EP2894212A1 - Verfahren und ausrüstung zur vorverarbeitung von organischer materie - Google Patents

Verfahren und ausrüstung zur vorverarbeitung von organischer materie Download PDF

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Publication number
EP2894212A1
EP2894212A1 EP13198283.7A EP13198283A EP2894212A1 EP 2894212 A1 EP2894212 A1 EP 2894212A1 EP 13198283 A EP13198283 A EP 13198283A EP 2894212 A1 EP2894212 A1 EP 2894212A1
Authority
EP
European Patent Office
Prior art keywords
hydrolysis reactor
pressure hydrolysis
pressure
organic matter
matter
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP13198283.7A
Other languages
English (en)
French (fr)
Inventor
Arto Lehtonen
Mika Ruusunen
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Biometa Finland Oy
Original Assignee
Biometa Finland 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 Biometa Finland Oy filed Critical Biometa Finland Oy
Priority to EP13198283.7A priority Critical patent/EP2894212A1/de
Publication of EP2894212A1 publication Critical patent/EP2894212A1/de
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C1/00—Pretreatment of the finely-divided materials before digesting
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C3/00—Pulping cellulose-containing materials

Definitions

  • the invention relates to preprocessing organic matter, such as liquid manure, particularly to thermal pressure hydrolysis of organic matter.
  • An object of the invention is thus to provide a method and equipment implementing the method so as to enable the aforementioned problems to be solved.
  • the object of the invention is achieved by a method and equipment which are characterized by what is stated in the independent claims. Preferred embodiments of the invention are disclosed in the dependent claims.
  • An advantage of the method and equipment according to the invention is efficient preprocessing of organic matter, which is based on a variable-volume pressure hydrolysis reactor and enables the organic matter to be in a form appropriate for possible further phases, such as biogas production, enabling for instance gas generation of biogas production to be made more efficient and an increase in the heat value of biogas to be made more efficient.
  • the invention enables the number of pumps to be reduced, which, in turn, reduces investment and service costs, and malfunction.
  • the equipment and method may be considered to relate to hydrolysis but, when viewed more broadly, pre-hydrolysis fractionation and/or post-hydrolysis pressure disintegration may also be involved.
  • a hydrolysis reactor R reference is made to Figures 2 to 6
  • a fractionator reference is made to Figures 1a, 1b , 2 to 3 , and 7 to 8 . Both, i.e. the hydrolysis reactor R and the fractionator D, are shown in Figures 2 to 3 .
  • An application of the invention is equipment for preprocessing organic matter, such as slurry, comprising a pressure hydrolysis reactor R and means for heating it HD.
  • the pressure hydrolysis reactor has an inlet IN for slurry, and an outlet OUT for processed slurry.
  • the pressure hydrolysis reactor R is provided with a movable piston P or another volume-change means P which is moved hydraulically by changing the inner hydraulic pressure of a pressurizing cylinder PC on the side of a rear surface of the piston P. Consequently, a variable-volume thermal pressure hydrolysis reactor R is achieved.
  • the piston P i.e. the volume-change means P, of the hydrolysis reactor R moves from left to right when the pressure of the reactor R is to be increased, and back to the left when the pressure of the reactor is to be decreased.
  • a rod of the piston P is indicated by designation PR, and in Figure 6 the piston rod PR lies retracted into its left extreme position, so the piston P is also in the left extreme position, i.e. the volume of the reactor R is then at its largest.
  • the piston P of the reactor R is substantially a solid piece.
  • the piston P is extendable in a longitudinal direction of the reactor, i.e. in a direction of travel of the piston P, since in such a case the piston forms a long thermal protection which prevents seals of the pressurizing cylinder PC from being damaged by the heat of the interior, i.e. a slurry chamber, of the reactor R.
  • the range of the piston P is greater than the length of travel of the piston P into the vacant interior of the reactor R; the length of travel of the piston P is for instance about half the length of the interior of the reactor R.
  • designation TSE refers to a temperature sensor for measuring temperature from the reactor R.
  • the equipment is based on batch production rather than on continuous production.
  • the volume of the hydrolysis reactor R is very small, e.g. 10 dm 3 , i.e. 10 litres, which is an appropriate size category for a single farm.
  • the reactor R is made of steel, and the piston R is a cast metal piece, for instance.
  • the means HD for heating the pressure hydrolysis reactor R comprise a heatable sheath of the pressure hydrolysis reactor R, i.e. the heating is indirect, heating the reactor R from outside the reactor chamber, rather than direct, in which case heating would be applied to the organic mass undergoing hydrolysis in the reactor R.
  • the equipment prior to the pressure hydrolysis reactor R the equipment comprises a fractionator D for dividing the slurry into liquid and residual slurry, which has a higher total solids content.
  • the fractionator D is connected to the inlet IN of the pressure hydrolysis reactor R in order to convey the residual slurry from the fractionator D to the pressure hydrolysis reactor R.
  • the fractionator D is not in direct immediate connection with the inlet of the pressure hydrolysis reactor R but, between the fractionator D and the pressure hydrolysis reactor R, a heat exchanger HEX is provided to serve as a preheater of the residual slurry.
  • the heat exchanger HEX is arranged to receive already processed residual slurry matter to be removed from the pressure hydrolysis reactor R.
  • a channel CH is provided between the outlet OUT of the pressure hydrolysis reactor R and the heat exchanger HEX in order to move the hydrolysis-processed mass to the heat exchanger HEX in order for the warm mass coming from the pressure hydrolysis reactor R to be able to release its heat to the mass entering the pressure hydrolysis reactor R, i.e. the residual slurry received from the fractionator D.
  • the hydrolysis reactor R is pressurized to a pressure of e.g. 160 bar by the volume-change piston P in the hydrolysis reactor R, and heated to a temperature of e.g. 160°C for 20 minutes, for instance.
  • an appropriate pressure range is between 20 bar and 165 bar, the temperature being at least 140 degrees Celsius, for at least 15 minutes.
  • the temperature is sufficiently high for the matter being processed to become hygienized.
  • the equipment comprises a removal means REM, such as a hydraulic cylinder, for moving the processed mass via the outlet OUT out of the reactor R; the removal means REM, such as an exhaust cylinder, thus moves the mass to the channel CH towards the heat exchanger HEX.
  • a removal means REM such as a hydraulic cylinder
