WO2012137192A1 - Dispositif pour valoriser des matières organiques, et produit obtenu - Google Patents

Dispositif pour valoriser des matières organiques, et produit obtenu Download PDF

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Publication number
WO2012137192A1
WO2012137192A1 PCT/ID2012/000002 ID2012000002W WO2012137192A1 WO 2012137192 A1 WO2012137192 A1 WO 2012137192A1 ID 2012000002 W ID2012000002 W ID 2012000002W WO 2012137192 A1 WO2012137192 A1 WO 2012137192A1
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WO
WIPO (PCT)
Prior art keywords
organic material
passageway
coal
coal product
screw
Prior art date
Application number
PCT/ID2012/000002
Other languages
English (en)
Inventor
IR. Harsudi SUPANDI
Original Assignee
Pt. Total Sinergy International
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Pt. Total Sinergy International filed Critical Pt. Total Sinergy International
Publication of WO2012137192A1 publication Critical patent/WO2012137192A1/fr

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Classifications

    • 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
    • C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
    • 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
    • C10B47/28—Other processes
    • C10B47/32—Other processes in ovens with mechanical conveying means
    • C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
    • 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
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
    • C10B57/10—Drying
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10F—DRYING OR WORKING-UP OF PEAT
    • C10F5/00—Drying or de-watering peat
    • C10F5/06—Drying or de-watering peat combined with a carbonisation step for producing turfcoal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining

