WO2014111734A1 - Appareil de traitement de déchets et production de biogaz - Google Patents

Appareil de traitement de déchets et production de biogaz Download PDF

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Publication number
WO2014111734A1
WO2014111734A1 PCT/GB2014/050160 GB2014050160W WO2014111734A1 WO 2014111734 A1 WO2014111734 A1 WO 2014111734A1 GB 2014050160 W GB2014050160 W GB 2014050160W WO 2014111734 A1 WO2014111734 A1 WO 2014111734A1
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Prior art keywords
passage
processing
waste
slurry
nozzle
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PCT/GB2014/050160
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English (en)
Inventor
Ross VINTEN
Olga KOROLEVA
Martin Butler
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Pursuit Marine Drive Limited
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Publication of WO2014111734A1 publication Critical patent/WO2014111734A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/02—Means for pre-treatment of biological substances by mechanical forces; Stirring; Trituration; Comminuting
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2866—Particular arrangements for anaerobic reactors
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/06—Means for pre-treatment of biological substances by chemical means or hydrolysis
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/09—Means for pre-treatment of biological substances by enzymatic treatment
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/20—Heating; Cooling
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/10—Temperature conditions for biological treatment
    • C02F2301/106—Thermophilic treatment
    • 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
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • This disclosure relates to waste processing and biogas production from materials, especially waste sludges and slurries such as sewage, but also to processing food or agricultural derived materials which have hitherto presented difficulties in processing for recycling or disposal.
  • Waste in the form of sludges and slurries can be processed in a number of ways including settling, mechanical separating, biological, microbiological, enzymatic, chemical, and thermal process steps. Typically a number of process stages are undertaken in succession over a period of time.
  • a portion of organic matter and suspended solids is removed from wastewater in settlement tanks.
  • the heavier material sinks to the tank floor to form a thick slurry known as primary sludge, which has to be removed for treatment.
  • the composition of primary sludge varies with catchment area but it typically has an extremely offensive odour, contains a high portion of organic matter and can be readily digested.
  • Primary sludge also typically contains very high levels of pathogens.
  • the liquid element from primary treatment also requires further treatment, referred to as secondary treatment, to remove the dissolved organic content.
  • secondary treatment One method to achieve this is the activated sludge (AS) process, where the liquid element from settled sewage is mixed with a blend of bacteria (activated sludge) in the presence of oxygen to facilitate bacterial growth.
  • the bacteria remove organic material dissolved in the liquid and following sufficient treatment the activated sludge settles; some is returned to re-seed new settled sewage inflow and the excess or surplus activated sludge (SAS) is removed and treated.
  • SAS is a brown floe with an earthy odour.
  • SAS is less readily digested as it is primarily made up of cellular material and biofilms and it is therefore beneficial to pre-treat SAS prior to digestion to rupture or lyse the cells and biofilms, releasing the organic content within the cell structures. When such lysis occurs, a marked increase in downstream biogas production is evident.
  • Biogas consists mainly of methane (CH4) and carbon dioxide (CO2).
  • the majority of sewage sludge arising from wastewater treatment in the UK is treated by anaerobic digestion (AD).
  • the sewage sludge treated is a combination of primary sludge and surplus activated sludge (SAS), produced from different processes at the wastewater treatment works.
  • Anaerobic digestion micro-organisms break down biodegradable material in the absence of oxygen. Anaerobic digestion reduces the volume and mass of input material through the biological conversion of organic material, namely volatile solids (VS) into biogas. The process also produces stabilised compost rich in nutrients and suitable for use on agricultural land.
  • VS volatile solids
  • waste sludges which contain substantial amounts of organic matter can be done for a number of purposes, such as disinfection to kill potential pathogens and fouling microorganisms, leading to improvement of potential for dewatering, and improved performance as a substrate for anaerobic digestion,
  • the performance of the anaerobic digestion in fermenters is measured by the amount of biogas production and the proportion of its highly valuable compound methane.
  • the released amount of the methane depends on the initial amount of the organic matter in the sludges and on its availability for biodegradation. It has been shown that a number of treatments such as thermal, ultrasonic, mechanical, chemical or enzymatic, can assist anaerobic digestion by breaking down ultrastructure of sludge, bacterial floes and biofilms and releasing organic compounds.
