WO2010139854A1 - Method of carrying out pyrolysis and pyrolysis apparatus - Google Patents

Method of carrying out pyrolysis and pyrolysis apparatus Download PDF

Info

Publication number
WO2010139854A1
WO2010139854A1 PCT/FI2010/050443 FI2010050443W WO2010139854A1 WO 2010139854 A1 WO2010139854 A1 WO 2010139854A1 FI 2010050443 W FI2010050443 W FI 2010050443W WO 2010139854 A1 WO2010139854 A1 WO 2010139854A1
Authority
WO
WIPO (PCT)
Prior art keywords
pyrolysis
solid fuel
drying
section
pyrolysis reactor
Prior art date
Application number
PCT/FI2010/050443
Other languages
French (fr)
Inventor
Pekka Jokela
Jani Lehto
Original Assignee
Upm-Kymmene Corporation
Metso Power Oy
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 Upm-Kymmene Corporation, Metso Power Oy filed Critical Upm-Kymmene Corporation
Priority to RU2011152323/05A priority Critical patent/RU2571638C2/en
Priority to CN201080031520.9A priority patent/CN102459517B/en
Priority to CA2764220A priority patent/CA2764220A1/en
Priority to EP10727761A priority patent/EP2438141A1/en
Priority to US13/375,351 priority patent/US9045694B2/en
Priority to BRPI1011095A priority patent/BRPI1011095A8/en
Publication of WO2010139854A1 publication Critical patent/WO2010139854A1/en

Links

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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
    • C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
    • C10B49/22—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/36—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed through which there is an essentially horizontal flow of particles
    • 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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
    • C10B49/10—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form according to the "fluidised bed" technique
    • 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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
    • 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
    • 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
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • 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
    • C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
    • C10B55/02—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials
    • C10B55/04—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials with moving solid materials
    • C10B55/08—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials with moving solid materials in dispersed form
    • C10B55/10—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials with moving solid materials in dispersed form according to the "fluidised bed" technique
    • 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
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/28—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material
    • C10G9/32—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material according to the "fluidised-bed" technique
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/002—Fluidised bed combustion apparatus for pulverulent solid fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/303—Burning pyrogases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • F23G2203/501—Fluidised bed furnace with external recirculation of entrained bed material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • F23G2203/504—Fluidised bed furnace with essentially horizontal flow of bed material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
    • 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

