CN101778926A - The method and apparatus that is used for the pyrolytic conversion of combustible matl - Google Patents
The method and apparatus that is used for the pyrolytic conversion of combustible matl Download PDFInfo
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- CN101778926A CN101778926A CN200880103022A CN200880103022A CN101778926A CN 101778926 A CN101778926 A CN 101778926A CN 200880103022 A CN200880103022 A CN 200880103022A CN 200880103022 A CN200880103022 A CN 200880103022A CN 101778926 A CN101778926 A CN 101778926A
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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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
-
- 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
- C10B1/00—Retorts
- C10B1/02—Stationary retorts
- C10B1/04—Vertical retorts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
- C10J3/30—Fuel charging devices
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/154—Pushing devices, e.g. pistons
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/12—Heating the gasifier
- C10J2300/1223—Heating the gasifier by burners
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/12—Heating the gasifier
- C10J2300/1269—Heating the gasifier by radiating device, e.g. radiant tubes
- C10J2300/1276—Heating the gasifier by radiating device, e.g. radiant tubes by electricity, e.g. resistor heating
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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)
- Processing Of Solid Wastes (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
Abstract
With combustible matl continuously or pulsation ground supply to reaction zone, this reaction zone and surrounding atmosphere isolation, and combustible matl moves to reaction zone gradually by reaction zone and exports along leaving the identical direction of direction of combustible matl with the gas that is discharged.Reaction zone is heated to following temperature: the value of this temperature increases along the direction of orientating reaction district outlet, yet is 12000C to the maximum.Then, the gas that is discharged is detached from non-gasification resistates discretely.Preferably with steam and/or water supply to combustible matl, and the effect of combustible matl by the combustible matl supplied with subsequently that before had been filled in the reaction zone move through reaction zone, wherein combustible matl is compressed.The equipment that is used for pyrolytic conversion comprises: a tamping unit (1); Reactor (2) comprises reaction zone (5); At least one well heater (3,13); And funnel (4), be used for non-gasification resistates (8).Reactor (2) has elongated shape, and its longitudinal axis is from 45 ° of vertical direction maximum deviation, wherein tamping unit (1) is arranged in the lowermost part of reactor (2), and the import that is used for the funnel (4) of non-gasification resistates (8) is positioned at the top part of reactor (2).Reactor (2) comprises reaction zone (5), and this reaction zone (5) contacts with at least one well heater (3,13).The funnel (4) that is used for non-gasification resistates (8) is connected to reactor (2) in reaction zone (5) top.The level cross-sectionn of reaction zone (5) is upwards narrowing down at least one part upward, and advantageously at least one inlet pipe (6) is directed in the reaction zone (5), as steam and/or water supplying pipe.Preferably, at least one pillar (9) is positioned at reactor (2), on its prolonging direction.Well heater (3,13) is electrically heated coil and/or burner.Tamping unit (1) comprises at least one piston (10), and this piston (10) advantageously has circular bottom part, arranges at least one pillar (9) or worm screw therein in the heart.Advantageously worm screw is coiled layout on every side at pillar (9).The filling orifice (14) of reactor (2) advantageously is provided with rib (15).
Description
Technical field
The present invention relates to be used for the method and apparatus of the pyrolytic conversion of combustible matl, and the production problem that relates to the inflammable gas of the energy that do not comprise tar and technical elements, and it relates to effective, the ecological utilization of solid matter or mixture simultaneously, this mixture has the solid matter of main content, as charcoal, wood chip or discarded organic residue, i.e. the fermentation sanitation waste of producing from agricultural or foodstuffs industry or other article that comprise free or organic constraint carbon.