  • the solid particles of manure or another slurry soften and their cellular structure breaks down through pressure and temperature.
  • a mixer MX is provided for mixing the slurry contained in the pressure hydrolysis reactor.
  • the mixer MX keeps the quality of the mass uniform, particularly in terms of temperature. Consequently, the time taken by the components of the slurry to biodegrade becomes shorter in anaerobic, i.e. oxygen-free, digestion.
  • the equipment prior to the fractionator D the equipment comprises a comminuting device CR for reducing the particle size of the slurry.
  • the comminuting device is a mechanical crusher, for instance.
  • the fractionator D comprises a press/pressurization piston DP generating pressurization in a fractionating chamber DCH and arranged to press the slurry against a screen filter F comprised by the fractionator D in order to separate liquid from the slurry, and thus to produce residual slurry having a higher total solids content for the pressure hydrolysis reactor R.
  • the inlet comprised by the fractionator D for the slurry is designated by DIN, and the outlet (for residual slurry) is designated by DOUT, which are controlled by valves DVIN and DVOUT.
  • the separation, i.e. fractionation, of manure or some such slurry into liquid and more solid matter is carried out by a fractionator D.
  • the slurry is pressed by means of pressure.
  • the pressurized liquid manure is pressed against a tight filter F.
  • liquid matter is separated into a fraction of its own to be processed, while the drier component, i.e. residual slurry, is moved from the fractionator D to the hydrolysis reactor R, in an embodiment via a heat exchanger HEX.
  • the equipment comprises a pressure disintegrator PD which is connected to the pressure hydrolysis reactor R and by means of which the slurry to be released from the pressure hydrolysis reactor R is with the pressure released from the pressure hydrolysis reactor R directed against a counterpart CP.
  • the exhaust cylinder REM is used for pressurizing the pipe system via the heat exchanger HEX to a quick-closing valve VPD of the pressure disintegrator PD, the rest of the solid particles being comminuted by the pressure disintegrator PD by means of pressure change and by impacting the slurry stream on the counterpart CP.
  • the solid matter of the slurry, i.e. residual slurry, received from the fractionator D and preheated by the heat exchanger HEX is conveyed through a supply valve V1 to the hydrolysis reactor R; in this connection, the pressurizing piston P, i.e. the volume-change means P, and the mixer MX of the reactor R retract simultaneously.
  • the hydrolysis reactor R is pressurized by the pressurizing piston P, i.e. the volume-change means P, of the pressurizing cylinder PC.
  • the heatable sheath of the reactor R heats the concentrated residual slurry to a temperature of 160°C for 20 minutes, the internal pressure of the reactor being 160 bar.
  • the means HD used for heating may be for instance electric resistances or, in a double-walled sheath, hot oil.
  • the processed residual slurry is conveyed to the exhaust cylinder REM by means of the pressurizing cylinder PC and the mixer MX, such as a mixing cylinder MX.
  • the removal means REM such as the exhaust cylinder REM, moves the processed residual slurry to the channel CH towards the heat exchanger HEX.
  • the cycle of the aforementioned type represents one operating cycle of the hydrolysis reactor R. Similar cycles are rerun.
  • pressure disintegrator is carried out.
  • the slurry mass is impacted with pressure on a fixed counterpart CP so that the organic matter processed in the hydrolysis reactor R is crushed into smaller pieces.
  • valves VIN and VOUT are ball valves controlled by a control unit CNTRL of the equipment.
  • the valve control may be pneumatic or electrical.
  • the method thus comprises using the thermal pressure hydrolysis for breaking down the cellular structure of organic matter.
  • the pressure hydrolysis reactor R is pressurized by the piston P or another volume-change means of the pressure hydrolysis reactor in order to subject the organic matter to a hydrolysis pressure effect.
  • the pressure hydrolysis reactor R is heated in order to subject the organic matter to a hydrolysis heat effect.
  • the purpose of the fractionator D is to separate liquid from the slurry in order for the mass to be moved to the hydrolysis reactor R to have a sufficiently high total solids TS content, in an embodiment at least 35%.
  • Slurry that has been mechanically comminuted by a crusher CR is moved by pumping to a fractionator D through a slurry supply valve DVIN.
  • a feed and transfer cylinder DREM and a press/pressurizing cylinder DPC of the fractionator retract into their extreme position and, by means of underpressure thus generated, enhance the filling up of the fractionator D with slurry.
  • the piston of the press cylinder DPC is indicated by designation DP.
  • the feed and transfer cylinder DREM is pushed next to the press/pressurizing cylinder DPC, partly pressurizing the slurry already. In such a case, some liquid already becomes released from the slurry through a liquid removal sieve or filter F.
  • the press cylinder DPC pushes the rest of the liquid being separated through the filter F as a flow LF, and thus a felt-like press-dried residue is formed inside the fractionator D from the solids.
  • designation DP3 shows the piston in its lower position, whereto it has been moved towards the filter F.
  • An outlet valve DVOUT is opened.
  • the feed and transfer cylinder DREM serving as a transfer cylinder, pushes the dried residue, i.e. residual matter, through the outlet valve DVOUT to the heat exchanger HEX, returning to an inlet valve DVIN.
  • the outlet valve DVOUT is closed.
  • the fractionator D has completed one operating cycle, starting its operation over again from the beginning.
  • the condensed residue i.e. residual slurry
  • the condensed residue is moved via the heat exchanger HEX to the hydrolysis reactor R.
  • a liquid fraction separated from the slurry in the fractionator D is conveyed to a collector tank.
  • a return motion of the press cylinder DPC i.e. the motion receding from the sieve F
  • Three locking positions are provided for the piston DP of the press cylinder DPC, i.e. an upper position indicated by designation DP, an intermediate position in the middle, wherein the piston DP yields to the motion of the piston of the feed and transfer cylinder DREM by means of which the piston of the feed and transfer cylinder moves the residual matter forward, the third position being a lower position indicated by designation DP3 when the piston has pressed the liquid through the sieve F.
  • the shape of the tip of the piston DP is hemispherical or has the shape of a cut-off of its calotte or vertex; this enables a uniform pressing to be achieved.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
EP13198283.7A 2013-12-19 2013-12-19 Verfahren und ausrüstung zur vorverarbeitung von organischer materie Withdrawn EP2894212A1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP13198283.7A EP2894212A1 (de) 2013-12-19 2013-12-19 Verfahren und ausrüstung zur vorverarbeitung von organischer materie