Definitions

  • the present invention relates to method for carrying out pyrolysis and more particularly to a method according to the preamble of claim 1.
  • the present invention further relates to a pyrolysis apparatus and more particularly to a pyrolysis apparatus according to preamble of claim 17.
  • pyrolysis means converting fuel in inert conditions and in high temperature into gaseous state, which forms oil-like, different or- ganic compounds comprising liquid as it condensed.
  • Inert conditions mean oxygen-free conditions where no combustion of the fuel occurs.
  • Tar burning is one example of long known prior art pyrolysis process.
  • a pyrolysis process is a process based on using a fluidized bed technique.
  • solid feedstock is fed to a reactor com- prising a fluidized bed of hot inert bed material e.g. sand.
  • Inert fluidizing gas is used to fluidize the bed.
  • the feedstock will mix with the bed material, pyrolyze and form pyrolysis gases that are conducted out from the reactor.
  • the heat for the pyrolysis process can be provided for example arranging the pyrolysis reactor next to a fuel burning fluidized bed and circulating the thus heated bed material to the pyrolysis reactor.
  • the solid feedstock used in pyrolysis is dried in a thermal dryer before it is fed to the pyrolysis reactor. Usually the dryer is a separate drying apparatus. Thus the biomass is first dried and then conducted to the pyrolysis reactor.
  • pyrolysis oil may be used as fuel or refined into different chemicals. Production of pyrolysis oil from different kinds of biomass, for example from wood fuels, is studied for replacing coal and heavy fuel oil. Pyrolysis oil produced by pyrolysis contains optimally 25 weight-% water. If the water content is much higher, the product may end up to unwanted phase separation and end use of the pyrolysis oil becomes difficult or alcohol has to be added to the pyrolysis oil.
  • the water content in pyrolysis oil has to be maintained in certain range.
  • Water or moisture content varies with different biomass for example wood, wood chips, peat or other biomass. Reaching the 25 weight-% water or moisture content in pyrolysis oils means that the biomass has to be dried to moisture content 10 weight-% at most, preferably about 4 to 10 weight-% and more preferably 5 to 8 weight-%.
  • the moisture content of the dried biomass affects the water content of the produced pyrolysis oil.
  • the problem with the prior art drying arrangements is that using separate drying apparatuses in drying of the biomass does not enable effective control of the water content of the produced pyrolysis oil. Thus it is difficult to adjust the pyrolysis process such that the water content produced pyrolysis oil is in optimal range.
  • the desired moisture content of the biomass is as low as mentioned above, the biomass residence time in a dryer of a smaller size is very long.
  • Another alternative is to increase the size of the dryer, which will result in increase of drying equipment investment price and space requirement.
  • An object of the invention is to provide a method and an apparatus avoiding the above described problems.
  • the objects of the present invention are achieved with a method ac- cording to the characterizing portion of claim 1 .
  • the objects of the present invention are further achieved with a pyrolysis apparatus according to the characterizing portion of claim 17.
  • This arrangement enables the moisture content of the pyrolysis oil to be controlled by controlling the drying of the biomass in the pyrolysis reactor to produce py- rolysis oil that will have the optimum water content. Control of the drying of the biomass can be integrated into the online pyrolysis oil water content analyser.
  • the advantage of the present invention is that it enables effective control of the water content of the produced pyrolysis oil by adjusting the drying of the biomass.
  • the drying zone is arranged inside the pyrolysis reactor. Thus the drying and the pyrolysis are carried out in the same reactor.
  • Another advantage is that the need for separate, expensive and space consuming dryer is eliminated.
  • Figure 1 is schematic view of a pyrolysis reactor arranged in connection with a bubbling fluidized bed boiler
  • Figure 2 shows a side view of one embodiment of a pyrolysis reac- tor according to the present invention
  • Figure 3 shows a top view of the pyrolysis reactor of figure 2;
  • Figure 4 schematic view of a pyrolysis reactor arranged in connection with a circulating fluidized bed boiler;
  • Figure 5 shows a detailed view of the pyrolysis reactor of figure 4
  • Figure 6 shows another embodiment of a pyrolysis reactor arranged in connection with a circulating fluidized bed boiler
  • Figure 7 shows detailed view of the pyrolysis reactor of figure 6.
  • the present invention relates to a method of carrying out pyrolysis process for solid fuel to produce pyrolysis oil.
  • the pyrolysis process carried out is preferably so called fast pyrolysis.
  • the pyrolysis process in the pyrolysis reactor is divided into drying for drying the biomass and pyrolysis for pyrolyzing the dried biomass.
  • the drying of the biomass is conducted in the drying zone of the pyrolysis reactor and the pyrolysis of the dried biomass is carried out in the pyrolysis zone.
  • the pyrolysis process is divided into a drying zone and a pyrolysis zone, the drying zone being arranged upstream from the pyrolysis zone in the movement direction of the biomass in the pyrolysis process.
  • solid fuel refers to all kind of substantially solid bio- mass that is pyrolyzed in a pyrolysis reactor.
  • the solid fuel can be any solid biomass, such as wood, wood chips, saw dust, firewood, forest residue, urban wood waste, by products and waste of the papermaking industry, lumber waste and peat. Even though the material to be pyrolyzed is called solid fuel, it should be noted that the material will not burn in the pyrolysis process, but releases combustable gases that may be condensed into liquid form.
  • pyrolysis gases refers to gases that are formed in pyrolysis and that will be condensated in the process to form pyrolysis oil.
  • moisture containing gases refers to gases separated from the solid fuel in the drying zone of the pyrolysis reactor prior to pyrolysis of the solid fuel in the pyrolysis zone.
  • the solid fuel is preferably dried to a moisture content of 10 weight- % at most, preferably about 4 to 10 weight-% and more preferably 5 to 8 weight-% in the drying zone.
  • the moisture content of the produced pyrolysis oil is analyzed for controlling the drying of the solid fuel in the drying zone.
  • the analysis of the moisture content of the produced pyrolysis oil may be done for example with online water content analyser.
  • the measurements may be used for controlling the drying process of the solid fuel in the drying zone by adjusting the removal rate of the moisture containing gases from the drying zone.
  • the drying of the solid fuel in the dry- ing zone may be controlled by adjusting residence time of the solid fuel in the drying zone.
  • the residence time of the solid fuel may be controlled by adjusting the movement speed of the solid fuel in the drying zone. Furthermore, the drying of the solid fuel in the drying zone may be controlled by controlling the temperature in the drying zone.
  • the above discussed methods for controlling the drying of the solid fuel may be used separately or in any combination. According to the above mentioned methods the water content of the produced pyrolysis oil may be controlled by adjusting the process parameters of the pyrolysis process itself, particularly in the drying zone of the pyrolysis reactor.
  • the pyrolysis process according to the present invention is carried out in connection with a fluidized bed boiler.
  • solid fuel is supplied to a pyrolysis reactor and heat required for the pyrolysis is brought to the pyrolysis reactor at least partly with solid, particle like, bed material of the fluidized bed boiler.
  • the bed material of the fluidized bed boiler is circulated through the pyrolysis reactor and fluidized in the pyrolysis reactor by fluidizing gas.
  • the temperature of the bed material 40 is approximately 850 0 C in the fluidized bed boiler 30 and approximately 700 0 C in the pyrolysis reactor 4.
  • the pyrolysis gases produced from the dried solid fuel in the pyrolysis reactor are condensed into liquid form as so called pyrolysis oil.
  • the bed material coming from the fluidized bed boiler and the solid fuel are passed through the pyrolysis reactor in transverse direc- tion in relation to the flow direction of the fluidizing gas in the pyrolysis reactor.
  • the pyrolysis reactor is divided into a drying zone and a pyrolysis zone in the movement direction of the solid fuel and the bed material for drying the solid fuel prior to the pyrolysis of the solid fuel in the pyrolysis reactor. This means that the heat and thermal energy brought to the pyrolysis reactor by the bed material is used for pyrolyzing the solid fuel in the pyrolysis zone as well as for drying the solid fuel in the drying zone.
  • the thermal energy of the bed material of a fluidized bed boiler is used as a source of thermal energy in the pyrolysis reactor.
  • the moisture containing gases separated from the solid fuel in the drying zone are removed from the drying zone and the dried solid fuel is passed to the pyrolysis zone to be pyrolyzed.
  • the pyrolysis gases comprising tar-rich gases are removed from the pyrolysis reactor in the pyrolyzing zone.
  • the bed material and the solid fuel are passed essentially in hori- zontal direction through the pyrolysis reactor.
  • the drying zone and the pyrolysis zone may be divided to two sections, a drying section and a pyrolysis sections by a separating wall. There are holes provided in the wall to enable the travelling of the bed material and solid fuel from the drying section to the pyrolysis section.
  • the bed material moves in the pyrolysis reactor according to the principle of communicating vessels, because when fluidized, it behaves the same way as fluids.
  • the speed of movement of the bed material and solid fuel can be expedited by positioning the fluidizing nozzles to provide the fluidizing air to the preferred direction.
  • the drying may be controlled in the drying zone by adjusting temperature of the solid bed material in the drying zone or before it is introduced to the drying zone.
  • the moisture containing gases removed from the solid fuel may be fed to the fluidized bed boiler to be incinerated.
  • the pyrolysis process according to the present invention may be carried out in connection of a bubbling fluidized bed boiler or a circulating fluidized bed boiler by feeding bed material from these boilers to the pyrolysis process.
  • FIG 1 it is schematically shown one embodiment of a pyrolysis apparatus according to the present invention arranged in connection with a bubbling fluidized bed boiler 30.
  • the boiler 30 comprises a combustion chamber 1 and a flue gas channel 2.
  • a bed material 40 composed of solid particle like material, such as sand or other inert material, is fluidized by a fluidizing air fed from the windbox 13 through fluidizing nozzles (not shown in the figure) to form a fluidized bed in the combustion chamber 1 .
  • Means for feeding liquid or solid fuel, fluidising gas and combustion air to the combustion chamber 1 are not shown.
  • the fuel used in the boiler 30 may be the same as the solid fuel pyrolyzed in the pyrolyzing apparatus, such as wood or other biomass fuel, but also coal, liquid fuel or some other fuel may be combusted in the boiler 30.
  • pyrolysis gases pyrolysis residue, coke, is formed from the pyrolyzed material.
  • the coke may be burned separately from the pyrolysis process, preferably in the boiler 30.
  • the pyrolysis apparatus comprises pyrolysis reactor 4, which is essentially a closed chamber.
  • the pyrolysis apparatus further comprises one or more pyrolysis gas outlets 6 for removing pyrolysis gases from the pyrolysis reactor 4 and a conduit 7 for conducting the pyrolysis gases to a condenser 8.
  • the pyrolysis gases are condensed in the condenser 8 in one or more steps for producing pyrolysis oil, which is further conducted out of the pyrolysis apparatus via conduit 9.
  • Gases that have not condensed in the condenser 8 are discharged via conduit 10 to be further processed. They may also be returned via conduit 36 to the pyrolysis reactor 4 and used as fluidizing gases 4 after they have been scrubbed. The gases that have not condensed may also be returned to the boiler 40.
  • the pyrolysis process is a continuous process utilizing the thermal energy of the bed material 40 of the fluidized bed boiler 30.
  • the pyrolysis reactor 1 is arranged in connection with the bubbling fluidized bed boiler such that the pyrolysis reactor 4 placed adjacent to the combustion chamber 1 and preferably they have a common wall 23.
  • FIG. 2 shows the schematic view of the pyrolysis reactor 4 of fig- ure 1 in detail.
  • the pyrolysis reactor 4 comprises one or more bed material inlets 11 for feeding hot bed material 40 into the pyrolysis reactor 4 from the combustion chamber 1 of the bubbling fluidized bed boiler 30 and one or more bed material outlets 12 for discharging the bed material 40 from the pyrolysis reactor 4 back to the combustion chamber 1 of the bubbling fluidized bed boiler 30.
  • the bed material inlets 11 and the bed material outlets 12 are arranged to the wall 23 that is common to the combustion chamber 1 and pyrolysis reactor 4.
  • the circulation of the bed material 40 through the pyrolysis reactor 4 via bed material inlets 11 and the bed material outlets 12 may be carried by means of communicating compartments.
  • the pyrolysis reactor 4 further comprises fluid- izing nozzles 5 attached on the bottom of the reactor 4 for supplying fluidizing gas into the pyrolysis reactor 4.
  • the fluidizing gas is any suitable inert gas, such as non-condensible gases that are produced in the pyrolysis, oxygen free circulating gases, or any other inert gas, such as nitrogen.
  • the fluidizing gas is supplied to the nozzles 5 from a windbox 13 that has a conduit 17 for introducing the fluidizing gas into it.