  • a method of processing biodegradable waste comprising: providing at least one waste processing device, the or each device having a processing passage with a passage inlet and a passage outlet, and a nozzle circumscribing the passage and opening into the passage between the passage inlet and passage outlet; directing a flow of a biodegradable waste slurry into the processing passage; and supplying a processing fluid to the nozzle and injecting the processing fluid through the nozzle into the waste slurry within the processing passage; wherein the processing fluid is supplied to the or each device at a temperature and pressure which results in the waste slurry leaving the passage outlet with an exit temperature of 45-160°C.
  • Biodegradable waste includes waste sludges or slurries such as sewage, as well as food waste and waste derived from agriculture.
  • the processing fluid may be supplied to the or each device at a temperature and pressure which results in the waste slurry leaving the passage outlet with an exit temperature of 95-130°C.
  • the nozzle of the or each device may have a nozzle throat whose cross sectional area is less than that of both a nozzle inlet and a nozzle outlet, and wherein the processing fluid is accelerated through the nozzle throat as it is injected into the passage.
  • the method may further comprise holding the processed slurry at the exit temperature and an associated exit pressure in a retention vessel downstream of the passage outlet for a predetermined period of time.
  • the method may further comprise passing the processed slurry from the retention vessel into a decompression vessel where the pressure of the slurry is rapidly reduced and any gaseous elements are drawn off from the slurry.
  • the method may further comprise passing the processed slurry into a digester downstream of the or each device, the digester being configure to facilitate anaerobic digestion of the processed slurry.
  • the processed slurry may be passed through a forced cooling device located between the or each processing device and the digester, such that the slurry entering the digester has an entry temperature of 30-55°C.
  • the method may further comprise introducing one or more chemical additives to the slurry before, during or after processing within the processing device.
  • the or each additive may be selected from the group comprising enzymes and chemical reagents.
  • a method of producing biogas from biodegradable waste comprising: providing at least one waste processing device, the or each device having a processing passage with a passage inlet and a passage outlet, and a nozzle circumscribing the passage and opening into the passage between the passage inlet and passage outlet; directing a flow of a biodegradable waste slurry into the processing passage; and supplying a processing fluid to the nozzle and injecting the processing fluid through the nozzle into the waste slurry within the processing passage, wherein the processing fluid is supplied to the or each device at a temperature and pressure which results in the waste slurry leaving the passage outlet with an exit temperature of 45-160°C; passing the processed slurry into a digester downstream of the or each device, the digester being configure to facilitate anaerobic digestion of the processed slurry; and recovering biogas generated in the digester.
  • the processing fluid may be supplied to the or each device at a temperature and pressure which results in the waste slurry leaving the passage outlet with an exit temperature of 95-130°C.
  • the method may further comprise holding the processed slurry at the exit temperature in a retention vessel downstream of the passage outlet for a predetermined period of time prior to passing the slurry into the digester.
  • the method may further comprise passing the processed slurry from the retention vessel into a decompression zone where the pressure of the slurry is rapidly reduced and any gaseous elements are drawn off from the slurry.
  • the processed slurry may be passed through a forced cooling device located between the or each processing device and the digester, such that the slurry entering the digester has an entry temperature of 30-55°C.
  • the method may further comprise introducing one or more chemical additives to the slurry before, during or after processing within the processing device.
  • the or each additive may be selected from the group comprising enzymes and chemical reagents.
  • a waste processing apparatus comprising: at least one waste processing device, the or each device having: a processing passage with a passage inlet and a passage outlet; and a nozzle circumscribing the passage and opening into the passage between the passage inlet and passage outlet; and a retention vessel downstream of the passage outlet, the retention vessel adapted to hold a waste slurry exiting the at least one device at an exit temperature and pressure for a predetermined period of time.
  • the nozzle of the or each device may have a nozzle throat whose cross sectional area is less than that of both a nozzle inlet and a nozzle outlet.
  • the apparatus may further comprise a decompression vessel downstream of the retention vessel.
  • the apparatus may further comprise a digester.
  • the apparatus may further comprise a forced cooling device located between the retention vessel and the digester.
  • the apparatus may comprise a plurality of waste processing devices connected to one another in series.
  • the apparatus may further comprise a separate retention vessel downstream of each of the plurality of waste processing devices.
