JP6544597B2 - Rotary kiln gasifier - Google Patents

Description

The present invention relates to a rotary kiln for gasifying treated products such as biomass .
Typical objects to be treated include biomass, coal, pulverized coal, and thermoplastic resins, but the combustible substance with a low fuel ratio generally existing in society also contains a large amount of water, etc. It is also applicable to low quality combustible substances.

Heretofore, there are treated products having a large fuel ratio of the produced substance, that is, the ratio of fixed carbon to volatile matter, for example, typically biomass, and as a format for gasifying these treated products,
(1) There is a method in which the combustion gas for partial combustion is blown upflow or downflow into the shaft furnace, and the processed material in the shaft furnace is pyrolyzed and gasified by the heat of partial combustion,
(2) "patent document 2" waste disposal method and apparatus,
Biomass gasification system, Cogeneration and feeding by carbonizing furnace, As in the biomass gasification method, there is a type using an indirect heating cocurrent rotary kiln, and as a type to volatilize or thermally decompose organic substances other than biomass, (3) As in the rotary kiln type material heating and drying apparatus, a form in which high temperature processing residues are circulated to the raw material input side by a recycling spiral chute provided inside or outside the rotary kiln, and the material is heated and dried, Symposium Director Howard H. Elliott "SYNTHETIC FUELS FROM OIL SHALE AND TAR SANDS" SYMPOSIUM PAPERS Presented May 17-19, 1983 Louisville, Kentucky, May 17, 1983, p. As shown in 473-488, a type adopted as a dry distillation furnace for oil shale, in which high temperature processing residue is recycled to the raw material input side by a recycling spiral chute provided inside the rotary kiln, Environmental Services & Regulation, Environmental Review of QE Pty Ltd, Oil Shale Technology Demonstration Plant, Gladstone, Queensland, The State of Queensland (Department of Environment and Heritage Protection), February 2013, p. As in 7 to 10, there is known a system adopted as a dry distillation furnace of oil shale, in which a high temperature processing residue is recycled to a raw material input side by a recycling spiral chute provided outside the rotary kiln.

Patent No. 5599015 gazette Rotary kiln type material heating drying device Patent No. 4154029 Waste disposal method and apparatus Patent No. 4312632 Biomass gasification system Patent No. 4502331 Cogeneration feed by carbonizing furnace Patent Document 1: JP-A-2005-12956 A method for gasifying biomass

Symposium Director Howard H. Elliott "SYNTHETIC FUELS FROM OIL SHALE AND TAR SANDS" SYMPOSIUM PAPERS Presented May 17-19, 1983 Louisville, Kentucky, May 17, 1983, p. 473-488 Environmental Services & Regulation, Environmental Review of QE Pty Ltd, Oil Shale Technology Demonstration Plant, Gladstone, Queensland, The State of Queensland (Department of Environment and Heritage Protection), February 2013, p. 7 to 10

In the background art (1), the uniformity of ventilation in the shaft furnace can not be maintained, the scale-up is limited, and it is limited to small-sized furnaces and is not economical. In addition, the occurrence of cluster-like coarse particles in the shaft furnace makes it easy to cause shelf suspension, resulting in unstable operation. Since (2) is an indirect heating system, the operating temperature is low, and the conversion rate of the heat of the processed product to the heat of the generated gas is low. In addition, the heat transfer efficiency is not economical because of limitations in scale-up. The rotary kiln is made of heat-resistant steel plate, so its life is short. (3), because the rotary kiln is made of heat-resistant steel plate, it gasifies the treated material such as biomass, which has a low operating temperature and a large ratio of fuel to produced, that is, the ratio of fixed carbon to volatile matter In order to meet the requirements for high temperature operation.