  • the fluidizing nozzles 5 are arranged at spaced intervals to cover the whole distance between the bed material inlets 11 and the bed material outlets 12 to provide a cross-flow of the fluidizing gas in relation to the movement direction of the bed material 40.
  • the fluidizing noz- zles 5 supply fluidizing gas substantially along the whole distance and the bed material and solid fuel are transported in fluidized state through the pyrolysis reactor.
  • the pyrolysis reactor 4 is divided between the bed material inlets 11 and the bed material outlets 12 to a drying section 4D and a pyrolysis section 4B.
  • the pyrolysis reactor 4 may further be divided into entry section 4A up- stream of the drying section 4D, the entry section 4A comprising the bed material inlets 11 , and into a discharge section 4C downstream of the pyrolysis section 4B, the discharge section 4C comprising the one or more bed material outlets 12, as shown in figure 2.
  • the solid fuel to be pyrolyzed may be supplied to the pyrolysis reac- tor 4 into the drying section 4D or into the entry section 4A.
  • the pyrolysis reactor 4 comprises one or more supply inlets 14 for supplying solid fuel to be pyrolyzed in to the pyrolysis reactor 4.
  • the solid fuel mixes with the bed material and moves in the pyrolysis reactor 4 along with it.
  • the bed material inlets 11 and the bed material outlets 12 are at a dis- tance from each other in the horizontal direction, from right to left in figure 2, and the drying section 4D and the pyrolysis section 4B are arranged between the bed material inlets 11 and the bed material outlets 12.
  • the drying section 4D is arranged prior the pyrolysis section 4B in the movement direction of the solid fuel for drying the solid fuel prior to pyrolysis of the solid fuel. Therefore, as the solid fuel moves in the pyrolysis reactor 4, it is first dried in the drying section 4D and then pyrolyzed in the pyrolysis section 4B. Thus the solid fuel remains in the drying section 4D only time needed for drying it, and is passed to the pyrolysis section 4B before the pyrolysis essentially starts.
  • the pyrolysis reactor 4 comprises also one or more pyrolysis gas outlets 6 for removing pyrolysis gases formed from the solid fuel out of the py- rolysis reactor 4.
  • the pyrolysis gas outlets 6 are arranged in the pyrolysis section 4B, as shown in figures 2 and 3.
  • One or more moisture outlets 20 are provided in the drying section 4D for removing the moisture containing gases separated from the solid fuel in the drying section 4D.
  • the moisture outlets 20 are arranged on the top wall 46 of the pyrolysis reactor 4 in the drying section 4D and the one or more pyrolysis gas outlets 6 are arranged on the top wall 46 of the pyrolysis reactor 4 in the pyrolysis section 4B.
  • the drying section 4D and the pyrolysis section 4B are separated from each other by means of a partition wall 22.
  • the partition wall 22 extends from the top wall 46 of the pyrolysis reactor 4 to a distance from the bottom 48 of the pyrolysis reactor 4, as shown in figure 2.
  • the moisture containing gases separated from the solid fuel in the drying section 4D raise upwardly with the fluidizing gas supplied from the bottom 48 of the pyrolysis reactor 4 and do not enter the pyrolysis section 4B.
  • the partition wall 22 may also extend little distance into the bed material 40 as shown in figure 2.
  • the mixture of bed mate- rial and solid fuel move towards the pyrolysis section 4B through the space between the partition wall 22 and the bottom of the pyrolysis reactor.
  • partition wall 22 may extend from the bottom 48 of the pyrolysis reactor 4 to a distance from the top wall 46 of the pyrolysis reactor 4. In that case fluidizing gas has to fed to the drying section 4D with such a speed that it transports the bed material 40 and the solid fuel over the partition wall 22.
  • a separator (not shown) has to be used in connection with the moisture outlet 20 for separating the bed material 40 from the moisture containing gases.
  • the pyrolysis reactor 4 is di- vided in the movement direction of the solid fuel into four sections: entry section 4A, drying section 4D, pyrolysis section 4B and discharge section 4C.
  • the entry section 4A comprises one or more bed material inlets 11 and it is arranged upstream of the drying section 4D.
  • the discharge section 4C comprises one or more bed material outlets 12 and is arranged downstream of the pyrolysis section 4B.
  • the entry section 4A and the drying section 4D are sepa- rated from each other by means of partition wall 24.
  • the drying section 4D and the pyrolysis section 4B are separated from each other by means of partition wall 22.
  • a partition wall 26 separates the pyrolysis section 4B and discharge section 4C.
  • the partition walls 24, 26 are arranged to extend from the top wall 46 of the pyrolysis reactor 4 to a distance from the bottom 48 of the pyrolysis reactor 4.
  • the partition walls may also be arranged, if preferred, to extend from the bottom 48 of the pyrolysis reactor 4 to a distance from the top wall 46 of the pyrolysis reactor 4. Since the fluidizing nozzles are distributed evenly between the bed material inlets 11 and bed material outlets, the fluidization is formed in every section.
  • Figure 3 shows schematically a top view of the pyrolysis reactor 4 of figure 2.
  • the bed material is supplied into the entry section 4A through bed material inlet 11 substantially in horizontal direction and the fuel to be pyro- lyzed is supplied into the entry section 4A also substantially horizontally direction, as shown in figure 3.
  • the mixture of bed material and fuel is passed horizontally to the drying section 4D where the fuel is dried and the moisture containing gases are removed from the drying section 4D through moisture outlet 20.
  • the mixture of bed material and dried fuel is further passed to the pyrolysis section 4B where the dried fuel is pyrolyzed for removing pyrolysis gases from the dried fuel.
  • the pyrolysis gases are removed from the pyrolysis section through pyrolysis gas outlets 6.
  • the bed material and remaining components of the fuel are then passed to the discharge section 4C from where they are removed from the pyrolysis reactor 4 through bed material outlet 12. As shown in figures 2 and 3, the bed material is passed substantially horizontally through the pyrolysis reactor 4 together with the fuel and the gases separated from the fuel are removed from the pyrolysis reactor substantially in vertical direction.
  • Figure 4 shows a pyrolysis apparatus provided in connection with a circulating fluidized bed boiler 50.
  • Arrow C shows the route of the bed material in the boiler 50.
  • the boiler comprises a combustion chamber 1 , flue gas chan- nel 2 and a separator 3 for separating the bed material from the flue gases.
  • the pyrolysis reactor 4 is arranged between the separator 3 and the combus- tion chamber 1 of the circulating fluidized bed boiler 50.
  • the bed material from the separator 3 is circulated through the pyrolysis reactor 4 into the combustion chamber 1 .
  • the bed material is fed to the pyrolysis reactor 4 via supply conduit 1 1 from the separator 3 and recycled back to the combustion chamber via re- cycle conduit 21 .
  • Figure 5 shows the pyrolysis reactor 4 of figure 4 in detail. It corresponds basically to the pyrolysis reactor of figures 2 and 3.
  • the material inlet 1 1 supplies the bed material to the entry section 4A.
  • the partition wall 24, that separates the entry section 4A and drying section 4D extends from the bottom 48 of the pyrolysis reactor 4 to a distance from the top wall 46 of the reactor 4.
  • the surface of the bed material in the entry section 4A extends substantially to the height of the partition wall 24.
  • the level of the bed material is lower than in the entry section. As is shown by the arrow C, the bed material travels from the entry section 4A through drying sec- tion 4D to the pyrolysis section 4B and finally to discharge section 4C.
  • the pyrolysis reactor 4 comprises a heat exchanger 15 in the entry section 4A for adjusting the temperature of the drying section 4D and/or pyrolysis section 4B.
  • the temperature of the bed material 40 in the drying section 4D may be adjusted by placing a heat exchanger either in the drying section 4D or prior to the drying section 4D.
  • the heat exchanger 15 may be connected to the control means for adjusting the drying of the solid fuel in the drying section 4D.
  • Figures 6 and 7 show another embodiment in which the pyrolysis rector 4 is arranged adjacent to a wall of the combustion chamber 1 of circulating fluidized bed boiler 50 such that the combustion chamber 1 and the pyrolysis reactor have a common wall 23.
  • the pyrolysis reactor 4 is downstream of the particle separator 3.
  • Figure 7 shows a horizontal cross- section view of the pyrolysis reactor 4 and the combustion chamber 1 of figure 6.
  • the bed recycle conduit 21 supplies bed material into the pyrolysis reactor 4 and one or more fuel inlets 14 is arranged to the recycle conduit 21 forming at least partly the entry section 4A of the pyrolysis reactor 4, as shown in figure 7.
  • the pyrolysis reactor 4 is further divided into drying section 4D and pyrolysis section 4B according to the present invention.
  • the drying section 4D and pyrolysis section 4B are arranged transversely in relation to the supply direction of the bed material.
  • the mixture of bed material and the fuel is passed from the entry section 4A into the drying section 4D and further into the pyrolysis section 4B.
  • the entry section 4A, drying section 4D, pyrolysis section 4B and discharge section may be implemented as described above in connection with figures 2, 3 and 5.
  • From the discharge section 4C the bed material and remaining of the fuel are supplied into the combustion chamber 1 through bed material outlets in the common wall 23.
  • the pyrolysis apparatus further comprises control system for controlling the drying of the solid fuel in the drying section 4D and consequently, for controlling the water content of the pyrolysis oil.
  • the control system is shown schematically in Figure 1.
  • the control system comprises a control unit 32 and a water content analyzer 34.
  • the water content analyser 34 analyzes the water content of the produced pyrolysis oil and it is preferably an on-line water content analyzer connected to conduit 9.
  • the control unit 32 comprises receiving means for receiving the measurement signals from the water content analyzer, calculating means for forming control signals and transmitting means for transmitting the formed control signals to the process.
  • the calculating means comprise algorithms for conditioning the measurement signals and forming the control signals for controlling the drying of the solid fuel in the dry- ing section 4D.
  • the control system also comprises signal transmitting lines for transmitting the control signals to the process. The signal transmitting lines are shown in Figure 1 as dashed lines.
  • the water content of the pyrolysis oil is controlled by controlling the drying of the solid fuel in the drying section 4D.
  • the measurement signals of the water content of the pyrolysis oil are transmitted from the analyzer 34 to the control unit 32 via line 25.
  • the control unit 32 forms control signals for the process i.e. for controlling the drying of the solid fuel.
  • the drying of the solid fuel may be accomplished in many ways, of which some examples are explained below.
  • the drying of the solid fuel may be controlled by adjusting the removal rate of moisture containing gases out of the drying section 4D.
  • the control means calculates and transmits control signals as a response to the moisture content of the produced pyrolysis oil for an adjusting means (not shown in the figure) that is connected to the moisture outlet 20.
  • the control signals are transmitted via line 38 to the control means.
  • the drying of the solid fuel may also be controlled by adjusting the residence time of the solid fuel in the drying section 4D. This is done by adjusting the move- ment speed of the solid fuel through drying zone. In this case, the control means calculate control signals for adjusting the velocity of the fluidizing gas fed in to the drying zone.
  • the control signals are transmitted via line 41 to the control means controlling the velocity of the fluidizing gas (not shown in the Figure).
  • the drying of the solid fuel may also be adjusted by controlling the supply rate of solid fuel into the pyrolysis reactor 4. Increasing the supply rate of the solid fuel and keeping other parameters constant may decrease the drying of the solid fuel, and vice versa.
  • the control signals for controlling the supply rate of the solid fuel into the pyrolysis reactor are transmitted to the fuel supply system (not shown in the Figure) via line 44.
  • the drying of the solid fuel may be controlled by adjusting the temperature in the drying section 4D. Temperature of the drying section may be adjusted by adjusting the temperature of the bed material in the drying section.
  • the temperature of the bed material may be adjusted with a heat exchanger 15 adapted for adjusting the temperature of the bed material 40 in the drying section 4D or prior to the drying section 4D.
  • the heat exchanger 15 may be placed in entry section 4A and/or in the drying section 4D, as shown in figure 5.
  • the control signals for the heat exchanger 15 are transmitted via line 42.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Dispersion Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Processing Of Solid Wastes (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention relates to a method of carrying out pyrolysis process in a pyrolysis reactor (4) for solid fuel to produce pyrolysis oil. The method comprises supplying solid fuel into a drying zone in the pyrolysis reactor (4) for removing moisture containing gases, drying the solid fuel in the drying zone and extracting the moisture containing gases re- moved from the solid fuel out of the pyrolysis reactor (4), passing the dried solid fuel from the drying zone to the pyrolysis zone of the pyrolysis reactor (4), pyrolyzing the dried solid fuel for separating pyrolysis gases from the dried solid fuel and conducting the pyrolysis gases from the pyrolysis reactor (4) to a condenser (8) for producing pyrolysis oil.