Definitions

  • This invention relates to a device for upgrading of organic materials, and more particularly to a device for pyrolysis of low rank coals and a resulting product.
  • Organic materials include coals, peat, biomass, garbage, etc. Large quantities of coal, including low rank coal, exist at many places in the world. Organic materials such as low rank coal have been considered as fuel and a source of energy. However, such low rank coal typically contains relatively large amounts of water - on the order of 30-60% by weight.
  • low-rank coal The physical structure of low-rank coal is understood to be determined by the effect of oxygen functional groups on hydrogen bonding and the role of moisture as a structural component. Phenolic groups provide a framework for hydrogen bonding, whereas carboxyl groups hinder such structuring. Roughly 20% of the total moisture is held tightly by hydrogen bonding and is believed to contribute to structural rigidity in low rank coals, wood and similar low-rank organic materials. The loss of this structure when coal is dried accounts for the problems of friability and dustiness. Dusty coal is difficult to work with for several reasons. These include the fact that the coal dust is prone to move with slight disturbances in the air, so during transportation and use the coal dust can easily spread in a relatively uncontrolled manner. Further, such coal dust is prone to combust too rapidly for many applications.
  • US Patent 5,322,530 to Merriam et al discloses another technique for upgrading the rank of coal by use of fluidized beds in a three step process (dryer, pyrolyzer, cooler), A fluidized bed is formed when a quantity of a solid particulate substance (such as coal ground to a very fine particulate) is placed under appropriate conditions to cause a solid/fluid mixture to behave as a fluid. This is achieved by the introduction of a fluid (often an inert gas) through the particulate medium.
  • a fluid often an inert gas
  • crushed coal is fed into a fluidized bed dryer and hot gas with low oxygen content is directly introduced to the coal as a drying gas.
  • the gas is a mixture of recycled gas and flue gas from a burner.
  • the coal After drying the coal is sent to a pyrolyzer, another fluidized bed which uses heat from a flue gas to heat the coal to produce tar-like pitch in the vapour state to coat the coal. From the pyrolyzer, the coal is sent to a cooler. The cooler is another fluidized bed which gradually brings the temperature down to above 220°F (104°C).
  • Merriam's fluidized beds are relatively expensive and use a direct heating agent. Such direct heating is difficult to control, and can lead to charring of some of the coal and uneven removal of volatiles. Further, many fluidized bed systems only work with a very narrow range of particle sizes. Too small and the fluid will blow the particles in an uncontrolled manner; too large and the particles will not react in a significant way.
  • a device for upgrading solid organic material comprises a heat source for heating a heat exchange medium, a housing having an inlet, and defining a material passageway adapted to receive the organic material from the inlet, a burner box adjacent the housing and defining a heat exchange medium passageway adapted to receive the heat exchange medium.
  • the organic material is physically separated from the heat exchange medium passageway.
  • a quencher is operatively connected to the material passageway and adapted to apply a quenching agent directly onto the organic material and thereby form a resulting product.
  • the resulting coal product has specific characteristics which can be preselected, including total water content, volatile matter, calorific value and HGI.
  • FIG. 6 is a cross section view taken through an optional tunnel drier of the embodiment of Fig. 3.
  • Fig. 7 is an schematic isometric view of an alternate embodiment of device for upgrading organic materials.
  • Fig. 8 is a side view of the device of Fig. 7.
  • Fig. 9 is a top view of the device of Fig. 7.
  • Fig. 10 is a block diagram of a device for upgrading organic material in accordance with another embodiment, optionally incorporating a flash drying stage and/or a flash setting stage.
  • Fig. 1 1 is a schematic view of a device for upgrading organic material, showing one embodiment with a flash drying stage.
  • Fig. 1 1 is a schematic view of a device for upgrading organic material, showing one embodiment with a flash drying stage.
  • Fig. 1 1 is a schematic view of a device for upgrading organic material, showing one embodiment with a flash drying stage.
  • FIG. 12 is an isometric view of a direct heating device in accordance with one embodiment.
  • Fig. 13 is a cross section view of the direct heating device of Fig. 11 , taken through a fuel inlet.
  • Fig. 14 is another cross section view of the direct heating device of Fig. 11 , shown facing the fuel inlet.
  • the appended drawings are not necessarily to scale, presenting a somewhat simplified representation of various features illustrative of the basic principles of the invention.
  • the specific design features of the device for upgradingorganic materials as disclosed here, including, for example, the specific dimensions of the housing will be determined in part by the particular intended application and use environment. Certain features of the illustrated embodiments have been enlarged or distorted relative to others to help provide clear
  • Fig. 1 shows an example of a device 10 and method for upgrading an organic material such as low rank coal. Substitution of other organic materials, such as biological sources of carbon (trees) or waste materials, is straightforward and will be readily apparent to those skilled in the art given the benefit of this disclosure. Upgrading is understood here to at least refer to increasing the calorific value of the organic material for a given mass, and typically comprises pyrolyzing a significant portion of the organic material.
  • the device comprises at least one heat source 90, an enclosure, a cooling device such as quencher 60, a controller 80 and related equipment.
  • the enclosure can comprise, for example, at least one screw heat exchanger 50 and a burner box 21.
  • the enclosure has a drying zone 20 and a setting zone 30.
  • the heat source heats the feed material in the drying zone, and also heats the feed material in the setting zone.
  • the heat source can be a single heat source, or a plurality of heat sources.
  • the quencher 60 would be positioned at or after a quality control zone 40.
  • the enclosure is a single enclosure such as a single screw heat exchanger and both a drier/drying zone and the setting zone are positioned within the single screw heat exchanger.
  • the screw heat exchanger comprises a housing 22, an inlet 26 into a material passageway 29, a screw 24 (which can comprise one continuous flange or a plurality of flanges), and an outlet 28.
