WO2024009117A1 - Method and apparatus for carbonizing sludge with organic content - Google Patents

Method and apparatus for carbonizing sludge with organic content Download PDF

Info

Publication number
WO2024009117A1
WO2024009117A1 PCT/HU2023/050043 HU2023050043W WO2024009117A1 WO 2024009117 A1 WO2024009117 A1 WO 2024009117A1 HU 2023050043 W HU2023050043 W HU 2023050043W WO 2024009117 A1 WO2024009117 A1 WO 2024009117A1
Authority
WO
WIPO (PCT)
Prior art keywords
reactor
carbonizer
biogas
sludge
drying
Prior art date
Application number
PCT/HU2023/050043
Other languages
French (fr)
Inventor
Szilvia KASZÁS
Original Assignee
Nova Nesa Hungary Új Tudományos Ismeretek Alkalmazása Zrt.
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 Nova Nesa Hungary Új Tudományos Ismeretek Alkalmazása Zrt. filed Critical Nova Nesa Hungary Új Tudományos Ismeretek Alkalmazása Zrt.
Publication of WO2024009117A1 publication Critical patent/WO2024009117A1/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
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/02—Multi-step carbonising or coking processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
    • B65G—TRANSPORT OR STORAGE DEVICES, e.g. CONVEYORS FOR LOADING OR TIPPING, SHOP CONVEYOR SYSTEMS OR PNEUMATIC TUBE CONVEYORS
    • B65G33/00—Screw or rotary spiral conveyors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
    • C02F11/123—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using belt or band filters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
    • C02F11/127—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering by centrifugation
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
    • C05F17/00—Preparation of fertilisers characterised by biological or biochemical treatment steps, e.g. composting or fermentation
    • C05F17/60—Heating or cooling during the treatment
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
    • C05F7/00—Fertilisers from waste water, sewage sludge, sea slime, ooze or similar masses
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/28—Other processes
    • C10B47/32—Other processes in ovens with mechanical conveying means
    • C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • 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
    • 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
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/40—Solid fuels essentially based on materials of non-mineral origin
    • C10L5/44—Solid fuels essentially based on materials of non-mineral origin on vegetable substances
    • C10L5/447—Carbonized vegetable substances, e.g. charcoal, or produced by hydrothermal carbonization of biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B1/00—Preliminary treatment of solid materials or objects to facilitate drying, e.g. mixing or backmixing the materials to be dried with predominantly dry solids
    • F26B1/005—Preliminary treatment of solid materials or objects to facilitate drying, e.g. mixing or backmixing the materials to be dried with predominantly dry solids by means of disintegrating, e.g. crushing, shredding, milling the materials to be dried
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
    • F26B17/02—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by belts carrying the materials; with movement performed by belts or elements attached to endless belts or chains propelling the materials over stationary surfaces
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F26B23/02—Heating arrangements using combustion heating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F26B23/02—Heating arrangements using combustion heating
    • F26B23/022—Heating arrangements using combustion heating incinerating volatiles in the dryer exhaust gases, the produced hot gases being wholly, partly or not recycled into the drying enclosure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/04—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour circulating over or surrounding the materials or objects to be dried
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B5/00—Drying solid materials or objects by processes not involving the application of heat
    • F26B5/08—Drying solid materials or objects by processes not involving the application of heat by centrifugal treatment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/10—Energy recovery
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/02—Combustion or pyrolysis
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/08—Drying or removing water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/24—Mixing, stirring of fuel components
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/28—Cutting, disintegrating, shredding or grinding
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/30—Pressing, compressing or compacting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/547—Filtration for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/34—Other details of the shaped fuels, e.g. briquettes
    • C10L5/36—Shape
    • C10L5/363—Pellets or granulates
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B2200/00—Drying processes and machines for solid materials characterised by the specific requirements of the drying good
    • F26B2200/18—Sludges, e.g. sewage, waste, industrial processes, cooling towers