Description

METHOD OF CARRYING OUT PYROLYSIS AND PYROLYSIS APPARATUS
FIELD OF THE INVENTION
The present invention relates to method for carrying out pyrolysis and more particularly to a method according to the preamble of claim 1. The present invention further relates to a pyrolysis apparatus and more particularly to a pyrolysis apparatus according to preamble of claim 17.
BACKGROUND OF THE INVENTION
In this application pyrolysis means converting fuel in inert conditions and in high temperature into gaseous state, which forms oil-like, different or- ganic compounds comprising liquid as it condensed. Inert conditions mean oxygen-free conditions where no combustion of the fuel occurs. Tar burning is one example of long known prior art pyrolysis process.
One possibility for a pyrolysis process is a process based on using a fluidized bed technique. In this process solid feedstock is fed to a reactor com- prising a fluidized bed of hot inert bed material e.g. sand. Inert fluidizing gas is used to fluidize the bed. The feedstock will mix with the bed material, pyrolyze and form pyrolysis gases that are conducted out from the reactor. The heat for the pyrolysis process can be provided for example arranging the pyrolysis reactor next to a fuel burning fluidized bed and circulating the thus heated bed material to the pyrolysis reactor. The solid feedstock used in pyrolysis is dried in a thermal dryer before it is fed to the pyrolysis reactor. Usually the dryer is a separate drying apparatus. Thus the biomass is first dried and then conducted to the pyrolysis reactor.
In the pyrolysis process fuel is pyrolyzed, formed gaseous com- pounds, i.e. pyrolysis gases are separated from the char residue and the pyrolysis gases are condensed into pyrolysis oil. Pyrolysis oil may be used as fuel or refined into different chemicals. Production of pyrolysis oil from different kinds of biomass, for example from wood fuels, is studied for replacing coal and heavy fuel oil. Pyrolysis oil produced by pyrolysis contains optimally 25 weight-% water. If the water content is much higher, the product may end up to unwanted phase separation and end use of the pyrolysis oil becomes difficult or alcohol has to be added to the pyrolysis oil. On the other hand, if the water content is too low, the viscosity of the pyrolysis oil will increase and end usage will get more difficult. This means that the water content in pyrolysis oil has to be maintained in certain range. Water or moisture content varies with different biomass for example wood, wood chips, peat or other biomass. Reaching the 25 weight-% water or moisture content in pyrolysis oils means that the biomass has to be dried to moisture content 10 weight-% at most, preferably about 4 to 10 weight-% and more preferably 5 to 8 weight-%.
The moisture content of the dried biomass affects the water content of the produced pyrolysis oil. The problem with the prior art drying arrangements is that using separate drying apparatuses in drying of the biomass does not enable effective control of the water content of the produced pyrolysis oil. Thus it is difficult to adjust the pyrolysis process such that the water content produced pyrolysis oil is in optimal range. Also, as the desired moisture content of the biomass is as low as mentioned above, the biomass residence time in a dryer of a smaller size is very long. Another alternative is to increase the size of the dryer, which will result in increase of drying equipment investment price and space requirement.
BRIEF DESCRIPTION OF THE INVENTION
An object of the invention is to provide a method and an apparatus avoiding the above described problems.
The objects of the present invention are achieved with a method ac- cording to the characterizing portion of claim 1 . The objects of the present invention are further achieved with a pyrolysis apparatus according to the characterizing portion of claim 17.
The preferred embodiments of the invention are disclosed in the dependent claims. In pyrolysis, when biomass is fed to the process, it will first dry and the pyrolysis of the biomass will occur after the drying. The drying and the pyrolysis have usually a definite border line. This phenomena is utilized in the present invention by conducting the drying of the biomass in the same process and reactor as pyrolysis. Therefore the pyrolysis process in a pyrolysis reactor is divided into drying zone and pyrolysis zone. The moisture separated from the biomass in the drying zone will be removed from the pyrolysis reactor and the dried biomass is further passed to the pyrolysis zone for pyrolysis. This arrangement enables the moisture content of the pyrolysis oil to be controlled by controlling the drying of the biomass in the pyrolysis reactor to produce py- rolysis oil that will have the optimum water content. Control of the drying of the biomass can be integrated into the online pyrolysis oil water content analyser.
The advantage of the present invention is that it enables effective control of the water content of the produced pyrolysis oil by adjusting the drying of the biomass. The drying zone is arranged inside the pyrolysis reactor. Thus the drying and the pyrolysis are carried out in the same reactor.
Another advantage is that the need for separate, expensive and space consuming dryer is eliminated.
BRIEF DESCRIPTION OF THE DRAWINGS
In the following the invention will be described in greater detail by means of preferred embodiments with reference to the at accompanying drawings, in which
Figure 1 is schematic view of a pyrolysis reactor arranged in connection with a bubbling fluidized bed boiler;
Figure 2 shows a side view of one embodiment of a pyrolysis reac- tor according to the present invention;
Figure 3 shows a top view of the pyrolysis reactor of figure 2; Figure 4 schematic view of a pyrolysis reactor arranged in connection with a circulating fluidized bed boiler;
Figure 5 shows a detailed view of the pyrolysis reactor of figure 4; Figure 6 shows another embodiment of a pyrolysis reactor arranged in connection with a circulating fluidized bed boiler; and
Figure 7 shows detailed view of the pyrolysis reactor of figure 6.
DETAILED DESCRIPTION OF THE INVENTION
The present invention relates to a method of carrying out pyrolysis process for solid fuel to produce pyrolysis oil. The pyrolysis process carried out is preferably so called fast pyrolysis. According to the basic principle of the present invention, the pyrolysis process in the pyrolysis reactor is divided into drying for drying the biomass and pyrolysis for pyrolyzing the dried biomass. The drying of the biomass is conducted in the drying zone of the pyrolysis reactor and the pyrolysis of the dried biomass is carried out in the pyrolysis zone. Thus the pyrolysis process is divided into a drying zone and a pyrolysis zone, the drying zone being arranged upstream from the pyrolysis zone in the movement direction of the biomass in the pyrolysis process.
In the present application and claims the following have meaning as defined below: The term "solid fuel" refers to all kind of substantially solid bio- mass that is pyrolyzed in a pyrolysis reactor. The solid fuel can be any solid biomass, such as wood, wood chips, saw dust, firewood, forest residue, urban wood waste, by products and waste of the papermaking industry, lumber waste and peat. Even though the material to be pyrolyzed is called solid fuel, it should be noted that the material will not burn in the pyrolysis process, but releases combustable gases that may be condensed into liquid form. The term "pyrolysis gases" refers to gases that are formed in pyrolysis and that will be condensated in the process to form pyrolysis oil. The term "moisture containing gases" refers to gases separated from the solid fuel in the drying zone of the pyrolysis reactor prior to pyrolysis of the solid fuel in the pyrolysis zone.
The solid fuel is preferably dried to a moisture content of 10 weight- % at most, preferably about 4 to 10 weight-% and more preferably 5 to 8 weight-% in the drying zone. During the pyrolysis process the moisture content of the produced pyrolysis oil is analyzed for controlling the drying of the solid fuel in the drying zone. The analysis of the moisture content of the produced pyrolysis oil may be done for example with online water content analyser. The measurements may be used for controlling the drying process of the solid fuel in the drying zone by adjusting the removal rate of the moisture containing gases from the drying zone. Alternatively the drying of the solid fuel in the dry- ing zone may be controlled by adjusting residence time of the solid fuel in the drying zone. The residence time of the solid fuel may be controlled by adjusting the movement speed of the solid fuel in the drying zone. Furthermore, the drying of the solid fuel in the drying zone may be controlled by controlling the temperature in the drying zone. The above discussed methods for controlling the drying of the solid fuel may be used separately or in any combination. According to the above mentioned methods the water content of the produced pyrolysis oil may be controlled by adjusting the process parameters of the pyrolysis process itself, particularly in the drying zone of the pyrolysis reactor.