  • At least one of the waste processing devices may be located within the retention vessel of the preceding waste processing device.
  • the apparatus may further comprise an enzyme entrainment unit having a hopper adapted to hold and deliver one or more enzymes into the processing passage either upstream of, downstream of, or at the nozzle.
  • Figure 1 shows a longitudinal cross-section through a waste processing device or fluid mover
  • Figures 2a, 2b and 2c show a schematic apparatus configuration using multiple waste processing devices in a continuous process line, particularly showing in Fig. 2a the waste processing devices in the process line, showing in Fig. 2b and optional retention module, and showing in Fig. 2c units for condensate and heat recovery and output of treated material;
  • Figure 3 is a graph representing results of tests conducted to determine the effect of unit exit temperature conducted in relation to methane production over a period of days;
  • Figure 4 is a graph representing results of tests conducted to determine the effect of variations in feed dry solids (DS) content on methane gas production.
  • Figure 5 is a graph representing test results showing the change in soluble chemical oxygen demand over a range of temperatures.
  • Such a fluid mover includes a hollow body provided with a straight-through passage of substantially constant cross section with an inlet at one end of the passage and an outlet at the other end of the passage for the entry and discharge respectively of a working fluid, a nozzle substantially circumscribing and opening into said passage intermediate the inlet and outlet ends thereof, an inlet communicating with the nozzle for the introduction of a processing fluid, a mixing chamber being formed within the passage downstream of the nozzle.
  • a dispersed droplet flow regime and a supersonic shock wave may be created within the mixing chamber by the introduction and condensation of the processing fluid via the nozzle.
  • the processing fluid is preferably a condensable fluid and may be a gas or vapour, for example steam, nitrogen or carbon dioxide, which may be introduced in either a continuous or discontinuous manner.
  • the fluid mover may include a hollow body provided with a straight-through passage of substantially constant cross section having an inlet at one end of the passage and an outlet at the other end of the passage for the entry and discharge respectively of a working fluid, a steam nozzle substantially circumscribing and opening into said passage intermediate the inlet and the outlets thereof, a steam inlet communicating with the nozzle for the introduction of steam, and a mixing chamber being formed in the passage downstream of the nozzle.
  • a pseudo-vena contracta or pseudo convergent/divergent section is generated, akin to the convergent/divergent section of conventional steam ejectors but without the physical constraints associated therewith since the relevant section is formed by the effect of the steam impacting upon the material or process fluid.
  • FIG. 1 A cross-sectional view of an embodiment of the fluid mover is shown in Fig. 1 wherein a fluid mover 1 comprises a housing 2 defining a passage 3 providing an inlet 4 and an outlet 5, the passage 3 being of substantially constant circular cross section.
  • the inlet 4 is formed at the front end of a protrusion 6 extending into the housing 2 and defining exteriorly thereof a plenum 8 for the introduction of a processing fluid, the plenum 8 being provided with an inlet 10.
  • the protrusion 6 defines internally thereof part of the passage 3.
  • the distal end 12 of the protrusion 6 remote from the inlet 4 is tapered on its relatively outer surface at 14 and defines an annular nozzle 16 between it and a correspondingly tapered part 18 of the inner wall of the housing 2, the nozzle 16 being in flow communication with the plenum 8. There may be an angle of between 1 and 70 degrees between the nozzle 16 and the longitudinal axis of the fluid mover.
  • the outer surface 14 of the protrusion 6 may lie at an angle of 1 to 70 degrees relative to the longitudinal axis. Preferably, there is an angle of between 1 and 40 degrees between the nozzle 16 and the longitudinal axis. Whilst the nozzle 16 is preferably a continuous, annular nozzle about the passage 3 the nozzle 16 may alternatively be a segmented, non-continuous nozzle made up of a plurality of distinct nozzle paths spaced circumferentially about the passage 3 and angled in the same manner as the single annular nozzle. In operation the inlet 4 may be connected to a source of a material or process fluid such as water.
  • the nozzle may have a nozzle inlet, a nozzle outlet and a nozzle throat portion intermediate the nozzle inlet and nozzle outlet, the throat portion having a cross sectional area which is less than that of both the nozzle inlet and nozzle outlet.
  • the decrease and increase in the cross-sectional area of the nozzle can be linear, or may have a more complex profile.