Definitions

  • the invention relates to a method for carbonizing sludge with organic content, wherein the term sludge can include river and/or lake sludge with organic material content, wherein prior to carbonization the material is chopped, mixed, and the water content thereof is removed in several steps, and at least one of the water removal steps is carried out by heating, and when the solid content of the material has reached at least 85 v% the carbonization is carried out at elevated temperature, and a portion of biogases developed during the carbonization is used for the heating during the drying step.
  • the invention also relates to an apparatus for carrying out the method.
  • the publication is silent concerning the design of the carbonizing reactor, the temperature required for the heating and the environmental conditions and the degree of energy utilization at the carbonizing process.
  • the task of the invention is to provide a method and an apparatus for carrying out the method which utilizes the values in the solid content of the sludge, which is highly economic because a substantial portion of the energy required for the reaction is provided by the biogases developed during the reaction, and the final product can be utilized as valuable fertilizer and/or as a pellet or brick fuel.
  • the invention is based on the discovery that a sufficiently dried and condensed sewage sludge that can also be a river or lake sludge with organic content can be carbonized in an oxygen free nitrogen atmosphere, and a portion of biogases developed in the reactor can be used for heating the reactor itself and in part also for the heating required for the drying, and the hot air flowing in the reactor can also be used for the drying of the sludge.
  • the energy required for the reaction is not too high, and water obtained during the drying process can be used for irrigation or as industrial water.
  • the costs of making the final product usable also as fertilizer are substantially below the costs of producing fertilizers with the same effect not to mention that the method substitutes an environmentally contaminating technology.
  • the utilization of the organic content is generally not among the first-ranking objectives.
  • the main objective is the energy utilization efficiency of the process and the re-utilization of the water included in the sludge without causing harm to the environment.
  • a further important aspect is the amount of energy to be supplied for obtaining the final product after the carbonization that has high carbon content and can be used either as a fertilizer or as a solid fuel.
  • Carbonization is an energy-demanding process, but with increasing the efficiency and the utilization of the developed biogases it is possible to convert all components of the sludge being as such harmful for the environment into materials appropriate for reutilization and minimizing the associated energy demand.
  • the invention provides an efficient solution for the task set and provides substantial advantages in both ways of using the final product, namely as a fertilizer or as pellet or brick fuel, as it has high energy efficiency.
  • Fig. 1 shows the functional layout of the sludge carbonizing apparatus according to the invention.
  • Pipe 1 designates the means interconnecting the illustrated technological units and they can be realized by worm gearing transport devices or conveyor lines with closed space that have the task of furthering the material with different solid material content towards the next technology unit.
  • comminutors 2 are used which are high power machines that cut and mix the material into small pieces.
  • drying units 3 are used that have the task of decreasing the degree of humidity of the material passed therethrough, whereby the material gets more compact.
  • the design of the drying units 3 can be different and can get the energy required for drying in different form.
  • fans 7 and filters 8 are often used, which have the task of screening or withholding the dust or other granular contaminations from the conveyed fluid or air and to transport the main medium.
  • the material to be carbonized is received by a feed chute 30.
  • stabilized sludge As a starting material pre-compressed stabilized sludge is used that has a solid material content of 15 to 25 volume % (in the following: v%) or from river or lake sludge that has at least 2 v% organic material content. It is preferred if the incoming sludge has been previously desiccated and stabilized.
  • stabilized sludge means that the incoming sludge has been previously pretreated e.g., by sedimentation using bacteria, and a dominant portion of the so obtained purified water is led away. Following the precompression, the solid content can be 15-20 v% and its organic content is at least 5 v%.
  • the pre-compression can take place is several steps or the lake or river sludge with high organic content can be carried out in the field by natural desiccation.
  • the consistency of the pre-compressed sludge is somewhat like a dough, and this material is transported e.g., by a dumper to the apparatus according to the invention, namely to the feed chute 30.
  • a first comminutor 2a is coupled, which crushes, mixes, and homogenizes the larger pieces in the incoming material into pieces of 15 to 20 mm size.
  • a first pipe la having a conveyor
  • a first dryer 3a which can be a centrifuging dryer, but this can be combined with a drying using heat.
  • Fig. 1 such a combined solution is shown.
  • the first dryer 3a Before use the first dryer 3a must be preheated to a temperature about 180°C, and when the internal temperature reaches the value of about 250°C, an exotherm reaction commences with the development of biogases, which are lead through tube 4a to a biogas container 5.
  • the heating of the first dryer 3a is provided in part by gas burners (not shown) and following the start of the carbonization process by the hot air generated in carbonizer reactor 16 (described later) fed back to the first dryer 3a. This feedback is driven by fan 7c, and the flow is provided through tube 12b.
  • the steam developed in the first dryer 3a is driven by fan 7a through pipe 9a and led through a steam filter 10 and arrives through pipe 9e to steam distiller tower 11 from where the so obtained condensed water will be forwarded to condensed water container 31.
  • the first dryer 3a By using the first dryer 3a a material is obtained with 30 to 50 v% solid material content. The extent of drying depends on the furthering speed i.e., on the time during which the material is kept in the first dryer 3a. Earlier reference was made to the advantages of the pre-drying of a highly diluted sludge. If this cannot be solved, then by increasing the drying time the first dryer 3a can be used for the drying of more diluted sludge, but such drying requires more energy, and in such case, it can be preferred to remove a portion of the excess water by mechanical centrifugation.
  • the pre-compacted dried material is conveyed through second pipe lb to the input of second dryer 3b, in which drying takes place by means of heat.
  • the temperature of the second dryer 3b can be heated also by biogas burners (not shown) supplied from the biogas container 5 and in addition to conventional gas heating by hot air fed back from the carbonizer reactor 16.
  • This biogas feedback branch is driven by fan 7d, and the hot air is supplied through tube 12c.
  • the design of the second dryer 3b is like that of the first dryer 3a but here there is no need to centrifugation, moreover due to the previously occurred exotherm reaction biogases were removed in the first dryer 3a.
  • the steam generated here are driven by fan 7b through pipe 9b to pipe 9e and from there to the steam distiller tower 11.