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP13198283.7A EP2894212A1 (de) 2013-12-19 2013-12-19 Verfahren und ausrüstung zur vorverarbeitung von organischer materie

Publications (1)

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EP2894212A1 true EP2894212A1 (de) 2015-07-15

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EP13198283.7A Withdrawn EP2894212A1 (de) 2013-12-19 2013-12-19 Verfahren und ausrüstung zur vorverarbeitung von organischer materie

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4468256A (en) * 1980-12-23 1984-08-28 Werner & Pfleiderer Process for the hydrolysis of cellulose from vegetable raw materials to glucose and apparatus for performing the process
WO1998014270A1 (en) * 1996-09-30 1998-04-09 Midwest Research Institute Hydrolysis and fractionation of lignocellulosic biomass
US20100116267A1 (en) * 2008-11-10 2010-05-13 Andritz Inc. Apparatus and method for treating, pressing and washing biomass
WO2013152771A1 (en) * 2012-04-11 2013-10-17 C.F. Nielsen A/S Method for processing a biomass containing lignocellulose

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4468256A (en) * 1980-12-23 1984-08-28 Werner & Pfleiderer Process for the hydrolysis of cellulose from vegetable raw materials to glucose and apparatus for performing the process
WO1998014270A1 (en) * 1996-09-30 1998-04-09 Midwest Research Institute Hydrolysis and fractionation of lignocellulosic biomass
US20100116267A1 (en) * 2008-11-10 2010-05-13 Andritz Inc. Apparatus and method for treating, pressing and washing biomass
WO2013152771A1 (en) * 2012-04-11 2013-10-17 C.F. Nielsen A/S Method for processing a biomass containing lignocellulose

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