According to the invention as claimed in claim 1,
The solid-gas reaction of the rotary kiln for gasification of processed material, such as biomass , is preheating and drying in the main zone of the front zone, thermal decomposition by the main reaction in the middle zone and partial heat generation in its middle zone, and water gas reaction in the main zone of the rear zone. And shift reaction, in which each zone proceeds in duplicate, and as a means to increase its solid-gas reaction efficiency, reducer-type short pipe pipe lifter 9a or neutral type pipe lifter 9b or short pipe pipe lifter in each zone A component to install 9c,
And, as a means to increase the thickness of the processed material layer of the pipe lifter scraping portion , the reverse spiral type pipe lifter 9d is installed in reverse spiral and reversely transported by the pipe lifter external protrusion or single in the gap of the pipe lifter. Or, a plurality of reverse feed chutes 10 are provided in a reverse spiral so that the processed material is fed back to the upstream side of the pipe lifter scraping part, and are reversely transported by the reverse transfer effect of the reverse feed chute 10 inside and outside Or the angle between the rotary kiln axial direction and the pipe lifter axial direction increases the thickness of the treated material by scraping the treated material on the front face of the pipe lifter opening 20 by the horizontal pipe lifter 9e arranged at an angle of repose or less of the treated material. Components,
And, a pipe lifter and backhaul shoots a portion of the outer surface, are not connected with the inner wall refractory of the rotary kiln, in contact or embedded in the inner wall refractory of the rotary kiln, the part of the other installed so as to protrude inside the rotary kiln By supporting the steel structure of the rotary kiln shell, it is possible to increase the dispersion efficiency of the scooped treated material inside the rotary kiln and to increase the solid-gas reaction efficiency in the rotary kiln.

The pipe lifter and the reverse feed chute 10 are made of heat-resistant steel, the support of which is fixed to the rotary kiln shell 19 and exerts no repulsive force with the refractory. The refractory is provided with a hole for partially embedding the pipe lifter or the reverse feed chute 10, but a cushion mortar or wool blanket is applied to the installation gap.
Thus, the refractory 11 is not different from the normal high temperature rotary kiln life.
The pipe lifter or the reverse feed chute 10 has a service limit in heat resistance, and the life limit is determined. For example, SUS310S or Hastelloy C276 has a certain strength even at 1000 ° C., and the practical use limit is ultra-high temperature. Moreover, replacement as consumables is easy, and the adverse effect on the operation rate of the entire equipment can be minimized.

According to the invention of claim 2, wherein, with respect to the inner diameter of the rotational locus cylindrical pipe lifter or backhaul chute 10, so that the discharge portion the inner diameter of the rotary kiln is reduced, the weir is provided, on its weir, suppress the emission As in the case of the reverse feed chute 10, it is provided with a through passage or opening inclined in the same reverse spiral direction. For this reason, at the discharge end of the rotary kiln, the non-reacted product is retained by the soot which inhibits the discharge, and the pipe lifter disperses the solid in gas into the rotary kiln and the reverse transfer by the reverse feed chute 10. , The unreacted residue of the treated product can be minimized. Although the processing route is not discharged from the passage or opening when the rotary kiln rotates forward, the passage or opening provided in the weir reverse discharges the residue in the rotary kiln, for example, at the time of shutdown, etc. Then, all the furnace residue can be discharged.

According to the present invention as set forth in claim 3, even if the pipe lifter or the reverse feed chute is provided with the vanes 21a or 21b to improve the scraping ability or the reverse feed ability, the number of installed pipe lifters can be reduced. And increase the solid-gas reaction efficiency in the rotary kiln. The blades 21a are scraping lifters provided on the outer surface of the pipe lifter or the reverse feed chute, and are added to the scraping amount inside the pipe lifter to increase the scraping amount. The vanes 21b are swirling vanes provided on the outer surface of the helical tube along the helical tube, and the total height of the helical vanes is increased to increase the amount of reverse feed.

