Schuster | Device for producing vegetable charcoal by pyrolysis of biomass |
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| CN102965129A (en) * | 2012-12-13 | 2013-03-13 | 山东汉菱电气有限公司 | Organic material gasification furnace |
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| CN102492432A (en) * | 2011-12-09 | 2012-06-13 | 新疆美特镁业有限公司 | Pulverized coal coking equipment and method |
| CN202898371U (en) * | 2012-11-13 | 2013-04-24 | 山东汉菱电气有限公司 | Weak-base source self-cleaning heat exchanger for purification, desulfurization, oil removal and dehydration of coal gas |
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- 2014-05-23 BR BR112015030168-1A patent/BR112015030168B1/en not_active IP Right Cessation
- 2014-05-23 WO PCT/CN2014/078332 patent/WO2014198180A1/en active Application Filing
- 2014-06-09 CN CN201420303706.0U patent/CN203923096U/en not_active Expired - Fee Related
- 2014-06-09 CN CN201410253099.6A patent/CN104232121B/en active Active
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| US4469488A (en) * | 1980-05-27 | 1984-09-04 | Albert Calderon | Method for gasifying coal |
| CN2457159Y (en) * | 2000-11-24 | 2001-10-31 | 浙江省林业科学研究院 | Tubular type movable bed dry distillation carbide furnace |
| CN2564574Y (en) * | 2002-03-29 | 2003-08-06 | 康成 | Vertical coke oven |
| CN1966609A (en) * | 2006-08-25 | 2007-05-23 | 神木县三江煤化工有限责任公司 | Low-temperature coal carbonization kiln |
| CN102965129A (en) * | 2012-12-13 | 2013-03-13 | 山东汉菱电气有限公司 | Organic material gasification furnace |
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| WO2017207104A1 (en) * | 2016-06-03 | 2017-12-07 | Bernd Schottdorf | Device and method for continuous production of vegetable carbon and vegetable carbon produced by said method |
Also Published As
| Publication number | Publication date |
|---|---|
| BR112015030168B1 (en) | 2021-04-27 |
| CN104232121B (en) | 2018-06-19 |
| BR112015030168A2 (en) | 2019-12-17 |
| WO2014198180A1 (en) | 2014-12-18 |
| CN203923096U (en) | 2014-11-05 |
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