  • first and second dryers 3a, 3b can be realized by a single larger dryer. From the second dryer 3b the material will have a higher degree of solid content of 85 to 90 v% and this material is passed through third pipe lc and through second comminutor 2b to feed input of the carbonizer reactor 16.
  • the third pipe lc is a further band conveyor with high slope angle. This further band is completely covered, and the transported material cannot get strayed, it has a long duration, a high efficiency with low noise and compact structure.
  • the carbonizer reactor 16 is designed according to the invention as a double walled, long tube or container rotated by motor 14 with a predetermined speed.
  • the reaction space is divided into two consecutively arranged parts, wherein the first part is constituted by the interior of the inner tube, in which there is a spirally arranged driving screw under the effect of which the fed dry material moves forward to the right direction and after leaving the end of the inner tube the material enters the second reaction space formed between the two tubes, in which the sense of the spiral is opposite to the sense in the first space, whereby the direction of the movement of the material gets reversed and the dry material obtained following the carbonization will be passed through a lock gate at the left end region of the carbonizer reactor 16 to feed input of a spiral worm type furthering means 23.
  • the afore described double-walled tube of the carbonizing reactor 16 is encircled by envelope 15 in which burners providing the required operation temperature of the carbonizing reactor 16 are arranged including biogas and gas burners 18, and the removal of the generated gases takes also place from this space.
  • the carbonizer reactor 16 Before use, the carbonizer reactor 16 should be preheated to at least 180 °C temperature that requires about 0.7 to 1 hour time.
  • the dry material s furthered by the spiral screw vanes with a speed determined by the revolution of the motor 14, and the parameters (including the temperature and the furthering speed) are adjusted by control unit 6 so that during the time spent by the material in the carbonizer reactor 16 the carbonization process gets completed.
  • the typical speed range of the double-walled container is adjusted between about 7 and 11 rev/min.
  • the space above the dry material is filled by biogas and nitrogen supplied by nitrogen generator 13.
  • the temperature required for the carbonization process is provided by the biogas and line gas burners 18 controlled by the control unit 6.
  • the hot air generated in the envelope 15 during the heating is led away by means of fans 7a and 7d through dust filters 8a, 8b and through tubes 12b and 12c to the dryers 3a and 3b as mentioned earlier.
  • Fig. 1 the lead-out elements of the carbonizer reactor 16 were indicated twice one after the other to illustrate thereby the high length of the carbonizing reactor 16. This indication was used only for the visualization because the appropriate lead-out tubes are arranged evenly distributed along the length of the reactor just as the burners 18. The presence of the envelope 15 has also been indicated schematically, which has also the task of holding the weight of the double-walled tube and the whole carbonizer reactor 16.
  • the line gas burners 18 are turned on and after about 15 minutes the flow of the material can be started because such a heating time is sufficient that the temperature in the carbonizer reactor 16 reaches the value of about 450 °C.
  • the aromatic ring compounds generated during the drying cycles will participate in further reactions at the carbonization temperature, and the components will be converted to combustible gases being a mixture of carbon and hydrogen and oxygen, like pure hydrogen, methane, and carbon-monoxide. Such reactions do not have separate phases and many reactions are embedded in each other. Attention should be made that temperature does not increase above 600 °C, and the adjustment should be set preferably between 450 and 550 °C.
  • the combustible biogases will be collected in tube 19 and a portion of them is sent to the burners 18 where under the prevailing high temperature it gets automatically ignited. Thereafter the line gas can be switched off and the process will be self-maintaining.
  • the excess biogases are sent through the tube 12 and a biogas filter 20 that separates the tar and wood acid components to a biogas cooling tower 21, and following the cooling it will be collected in a biogas container 22 which is also connected to the other biogas container 5 shown at the left side of the drawing.
  • the heat utilization efficiency of the apparatus using a double returning heating process is high, and the material does not get into contact with the removed smoke, with the gases and does not contaminate air. In comparison with a conventional heating system using a single tube, the heat utilization efficiency has more than doubled.
  • the thermal efficiency of the apparatus can reach the range of 70 % to 90%.
  • the carbonized final product made in the carbonizer reactor 16 is sent through a worm driven and water-cooled transport system 23 to a third comminutor 2c where it is crashed to the size of the required final product and gets homogenized.
  • the respective technology units of the apparatus are controlled by the central controller 6, which adjusts the temperature required for the carbonization and the associated transport and flow rates, whereas it measures the values of the parameters present in these technology units that characterize the associated sections of the process.
  • the final product leaving the carbonizer reactor 16 is substantially bio coal with a calorimetric value of 45 - 55 MJ/kg that is even higher than that of black coal.
  • the final product is intended for heating purposes, then for making brick fuel or pellets it is advisable to be mixed with other natural materials having a lower calorimetric value.
  • Such can be e.g., wood cuttings, wood pellets, or agricultural dry waste.
  • the bio carbon obtained by carbonization has high nitrogen, phosphor, and calcium content, and it can be used in granulated or pellet from as a fertilizer or as a material substituting fertilizers and dispersed on the field using modern fertilizer distributing machines.
  • the generated bio carbon is processed depending on its final use, which can be a processing unit 24 and the following unit is a granulating, pellet making device 25 from which the final product is fed to a bagging machine 26.
  • the apparatus can be made also in different arrangement of units, like the two separate dyers can be replaced by a single dryer, or the centrifugal dryer will not be needed, or the hot air heating of the dryer can be left out, but such modifications will not influence the essence of the invention according to which from the initial sludge that represented a dangerous waste without value, a final product has been made with high value, and the waste water has been treated that can be used for irrigation.
  • the energy usage is preferred, because a portion of the energy required for the carbonization is utilized for drying the sludge, and the generated biogases decrease the amount of gas required for the drying and for the carbonization.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Hydrology & Water Resources (AREA)
  • Materials Engineering (AREA)
  • Sustainable Development (AREA)
  • Molecular Biology (AREA)
  • Microbiology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Biotechnology (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Biochemistry (AREA)
  • Treatment Of Sludge (AREA)