Background technology
Be known that the gasification of organism itself and the parallel generation of its multiple modification and three kinds of products interrelate, these three kinds of product instant heatings are separated gas, condensable substances (as tar) and not gasifiable resistates.The shortcoming of the pyrolysis gas of Chan Shenging is in such a way, and it not only comprises solid particulate but also comprise coagulated substance.Pyrolysis gas is processed in generating the most frequently, and its insufficient purity causes the sedimental generation of burn into of material or the like problem.Be known that such problem is by solving the other processing of pyrolysis gas (i.e. removing or decompose by tar).Catalytic pyrolysis process is known, is included in the process that is applied to tar and its composition on the crystal grain bed (grain bed).Temperature effective and katalysis that tar decomposes owing to some phase that comprises in the crystal grain bed take place.In the efficient of decomposing on the bed process of carrying out in the temperature range from 600 ℃ to height to 900 ℃ is 60% to 90%, and this decompositions bed comprises lime, rhombspar, reaches aluminum oxide and silicon carbide as catalyzer.Another kind of known possibility is the use of disc filter, and this disc filter is filled with and powder nickel and magnesium oxide blended aluminum oxide mutually.The optimum temps that is used for this process is 850 ℃.In addition, the crystal grain bed that forms by the rhombspar by the nickel modification also is known.This process occurs under the higher temperature.Because the shortcoming of process described above comprises the susceptibility for the existence of sulphur compound, so calcium oxide also adds on the rhombspar usually.Also be known that natural catalyst,, also can be used for catalysis type tar and decompose as the mixture of Wingdale, peridotites and rhombspar or zeolite.Catalytic effect is a feature with the material with the ferric oxide (as spathic iron ore or limonite) that increases content also.Not enough efficient-its maximum that catalytic tar is decomposed is 75%, is the shortcoming of the use of these catalyzer.The common drawback of all catalytic processs be the necessity upgraded of crystal grain bed, all the components available, dispose or about the problem of the recovery of the bad material of decomposition that uses about environmental friendliness.Another weakness of catalytic process is that they occur under the elevated temperature, and it has increased the energy expenditure of technology.
Summary of the invention
Above-mentioned shortcoming is solved by the method and apparatus that is used for the pyrolytic conversion of combustible matl according to the present invention.
Essence of the present invention is, combustible matl is supplied to reaction zone with pulsing continuously or, and this reaction zone and surrounding atmosphere are isolated, after this, combustible matl moves to the reaction zone outlet along leaving the identical direction of direction of combustible matl with the gas that is discharged gradually by reaction zone.Reaction zone is heated to following temperature: the value of this temperature increases along the direction of orientating reaction district outlet, yet is 1200 ℃ to the maximum.After the passing through of reaction zone, the gas that is discharged is detached from non-gasification resistates discretely at combustible matl.Selectively, before combustible matl enters reaction zone and/or its when the reaction zone, take water vapor and/or water to combustible matl.Can select in the example at another, the combustible matl that before had been filled in the reaction zone moves through reaction zone by the effect of the combustible matl of supply subsequently.Selectively, combustible matl is compressed at least a portion when moving through reaction zone.
Described equipment comprises at least one tamping unit, comprises the reactor of reaction zone, at least one well heater and be used for the funnel of non-gasification resistates, the essence of this equipment is, reactor has elongated shape, and its longitudinal axis is from 45 ° of vertical direction maximum deviation, wherein tamping unit is arranged in the lowermost part of reactor, and non-gasification resistates funnel inlet is arranged in the top part of reactor.In addition, reactor comprises reaction zone, and this reaction zone contacts with at least one well heater.Non-gasification resistates funnel is being connected on the reactor above the reaction zone.Selectively, the level cross-sectionn of reaction zone is upwards narrowing down at least one part upward.Can select in the example at another, at least one supply-pipe is directed in the reaction zone, as steam and/or water supplying pipe.Selectively, at least one pillar is positioned at reactor on its prolonging direction.Can select in the example at another, well heater is electrically heated coil and/or burner.Tamping unit selectively comprises at least one piston, and this piston advantageously has circular bottom part, arranges at least one pillar or worm screw therein in the heart, and advantageously worm screw coiling around pillar is arranged.If the reactor filling orifice is provided with rib, then realize the favourable example selected, this rib advantageously comprises towards the upwardly extending conical surface in the side of reaction zone.