In one preferred embodiment, the pyrolysis process according to the present invention is carried out in connection with a fluidized bed boiler. In that case solid fuel is supplied to a pyrolysis reactor and heat required for the pyrolysis is brought to the pyrolysis reactor at least partly with solid, particle like, bed material of the fluidized bed boiler. The bed material of the fluidized bed boiler is circulated through the pyrolysis reactor and fluidized in the pyrolysis reactor by fluidizing gas. The temperature of the bed material 40 is approximately 850 0C in the fluidized bed boiler 30 and approximately 700 0C in the pyrolysis reactor 4. The pyrolysis gases produced from the dried solid fuel in the pyrolysis reactor are condensed into liquid form as so called pyrolysis oil. Preferably in the method the bed material coming from the fluidized bed boiler and the solid fuel are passed through the pyrolysis reactor in transverse direc- tion in relation to the flow direction of the fluidizing gas in the pyrolysis reactor. According to the method carried out in connection with a fluidizing bed boiler the pyrolysis reactor is divided into a drying zone and a pyrolysis zone in the movement direction of the solid fuel and the bed material for drying the solid fuel prior to the pyrolysis of the solid fuel in the pyrolysis reactor. This means that the heat and thermal energy brought to the pyrolysis reactor by the bed material is used for pyrolyzing the solid fuel in the pyrolysis zone as well as for drying the solid fuel in the drying zone. That means that the thermal energy of the bed material of a fluidized bed boiler is used as a source of thermal energy in the pyrolysis reactor. The moisture containing gases separated from the solid fuel in the drying zone are removed from the drying zone and the dried solid fuel is passed to the pyrolysis zone to be pyrolyzed. The pyrolysis gases comprising tar-rich gases are removed from the pyrolysis reactor in the pyrolyzing zone.
The bed material and the solid fuel are passed essentially in hori- zontal direction through the pyrolysis reactor. The drying zone and the pyrolysis zone may be divided to two sections, a drying section and a pyrolysis sections by a separating wall. There are holes provided in the wall to enable the travelling of the bed material and solid fuel from the drying section to the pyrolysis section. The bed material moves in the pyrolysis reactor according to the principle of communicating vessels, because when fluidized, it behaves the same way as fluids. The speed of movement of the bed material and solid fuel can be expedited by positioning the fluidizing nozzles to provide the fluidizing air to the preferred direction.
By dividing the pyrolysis reactor into different sections, it is possible to remove the moisture containing gases separated from the solid fuel in the drying zone and the pyrolysis gases separated in the pyrolysis zone separately and use them in different purposes. Both of these gases rise upwards, above the fluidized bed in the pyrolysis reactor and can be removed from the reactor. No separate gas removing or bed material removing equipment is needed. The drying may be controlled in the drying zone by adjusting temperature of the solid bed material in the drying zone or before it is introduced to the drying zone. The moisture containing gases removed from the solid fuel may be fed to the fluidized bed boiler to be incinerated. The pyrolysis process according to the present invention may be carried out in connection of a bubbling fluidized bed boiler or a circulating fluidized bed boiler by feeding bed material from these boilers to the pyrolysis process.
In figure 1 it is schematically shown one embodiment of a pyrolysis apparatus according to the present invention arranged in connection with a bubbling fluidized bed boiler 30. The boiler 30 comprises a combustion chamber 1 and a flue gas channel 2. A bed material 40 composed of solid particle like material, such as sand or other inert material, is fluidized by a fluidizing air fed from the windbox 13 through fluidizing nozzles (not shown in the figure) to form a fluidized bed in the combustion chamber 1 . Means for feeding liquid or solid fuel, fluidising gas and combustion air to the combustion chamber 1 are not shown. The fuel used in the boiler 30 may be the same as the solid fuel pyrolyzed in the pyrolyzing apparatus, such as wood or other biomass fuel, but also coal, liquid fuel or some other fuel may be combusted in the boiler 30. Besides pyrolysis gases, pyrolysis residue, coke, is formed from the pyrolyzed material. The coke may be burned separately from the pyrolysis process, preferably in the boiler 30. The pyrolysis apparatus comprises pyrolysis reactor 4, which is essentially a closed chamber. The pyrolysis apparatus further comprises one or more pyrolysis gas outlets 6 for removing pyrolysis gases from the pyrolysis reactor 4 and a conduit 7 for conducting the pyrolysis gases to a condenser 8. The pyrolysis gases are condensed in the condenser 8 in one or more steps for producing pyrolysis oil, which is further conducted out of the pyrolysis apparatus via conduit 9. Gases that have not condensed in the condenser 8 are discharged via conduit 10 to be further processed. They may also be returned via conduit 36 to the pyrolysis reactor 4 and used as fluidizing gases 4 after they have been scrubbed. The gases that have not condensed may also be returned to the boiler 40.
The pyrolysis process is a continuous process utilizing the thermal energy of the bed material 40 of the fluidized bed boiler 30. As shown in figure 1 , the pyrolysis reactor 1 is arranged in connection with the bubbling fluidized bed boiler such that the pyrolysis reactor 4 placed adjacent to the combustion chamber 1 and preferably they have a common wall 23.
Figure 2 shows the schematic view of the pyrolysis reactor 4 of fig- ure 1 in detail. The pyrolysis reactor 4 comprises one or more bed material inlets 11 for feeding hot bed material 40 into the pyrolysis reactor 4 from the combustion chamber 1 of the bubbling fluidized bed boiler 30 and one or more bed material outlets 12 for discharging the bed material 40 from the pyrolysis reactor 4 back to the combustion chamber 1 of the bubbling fluidized bed boiler 30. The bed material inlets 11 and the bed material outlets 12 are arranged to the wall 23 that is common to the combustion chamber 1 and pyrolysis reactor 4. The circulation of the bed material 40 through the pyrolysis reactor 4 via bed material inlets 11 and the bed material outlets 12 may be carried by means of communicating compartments. The pyrolysis reactor 4 further comprises fluid- izing nozzles 5 attached on the bottom of the reactor 4 for supplying fluidizing gas into the pyrolysis reactor 4. The fluidizing gas is any suitable inert gas, such as non-condensible gases that are produced in the pyrolysis, oxygen free circulating gases, or any other inert gas, such as nitrogen. The fluidizing gas is supplied to the nozzles 5 from a windbox 13 that has a conduit 17 for introducing the fluidizing gas into it. The fluidizing nozzles 5 are arranged at spaced intervals to cover the whole distance between the bed material inlets 11 and the bed material outlets 12 to provide a cross-flow of the fluidizing gas in relation to the movement direction of the bed material 40. Thus the fluidizing noz- zles 5 supply fluidizing gas substantially along the whole distance and the bed material and solid fuel are transported in fluidized state through the pyrolysis reactor. The pyrolysis reactor 4 is divided between the bed material inlets 11 and the bed material outlets 12 to a drying section 4D and a pyrolysis section 4B. The pyrolysis reactor 4 may further be divided into entry section 4A up- stream of the drying section 4D, the entry section 4A comprising the bed material inlets 11 , and into a discharge section 4C downstream of the pyrolysis section 4B, the discharge section 4C comprising the one or more bed material outlets 12, as shown in figure 2.
The solid fuel to be pyrolyzed may be supplied to the pyrolysis reac- tor 4 into the drying section 4D or into the entry section 4A. For that the pyrolysis reactor 4 comprises one or more supply inlets 14 for supplying solid fuel to be pyrolyzed in to the pyrolysis reactor 4. The solid fuel mixes with the bed material and moves in the pyrolysis reactor 4 along with it. According to the figure 2, the bed material inlets 11 and the bed material outlets 12 are at a dis- tance from each other in the horizontal direction, from right to left in figure 2, and the drying section 4D and the pyrolysis section 4B are arranged between the bed material inlets 11 and the bed material outlets 12. The drying section 4D is arranged prior the pyrolysis section 4B in the movement direction of the solid fuel for drying the solid fuel prior to pyrolysis of the solid fuel. Therefore, as the solid fuel moves in the pyrolysis reactor 4, it is first dried in the drying section 4D and then pyrolyzed in the pyrolysis section 4B. Thus the solid fuel remains in the drying section 4D only time needed for drying it, and is passed to the pyrolysis section 4B before the pyrolysis essentially starts.
The pyrolysis reactor 4 comprises also one or more pyrolysis gas outlets 6 for removing pyrolysis gases formed from the solid fuel out of the py- rolysis reactor 4. The pyrolysis gas outlets 6 are arranged in the pyrolysis section 4B, as shown in figures 2 and 3. One or more moisture outlets 20 are provided in the drying section 4D for removing the moisture containing gases separated from the solid fuel in the drying section 4D. The moisture outlets 20 are arranged on the top wall 46 of the pyrolysis reactor 4 in the drying section 4D and the one or more pyrolysis gas outlets 6 are arranged on the top wall 46 of the pyrolysis reactor 4 in the pyrolysis section 4B.
The drying section 4D and the pyrolysis section 4B are separated from each other by means of a partition wall 22. The partition wall 22 extends from the top wall 46 of the pyrolysis reactor 4 to a distance from the bottom 48 of the pyrolysis reactor 4, as shown in figure 2. The moisture containing gases separated from the solid fuel in the drying section 4D raise upwardly with the fluidizing gas supplied from the bottom 48 of the pyrolysis reactor 4 and do not enter the pyrolysis section 4B. The partition wall 22 may also extend little distance into the bed material 40 as shown in figure 2. The mixture of bed mate- rial and solid fuel move towards the pyrolysis section 4B through the space between the partition wall 22 and the bottom of the pyrolysis reactor. Alternatively partition wall 22 may extend from the bottom 48 of the pyrolysis reactor 4 to a distance from the top wall 46 of the pyrolysis reactor 4. In that case fluidizing gas has to fed to the drying section 4D with such a speed that it transports the bed material 40 and the solid fuel over the partition wall 22. Furthermore, in this embodiment, a separator (not shown) has to be used in connection with the moisture outlet 20 for separating the bed material 40 from the moisture containing gases.