Abstract

Method and apparatus for carbonizing sludge with organic content, wherein a pre- dried sludge is processed and the material is moved in a closed space till carbonization, and the major part of water content thereof is removed mostly by heating until the solid content of the material has reached at least 85 v%, then the materiel is fed into the carbonizer reactor (16) being a rotated double-walled container, and the material is passed twice along the carbonizer reactor (16) in opposite directions at a temperature between 450°C and 600 °C in an oxygen free environment in the presence of nitrogen, wherein the generated biogases are lead out, and used in part for the heating of the reactor and in part for the drying, and the hot air generated in the carbonizer reactor is used for drying, and the bio coal obtained in the reactor is cooled and processed either as bio fertilizer or as a heating material.

Description

Method and apparatus for carbonizing sludge with organic content
The invention relates to a method for carbonizing sludge with organic content, wherein the term sludge can include river and/or lake sludge with organic material content, wherein prior to carbonization the material is chopped, mixed, and the water content thereof is removed in several steps, and at least one of the water removal steps is carried out by heating, and when the solid content of the material has reached at least 85 v% the carbonization is carried out at elevated temperature, and a portion of biogases developed during the carbonization is used for the heating during the drying step. The invention also relates to an apparatus for carrying out the method.
For sewage sludge treatment and for the carbonization of the organic content therein several solutions are known. Of such solutions CN 212559898 U can be mentioned, in which the water content is removed by the application of heat, and in a carbonizing reactor from the dry content of the sludge a coal-like final product is made, wherein a portion of the required heat is provided by the feedback of the generated organic gases.
The publication is silent concerning the design of the carbonizing reactor, the temperature required for the heating and the environmental conditions and the degree of energy utilization at the carbonizing process.
In CN215403719 U the removal of water takes place by a carbon filter, in which the powdered coal obtained during the carbonization is used. The utility model is silent concerning the circumstances of the carbonization.
The task of the invention is to provide a method and an apparatus for carrying out the method which utilizes the values in the solid content of the sludge, which is highly economic because a substantial portion of the energy required for the reaction is provided by the biogases developed during the reaction, and the final product can be utilized as valuable fertilizer and/or as a pellet or brick fuel.
The invention is based on the discovery that a sufficiently dried and condensed sewage sludge that can also be a river or lake sludge with organic content can be carbonized in an oxygen free nitrogen atmosphere, and a portion of biogases developed in the reactor can be used for heating the reactor itself and in part also for the heating required for the drying, and the hot air flowing in the reactor can also be used for the drying of the sludge.
As a result, the energy required for the reaction is not too high, and water obtained during the drying process can be used for irrigation or as industrial water. The costs of making the final product usable also as fertilizer are substantially below the costs of producing fertilizers with the same effect not to mention that the method substitutes an environmentally contaminating technology.
In the elimination of sewage sludges with organic content the utilization of the organic content is generally not among the first-ranking objectives. Where carbonization is used, the main objective is the energy utilization efficiency of the process and the re-utilization of the water included in the sludge without causing harm to the environment.
A further important aspect is the amount of energy to be supplied for obtaining the final product after the carbonization that has high carbon content and can be used either as a fertilizer or as a solid fuel.
Carbonization is an energy-demanding process, but with increasing the efficiency and the utilization of the developed biogases it is possible to convert all components of the sludge being as such harmful for the environment into materials appropriate for reutilization and minimizing the associated energy demand.
According to the invention a method and an apparatus have been provided for the carbonization of sludge with organic content, in which the steps defined in the attached claims are carried out. The structure of the apparatus for carrying out the method is defined in the attached apparatus claims.
The invention provides an efficient solution for the task set and provides substantial advantages in both ways of using the final product, namely as a fertilizer or as pellet or brick fuel, as it has high energy efficiency.
The method and apparatus according to the invention will now be described in connection with an example thereof, wherein reference will be made to the accompanying drawing. In the drawing:
Fig. 1 shows the functional layout of the sludge carbonizing apparatus according to the invention.
In the apparatus according to the invention there are several units performing the same or nearly the same function which were indicated by identical refence numerals, wherein the distinction between them is shown by a letter following the same number. Pipe 1 designates the means interconnecting the illustrated technological units and they can be realized by worm gearing transport devices or conveyor lines with closed space that have the task of furthering the material with different solid material content towards the next technology unit.
Gases are led by tubes 12 and liquids by pipes 9.
In certain places of the apparatus comminutors 2 are used which are high power machines that cut and mix the material into small pieces.