The advantage of described method and apparatus is, the gas that is produced does not comprise tar, and this helps the operation of losing efficacy of the nothing of the technology of being associated.The gas that is produced has high calorific value, decomposes the combustible material that produces because it is added with by tar.Described method is controlled by temperature regulation with by the supply of combustible matl easily.Described method be also advantageous in that energy requirement is low.In addition, the gas that is produced can be used in the technology of being associated.Another advantage is, all organic constraints or freely carbon can change into gas.Be also advantageous in that process can be moved continuously, the gas that is produced has even composition, and the amount of solid residue is minimized, and solid residue also can be removed from reaction zone continuously.For the process steam blast that in reactor, moves or the advantage of water supply be, make in non-gasification resistates freely or the amount of the carbon of organic constraint minimize, because it has the generation of hydrogen simultaneously by having converted carbon monoxide to the water reaction, this makes plant efficiency be promoted.
The advantage of described equipment is that it has simple and compact design, because all processes all occur in the reaction zone, described all processes that is heating, gasification, reduction reaction and selectable aqueous vapor body produce.Other advantage comprises the mutability of physicals of mutability, the combustible matl of capacity, for example liquid portion of different grain size or different content.Also have following advantage: described equipment can be designed to movably.Another advantage is, need not institute's pyrolytic gas is exported analysis, and described equipment do not rely on other technology, as gas processing device.
Description of drawings
Fig. 1 represents the synoptic diagram according to the equipment of example 4, and Fig. 2 represents the equipment according to example 5.
Embodiment
Example 1
In example 1, combustible matl is the fermentation sanitation waste (fermentatively hygienized waste) from agricultural or foodstuffs industry production.Combustible matl is supplied to reaction zone continuously, and this reaction zone is heated by gas burner, and isolates with surrounding atmosphere.When by system, combustible matl is exposed under the temperature that raises gradually, produces the gas by combustible matl, and this gas is exposed to than under the higher temperature of the temperature of combustible matl (gas produces from this combustible matl).When gas was by combustible matl, chemical reaction was carrying out, and caused the gasification of interpolation part (additional portions) of combustible matl and the variation of gas chemical ingredients.Be heated to during 150 ℃, water evaporation and absorption gas are as the CO that discharges in the first batch
2And CH
4Temperature about 250 ℃ is being represented and is being attended by CO
2The organic compound cracked that produces with CO begins.Be higher than under 300 ℃ the temperature, division (fission) reaction continues, and produces CO
2And CO, and begin to cause producing CH
4And H
2Other decomposition reaction.Be higher than under 350 ℃ the temperature, tar material begins to discharge, and combustible matl loses the resistates of constraint hydrogen and oxygen.Be higher than under 550 ℃ the temperature, in fact raw organic material resolves into carbon, the gas that has discharged and tar material.If temperature continues to raise, be higher than 700 ℃ temperature, will the decomposition of tar material and the generation of hydrogen take place.Be higher than under 800 ℃ the temperature, Bu Duaer (Boudouard) reaction begins to manifest, and causes CO content to increase gradually, and simultaneously, the CO in gas
2And O
2Content reduces.Simultaneously, because the decomposition of the division of tar material and steam produces other hydrogen partial,, form this steam when combustible matl passes through previous heating phase time at a lower temperature.This decomposition occurs on the carbon field of abundant heat (full-hot), and causes the carbon content in combustible matl to reduce, and causes the carbon content in gas to increase simultaneously.
Just deviate from reaction zone to a spool (shaft) and locate in case combustible matl, has the not flammable resistates of the temperature that is not more than 1200 ℃ by reaction zone, it is collected at this place, and removes termly from this.
Example 2
Example 2 is that with the difference of example 1 reaction zone is electrically heated, and the combustible matl that forms weighting material is batched termly by pre-determined volume in the equipment, and the steam content in reaction zone increases by supplying with steam from external source.In this case, H
2Want much strong with the generation of CO, and the amount of non-gasification resistates is lower, because almost be not included in free carbon wherein, also without any other organic carbon compound.
Example 3
Example 3 is that with the difference of example 1 combustible matl comprises minimum 30% tire.