  • One such profile might be that the stream-wise cross-section is substantially the same as that of a De Laval nozzle, which has a cross-section of an hour-glass-type shape.
  • Such a fluid mover is adopted as a waste processing device or reactor in the present disclosure.
  • multiple "fluid movers” may be used as waste processing devices arranged in series or positioned in a reticulation apparatus allowing for optional by-pass when required.
  • a modular construction using a manifold connection between multiple waste processing devices arranged in parallel allows additional banks of fluid movers to expand an installation upon demand.
  • the waste processing devices may be positioned in series in a process line with optional by-pass for each device, and with each device in fluid communication with a supply of thermal processing fluid.
  • the waste processing device provides multiple functions including heat and energy transfer to a fluid to be processed which is fed through the waste processing device, throughput of material being processed to a downstream stage, and disintegration and or dispersal of materials which may have been compacted or agglomerated in the feed material.
  • the thermal processing fluid may be steam.
  • Thermal processing may comprise thermal hydrolysis.
  • the apparatus may comprise means for introducing hydrolytic enzymes [in either liquid or powder forms) to the material to be processed in the waste processing device.
  • the apparatus may comprise at least one retention vessel for holding thermally processed material downstream of at least one waste processing device. This prolongs retention time between thermal processing in at least one waste processing device and further downstream processing of the thermally processed material.
  • multiple sequential retention vessels may be employed.
  • a "vessel" may be a dedicated tank or container, but also encompasses a tube or passage within which the processed material may be held for a predetermined retention time.
  • the apparatus may be configured such that in relation to at least one waste processing device of a series of such waste processing devices, a further waste processing device is located within a retention vessel associated with the at least one waste processing device. Successive waste processing devices respectively may be located within the retention vessel associated with a preceding waste processing device.
  • This configuration allows for example a first waste processing device to conduct a first process such as primarily temperature elevation, and to pressurise the temperature elevated material to a desired pressure, and a subsequent waste processing device housed in the retention vessel to operate from those conditions i.e. to maintain the pressure etc. when further processing the material.
  • This configuration can be employed in a successive nature so as to progressively lower the operating pressure within each subsequent processing/retention section.
  • a plurality of waste processing devices may be assembled into a modular unit using manifold connectors to connect the plurality of waste processing devices in parallel.
  • the respective modular units may be connected in series.
  • the retention vessel may be a retention tank or a length of process line pipe for example an additional loop in the process line to be used for retention of thermally processed material or optionally by-passed.
  • the apparatus may comprise a decompression vessel, or "flash tank", downstream of at least one waste processing device.
  • a flash tank allows violent decompression of the process material, for example to further aid mechanical disruption of cells.
  • Condensate recovery apparatus such as a gas scrubbers or condensers may be employed to recover gaseous material such as VFAs [volatile fatty acids) and return them to the process line downstream.
  • the apparatus may comprise a line pipe of significantly greater cross-sectional dimension than the process line pipe downstream of the waste processing device(s).
  • Other forms of pressure relief such as relief valves may be included as processing and safety aids.
  • the apparatus may comprise an enzyme entrainment unit utilising a waste processing device adapted to introduce enzymes from a hopper associated therewith to the process line.
  • This specifically-designed entrainment unit can facilitate either fluid or powder delivery to the process stream.
  • the delivery zone can either be positioned upstream of the processing nozzle, downstream of the processing nozzle or immediately adjacent the nozzle depending on the properties of the enzyme material to be entrained. Compressed air may be used to facilitate enzyme introduction via the waste processing device instead of steam when no further heating is required.
  • the apparatus may comprise a digester for receiving thermally processed material from the waste processing device(s).
  • the digester may be configured to facilitate and promote anaerobic digestion of the thermally processed material such as a parallel arrangement depending on volumetric flow.
  • the apparatus may be employed in a apparatus utilising a range of temperatures at different stages and the waste processing devices may be operated within different temperature ranges.
  • the apparatus may comprise a forced cooling device to provide for an appropriate temperature of thermally processed material into the digester.
  • the temperature may be less than 55 °C, preferably above 30 °C to be appropriate for anaerobic digestion.
  • the apparatus may be configured for continuous processing of waste.
  • the apparatus may receive a feed stream or influent of waste material for processing in a continuous manner.