In other distinct parts of the apparatus drying units 3 are used that have the task of decreasing the degree of humidity of the material passed therethrough, whereby the material gets more compact. At different locations of the apparatus the design of the drying units 3 can be different and can get the energy required for drying in different form.
Following the drying units 3 fans 7 and filters 8 are often used, which have the task of screening or withholding the dust or other granular contaminations from the conveyed fluid or air and to transport the main medium.
At the input side of the apparatus the material to be carbonized is received by a feed chute 30. As a starting material pre-compressed stabilized sludge is used that has a solid material content of 15 to 25 volume % (in the following: v%) or from river or lake sludge that has at least 2 v% organic material content. It is preferred if the incoming sludge has been previously desiccated and stabilized. The term "stabilized sludge" means that the incoming sludge has been previously pretreated e.g., by sedimentation using bacteria, and a dominant portion of the so obtained purified water is led away. Following the precompression, the solid content can be 15-20 v% and its organic content is at least 5 v%. The pre-compression can take place is several steps or the lake or river sludge with high organic content can be carried out in the field by natural desiccation. The consistency of the pre-compressed sludge is somewhat like a dough, and this material is transported e.g., by a dumper to the apparatus according to the invention, namely to the feed chute 30.
To the bottom of the chute 30 a first comminutor 2a is coupled, which crushes, mixes, and homogenizes the larger pieces in the incoming material into pieces of 15 to 20 mm size. From the first comminutor 2a the homogenized and crushed material is fed through a first pipe la having a conveyor to a first dryer 3a which can be a centrifuging dryer, but this can be combined with a drying using heat. In Fig. 1 such a combined solution is shown. In case of heat drying, before use the first dryer 3a must be preheated to a temperature about 180°C, and when the internal temperature reaches the value of about 250°C, an exotherm reaction commences with the development of biogases, which are lead through tube 4a to a biogas container 5. The heating of the first dryer 3a is provided in part by gas burners (not shown) and following the start of the carbonization process by the hot air generated in carbonizer reactor 16 (described later) fed back to the first dryer 3a. This feedback is driven by fan 7c, and the flow is provided through tube 12b. The steam developed in the first dryer 3a is driven by fan 7a through pipe 9a and led through a steam filter 10 and arrives through pipe 9e to steam distiller tower 11 from where the so obtained condensed water will be forwarded to condensed water container 31.
By using the first dryer 3a a material is obtained with 30 to 50 v% solid material content. The extent of drying depends on the furthering speed i.e., on the time during which the material is kept in the first dryer 3a. Earlier reference was made to the advantages of the pre-drying of a highly diluted sludge. If this cannot be solved, then by increasing the drying time the first dryer 3a can be used for the drying of more diluted sludge, but such drying requires more energy, and in such case, it can be preferred to remove a portion of the excess water by mechanical centrifugation.
The pre-compacted dried material is conveyed through second pipe lb to the input of second dryer 3b, in which drying takes place by means of heat. The temperature of the second dryer 3b can be heated also by biogas burners (not shown) supplied from the biogas container 5 and in addition to conventional gas heating by hot air fed back from the carbonizer reactor 16. This biogas feedback branch is driven by fan 7d, and the hot air is supplied through tube 12c. The design of the second dryer 3b is like that of the first dryer 3a but here there is no need to centrifugation, moreover due to the previously occurred exotherm reaction biogases were removed in the first dryer 3a. The steam generated here are driven by fan 7b through pipe 9b to pipe 9e and from there to the steam distiller tower 11.
It is noted that the first and second dryers 3a, 3b can be realized by a single larger dryer. From the second dryer 3b the material will have a higher degree of solid content of 85 to 90 v% and this material is passed through third pipe lc and through second comminutor 2b to feed input of the carbonizer reactor 16. The third pipe lc is a further band conveyor with high slope angle. This further band is completely covered, and the transported material cannot get strayed, it has a long duration, a high efficiency with low noise and compact structure.
The carbonizer reactor 16 is designed according to the invention as a double walled, long tube or container rotated by motor 14 with a predetermined speed. The reaction space is divided into two consecutively arranged parts, wherein the first part is constituted by the interior of the inner tube, in which there is a spirally arranged driving screw under the effect of which the fed dry material moves forward to the right direction and after leaving the end of the inner tube the material enters the second reaction space formed between the two tubes, in which the sense of the spiral is opposite to the sense in the first space, whereby the direction of the movement of the material gets reversed and the dry material obtained following the carbonization will be passed through a lock gate at the left end region of the carbonizer reactor 16 to feed input of a spiral worm type furthering means 23.
The afore described double-walled tube of the carbonizing reactor 16 is encircled by envelope 15 in which burners providing the required operation temperature of the carbonizing reactor 16 are arranged including biogas and gas burners 18, and the removal of the generated gases takes also place from this space.
Before use, the carbonizer reactor 16 should be preheated to at least 180 °C temperature that requires about 0.7 to 1 hour time.