  • a rotary valve may be positioned at the inlet, the outlet, or both the inlet and outlet to help isolate the material passageway 29 from the outside environment.
  • the housing 22 acts as a drier, as the feed material is dried in the material passageway inside the housing.
  • the housing also acts as a location for setting the feed material, where vplatiles are emitted.
  • At least partially surrounding the housing 22 is a jacket or burner box/firebox 21 which defines a heat exchange medium passageway 23 which is operatively connected to the heat source.
  • heating of the organic material occurs indirectly. This advantageously helps to ensure more even and complete heating of the feed material and avoid excessive drying, especially on the surface of smaller particles.
  • the material passageway has at least a lower portion which is formed as a lower part of a cylindrical tube with a generally semi-circular cross section corresponding to each screw.
  • the lower portion can extend about 1 ⁇ 2 of a circle, for example.
  • the flanges of the screw extend from a central trunk located along an axis of rotation and extend along the material passageway.
  • the cross section extends from the axis of rotation to an inner wall of the material passageway.
  • the flanges have a width which, in combination with a portion of the central trunk extending from the axis of rotation, is nearly the same but somewhat less (i.e., at least 85%, more preferably, at least 95%) than a radius of the cross section of the lower portion of the material passageway. (Of course, the flange does not extend beyond the inner wall of the material passageway.)
  • the heat is supplied by a heat exchange medium produced by the heat source(s), which can be, for example, exhaust gases from one or more gasification burners 90. These exhaust gases enter the heat exchange medium passageway 23 and heat the burner box/firebox.
  • the heat source 90 can be a gasification burner and the heat exchange medium hot exhaust gases generated by the gasification burner.
  • the burner can use coal as a fuel source.
  • the coal used at the burner may be prescreened for size prior to introduction into the material passageway within the housing.
  • upgraded coal fines generated by the device 10 may be used as a source of fuel.
  • some heat from the burner or optionally from a separate burner when the heat source is more than one burner may be used to merely dry the coal in another drier 70, which can comprise, for example, another auger/screw heat exchanger.
  • drier 70 no setting would be required. Small particles or fines dried by this drier also may be used as a source of fuel in the gasification burner.
  • coal fines also may be segregated out of the coal introduced at the inlet and either used in the burner or returned to the mine or otherwise used.
  • the device and method described herein allow for a wider range of coal particles than would be possible with fluidized bed systems, coal particles that are too large will not be completely heated to a necessary temperature range, and those that are too small are difficult to work with and often not desired by end use customers.
  • Drying of the feed material occurs in the drying zone 20.
  • low rank coals contain 40-60% water, and water vapour is typically the first component material to be emitted by coal particles in a heating process.
  • the drying zone typically operates at a drying temperature range from ambient to about 400°C, depending on the type of feed material introduced.
  • the exhaust air used may be several hundred degrees warmer.
  • a motor 27 controls auger rotation speed.
  • the length of the auger also can be varied to control the time the feed material is exposed to heat.
  • the temperature of the firebox and the time in the drying zone must be sufficient to evaporate a large percentage of the water present in the feed material. However, it is not necessary to eliminate all water from the feed material.
  • Maximum temperatures are limited by the temperatures of the incoming heat transfer medium. For gasification burners, typical exhaust gas temperatures will not exceed 1600°C, and the exhaust gas is typically mixed with ambient air so as to be introduced into the heat exchange medium passageway at temperatures around 500-800°.
  • Such temperatures can be sufficient for drying and for setting the organic material.
  • Most of the energy imparted to the feed material at the drying stage is used to liberate water as steam.
  • no additional inert gas in required to be pumped into the housing. Rather, steam and/or superheated steam can be retained in the material passageway of the housing such that an overpressure above atmospheric pressure is maintained.
  • Such overpressure can be above atmospheric and is typically no more than 5 bar, and more typically less than 2 bar. Positive pressure keeps oxygen containing air out of the material passageway, allowing for at least some pyrolysis of the feed material.
  • Volatile matter in organic materials such as coal refer to the components of coal, except for moisture, which are liberated at high temperature in low levels of or absence of oxygen. This is usually a mixture of compounds with carboxyl (-COOH) and hydroxyl (-OH) groups, short and long chain hydrocarbons, aromatic hydrocarbons and some sulfur and sulfur- containing compounds.
  • carboxyl -COOH
  • hydroxyl -OH
  • the steps of drying and setting and the drying and setting zones are not absolutes. Rather, initial heating of the fuel releases water principally, but may also release some volatile matter. Continued heating evolves the compounds with the carboxyl and hydroxyl groups, then the short chain hydrocarbons.
  • At least the step of setting the feed material can occur in an enclosure with a pressurization apparatus pressurized to above atmospheric pressure.
  • a pressurization apparatus pressurized to above atmospheric pressure.
  • a longer length of time is required for drying than for setting due to higher energy requirements to evaporate water from the feed material.
  • a pressure above atmosphere may be maintained at both zones 20, 30 during operation.
  • the pressurization apparatus uses steam and/or superheated steam and volatile matter emitted from the coal feed material as the source of gases for maintaining the overpressure.
  • the pressurization apparatus can comprise the housing 22 of the screw heat exchanger 50 working in combination and any feed material positioned in the material passageway 29, without any additional valves to cap the device, as for many types of organic materials sufficient overpressure may be maintained merely by
  • the enclosure need not be completely sealed off from the outside environment.
  • at least one valve may be operatively connected to the material passageway to seal the material passageway from the external environment.