According to the present invention according to claim 4, a part of the lower sedimentation residue of the secondary homogenization furnace 15 disposed at the rotary kiln outlet is taken out with air blocking, and circulated to the feeding hopper 1 disposed at the rotary kiln inlet . The gasification rate can be further improved. The rotary kiln is in a dusting environment due to a highly efficient lifter effect, unreacted carbon is scattered to the homogenization furnace 15, and some of the coarse particles settle to the bottom, but the sedimentation residue is extracted to the outside and put into the input hopper. If it returns, gasification efficiency can be raised.

According to the fifth aspect of the present invention, steam and oxygen are obtained by adding oxygen to superheated steam to the combustion supporting gas using partial combustion heat of the treated material as a heat source for solid-gas reaction in the rotary kiln. Use a mixed gas as the main component.
Solid-gas reaction governed by the unreacted core model proceeds from the surface layer, and proceeds with residual heat drying, partial combustion and thermal decomposition due to its heat generation, water gas reaction and shift reaction, but if nitrogen is not contained in the supporting gas, The reaction proceeds faster due to heat balance. And the partial pressure of water vapor is important as well as the temperature conditions in promoting the water gas reaction and the shift reaction. According to the first, second, or third aspect of the present invention, the main components of the support gas are water vapor and oxygen, so that the gasification efficiency of the solid raw material is increased and the quality of the generated gas is improved. Oxygen can be easily obtained from air, usually by means of a PSA oxygen generator.

The following can be achieved by the present invention.
(1) Solid dispersion in gas by a pipe lifter is possible at high temperature operation at 850 ° C to 1000 ° C.

The pipe lifter does not embed the mounting anchor in the refractory 11 and does not connect with the refractory 11, but only freely fits in the refractory hole, and its support is fixed to the steel structure of the rotary kiln shell 19 The operating temperature can be set up to the heat limit of the pipe lifter.
Refractory 11 can be designed at a temperature of 1000 ° C. or more by a conventional heat-resistant design.

(2) The high temperature operation can rapidly promote the water gas reaction and the shift reaction in an integrated rotary kiln.

The water gas reaction generally develops at 800 ° C. or higher, and the reaction temperature increases as the temperature rises. The advantage of high-temperature operation is great because the conversion of fixed carbon to combustible gas depends on the water gas reaction, for example for biomass, which is a processed product having a large fuel ratio of the produced substance, ie the ratio of fixed carbon to volatile matter.

(3) Gasification reaction rate is high due to the solid-in-gas dispersion effect

Ventilation of surface gases is important because solid-gas reactions governed by the unreacted core model proceed from the surface. Since the solid is forcibly dispersed in the gas by the pipe lifter, the gas on the surface layer is always replaced, and the atmosphere conditions in which the reaction proceeds can be formed for drying of the solid, pyrolysis gasification, and water gas reaction.

(4) Solid-in-gas dispersion efficiency is high.

The thickness of the processed material layer in the scraping zone to the pipe lifter is the reverse spiral arrangement of the pipe lifter 9d or the reverse feed effect by the reverse feed chute 10, the scraping effect of the pipe lifter 9e, or the storage effect by the weir provided in the rotary kiln discharge part Can be large. As a result, the amount of scraping into the pipe lifter increases, and the amount of dispersed material in the gas can be properly planned. In any of the above cases, if the pipe lifter or the reverse feed lifter is provided with the vanes 21a and 21b, the in-gas solid dispersion efficiency can be further enhanced.

(5) The gasification efficiency of the solid raw material is high, and the quality of generated gas is excellent.

The gasification efficiency of the solid material is high because the treated material is partially burned with the mixed gas consisting mainly of steam and oxygen, with oxygen added to the superheated steam obtained by heat exchange with the waste heat of the rotary kiln generating gas , The calorific value of the generated gas is large. Further, the partial pressure of water vapor can be increased, and the water gas reaction can be promoted.
On the other hand, when the treated product is a dried product, a practically sufficient calorific value of the generated gas can be obtained even if air is used instead of oxygen.