The dry material s furthered by the spiral screw vanes with a speed determined by the revolution of the motor 14, and the parameters (including the temperature and the furthering speed) are adjusted by control unit 6 so that during the time spent by the material in the carbonizer reactor 16 the carbonization process gets completed. The typical speed range of the double-walled container is adjusted between about 7 and 11 rev/min.
In the interior space of the carbonizer reactor 16 oxygen is not present, the space above the dry material is filled by biogas and nitrogen supplied by nitrogen generator 13. The temperature required for the carbonization process is provided by the biogas and line gas burners 18 controlled by the control unit 6. The hot air generated in the envelope 15 during the heating is led away by means of fans 7a and 7d through dust filters 8a, 8b and through tubes 12b and 12c to the dryers 3a and 3b as mentioned earlier.
In Fig. 1 the lead-out elements of the carbonizer reactor 16 were indicated twice one after the other to illustrate thereby the high length of the carbonizing reactor 16. This indication was used only for the visualization because the appropriate lead-out tubes are arranged evenly distributed along the length of the reactor just as the burners 18. The presence of the envelope 15 has also been indicated schematically, which has also the task of holding the weight of the double-walled tube and the whole carbonizer reactor 16.
Following the preheating, in the carbonizer reactor 16 the line gas burners 18 are turned on and after about 15 minutes the flow of the material can be started because such a heating time is sufficient that the temperature in the carbonizer reactor 16 reaches the value of about 450 °C. During carbonization the aromatic ring compounds generated during the drying cycles will participate in further reactions at the carbonization temperature, and the components will be converted to combustible gases being a mixture of carbon and hydrogen and oxygen, like pure hydrogen, methane, and carbon-monoxide. Such reactions do not have separate phases and many reactions are embedded in each other. Attention should be made that temperature does not increase above 600 °C, and the adjustment should be set preferably between 450 and 550 °C.
The combustible biogases will be collected in tube 19 and a portion of them is sent to the burners 18 where under the prevailing high temperature it gets automatically ignited. Thereafter the line gas can be switched off and the process will be self-maintaining. The excess biogases are sent through the tube 12 and a biogas filter 20 that separates the tar and wood acid components to a biogas cooling tower 21, and following the cooling it will be collected in a biogas container 22 which is also connected to the other biogas container 5 shown at the left side of the drawing.
In the process described there are no contaminating smoke emissions, and this is very environmentally friendly and meets national environmental protection standards.
The heat utilization efficiency of the apparatus using a double returning heating process is high, and the material does not get into contact with the removed smoke, with the gases and does not contaminate air. In comparison with a conventional heating system using a single tube, the heat utilization efficiency has more than doubled. The thermal efficiency of the apparatus can reach the range of 70 % to 90%.
The carbonized final product made in the carbonizer reactor 16 is sent through a worm driven and water-cooled transport system 23 to a third comminutor 2c where it is crashed to the size of the required final product and gets homogenized.
The respective technology units of the apparatus are controlled by the central controller 6, which adjusts the temperature required for the carbonization and the associated transport and flow rates, whereas it measures the values of the parameters present in these technology units that characterize the associated sections of the process.
The final product leaving the carbonizer reactor 16 is substantially bio coal with a calorimetric value of 45 - 55 MJ/kg that is even higher than that of black coal. In case the final product is intended for heating purposes, then for making brick fuel or pellets it is advisable to be mixed with other natural materials having a lower calorimetric value. Such can be e.g., wood cuttings, wood pellets, or agricultural dry waste.
The bio carbon obtained by carbonization has high nitrogen, phosphor, and calcium content, and it can be used in granulated or pellet from as a fertilizer or as a material substituting fertilizers and dispersed on the field using modern fertilizer distributing machines.
In this way in the apparatus the generated bio carbon is processed depending on its final use, which can be a processing unit 24 and the following unit is a granulating, pellet making device 25 from which the final product is fed to a bagging machine 26.
In the foregoing an exemplary embodiment of the apparatus according to the invention has been described. The apparatus can be made also in different arrangement of units, like the two separate dyers can be replaced by a single dryer, or the centrifugal dryer will not be needed, or the hot air heating of the dryer can be left out, but such modifications will not influence the essence of the invention according to which from the initial sludge that represented a dangerous waste without value, a final product has been made with high value, and the waste water has been treated that can be used for irrigation. Furthermore, the energy usage is preferred, because a portion of the energy required for the carbonization is utilized for drying the sludge, and the generated biogases decrease the amount of gas required for the drying and for the carbonization. It has been also mentioned that for the method according to the invention not only conventional waste sludge can be used but also sludge with high organic material content which can be present in lakes and ponds in case of which a preliminary drying can be made. Unfortunately, such contaminated lakes and ponds can often be found, and the cleaning of them and their transformation to have living water requires the removal of the contaminated sludge, and without the present invention this represents a task connected with high energy and labor.