In the embodiment shown in Figure 2, the pyrolysis reactor 4 is di- vided in the movement direction of the solid fuel into four sections: entry section 4A, drying section 4D, pyrolysis section 4B and discharge section 4C. The entry section 4A comprises one or more bed material inlets 11 and it is arranged upstream of the drying section 4D. The discharge section 4C comprises one or more bed material outlets 12 and is arranged downstream of the pyrolysis section 4B. The entry section 4A and the drying section 4D are sepa- rated from each other by means of partition wall 24. The drying section 4D and the pyrolysis section 4B are separated from each other by means of partition wall 22. A partition wall 26 separates the pyrolysis section 4B and discharge section 4C.The partition walls 24, 26 are arranged to extend from the top wall 46 of the pyrolysis reactor 4 to a distance from the bottom 48 of the pyrolysis reactor 4. The partition walls may also be arranged, if preferred, to extend from the bottom 48 of the pyrolysis reactor 4 to a distance from the top wall 46 of the pyrolysis reactor 4. Since the fluidizing nozzles are distributed evenly between the bed material inlets 11 and bed material outlets, the fluidization is formed in every section. Figure 3 shows schematically a top view of the pyrolysis reactor 4 of figure 2. The bed material is supplied into the entry section 4A through bed material inlet 11 substantially in horizontal direction and the fuel to be pyro- lyzed is supplied into the entry section 4A also substantially horizontally direction, as shown in figure 3. From the entry section the mixture of bed material and fuel is passed horizontally to the drying section 4D where the fuel is dried and the moisture containing gases are removed from the drying section 4D through moisture outlet 20. The mixture of bed material and dried fuel is further passed to the pyrolysis section 4B where the dried fuel is pyrolyzed for removing pyrolysis gases from the dried fuel. The pyrolysis gases are removed from the pyrolysis section through pyrolysis gas outlets 6. The bed material and remaining components of the fuel are then passed to the discharge section 4C from where they are removed from the pyrolysis reactor 4 through bed material outlet 12. As shown in figures 2 and 3, the bed material is passed substantially horizontally through the pyrolysis reactor 4 together with the fuel and the gases separated from the fuel are removed from the pyrolysis reactor substantially in vertical direction.
Figure 4 shows a pyrolysis apparatus provided in connection with a circulating fluidized bed boiler 50. Arrow C shows the route of the bed material in the boiler 50. The boiler comprises a combustion chamber 1 , flue gas chan- nel 2 and a separator 3 for separating the bed material from the flue gases. The pyrolysis reactor 4 is arranged between the separator 3 and the combus- tion chamber 1 of the circulating fluidized bed boiler 50. The bed material from the separator 3 is circulated through the pyrolysis reactor 4 into the combustion chamber 1 . The bed material is fed to the pyrolysis reactor 4 via supply conduit 1 1 from the separator 3 and recycled back to the combustion chamber via re- cycle conduit 21 .
Figure 5 shows the pyrolysis reactor 4 of figure 4 in detail. It corresponds basically to the pyrolysis reactor of figures 2 and 3. The material inlet 1 1 supplies the bed material to the entry section 4A. The partition wall 24, that separates the entry section 4A and drying section 4D extends from the bottom 48 of the pyrolysis reactor 4 to a distance from the top wall 46 of the reactor 4. The surface of the bed material in the entry section 4A extends substantially to the height of the partition wall 24. In the following sections 4D, 4B and 4C the level of the bed material is lower than in the entry section. As is shown by the arrow C, the bed material travels from the entry section 4A through drying sec- tion 4D to the pyrolysis section 4B and finally to discharge section 4C. From there it is transported back to the combustion chamber 1 through bed material outlet 12 and via recycle conduit 21 . In figure 5 the pyrolysis reactor 4 comprises a heat exchanger 15 in the entry section 4A for adjusting the temperature of the drying section 4D and/or pyrolysis section 4B. The temperature of the bed material 40 in the drying section 4D may be adjusted by placing a heat exchanger either in the drying section 4D or prior to the drying section 4D. Thus it is possible to arrange the heat exchanger 15 also in the drying section 4D. The heat exchanger 15 may be connected to the control means for adjusting the drying of the solid fuel in the drying section 4D. Figures 6 and 7 show another embodiment in which the pyrolysis rector 4 is arranged adjacent to a wall of the combustion chamber 1 of circulating fluidized bed boiler 50 such that the combustion chamber 1 and the pyrolysis reactor have a common wall 23. In this embodiment the pyrolysis reactor 4 is downstream of the particle separator 3. Figure 7 shows a horizontal cross- section view of the pyrolysis reactor 4 and the combustion chamber 1 of figure 6. The bed recycle conduit 21 supplies bed material into the pyrolysis reactor 4 and one or more fuel inlets 14 is arranged to the recycle conduit 21 forming at least partly the entry section 4A of the pyrolysis reactor 4, as shown in figure 7. The pyrolysis reactor 4 is further divided into drying section 4D and pyrolysis section 4B according to the present invention. The drying section 4D and pyrolysis section 4B are arranged transversely in relation to the supply direction of the bed material. The mixture of bed material and the fuel is passed from the entry section 4A into the drying section 4D and further into the pyrolysis section 4B. The entry section 4A, drying section 4D, pyrolysis section 4B and discharge section may be implemented as described above in connection with figures 2, 3 and 5. From the discharge section 4C the bed material and remaining of the fuel are supplied into the combustion chamber 1 through bed material outlets in the common wall 23.
The pyrolysis apparatus further comprises control system for controlling the drying of the solid fuel in the drying section 4D and consequently, for controlling the water content of the pyrolysis oil. The control system is shown schematically in Figure 1. The control system comprises a control unit 32 and a water content analyzer 34. The water content analyser 34 analyzes the water content of the produced pyrolysis oil and it is preferably an on-line water content analyzer connected to conduit 9. The control unit 32 comprises receiving means for receiving the measurement signals from the water content analyzer, calculating means for forming control signals and transmitting means for transmitting the formed control signals to the process. The calculating means comprise algorithms for conditioning the measurement signals and forming the control signals for controlling the drying of the solid fuel in the dry- ing section 4D. The control system also comprises signal transmitting lines for transmitting the control signals to the process. The signal transmitting lines are shown in Figure 1 as dashed lines.
The water content of the pyrolysis oil is controlled by controlling the drying of the solid fuel in the drying section 4D. The measurement signals of the water content of the pyrolysis oil are transmitted from the analyzer 34 to the control unit 32 via line 25. The control unit 32 forms control signals for the process i.e. for controlling the drying of the solid fuel.
The drying of the solid fuel may be accomplished in many ways, of which some examples are explained below. The drying of the solid fuel may be controlled by adjusting the removal rate of moisture containing gases out of the drying section 4D. The control means calculates and transmits control signals as a response to the moisture content of the produced pyrolysis oil for an adjusting means (not shown in the figure) that is connected to the moisture outlet 20. The control signals are transmitted via line 38 to the control means. The drying of the solid fuel may also be controlled by adjusting the residence time of the solid fuel in the drying section 4D. This is done by adjusting the move- ment speed of the solid fuel through drying zone. In this case, the control means calculate control signals for adjusting the velocity of the fluidizing gas fed in to the drying zone. The control signals are transmitted via line 41 to the control means controlling the velocity of the fluidizing gas (not shown in the Figure). The drying of the solid fuel may also be adjusted by controlling the supply rate of solid fuel into the pyrolysis reactor 4. Increasing the supply rate of the solid fuel and keeping other parameters constant may decrease the drying of the solid fuel, and vice versa. The control signals for controlling the supply rate of the solid fuel into the pyrolysis reactor are transmitted to the fuel supply system (not shown in the Figure) via line 44. Furthermore, the drying of the solid fuel may be controlled by adjusting the temperature in the drying section 4D. Temperature of the drying section may be adjusted by adjusting the temperature of the bed material in the drying section. The temperature of the bed material may be adjusted with a heat exchanger 15 adapted for adjusting the temperature of the bed material 40 in the drying section 4D or prior to the drying section 4D. The heat exchanger 15 may be placed in entry section 4A and/or in the drying section 4D, as shown in figure 5. The control signals for the heat exchanger 15 are transmitted via line 42.
It will be obvious to a person skilled in the art that, as the technology advances, the inventive concept can be implemented in various ways. The invention and its embodiments are not limited to the examples described above but may vary within the scope of the claims.