Example 4
Be used for the combustible matl pyrolytic conversion is become pyrolysis gas and non-gasification resistates according to example 4
8Equipment comprise: tamping unit
1Reactor
2, comprise reaction zone
5Low-temperature heater
3And high temperature heater (HTH)
13And funnel
4, be used for non-gasification resistates
8By thermofin
12The reactor that covers
2Have elongated shape, its longitudinal axis is vertical.Tamping unit
1Be positioned at reactor
2Lowermost part in, and be used for non-gasification resistates
8Funnel
4Import be positioned at reactor
2The top part in.Reactor
2 Comprise reaction zone
5, this reaction zone
5With two well heaters
3,
13All contact.Pneumatic outlet
16At reactor
2The vertex place be directed into reactor 2.With high temperature heater (HTH)
13Reaction zone in the contacted part
5The level cross-sectionn along upward to and reduce.Be used for supplying with the inlet pipe of steam and/or water
6Be directed to reaction zone
5In.Pillar
9Also be positioned at reactor
2In, along reactor
2Longitudinal axis.
Low-temperature heater
3And high temperature heater (HTH)
13All represent electrically heated coil (spiral).Tamping unit
1Comprise piston
10, this piston
10Have circular bottom part, arrange pillar therein in the heart
9Reactor
2Filling orifice
14Be provided with rib
15Rib
15Have frustoconical shape, its big bottom is positioned at reaction zone
5That side on.Equipment according to this example is worked by the mode of describing in example 2.
Example 5
Difference according to example 5 equipment that is used for the combustible matl pyrolytic conversion and the equipment of describing in example 4 is that any inlet pipe 6 is directed into reaction zone
5In, be used for supplying with steam and/or water, and low-temperature heater
3And high temperature heater (HTH)
13All represent gas burner, reactor
2Filling orifice
14Be not provided with rib
15, and tamping unit
1Comprise worm screw
7, this worm screw
7At pillar
9Coiling is on every side arranged.Equipment according to this example is worked by the mode of describing in example 1.
Industrial applicibility
The mixture that the present invention can be used to process all solids article or mainly has solid article, these solid articles comprise free or organic constraint carbon, perhaps for solid article gasification or concentrating for the material that forms flammable residue not.
Claims (according to the modification of the 19th of treaty)
1. the method for combustible matl pyrolytic conversion, wherein combustible matl is supplied to reaction zone with pulsing continuously or, this reaction zone and surrounding atmosphere are isolated, after this, combustible matl is along leaving the identical direction of direction of combustible matl with the gas that is discharged, move to the reaction zone outlet gradually by reaction zone, it is characterized in that, reaction zone is heated to following temperature: the value of this temperature increases along the direction of orientating reaction district outlet, yet be 1200 ℃ to the maximum, combustible matl is compressed at least a portion when moving through reaction zone, and subsequently, after the passing through of reaction zone, the gas that is discharged is detached from non-gasification resistates discretely at combustible matl.
2. method according to claim 1 is characterized in that, before combustible matl enters reaction zone and/or its when the reaction zone, take water vapor and/or water to combustible matl.
3. method according to claim 1 is characterized in that, the combustible matl that before has been filled in the reaction zone moves through reaction zone by the effect of the combustible matl of supply subsequently.
4. be used for combustible matl (11) pyrolytic conversion is become the equipment of pyrolysis gas and non-gasification resistates (8), comprise: tamping unit (1); Reactor (2) comprises reaction zone (5) and at least one well heater (3,13); And funnel (4), be used for non-gasification resistates (8), it is characterized in that, reactor (2) has elongated shape, and its longitudinal axis is from 45 ° of vertical direction maximum deviation, wherein tamping unit (1) is arranged in the lowermost part of reactor (2), and the import that is used for the funnel (4) of non-gasification resistates (8) is positioned at the top part of reactor (2), and reactor (2) also comprises reaction zone (5), this reaction zone (5) and at least one well heater (3,13) contact, the funnel (4) that is used for non-gasification resistates (8) is connected to reactor (2) in reaction zone (5) top, it is characterized in that, the level cross-sectionn of reaction zone (5) is upwards narrowing down at least one part upward, and at least one pillar (9) is positioned at reactor (2) on its prolonging direction.