  • the controller can also control flow rates at the sprays.
  • a temperature controller is part of the controller and can control temperature so as to define a drying zone in the material passageway 29 heated to the drying temperature range, and a setting zone in the material passageway heated to the setting temperature range. As noted previously, the setting temperature range is greater than the drying temperature range.
  • the resultant coal product can have some or all of the following properties, as desired: coal particles having an average HGI of 45-60, a particle size in a range between 5 mm and 30 mm, with some of the coal particles being of a larger particle size in the range of 20-30 mm, and some of the coal particles being of a smaller particle size in the range of 5 mm to 6.5 mm.
  • the larger coal particles have a total moisture content which is larger closer to the centre than it is at the exterior, and a reflectance which is lower closer to the centre than it is at the exterior. The change in reflectance is a result of the heating being applied to the surface.
  • the resultant coal particles can also have a calorific value which varies by size of the particle.
  • the smaller particle size has a calorific value that is higher than a calorific value of the larger particle size of the resulting coal product.
  • An amount of dry, ash-free volatile matter of the resulting coal product of the larger particle size can be larger than an amount of dry, ash-free volatile matter of the resulting coal product of the smaller particle size.
  • the examples in the tables below are for several different kinds of starting organic material including a low rank coal such as a lignite, and an intermediate rank coal such as sub-bituminous coal.
  • the resulting products are partially a function of the organic material used as a starting feed material, but also can be tailored beyond the ranges listed, if desired. For example, if very low amounts of moisture are desired in the resulting product, the drying stage can be extended. If lower HGI levels are requested, quenching speed can be increased.
  • the device and process disclosed herein creates a significant percentage difference between the starting organic material and the resulting product in terms of HGI, calorific value, moisture content, oxygen and hydrogen content, are available in the ranges shown in the tables.
  • "daf refers to dry ash free coal
  • ar refers to as received.
  • Link 91 effectively connects the housing to the burner box such that volatile matter emitted by the feed material is burned by the heat source, and thereby advantageously use some of what might otherwise be a waste product as a combustible source of heat for operating the device.
  • Valves may be positioned at any or all of the chimneys and at the inlet and outlet as part of the pressurization apparatus. The valves are operatively connected to the material passageway and can vent steam and/or volatile matter from the material passageway when pressure in the material passageway exceeds a predetermined limit.
  • Fig. 4 also shows that burner boxes 123 and 223 are set at different heights.
  • Fig. 7 shows another embodiment of a device 210 for upgrading solid organic material such as coal suitable for large volume operations.
  • the device is scalable and modular, and so can advantageously be adjusted for different volume operations.
  • the drying zone 220 comprises a plurality (here six) of screw heat exchangers
  • a setting zone 230 comprises a plurality (here six) of screw heat exchangers
  • a quality control zone 240 comprises another plurality (again six) of screw heat exchangers.
  • a separate screw is used with each screw heat exchanger.
  • a pulverizer 340 may be used to ensure particle sizes no greater than a predetermined maximum such as 30 mesh (0.595 mm), for example. This will help ensure more thorough combustion.
  • the burner box 323 operatively connects all of the burners together and defines the heat exchange medium passageway.
  • the hot exhaust air from the burners 90 may deposit particulates in the burner box 323 which can be removed intermittently to help reduce the amount of solid products of combustion.
  • the passageway is adjacent at least one housing of a screw heat exchanger. That is, a wall of the burner box is next to or part of a wall which defines the heat exchange medium passageway. In this way heat transfer can occur from the heat exchange medium to the solid organic material indirectly, with the wall or walls physically separated the exhaust gas from the solid organic material, and therefore advantageously uniformly heating the solid organic material, generally without the exhaust gas directly contacting the feed material.
  • the burner box effectively supplies heat to all 18 screws. The feed organic material is pushed by screws so as to travel through the several zones 220, 230, 240.
  • the feed material may be quenched using a quencher spraying fluid directly onto the feed material to form a resulting product in a similar manner as discussed above.
  • the burner box 323 can be operatively connected to an exhaust port or flue gas stack 290 to vent exhaust gas.
  • the exhaust port may be operatively connected to a turbine, such that waste heat can be used to generate electricity.
  • the order of the device 210 and a turbine may be reversed.
  • exhaust gases from the burners may be used in the most efficient manner to capture a large amount of the heat from the exhaust gas.
  • exhaust gas from the heat sources 90 transfers their heat indirectly to the organic material, liberating emissions such as steam and volatiles.
  • Chimneys 225, 235 and 245 may be provided at each stage to vent these emissions from the solid organic material.
  • emissions generated as a result of the process can be at least partially captured.
  • steam is mostly emitted.
  • Such steam can be captured, filtered and purified, and/or put to work in a steam turbine to generate electricity.
  • water may be collected and used as desired.
  • Any of the aforementioned embodiments may be used in combination with a steam turbine and generator.
  • volatiles (which primarily tend to be emitted at the higher temperatures of the later setting zone 230 and quality control zone 240) may be captured and processed as well.
  • the controller may also control rate of application of the quenching agent, and rate of speed of the conveyor belts and related assemblies 300, 302, as needed, so that all elements of the device function together to ensure continuous upgrading of low rank organic materials.
  • Fig. 10 shows an additional, faster or flash drying stage.
  • Figs. 12-14 show one embodiment of a direct heating device suitable for use as part of the flash drying stage and/or the flash setting stage.