The rotary kiln cross section shows an AA arrow in FIG. 2 and a DD arrow in FIG. 7 in the entire rotary kiln according to the present invention. The rotary-kiln inner surface expanded view which concerns on this invention shows the example of arrangement | positioning of various pipe lifters. (The first stage is a combination of reducer type short pipe lifter 9a, the middle stage is a combination of neutral arrangement type 9b and reverse spiral arrangement type 9d of circular pipe lifter, and the second stage is a combination of neutral arrangement type 9b of circular pipe lifter and reverse spiral arrangement type 9d , And a combination of a short pipe pipe lifter 9c and a reverse feed pipe chute 10) The rotary-kiln inner surface expanded view which concerns on this invention shows the example of arrangement | positioning of various pipe lifters. (The combination of the short pipe lifter 9c and the reverse feed pipe chute 10 in FIG. 2 is replaced with a horizontal circular pipe lifter 9e group arranged at a repose angle of the processing object or less) 2 illustrates two pipe lifter examples used in the present invention. (A) A reducer type short pipe pipe lifter 9a is shown. (B) The circular pipe lifter 9b arrange | positioned more than the repose angle of a processed material is shown. The horizontal- tube-pipe lifter 9e arrange | positioned by the repose angle of the processed material used by this invention or less ( the example of this figure is inclination | tilt angle 0 degree) is shown. (A) The EE arrow view of FIG. 3 is shown. (B) The F-F arrow view of FIG. 3 is shown. It is a partial detail view of two example tow passage 13 according to the present invention. (A) where the through passage 13 extends over two blocks of brick (b) the through passage 13 extends over one block of brick The example which added the pipe lifter is shown in the rotary-kiln inner surface development view which concerns on this invention. The example which reduced the installation quantity by providing a blade | wing in a pipe lifter is shown with the rotary-kiln internal surface development view which concerns on this invention. The cross section of various pipe lifters which provided the blade | wing is shown. (A) The GG arrow view of FIG. 8 is shown. (B) View HH in FIG. (C) I-I arrow view of FIG.

Hereinafter, the present invention will be described in detail with reference to FIGS. 1, 2, 3, 4, 5, 6, 7, 8, and 9.
FIG. 1 is a cross-sectional view showing an overall view of a rotary kiln according to the present invention.
FIG. 2 is an inner development view of a rotary kiln according to the present invention, showing an example of arrangement of various pipe lifters.

As shown in Figure 1,
The material to be treated is fed from the feeding hopper 1 through the double seal valve 2 and the feeding chute 3 while maintaining the seal between the inside of the rotary kiln and the atmosphere.
The treated material is preheated and dried in the preheating drying zone in the former stage, but the solid-gas reaction is governed by the unreacted core model, so the thermal decomposition reaction locally starts in the solid surface, and the result The combustible gas generated burns, and the heat of combustion is effectively used for residual heat drying.
The particle size of the solid also affects the reaction rate, and it is important that the wood-based material is shredded into chips. In the middle stage, the main reaction shifts to pyrolysis after the preheating drying is almost complete. As in the case of preheating and drying, since the thermal decomposition reaction is governed by the unreacted core model, solid-in-gas dispersion is important.
In the latter stage, the volatile substances in the solid are almost completely transferred into the gas, and the residue of the processed matter is mainly carbon. Because carbon gasification relies on a water gas reaction, solid-in-gas dispersion in the presence of sufficient water vapor is important. Since the inside of the rotary kiln is a dusting environment due to the pipe lifter effect, carbon residue is scattered to the secondary homogenization furnace, and unreacted coarse particles settle in the lower part. Sediment residue can be effectively used as solid fuel, but it is also valuable as a gasification raw material, and if part is returned to the input hopper, the gasification efficiency of the entire facility can be increased.