  • An interrupted or semi-continuous process is also contemplated.
  • the apparatus may receive continual supplies of waste material for processing. Processed material may be removed in a similar manner.
  • the apparatus may be operated at a temperature range below 160 °C which is significantly lower than conventional commercial thermal hydrolysis processes.
  • the process fluid, or waste slurry may be heated by a waste processing device to a temperature of 45-160°C by high velocity, preferably supersonic injection of steam or an alternative processing fluid.
  • the temperature range may be 95-130 °C.
  • the heating may be achieved within seconds, typically under 20 seconds. At atmospheric pressure, the temperature may be reached in under 10 seconds typically from 1 to 4 seconds, and may be conducted in a pressurised apparatus of between 1 and 3 barg.
  • the process may be operated continuously, or semi-continuously and as an on-line "live" process associated with a material processing plant, such as a waste treatment or fluid remediation plant In this way the apparatus is integrated into an existing (retrofitted) waste treatment plant.
  • a waste processing apparatus comprises four waste processing devices installed in a process line in series with optional by-pass.
  • the units in this embodiment have 25 mm bore, but other embodiments may have units selected from units of 13 to 47 mm bore, and each unit may have the same, different, or a progressively differing bore size.
  • These units serve as reactors for a continuous processing of a material which requires thermal processing at least
  • a heat transfer fluid for thermal processing of materials and for operating the waste processing devices to achieve the desired disruptive effect on throughput materials is introduced to the waste processing devices.
  • steam is produced in a boiler and a steam line connected with the respective waste processing devices supplies steam via a steam control valve to regulate steam pressure.
  • a steam pressure of 8 barg (800 kPa) at a temperature of 175°C is used in this embodiment to provide heating of the process material up to 95 -130°C , or up to 160°C.
  • Process material in the form of a waste sludge or slurry may be introduced to a process feed line for the waste processing devices continuously from a feed vessel of sufficient capacity to prevent the feed to waste processing devices being interrupted.
  • process material in the form of sludge is collected in an intermediate bulk container (IBC] and fed into a process feed line for the units using a positive displacement pump, for example a peristaltic pump, with a flow rate appropriate for the bore of process material unit
  • the flow rate may be in the range of from about 45 to about 180 litres per minute. Considering a 13 mm bore waste processing device, a flow rate of from 45 to 80 litres per minute is appropriate.
  • the treated slurry can be collected in an outflow tank and access or sampling ports may be provided to allow samples to be taken from both the slurry upstream of the waste processing device and from the outflow tank.
  • the waste processing apparatus is provided on a mobile platform or readily moved skid units.
  • One such skid unit would include a silo with integrated live bottom hopper (i.e. equipped to dose or meter out materials from the hopper], a pump, positive displacement type, variable speed, inverter driven, capable of back-mixing and accepting dilution water and/or liquid sludge, hot condensate (from a steam flashing process step] 24 bar pressure (2.4 MPa], a waste processing device and associated steam injection valves, additional process controls including valves and instrumentation such as flow meter (for process material sludge and process diluent, solids meter, level monitoring and transmitter, contingency measures including pump protection devices including high temperature relay and over pressure transmitter.
  • a silo with integrated live bottom hopper i.e. equipped to dose or meter out materials from the hopper
  • a pump positive displacement type, variable speed, inverter driven, capable of back-mixing and accepting dilution water and/or liquid sludge
  • Another skid unit may include a steam absorption vessel, a pipe reactor, a flash tank, condensate separator, condensate recycle pump, hydrolysed sludge recirculation pump, associated valves and instrumentation, for example temperature and pressure monitoring transmitters, pressure relief valves.
  • a further skid unit may include facilities for hydrolysed sludge dilution, foul gas injection to hydrolysed sludge, heat recovery including heat exchanger means optionally replaced or supplemented with an air blast cooler, heat recovery for steam boiler feed water pre-heating, dual fuel steam boiler (fuel oil / gas (biogas, natural gas, syngas etc.), instrumentation, for example flowmeter [steam], temperature and pressure monitoring transmitters, relief valves.
  • heat exchanger means optionally replaced or supplemented with an air blast cooler
  • steam boiler feed water pre-heating dual fuel steam boiler (fuel oil / gas (biogas, natural gas, syngas etc.), instrumentation, for example flowmeter [steam], temperature and pressure monitoring transmitters, relief valves.