5. the equipment that is used for the combustible matl pyrolytic conversion according to claim 4 is characterized in that, at least one inlet pipe (6) is directed in the reaction zone (5), as steam and/or water supplying pipe.
6. the equipment that is used for the combustible matl pyrolytic conversion according to claim 4 is characterized in that, well heater (3,13) is electrically heated coil and/or burner.
7. the equipment that is used for the combustible matl pyrolytic conversion according to claim 4 is characterized in that, tamping unit (1) comprises at least one piston (10), and this piston (10) advantageously has circular bottom part, arranges at least one pillar (9) therein in the heart.
8. the equipment that is used for the combustible matl pyrolytic conversion according to claim 4 is characterized in that, tamping unit (1) comprises at least one worm screw (7), and advantageously at least one worm screw (7) is coiled layout on every side at pillar (9).
9. the equipment that is used for the combustible matl pyrolytic conversion according to claim 4, it is characterized in that, (2) filling orifice (14) of reactor (2) is provided with rib (15), and this rib (15) advantageously has at the conical surface towards the upwardly extending rib in the side of reaction zone (15).
Claims (12)
1. the method for combustible matl pyrolytic conversion, it is characterized in that, the present invention supplies to reaction zone with combustible matl with pulsing continuously or, this reaction zone and surrounding atmosphere are isolated, after this, combustible matl is along leaving the identical direction of direction of combustible matl with the gas that is discharged, move to the reaction zone outlet gradually by reaction zone, and reaction zone is heated to following temperature: the value of this temperature increases along the direction of orientating reaction district outlet, yet be 1200 ℃ to the maximum, and after the passing through of reaction zone, the gas that is discharged is detached from non-gasification resistates discretely at combustible matl.
2. method according to claim 1 is characterized in that, before combustible matl enters reaction zone and/or its when the reaction zone, take water vapor and/or water to combustible matl.
3. method according to claim 1 is characterized in that, the combustible matl that before has been filled in the reaction zone moves through reaction zone by the effect of the combustible matl of supply subsequently.
4. method according to claim 1 is characterized in that combustible matl is compressed at least a portion when moving through reaction zone.
5. be used for combustible matl (11) pyrolytic conversion is become the equipment of pyrolysis gas and non-gasification resistates (8), comprise: tamping unit (1); Reactor (2) comprises reaction zone (5) and at least one well heater (3,13); And funnel (4), be used for non-gasification resistates (8), it is characterized in that, reactor (2) has elongated shape, and its longitudinal axis is from 45 ° of vertical direction maximum deviation, wherein tamping unit (1) is arranged in the lowermost part of reactor (2), and the import that is used for the funnel (4) of non-gasification resistates (8) is positioned at the top part of reactor (2), and reactor (2) also comprises reaction zone (5), this reaction zone (5) and at least one well heater (3,13) contact, the funnel (4) that is used for non-gasification resistates (8) is connected to reactor (2) in reaction zone (5) top.
6. the equipment that is used for the combustible matl pyrolytic conversion according to claim 5 is characterized in that, the level cross-sectionn of reaction zone (5) is upwards narrowing down at least one part upward.
7. the equipment that is used for the combustible matl pyrolytic conversion according to claim 5 is characterized in that, at least one inlet pipe (6) is directed in the reaction zone (5), as steam and/or water supplying pipe.
8. the equipment that is used for the combustible matl pyrolytic conversion according to claim 5 is characterized in that, at least one pillar (9) is positioned at reactor (2) on its prolonging direction.
9. the equipment that is used for the combustible matl pyrolytic conversion according to claim 5 is characterized in that, well heater (3,13) is electrically heated coil and/or burner.
10. the equipment that is used for the combustible matl pyrolytic conversion according to claim 5 is characterized in that, tamping unit (1) comprises at least one piston (10), and this piston (10) advantageously has circular bottom part, arranges at least one pillar (9) therein in the heart.
11. the equipment that is used for the combustible matl pyrolytic conversion according to claim 5 is characterized in that, tamping unit (1) comprises at least one worm screw (7), and advantageously at least one worm screw (7) is coiled layout on every side at pillar (9).