In the preheating drying zone, as shown in FIG. 2, if the pipe lifter 9a is properly arranged, smooth scraping into the pipe lifter, and smooth drop without bridge retention from the pipe lifter can be achieved, the solid is in the gas. Can be efficiently distributed. As a result, due to the heat transfer efficiency and the diffusion of the solid surface gas, the reaction rate becomes much higher.
The processed material immediately after the introduction has a large internal friction resistance, and there is a concern about hanging the shelf in the pipe lifter, so a reducer type short pipe pipe lifter as shown in FIG. 2, FIG. 4 (a) and FIG. Adoption of is recommended.

The thermal decomposition reaction accelerates in the middle of the rotary kiln and accelerates, and is almost completed after the solid reaches a predetermined reaction temperature.
The main reactions in this middle stage are the thermal decomposition reaction and the water gas reaction, and in both cases, the dispersion of the solid in the gas is important.
For this reason, as shown in FIG. 2, the pipe lifter 9b and the pipe lifter 9d are effectively arranged to enhance the solid dispersion effect in the gas.
That is, as shown in FIG. 4 (b), while all have a sufficient scraping volume, the pipe lifter 9d can be installed in a reverse spiral to enable reverse feeding of the processed material in the furnace, and as a result, The thickness of the treated material layer in the pipe lifter installation zone can be increased.
As a result, the volumetric efficiency of getting into the pipe lifter can be increased, and as a result, the amount of dispersed solids in gas can be increased.

As the processed material goes to the later stage, the main reaction is a water gas reaction and a shift reaction.
At the same time, volatile substances in the processed material are almost eliminated and carbon residue is mainly contained.
The water gas reaction proceeds by efficiently dispersing the carbon-based treated matter in the gas.
As shown in FIG. 2, the pipe lifter at the rear stage properly arranges the pipe lifter 9b, the pipe lifter 9d, and the pipe lifter 9c. In the pipe lifter 9c of the final stage, a reverse feed chute 10 is provided in the gap, and the reverse feed inside and outside the reverse feed chute 10 prevents the discharge of unreacted carbon residue as much as possible.
Also for the same purpose, as shown in FIG. 1, FIG. 2, FIG. 3, FIG. 5 (a), FIG. 7 and FIG. 8, a crucible 12 is provided at the end of the rotary kiln furnace to prevent discharge of unreacted carbon residue. doing.

As shown in FIGS. 3, 5, 8 and 9 (c), there are other types of pipe lifters after the processed material becomes fine particles.
A pipe lifter 9e is provided in the rotary kiln axial direction, and a plurality of openings 20 are provided on the side of the pipe lifter 9e. The protrusion from the wall surface of the pipe lifter 9e allows the processed material to be scraped to the front of the opening 20, so that it can be efficiently penetrated into the pipe lifter.
The processed material scraped from the opening is discharged into the rotary kiln furnace with the opening as a discharge port as the pipe lifter rises and reverses, and the solid-in-gas dispersion can be efficiently achieved.
Furthermore, as a means to increase the scraping effect and to increase the scraping amount, a blade 21a is provided on the outer surface of the pipe lifter 9e.

The rotary kiln according to the present invention is provided with a reverse feed function as shown in FIGS. 2, 3, 7 and 8. However, at the time of operation shutdown, the discharge of in-furnace residue will be hindered.
For this reason, when the operation is stopped, the rotary kiln is reversely rotated, and the reverse spiral tube rotates forward, so that the processed material inside and outside the pipe lifter can be discharged promptly toward the discharge part.
Further, by providing an inclined weir through passage as shown in FIG. 6, the weir portion of the end of the rotary kiln furnace can suppress the discharge in forward rotation and can advance the discharge in reverse rotation.
The same effect can be expected even if the ridge is inclined to form a groove and the open ridge is provided.

FIG. 7 shows an example in which the maximum number of installable pipe lifters is disposed on the inner surface of the rotary kiln. That is, the total number of installed pipe lifters and reverse feed chutes is 44 in the arrangement of FIG. 2 and 66 in the arrangement of FIG.
Thus, the number and combination of various pipe lifters can be selected according to the characteristics of the processing object.