Claims

Claims:
1. Method for carbonizing sludge with organic content, wherein the term sludge can include river and/or lake sludge with organic material content, wherein prior to carbonization the material is chopped, mixed, and the water content thereof is removed in several steps, and in at least one of the water removal steps the removal is carried out by heating, and when the solid content of the material has reached at least 85 v% the carbonization is carried out at elevated temperature, and a portion of biogases developed during the carbonization is used for generating the heat for the drying, characterized by the steps of during the drying step the pre-dried material is kept at a temperature between 180 °C and 280 °C when biogases are removed, then the material with at least 85 v% solid content is passed twice along carbonizer reactor (16) at a temperature between 450°C and 600 °C in an oxygen free environment in the presence of nitrogen, wherein the carbonizer reactor (16) is a double-walled container, wherein during the first passage the material is led along the internal space of the double-walled container in a first direction, and then led through the space formed between the two walls of the container in a second direction opposite to the first direction, and during said passage biogases are generated which are lead out, filtered and used at least in part for the heating of the carbonizer reactor (16) and for the drying, and the so obtained bio-coal is cooled and led away and according to the final destination thereof being processed as a fertilizer or as a heating material.
2. The method as claimed in claim 1, wherein the double-walled container of the carbonizer reactor (16) being rotated for moving the material contained therein, and the heat required for the carbonization is provided by gas and biogas burners (18) arranged in an envelope (15) surrounding said double walled container.
3. The method as claimed in claim 2, wherein hot air generated in the interior of the envelope (15) is fed back to the heating of the one or more dryers (3a, 3b).
4. The method as claimed in any of claims 1 to 3, wherein the water content removed from the starting material and obtained during said drying steps is filtered and when needed is condensed and being led away and stored.
5. The method as claimed in any of claims 1 to 3, wherein the removal of water content is carried out in a plurality of steps and the first removal step is made by centrifuging or by pressing.
6. The method as claimed in any of claims 1 to 5, wherein the drying made by the application of heat is carried out in two steps, and in both steps the hot air and biogases generated in the carbonizing reactor (16) are utilized for heating, and the extracted water present in the form of steam being filtered, condensed, led away, and stored.
7. The method as claimed in any of claims 1 to 6, wherein the generated biogases being first filtered, then cooled and stored in container (22, 5) and fed from here to the burners (18).
8. The method as claimed in any of claims 1 to 7, wherein preheating the carbonizer reactor (16) before its use for carbonization at a temperature of at least 180 °C.
9. Sludge carbonizing apparatus for carrying out the method as claimed in any of claims 1 to 8, comprising a chute (30) for receiving an initial pre-compacted sludge, then at least one comminutor (2), at least one drying unit (3) and a carbonizer reactor (16), characterized in that the carbonizer reactor (16) is designed as a double-walled elongated container rotated around its own axis and having two interior spaces to which a nitrogen generator (13) is connected and being closed from air, in the two interior spaces diverting means being arranged that move the material in opposite axial directions in the respective interior spaces, an envelope (15) is arranged around the double-walled container, and in the space between the envelope (15) and the double-walled container biogas and gas burners (18) are arranged, and biogas tubes led from said interior spaces to biogas cooling tower (21) from where biogas is supplied at least to the biogas burners (18) heating the carbonizer reactor (16), and hot air generated around the carbonizer reactor (16) is led through hot air tubes (12) to at least one of said dryers (3a, 3b).
10. The apparatus as claimed in claim 9, comprising at least two sludge dryers (3a, 3b), and the chute (30) is connected through a first comminutor (2a) to the first dryer (3a) which is provided with a centrifuging or compressing water removal unit and has a heated drying portion.
11. The apparatus as claimed in claim 10, wherein the output of the first dryer (3a) is led to a second dryer (3b) that comprises biogas/natural gas burners (18) and being also heated by the hot air supplied from the carbonizer reactor (16).
12. The apparatus as claimed in claims 9 or 10, wherein all tubes and pipes through which the material is proceeding towards the carbonizer reactor (16) being designed as closed space worm gearing furthering lines or as conveyor lines (la, lb, lc).
13. The apparatus as claimed in any of claims 9 to 12, wherein the liquid component generated in said dryers (3a, 3b) being led and condensed in steam form through a steam distiller tower (11) and from here to a condensed water container (31).
14. The apparatus as claimed in any of claims 9 to 13, wherein the output of the carbonizer reactor (16) supplying bio coal is connected through a water-cooled screw-type transport system to a processing unit (24 or 25) making bio fertilizer or pellets.
15. The apparatus as claimed in any of claims 9 to 13, wherein from the carbonizer reactor (16) a biogas tube (12) is connected to a biogas filter (20) and from here to a biogas cooling tower (21) to biogas container (22).
PCT/HU2023/050043 2022-07-07 2023-07-05 Method and apparatus for carbonizing sludge with organic content WO2024009117A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
HUP2200257 2022-07-07
HU2200257A HUP2200257A1 (en) 2022-07-07 2022-07-07 Process and equipment for carbonizing sewage sludge