Abstract

L'invention concerne un dispositif pour valoriser une matière organique solide, qui comprend: un corps comportant un orifice d'entrée et qui définit un passage de matière conçu pour recevoir la matière organique provenant de l'orifice d'entrée; un carter de brûleur, qui se situe de façon adjacente au corps et définit un passage de milieu d'échange de chaleur conçu pour recevoir un milieu d'échange de chaleur. La matière organique est séparée physiquement du passage de milieu d'échange de chaleur. Un élément d'extinction, relié exploitable au passage de matière, est conçu pour appliquer un agent extincteur directement sur la matière organique et former ainsi un produit obtenu. Le produit de charbon obtenu présente des caractéristiques spécifiques pouvant être présélectionnées, y compris la teneur totale en eau, les matières volatiles, la valeur calorifique et l'indice de broyabilité Hardgrove (HGI).
PCT/ID2012/000002 2011-04-07 2012-04-05 Dispositif pour valoriser des matières organiques, et produit obtenu WO2012137192A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SG201102492 2011-04-07
SG201102492-4 2011-04-07

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WO2012137192A1 true WO2012137192A1 (fr) 2012-10-11

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014173054A1 (fr) * 2013-04-26 2014-10-30 郑州永通特钢有限公司 Système et procédé de distillation sèche et d'extinction pour poudre de lignite

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5254139A (en) * 1991-08-05 1993-10-19 Adams Robert J Method for treating coal
JPH08259953A (ja) * 1995-03-22 1996-10-08 Nippon Steel Corp コークス製造用石炭の事前処理方法
JPH09279151A (ja) * 1996-04-12 1997-10-28 Nippon Steel Corp コークス炉装入石炭の粉砕方法
US6447559B1 (en) * 1999-11-05 2002-09-10 Saudi American Minerals Inc. Treatment of coal
WO2009128819A1 (fr) * 2008-04-15 2009-10-22 Larry Hunt Procédé de valorisation de charbon

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5254139A (en) * 1991-08-05 1993-10-19 Adams Robert J Method for treating coal
JPH08259953A (ja) * 1995-03-22 1996-10-08 Nippon Steel Corp コークス製造用石炭の事前処理方法
JPH09279151A (ja) * 1996-04-12 1997-10-28 Nippon Steel Corp コークス炉装入石炭の粉砕方法
US6447559B1 (en) * 1999-11-05 2002-09-10 Saudi American Minerals Inc. Treatment of coal
WO2009128819A1 (fr) * 2008-04-15 2009-10-22 Larry Hunt Procédé de valorisation de charbon

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
PATENT ABSTRACTS OF JAPAN *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014173054A1 (fr) * 2013-04-26 2014-10-30 郑州永通特钢有限公司 Système et procédé de distillation sèche et d'extinction pour poudre de lignite

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