FIG. 8 shows an example in which blades 21a and 21b are added to the outer surface of the pipe lifter. The vanes 21a are general lifter vanes provided in the rotary kiln axial direction, and the amount of scraping is added to the amount of scraping of the pipe lifter. The blade 21b is a blade along a spiral tube, which can increase the scraping height of the spiral tube, increase the reverse feed amount, increase the height of the treated layer in the zone, and increase the scraping efficiency.
In this arrangement, the total number of installed pipe lifters is 26, and the addition of vanes can reduce the number of installed pipe lifters.

Hereinafter, embodiments of the present invention will be described based on FIGS. 1, 2, 3, 4, 5, 6, 7, 8, and 9.

Fig. 1, Fig. 2, Fig. 4 and Fig. 6 are rotary kiln type gasifiers used for generating combustible gas with biomass as a raw material.
The raw material is wood chips, and the main reaction in the front stage of the rotary kiln is preheating and drying, the main reaction in the middle stage is thermal decomposition and water gas reaction, and the main reaction in the second stage is water gas reaction and shift reaction. Since the reaction of the solid is governed by the unreacted core model, the main reaction does not change independently in the former, middle and latter stages, and the main reaction in each stage is the solid particle size, the solid surface Due to fluctuations in conditions such as temperature or surface gas diffusion, overlapping occurs between stages.

The treated product in the former stage has a large internal friction resistance inherent to the wood chip, and has a grain size mainly composed of coarse particles, and the raw material properties remain. The pipe lifter provided at the front stage adopts a reducer type short pipe pipe lifter as shown in FIG. 4a. This is in order to emphasize the ease of scraping the processed product into the pipe lifter and the fact that the processed product lifted upward does not stay in the pipe lifter but falls smoothly. After being lifted to the top, the treatment is dispersed in the gas and drying proceeds efficiently. In particular, with respect to fine particles, part of the treated surface layer ends dry preheating, and thermal decomposition and gasification of volatile components starts. The combustible pyrolysis gas is burned by the partial combustion supporting gas, and the heat of combustion promotes preheating and drying.

In the middle stage, the temperature of the particles of the treated product is increased as it approaches the gas temperature from before and after the internal moisture evaporates and disappears, and simultaneously the thermal decomposition proceeds. The pyrolysis gas present in the gas as a result of the pyrolysis is further decomposed in the presence of water vapor by the water gas reaction, whereby the decomposition of the polymeric hydrocarbon proceeds and is converted to a hydrogen and carbon monoxide-based gas. In the processed product, the drying is almost completed, the internal friction resistance is reduced, and the particle diameter is reduced due to the physical collision between particles, and the fluidity is increased. In the middle stage, pipe lifters 9b and 9d are installed to increase the amount of scraping. Also, in order to increase the scraping efficiency, a pipe lifter 9d installed in a reverse spiral is used to reversely transfer the processed material and to increase the layer thickness of the middle-stage processed material. As a result, the amount of scraping of the pipe lifter is significantly increased.

At the second stage, the remaining solid carbon is scraped up by the pipe lifters 9b, 9d and 9c, and the finely divided solid carbon is finally gasified by the water vapor reaction mostly by the water vapor in the gas. As a means to increase the amount of dispersion in gas in this process, first, it is reversely sent by the pipe lifter 9d to increase the layer thickness of the zone and to increase the scraping efficiency. In addition, a crucible is provided at the bottom of the rotary kiln furnace, unreacted carbon residue is retained, and the treated material is fed backward from the downstream side of the pipe lifter 9c by the reverse feed chute 10 to increase the treated material bed height. In the zone where the layer thickness is increased, it is scraped up by the pipe lifter 9c and dispersed in the gas in the furnace.