Claims

1. A method of carrying out pyrolysis process in a pyrolysis apparatus for solid fuel to produce pyrolysis oil, characterized in that the pyrolysis process is carried out in connection with a fluidized bed boiler (30) and supplying heat required for the pyrolysis process at least partly by bed material of the fluidized bed boiler (30), the method comprising steps of:
- supplying solid fuel into a drying zone in the pyrolysis reactor (4);
- drying the solid fuel in the drying zone and removing moisture containing gases from the solid fuel; - passing the dried solid fuel and the bed material essentially horizontally from the drying zone to the pyrolysis zone arranged sequentially in horizontal direction in the pyrolysis reactor (4);
- pyrolyzing the dried solid fuel for separating pyrolysis gases from the dried solid fuel; and - conducting the pyrolysis gases from the pyrolysis reactor (4) to a condenser (8) for producing pyrolysis oil.
2. A method according to claim 1, characterized by conducting the moisture containing gases out of the pyrolysis reactor (4) in the drying zone.
3. A method according to claim 1 or 2, characterized by controlling moisture content of the pyrolysis oil by adjusting the drying of the solid fuel in the drying zone.
4. A method according to claim 3, characterized by analysing the moisture content of the produced pyrolysis oil for controlling the drying of the solid fuel in the drying zone.
5. A method according to claim 3 or 4, characterized by adjusting residence time of the solid fuel in the drying zone.
6. A method according to claim 5, characterized by adjusting the residence time of the solid fuel in the drying zone by adjusting the movement speed of the solid fuel through drying zone.
7. A method according to claim 3 or 4, characterized by adjusting the temperature in the drying zone.
8. A method according to claim 3 or 4, characterized by adjusting the supply rate of solid fuel into the pyrolysis reactor (4).
9. A method according to claim 3 or 4, characterized by ad- justing the removal rate of moisture containing gases from the drying zone.
10. A method according to the any one of claims 1 to 9, c h a r a c - t e r i z e d by drying the solid fuel in the drying zone to moisture content 4 to 10weight-%.
11. A method according to any one of claims 1 to 10, characterized by carrying out the pyrolysis process using the bed material of the fluidized bed boiler (30) which bed material of the fluidized bed boiler (30) is circulated through the pyrolysis reactor and fluidized in the pyrolysis reactor by fluidizing gas, the pyrolysis gases separated from the solid fuel in the pyrolysis reactor are condensed in to liquid form as so called pyrolysis oil, in which method the bed material of the fluidized bed boiler (30) and the solid fuel are passed through the pyrolysis reactor (4) in transverse direction in relation to the flow direction of the fluidizing gas.
12. A method according to claim 11, characterized by pass- ing the bed material and the solid fuel essentially in horizontal direction through the pyrolysis reactor (4), and that the fluidizing gas is fed to the pyrolysis process underneath the bed material.
13. A method according to any one of claims 10 to 12, character i z e d by controlling temperature in the drying zone by adjusting tempera- ture of the bed material supplied to the drying zone of the pyrolysis reactor (4).
14. A method according to any one of claims 10 to 12, character i z e d by adjusting the drying of the solid fuel in the drying zone by adjusting the speed of the fluidizing gas fed in to the drying zone.
15. A method according to the any one of claims 10 to 14, c h a r - acterized by feeding bed material to the pyrolysis process from a fluidized bed boiler (30) being selected from one of the following: bubbling fluidized bed boiler and circulating fluidized bed boiler.
16. A method according to the any one of claims 10 to 14, c h a r - acterized by using wood, wood chips, saw dust, peat or any other solid biomass as solid fuel to be pyrolyzed.
17. A pyrolysis apparatus comprising a pyrolysis reactor (4) for pyro- lyzing solid fuel and a condenser (8) for condensing pyrolysis gases separated from the solid fuel into pyrolysis oil, characterized in that the pyrolysis reactor (4) is arranged in connection with a fluidized bed boiler (30) for supply- ing heat required for the pyrolysis of the solid fuel at least partly by bed material of the fluidized bed boiler (30), and that the pyrolysis reactor (4) comprises a drying section (4D) for drying solid fuel supplied to the pyrolysis reactor and a pyrolysis section (4B) for pyrolyzing the solid fuel dried in the drying section (4D) and for conducting pyrolysis gases separated from the solid fuel to the condenser (8), and that the drying section (4D) and the pyrolysis section (4B) are arranged sequentially in horizontal direction such that bed material and the dried solid fuel are passed essentially in horizontal direction from the drying section (4D) to the pyrolysis section (4B)..
18. A pyrolysis apparatus according to claim 17, characterized in that the apparatus is arranged to remove moisture containing gases from the solid fuel (4) in the drying section (4D).
19. A pyrolysis apparatus according to claim 17 or 18, character i z e d in that the apparatus comprises control means (32) for controlling the drying of the solid fuel in the drying section (4D) as a response to the moisture content of the produced pyrolysis oil.
20. A pyrolysis apparatus according to claim 19, characterized in that control means (32) comprise water content analyser (34) for measuring the water content of the produced pyrolysis oil.
21. A pyrolysis apparatus according to any one of claims 17 to 20, characterized in that the control means are arranged to adjust the movement speed of the solid fuel or the solid particle bed material in the drying section (4D), and/or to adjust the temperature in the drying section (4D) by means of the heat exchanger (15) and/or to adjust supply rate of solid fuel into the pyrolysis reactor (4) and/or to adjust the removal rate of the moisture containing gases from the drying section (4D).
22. A pyrolysis apparatus according to any one of claims 17 to 21, characterized in that the pyrolysis reactor (4) further comprises:
- one or more solid fuel inlets (14) for supplying solid fuel to be pyro- lyzed in to the pyrolysis reactor (4);
- one or more bed material inlets (11) for feeding hot solid particle bed material into the pyrolysis reactor (4);
- one or more bed material outlets (12) for discharging the hot solid particle material from the pyrolysis reactor (4);
- fluidizing nozzles (5) for supplying fluidizing gas into the pyrolysis reactor (4), the fluidizing nozzles (5) being arranged between the bed material inlets (11) and the bed material outlets (12) to provide a cross-flow of the fluidizing gas in relation to the movement direction of the solid fuel and the bed ma- terial;
- one or more pyrolysis gas outlets (6) for extracting pyrolysis gases separated from the solid fuel out of the pyrolysis reactor (4).
23. A pyrolysis apparatus according to claim 22, character- i z e d in that that the control means are arranged to adjust temperature of the bed material fed into the pyrolysis reactor and/or to adjust the speed of the flu- idizing gas supplied to the drying section (4D) of the pyrolysis reactor (4).
24. A pyrolysis apparatus according to any one of claims 17 to 23, characterized in that pyrolysis reactor (4) comprises a heat exchanger (15) for adjusting the temperature of the drying section (4D) and/or pyrolysis section (4B).
25. A pyrolysis apparatus according to claim 24, characterized in that the heat exchanger (15) is adapted for adjusting the temperature of the solid particle bed material in the drying section (4D) or prior to the drying section (4D).
26. A pyrolysis apparatus according to any one of claims 22 to 25, characterized in that the fluidizing gas is fed to the pyrolysis process underneath the fluidized bed.
27. A pyrolysis apparatus according to any one of claims 17 or 26, characterized in that the drying section (4B) comprises one or more moisture outlets (20) for exhausting the moisture containing gas from the drying section (4D).
28. A pyrolysis apparatus according to any one of claims 17 to 27, characterized in that drying section (4D) and the pyrolysis section (4B) are separated from each other by means of a partition wall (22).
29. A pyrolysis apparatus according to claim 28, characterized in that the pyrolysis reactor comprises a top wall (46) and a bottom (48) and that the partition wall (22) extends from the top wall (46) to a distance from the bottom (48) of the pyrolysis reactor (4).
30. A pyrolysis apparatus according to claim 28, characterized in that the partition wall (22) extends from the bottom (48) of the pyrolysis reactor (4) to a distance from the top wall (46) of the pyrolysis reactor (4).
31. A pyrolysis apparatus according to any one of claims 17 to 30, characterized in that pyrolysis reactor (4) is further divided in the movement direction of the solid fuel into entry section (4A) upstream of the drying section (4D), the entry section (4A) comprising the one or more bed ma- terial inlets (11), and into a discharge section (4C) downstream of the pyrolysis section (4B), the discharge section (4C) for discharging bed material from the pyrolysis reactor (4)..
32. A pyrolysis apparatus according to claim 31, character- i z e d in that the entry section (4A) and the drying section (4D) as well as the pyrolysis section (4B) and the discharge section (4A) are separated from each other by means of partition walls (24, 26) extending from the top wall (46) of the pyrolysis reactor (4) to a distance from the bottom (48) of the pyrolysis reactor (4).
33. A pyrolysis apparatus according to any one of claims 17 to 32, characterized in that pyrolysis reactor (4) is arranged in immediate connection with a bubbling fluidized bed boiler (30) for circulating bed material of the bubbling fluidized bed boiler (30) through the pyrolysis reactor (4).
34. A pyrolysis apparatus according to any one of claims 17 to 32, characterized in that pyrolysis reactor (4) is arranged in connection with a circulating fluidized bed boiler (30) for circulating bed material of the circulating fluidized bed boiler (30) through the pyrolysis reactor (4).
35. A pyrolysis apparatus according to claim 34, characterized in that the circulating fluidized bed boiler (30) comprises a separator (3) for separating bed material from the flue gases, and that the pyrolysis reactor (4) is arranged between the separator (3) and the combustion chamber of the circulating fluidized bed boiler (30) for circulating the solid particle bed material from the separator (3) through the pyrolysis reactor (4) into the combustion chamber.
36. Use of a pyrolysis apparatus for drying solid fuel in a pyrolysis reactor (4) which comprises a drying section (4D) and a pyrolysis section (4B) the drying section (4D) being arranged upstream of the pyrolysis section (4B).
PCT/FI2010/050443 2009-06-02 2010-06-01 Method of carrying out pyrolysis and pyrolysis apparatus WO2010139854A1 (en)

Priority Applications (6)

Application Number Priority Date Filing Date Title
RU2011152323/05A RU2571638C2 (en) 2009-06-02 2010-06-01 Pyrolysis method and pyrolysis device
CN201080031520.9A CN102459517B (en) 2009-06-02 2010-06-01 Method of carrying out pyrolysis and pyrolysis apparatus
CA2764220A CA2764220A1 (en) 2009-06-02 2010-06-01 Method of carrying out pyrolysis and pyrolysis apparatus
EP10727761A EP2438141A1 (en) 2009-06-02 2010-06-01 Method of carrying out pyrolysis and pyrolysis apparatus
US13/375,351 US9045694B2 (en) 2009-06-02 2010-06-01 Method of carrying out pyrolysis and pyrolysis apparatus
BRPI1011095A BRPI1011095A8 (en) 2009-06-02 2010-06-01 METHOD FOR PERFORMING PYROLYSIS AND PYROLYSIS APPARATUS