  • the apparatus may be used in:
  • the apparatus can also be utilised for pre- treatment of:
  • farm animal manure (such as chicken, pig, cow manure).
  • waste processing device (reactor) technology considered to be specific to the waste water industry.
  • the apparatus and methods of the present invention may be utilised for thermal pasteurisation below 100 °C via in-line processing of waste sludges at atmospheric pressure, the waste sludge is introduced to a waste processing device as described herein.
  • Introduction of a thermal processing fluid such as steam to the thermal processing fluid inlet may elevate the temperature of the waste sludge to below 95 °C.
  • a method of in-line processing of waste sludges at temperatures higher than 95 °C but lower than 130 °C for increased methane production is provided.
  • a method of in-line processing of waste sludges with enzymatic and/or chemical treatment at temperatures below 130 °C for increased methane production by introducing enzymes and/or chemical reagents by means of a waste processing device of the aforesaid type.
  • Another embodiment provides an apparatus for treating waste water sludge such as sewage sludge.
  • the apparatus includes a steam generator and steam lines to feed steam to the thermal processing fluid inlet of the waste processing device, a retention tank or vessel associated with at least one waste processing device, and a downstream digester for receiving materials processed in the waste processing devices.
  • the digester may be configured to promote and facilitate anaerobic digestion of materials received from the waste processing devices.
  • the apparatus may comprise a pump, for example a positive displacement pump for delivering sludge to the waste processing device or to facilitate discharge of processed materials.
  • a pump for example a positive displacement pump for delivering sludge to the waste processing device or to facilitate discharge of processed materials.
  • the apparatus may comprise a forced cooling device.
  • the forced cooling device may be used for regulating the temperature of materials output from the waste processing devices prior to addition of enzyme and another process step using the described apparatus, or prior to digestion in the digester.
  • Thickened SAS of 4.5 - 5.5% DS was tested under the following waste processing device running conditions: Waste processing device apparatus configuration of (a) 4 waste processing devices at standard setting without fluid retention pipe and (b) 4 waste processing devices respectively equipped with fluid retention pipe;
  • the samples were collected immediately following waste processing device treatment of the thickened SAS.
  • the samples were sent for analysis at a commercial water testing laboratory; the parameters analysed were pH, DS, VS, alkalinity, VFAs, ammonia, total chemical oxygen demand (COD) and sCOD.
  • Figure 5 is a graph representing test results showing the change in soluble chemical oxygen demand over a range of temperatures. It will be noted that a pair of results are shown for sCOD when the waste is processed using the waste processing device in its standard setting, i.e. without retention vessel, both of which are labelled "PDX_SAS" It will be appreciated that it is the (upper) PDX_SAS trace with the greater sCOD values in the figure 5 graph which reflects the sCOD results set out in table 1.
  • the presence of the retention pipe allows longer sludge retention with increasing methane yield compared to the standard settings.
  • the increase in methane yield at 95°C with the retention pipe was up to 21% compared to the control. This level of increase in biogas production would typically be considered significant.
  • Thickened SAS at approximately 7.6%, 8.2% and 14.7% DS were tested under the following waste processing device running conditions:
  • Waste processing device apparatus configuration of (a) 4 waste processing devices at standard setting without fluid retention pipe and (b) 4 waste processing devices with fluid retention pipe;
  • waste processing device pre-treatment solubilises sludge and produces a material that can be more rapidly digested.
  • the settings of the batch digester test, and in particular the ratio between the inoculum and the substrate, has large importance in the development of the gas production as the methanogenic process can be delayed due to a high organic loading, as seen for the high volumes tests.
  • tests 1 and 2 demonstrated a moderate increase in biogas production of up to 21% compared to the control at the highest temperatures.
  • the ability to replicate the results impacts the significance of this data; some variation was seen between the tests, which suggests that the performance of the waste processing device technology is influenced significantly by the inherent variability of the feedstock.
  • the data indicates improved performance when processing higher dry solids sludge. It is anticipated that the disclosed technology will process sludge with up to 15% dry solids to operate in the preferred "fluid" region of supply material.
  • the hydrolysed sludge may be at a temperature below 35 °C, before addition of the enzymes or inoculum addition (which can be done via mixing through material entraining unit reactor processing], with an exit temperature which may be below 50 °C prior to anaerobic digestion.