Thus, carbon particles discharged from the furnace bottom can be minimized by gasifying the carbon particles by the water gas reaction in the first, middle and second stages.
A part of the unreacted carbon residue collected and deposited in the lower part of the furnace hood is discarded as it is or as a fuel in the entire equipment system, generally as a heating fuel for combustion air or as a drying fuel for raw materials Improve the thermal efficiency of equipment by making effective use of it. Or transfer and circulate upstream, mix it with the materials of the rotary kiln and reuse it. In addition, when the transfer residue is pseudo-particulate, it goes through a grinding process.
There are the above three methods.
When importance is placed on the amount of power generation, it is desirable to use the third carbon residue circulation system in using carbon residues.
In addition, some unreacted carbon residues that fly off downstream without settling in the furnace end hood 14 are finally gasified by a water gas reaction in the furnace end hood space and the subsequent secondary homogenization furnace space.
Since wood-based biomass is a relatively pure carbonaceous fuel, the heat utilization efficiency of carbon determines the thermal efficiency of the entire facility.

  1, 3, 4, 5, and 6 show a rotary kiln type gasification furnace used for generating combustible gas from biomass as a raw material, and the pipe of the latter stage relative to Example 1 It is the Example which changed the lifter.

In the final stage of the latter stage, the processed material is fine-grained and provided in the axial direction, and a pipe lifter 9e in which some of the pipe lifters project into the furnace is effective.
This can be efficiently scraped into the opening 20 of the pipe lifter 9e due to the increase in the thickness of the treated substance by the crucible 12 provided at the bottom of the furnace and the scraping effect of the treated substance by the projecting portion in the furnace of the pipe lifter 9e. At the same time, the pipe lifter 9e protruding into the rotary kiln can be lifted by itself. Due to these two effects, the treatment scraped up at the top is dispersed in a large amount in the gas.

Figures 1, 4, 6 and 7 show a rotary kiln type gasification furnace used to generate combustible gas from biomass as a raw material, and compared with Example 1, a pipe lifter was added to the installation limit It is the Example arrange | positioned.

It is common for the properties of the treated material to change significantly. Although the pipe lifters are properly arranged, the number of installed pipe lifters can be changed according to the properties of the processed material.
Compared to the first embodiment, the reducer-type short tube pipe lifter 9a at the front stage is doubled, and the middle pipe lifters 9b and 9d are expanded by about 1.5 times.
Thus, depending on the properties of the processed material, the pipe lifter is increased or decreased and the individual pipe lifter lifting capability is adjusted.

1, 8 and 9 show a rotary kiln type gasification furnace used for generating combustible gas from biomass as a raw material, and Example 2 reduces the front, middle and rear pipe lifters. However, in order to further increase the scraping effect, this embodiment is an embodiment in which the blades 21a and 21b are added.

In the third embodiment, the pipe lifter is added according to the property of the processing object. However, since the pipe lifter is a metal consumable, it is desirable to reduce it as much as possible.
Therefore, in the fourth embodiment, the blades 21a and 21b are added to each pipe lifter to increase the amount of scraping and the amount of reverse feeding. The blade 21a is a scraping lifter, and the scraped scraping amount increases. The height of the spiral tube is increased by the blade 21b, and the amount of reverse feed is increased by that amount, and the scraping efficiency is improved.

The patented invention can, in particular, meet the following requirements.
(1) It is required that a series of processes such as drying, thermal decomposition, water gas reaction, shift reaction, etc. be completed in a single rotary kiln in a furnace.
(2) It is required that the atmosphere in the furnace is high temperature, each processing step can be performed with high efficiency, the conversion rate of the combustible gas of the raw material is high, and the heat recovery efficiency and the power generation efficiency by the combustible gas are high.
(3) The rotary kiln is required to be compact and inexpensive.
(4) It is required to easily replace consumable parts in a short time.
The above requirements are usually required for rotary kilns used for pretreatment for metal refining, rotary kilns used for dry distillation, carbonization, etc., in addition to the gasification rotary kiln used for biomass gasification power generation equipment. Ru.