12. the equipment that is used for the combustible matl pyrolytic conversion according to claim 5, it is characterized in that, (2) filling orifice (14) of reactor (2) advantageously is provided with rib (15), and this rib (15) advantageously has at the conical surface towards the upwardly extending rib in the side of reaction zone (15).
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CZPV2007-553 | 2007-08-16 | ||
| CZ20070553A CZ2007553A3 (en) | 2007-08-16 | 2007-08-16 | Method of and apparatus for pyrolytic conversion of combustible material |
| PCT/CZ2008/000052 WO2009021471A2 (en) | 2007-08-16 | 2008-05-12 | Method and equipment for pyrolytic conversion of combustible material |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101778926A true CN101778926A (en) | 2010-07-14 |
Family
ID=39820945
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200880103022A Pending CN101778926A (en) | 2007-08-16 | 2008-05-12 | The method and apparatus that is used for the pyrolytic conversion of combustible matl |
Country Status (7)
| Country | Link |
|---|---|
| US (1) | US20100140074A1 (en) |
| EP (1) | EP2197982A2 (en) |
| JP (1) | JP2010536536A (en) |
| CN (1) | CN101778926A (en) |
| CZ (1) | CZ2007553A3 (en) |
| RU (1) | RU2010107304A (en) |
| WO (1) | WO2009021471A2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105012267A (en) * | 2015-08-19 | 2015-11-04 | 海南科进生物制药有限公司 | Rebamipide tablet and preparation method thereof |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CZ306173B6 (en) * | 2012-06-28 | 2016-09-07 | Polycomp, A.S. | Line for the treatment of waste containing predominantly plastics and cellulose and method of treating waste on that line |
Family Cites Families (8)
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|---|---|---|---|---|
| BE487697A (en) * | ||||
| US4004982A (en) * | 1976-05-05 | 1977-01-25 | Union Oil Company Of California | Superatmospheric pressure shale retorting process |
| JPH0192291A (en) * | 1987-10-02 | 1989-04-11 | Kanagawa Pref Gov | Dry distillation apparatus |
| DE19928581C2 (en) * | 1999-06-22 | 2001-06-28 | Thermoselect Ag Vaduz | Process and device for the disposal and utilization of waste goods |
| JP4938920B2 (en) * | 2000-02-29 | 2012-05-23 | 三菱重工業株式会社 | Biomass gasification furnace and biomass gasification system |
| JP2003221111A (en) * | 2002-01-31 | 2003-08-05 | Oriental Kiden Kk | Dioxin volatilization and separation device |
| JP2005179509A (en) * | 2003-12-19 | 2005-07-07 | Matsushita Electric Ind Co Ltd | Method of heating |
| JP2006143983A (en) * | 2004-10-20 | 2006-06-08 | Mitsui Eng & Shipbuild Co Ltd | Method of operating gasifier and gasifier |
-
2007
- 2007-08-16 CZ CZ20070553A patent/CZ2007553A3/en unknown
-
2008
- 2008-05-12 RU RU2010107304/05A patent/RU2010107304A/en not_active Application Discontinuation
- 2008-05-12 EP EP08757906A patent/EP2197982A2/en not_active Withdrawn
- 2008-05-12 US US12/671,696 patent/US20100140074A1/en not_active Abandoned
- 2008-05-12 JP JP2010520414A patent/JP2010536536A/en active Pending
- 2008-05-12 WO PCT/CZ2008/000052 patent/WO2009021471A2/en active Application Filing
- 2008-05-12 CN CN200880103022A patent/CN101778926A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105012267A (en) * | 2015-08-19 | 2015-11-04 | 海南科进生物制药有限公司 | Rebamipide tablet and preparation method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| RU2010107304A (en) | 2011-09-10 |
| CZ2007553A3 (en) | 2009-02-25 |
| WO2009021471A4 (en) | 2009-05-28 |
| JP2010536536A (en) | 2010-12-02 |
| WO2009021471A3 (en) | 2009-04-09 |
| US20100140074A1 (en) | 2010-06-10 |
| EP2197982A2 (en) | 2010-06-23 |
| WO2009021471A2 (en) | 2009-02-19 |
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