Publications (1)

Publication Number Publication Date
WO2024009117A1 true WO2024009117A1 (en) 2024-01-11

Family

ID=89658296

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/HU2023/050043 WO2024009117A1 (en) 2022-07-07 2023-07-05 Method and apparatus for carbonizing sludge with organic content

Country Status (2)

Country Link
HU (1) HUP2200257A1 (en)
WO (1) WO2024009117A1 (en)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100935446B1 (en) * 2009-08-13 2010-01-06 주식회사 아이디알시스템 Method of device for high water content of drying and carbonizing
CN112079547A (en) * 2020-08-21 2020-12-15 武汉齐宇天下环境科技有限公司 Multistage pyrolysis and carbonization integrated sludge treatment method
EP3862410A1 (en) * 2018-10-02 2021-08-11 Evoluciones Tecnológicas Madrileñas, S. L. Pyrolysis method with rapid decompression

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100935446B1 (en) * 2009-08-13 2010-01-06 주식회사 아이디알시스템 Method of device for high water content of drying and carbonizing
EP3862410A1 (en) * 2018-10-02 2021-08-11 Evoluciones Tecnológicas Madrileñas, S. L. Pyrolysis method with rapid decompression
CN112079547A (en) * 2020-08-21 2020-12-15 武汉齐宇天下环境科技有限公司 Multistage pyrolysis and carbonization integrated sludge treatment method

Also Published As

Publication number Publication date
HUP2200257A1 (en) 2024-01-28

Similar Documents

Publication Publication Date Title
KR100502965B1 (en) Method for the thermal utilization of spent grain
US5194069A (en) Method and apparatus for refinement of organic material
JP6124494B1 (en) Plant biomass semi-carbide production equipment
US20010011457A1 (en) Apparatus and method for resource recovery from organic substance
JP2008519687A (en) Slurry dehydration and conversion of biosolids into renewable fuels
WO2005123885A1 (en) Method and apparatus for drying wet bio-solids using excess heat recovered from cement manufacturing process equipment
CN203265240U (en) Device for preparing fuel gas by utilizing domestic garbage and generating power by utilizing fuel gas
US20120017498A1 (en) System and Method for Obtaining Combinations of Coal and Biomass Solid Fuel Pellets with High Caloric Content
CN210176701U (en) System for municipal sludge deep reduction treatment
WO2012093982A1 (en) Pyrolysis plant for processing carbonaceous feedstock
KR101152613B1 (en) System for treating sludge or waste having a by-pass line
KR101999650B1 (en) Hybrid Sludge Fuel, Manufacturing Method and System of Fuel Production thereof
JP7268647B2 (en) Sludge-to-fuel device, sludge-to-fuel system, sludge-to-fuel factory, and sludge-to-fuel method
KR101860041B1 (en) Hybrid Sludge Fuel, Manufacturing Method and System of Fuel Production thereof
CN111718095A (en) Municipal sludge pyrolysis carbonization treatment system and treatment process
TWM608219U (en) Recycling regeneration device
WO2024009117A1 (en) Method and apparatus for carbonizing sludge with organic content
CN105371280B (en) The apparatus and method that a kind of solid waste organic substance cleaning is burned
CN115666805A (en) Waste biomass gasification treatment device and waste biomass gasification treatment method
JP2020055004A (en) Waste treatment system
CN213388279U (en) Municipal sludge pyrolysis carbonization treatment system
JP2019147881A (en) Apparatus for converting sludge into fuel, system for converting sludge into fuel, sludge fuel utilization type factory and method for producing solid fuel
RU104672U1 (en) SOLID WASTE PROCESSING PLANT
RU2408820C1 (en) Installation for multi-phase pyrolysis of organic raw material
CN105753274B (en) A kind of sludge treatment system and disposing technique

Legal Events

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

Ref document number: 23758712

Country of ref document: EP

Kind code of ref document: A1