DESCRIPTION OF SYMBOLS 1 ... input hopper 2 ... double seal valve 3 ... input chute 4 ... furnace front hood 5a, 5b ... rotary body seal device 6 ... rotary kiln 7a, 7b ... tire 8 ... drive gear cover 9a, 9b, 9c, 9d, 9e ... Pipe lifter 10 ... Reverse feed chute 11 ... Refractory 12 ... 堰 13 ... Perforating passage 14 ... Furnace butt hood 15 ... Secondary homogenization furnace 16 ... Supporting gas injection tube 17 ... Fixed bolt 18 ... Thermal insulation 19 ... Rotary kiln outside Shell 20 ... opening 21a, 21b ... feather

Claims (5)

The solid-gas reaction of the rotary kiln for gasification of processed material, such as biomass , is preheating and drying in the main zone of the front zone, thermal decomposition by the main reaction in the middle zone and partial heat generation in its middle zone, and water gas reaction And shift reaction, in which each zone proceeds in duplicate, and as a means to increase its solid-gas reaction efficiency, reducer-type short pipe pipe lifter 9a or neutral type pipe lifter 9b or short pipe pipe lifter in each zone A component to install 9c,
And, as a means to increase the thickness of the processed material layer of the pipe lifter scraping portion , the reverse spiral type pipe lifter 9d is installed in reverse spiral and reversely transported by the pipe lifter external protrusion or single in the gap of the pipe lifter. Or, a plurality of reverse feed chutes 10 are provided in a reverse spiral so that the processed material is fed back to the upstream side of the pipe lifter scraping part, and are reversely transported by the reverse transfer effect of the reverse feed chute 10 inside and outside Or the angle between the rotary kiln axial direction and the pipe lifter axial direction increases the thickness of the treated material by scraping the treated material on the front face of the pipe lifter opening 20 by the horizontal pipe lifter 9e arranged at an angle of repose or less of the treated material. Components,
And, a pipe lifter and backhaul shoots a portion of the outer surface, are not connected with the inner wall refractory of the rotary kiln, in contact or embedded in the inner wall refractory of the rotary kiln, the part of the other installed so as to protrude inside the rotary kiln The rotary kiln characterized in that its support is fixed to the steel structure of the rotary kiln shell to increase the dispersion efficiency of the scooped processed material inside the rotary kiln and to increase the solid-gas reaction efficiency in the rotary kiln. Gasifier. A weir is provided so that the inside diameter of the discharge cylinder of the rotary lifter is smaller than the inside diameter of the rotation trajectory cylinder of the pipe lifter or the reverse feed chute 10, and the weir is inclined in the reverse spiral direction to suppress discharge . The rotary kiln type gasification furnace according to claim 1, wherein a through passage or an opening is provided. By adding blades 21a or 21b to the pipe lifter or reverse feed chute to improve the raking ability or reverse feed ability and reduce the number of installed pipe lifters, the solid-gas reaction efficiency in the rotary kiln can be maintained. The rotary kiln type gasification furnace according to claim 1 or 2, characterized in that it is enlarged. A part of the lower sedimentation residue of the secondary homogenization furnace 15 disposed at the rotary kiln outlet is extracted while air blocking and circulated to the feeding hopper 1 disposed at the rotary kiln inlet to further improve the gasification rate of unreacted carbon The rotary kiln gasification furnace according to claim 1, 2 or 3. As the heat source for solid-gas reaction in the rotary kiln, partial combustion heat of the treated material was used, and oxygen was added to the combustion support gas for the superheated steam obtained by heat exchange with waste heat of rotary kiln generated gas. 5. The rotary kiln gasification furnace according to claim 1, wherein a mixed gas containing water vapor and oxygen as main components is used.