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FI20095614A FI125814B (en) 2009-06-02 2009-06-02 Method for performing pyrolysis and pyrolysis apparatus
FI20095614 2009-06-02

Publications (1)

Publication Number Publication Date
WO2010139854A1 true WO2010139854A1 (en) 2010-12-09

Family

ID=40825317

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/FI2010/050443 WO2010139854A1 (en) 2009-06-02 2010-06-01 Method of carrying out pyrolysis and pyrolysis apparatus

Country Status (9)

Country Link
US (1) US9045694B2 (en)
EP (1) EP2438141A1 (en)
CN (1) CN102459517B (en)
BR (1) BRPI1011095A8 (en)
CA (1) CA2764220A1 (en)
FI (1) FI125814B (en)
RU (1) RU2571638C2 (en)
UY (1) UY32661A (en)
WO (1) WO2010139854A1 (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013135973A1 (en) 2012-03-16 2013-09-19 Upm-Kymmene Corporation A process for upgrading pyrolysis oil, treated pyrolysis oil and the use thereof
US20200141570A1 (en) * 2017-06-09 2020-05-07 Bioshare Ab Recovery of chemicals from fuel streams

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9441887B2 (en) 2011-02-22 2016-09-13 Ensyn Renewables, Inc. Heat removal and recovery in biomass pyrolysis
US10041667B2 (en) 2011-09-22 2018-08-07 Ensyn Renewables, Inc. Apparatuses for controlling heat for rapid thermal processing of carbonaceous material and methods for the same
US10400175B2 (en) 2011-09-22 2019-09-03 Ensyn Renewables, Inc. Apparatuses and methods for controlling heat for rapid thermal processing of carbonaceous material
CN103031135B (en) * 2012-12-18 2014-07-30 中国科学院过程工程研究所 Fluidized bed hierarchical coal pyrolysis reactor and coal pyrolysis method
FI125541B (en) * 2014-04-24 2015-11-30 Torrec Oy Torrefiointilaite
FI126482B (en) * 2014-09-19 2016-12-30 Adamatic Oy Pyrolysis device and pyrolysis process
FI127201B (en) * 2015-04-17 2018-01-31 Valmet Technologies Oy Catalytic refining of pyrolysis vapors
WO2018125753A1 (en) 2016-12-29 2018-07-05 Ensyn Renewables, Inc. Demetallization of liquid biomass
CN110079350B (en) * 2019-05-30 2021-08-03 青岛科技大学 Biomass thermal cracking production process taking multi-chamber fluidized bed reactor as core

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4274941A (en) * 1974-10-10 1981-06-23 Bergwerksverband Gmbh Process for generating combustible gases, liquid coal byproducts and superheated steam from coal
WO2005033250A2 (en) * 2003-10-02 2005-04-14 Ebara Corporation Gasification method and apparatus
WO2009047387A1 (en) * 2007-10-11 2009-04-16 Valtion Teknillinen Tutkimuskeskus Method for carrying out pyrolysis
WO2009047392A1 (en) * 2007-10-11 2009-04-16 Valtion Teknillinen Tutkimuskeskus Apparatus for producing a pyrolysis product
EP2107098A2 (en) * 2008-03-31 2009-10-07 Metso Power Oy A pyrolysis method in connection with a boiler and a pyrolysis apparatus
EP2107099A2 (en) * 2008-03-31 2009-10-07 Metso Power Oy A method for performing pyrolysis and a pyrolysis apparatus

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2076272C1 (en) * 1995-07-07 1997-03-27 Григорий Исакович Двоскин Device for reworking solid wastes
JPH10237453A (en) * 1997-02-21 1998-09-08 Ube Ind Ltd Heat treatment apparatus for organic waste or the like
EP1043385A4 (en) * 1997-12-18 2008-08-06 Ebara Corp Fuel gasifying system
DE19930071C2 (en) * 1999-06-30 2001-09-27 Wolfgang Krumm Method and device for pyrolysis and gasification of organic substances and mixtures
CN1225521C (en) * 2000-05-29 2005-11-02 山东理工大学 Quickly thermolyzing and liquefying apparatus for centrifugal separated biomass
JP2002121559A (en) * 2000-10-13 2002-04-26 Oyodo Komatsu Kk Process and device for treating waste material
FI20055063A (en) * 2005-02-11 2006-08-12 Kvaerner Power Oy Method for reducing nitrogen oxide emissions from a fluidized bed boiler and air distribution system for a fluidized bed boiler
CN101139532B (en) * 2006-09-08 2010-12-29 中国科学院过程工程研究所 Solid fuel decoupling fluidized bed gasification method and device
DE102008017815B4 (en) * 2008-04-08 2012-01-26 Fischer Seats International Gmbh Energy absorption system
CN101343547A (en) * 2008-09-02 2009-01-14 中国科学院广州能源研究所 Apparatus and method for preparing biological oil with biomass vacuum thermal cracking and classification

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4274941A (en) * 1974-10-10 1981-06-23 Bergwerksverband Gmbh Process for generating combustible gases, liquid coal byproducts and superheated steam from coal
WO2005033250A2 (en) * 2003-10-02 2005-04-14 Ebara Corporation Gasification method and apparatus
WO2009047387A1 (en) * 2007-10-11 2009-04-16 Valtion Teknillinen Tutkimuskeskus Method for carrying out pyrolysis
WO2009047392A1 (en) * 2007-10-11 2009-04-16 Valtion Teknillinen Tutkimuskeskus Apparatus for producing a pyrolysis product
EP2107098A2 (en) * 2008-03-31 2009-10-07 Metso Power Oy A pyrolysis method in connection with a boiler and a pyrolysis apparatus
EP2107099A2 (en) * 2008-03-31 2009-10-07 Metso Power Oy A method for performing pyrolysis and a pyrolysis apparatus

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013135973A1 (en) 2012-03-16 2013-09-19 Upm-Kymmene Corporation A process for upgrading pyrolysis oil, treated pyrolysis oil and the use thereof
US10106750B2 (en) 2012-03-16 2018-10-23 Upm-Kymmene Corporation Process for upgrading pyrolysis oil, treated pyrolysis oil and the use thereof
US20200141570A1 (en) * 2017-06-09 2020-05-07 Bioshare Ab Recovery of chemicals from fuel streams
US11859812B2 (en) * 2017-06-09 2024-01-02 Bioshare Ab Recovery of chemicals from fuel streams

Also Published As

Publication number Publication date
BRPI1011095A2 (en) 2018-02-06
US20120073185A1 (en) 2012-03-29
BRPI1011095A8 (en) 2018-05-08
CN102459517A (en) 2012-05-16
RU2011152323A (en) 2013-07-20
FI20095614A (en) 2010-12-03
FI125814B (en) 2016-02-29
EP2438141A1 (en) 2012-04-11
CA2764220A1 (en) 2010-12-09
FI20095614A0 (en) 2009-06-02
US9045694B2 (en) 2015-06-02
UY32661A (en) 2010-12-31
CN102459517B (en) 2014-06-18
RU2571638C2 (en) 2015-12-20

Similar Documents

Publication Publication Date Title
US9045694B2 (en) Method of carrying out pyrolysis and pyrolysis apparatus
CN101619221B (en) A pyrolysis method in connection with a boiler and a pyrolysis apparatus
US7214252B1 (en) Method and device for pyrolyzing and gasifying organic substances or substance mixtures
CA2660925C (en) A method for performing pyrolysis and a pyrolysis apparatus
FI76114B (en) FOERFARANDE FOER PYROLYSERING AV LIGNOCELLULOSAHALTIGA AEMNEN OCH ANORDNING FOER GENOMFOERANDE AV FOERFARANDET.
US10059883B2 (en) Method for producing a pyrolysis product
US20100037805A1 (en) Method of and Apparatus for Controlling the Temperature of a Fluidized Bed Reactor
Aydar et al. Effect of the type of gasifying agent on gas composition in a bubbling fluidized bed reactor
US20240093865A1 (en) Bubbling Fluidized Bed Reactor
EP1187893B1 (en) Process for the gasification of carbonaceous material
JP4998551B2 (en) Fluidized bed gasification facility
US10023803B2 (en) Method for performing pyrolysis and a pyrolysis apparatus
CA1096707A (en) Fluidized-bed compact boiler and method of operation
CN105647552B (en) A kind of dry distillation of coal and coal catalytic cracking combination process
US4945656A (en) Circulating fluidised bed apparatus
US4471723A (en) Heat recovery method and installation, particularly for cooling ash
KR100460217B1 (en) Coal Gasifier using Downer Region in a Circulating Fluidized Bed Reactor
FI68074C (en) FOER FARANDE OCH ANORDNING FOR THERMAL BEHANDLING AV KOLVAETEHALTIGA MATERIAL

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 201080031520.9

Country of ref document: CN

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 10727761

Country of ref document: EP

Kind code of ref document: A1

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
WWE Wipo information: entry into national phase

Ref document number: 13375351

Country of ref document: US

WWE Wipo information: entry into national phase

Ref document number: 2764220

Country of ref document: CA

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 2834/MUMNP/2011

Country of ref document: IN

REEP Request for entry into the european phase

Ref document number: 2010727761

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2010727761

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2011152323

Country of ref document: RU

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: PI1011095

Country of ref document: BR

ENP Entry into the national phase

Ref document number: PI1011095

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20111202