  • the process may employ a number of additional steps to effectively integrate into a conventional AD plant
  • water should be used efficiently and heat recycling employed via heat exchangers or other means where possible.
  • the sludge discharged from the thermal pre-treatment process should be allowed to cool using forced cooling if necessary before being fed to anaerobic digesters.
  • the heat recovered from the cooling stage may be utilised to pre-heat the incoming sludge feed to help with the overall energy balance.
  • Any gaseous emissions as a result of thermal hydrolysis, containing volatile fatty acids (VFAs), may be captured in an appropriate condenser unit and returned to the process flow on the way to anaerobic digesters.
  • VFAs volatile fatty acids
  • a pilot-scale waste processing apparatus for combined waste pre-treatment is designed to operate with either four waste processing device 13 mm bore or two waste processing device 25 m bore (reactors).
  • the waste processing device apparatus can be configured to act as an in-line continuous, or semi-continuous processing unit for waste water sludges, and macerated food or agricultural waste slurries.
  • the pilot apparatus is designed to be capable of processing a maximum of 89.4 tonnes in a 24hr continuous operation. If higher throughput capacity is required parallel banks of two or more waste processing device 25 mm bore units, can be added in series to the process line as a modular upgrade. This would double throughput capacity for each bank added. Upgrades can be done on an individual installation basis. The number and size of tanks or piping would depend on both individual specification and physical footprint restrictions.
  • the waste processing device continuous apparatus for combined waste pre-treatment apparatus may have the following maximum dimensions:
  • the height of the standard programmable logic control (PLC) box if located directly at the point of installation will increase the maximum height of this apparatus to 2.2m.
  • PLC programmable logic control
  • the waste processing device continuous apparatus for combined waste pre- treatment would be capable of processing macerated mixed food/ agricultural waste slurries passed through a 1.2mm screen with a solids maximum of 18% w/w, and waste water sludges with a solids maximum of 15% w/w.
  • Output materials may be filled into insulated tanks or held in residence tubes for a 1 hour thermal hold.
  • the apparatus may be completely automated.
  • the PLC interface may be installed in the same physical location as the apparatus.
  • the apparatus could be retro-fitted into existing transfer pipelines.
  • the apparatus may be used in a covered or sheltered installation site.
  • the apparatus comprises a process line 20 in which a number of waste processing devices 21 are installed in series (Fig. 2a).
  • the waste processing devices 21 are connected to regulated steam lines 23 such that steam may be supplied to the nozzles of each device.
  • the process line 20 Downstream of the devices 21 the process line 20 may be connected with an optional retention vessel 25 (Fig. 2b) for retaining the processed materials/waste for a predetermined amount of time.
  • the output from the process line 20 may be passed through a final stage of condensate and heat recovery employing an optional decompression vessel, or flash tank 30 (Fig. 2c).
  • the flash tank 30 includes a condensate line 32 which draws off any gaseous elements from the flash tank 30 while the waste slurry or sludge continues downstream, possibly to a digester (not shown).
  • sCOD increase % n/a 686.67 : 766.67 678.67 558.7 796
  • sCOD/DS increase % n/a 684.87 ; 789.1 714.15 598.73 850.5 861.33
  • VFA increase % n/a 222.73 i 215.15 193.94 275.76 268.18 200

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Abstract

L'invention concerne un procédé de traitement de déchets biodégradables. Le procédé comprend la fourniture d'au moins un dispositif de traitement de déchets (21), le ou chaque dispositif (21) présentant une voie de traitement (3) dotée d'une entrée (4) de voie et d'une sortie (5) de voie et une buse (16) encerclant la voie (3) et s'ouvrant dans la voie (3) entre l'entrée (4) de voie et la sortie (5) de voie. Le procédé comprend en outre l'orientation d'un flux d'une suspension de déchets biodégradables dans la voie de traitement (3) et l'alimentation de la buse (16) en fluide de traitement et l'injection du fluide de traitement au travers de la buse (16) dans la suspension de déchets se trouvant dans la voie de traitement (3). Le ou chaque dispositif (21) est alimenté en fluide de traitement à une température et une pression qui résultent en ce que la suspension de déchets quitte la sortie (5) de voie à une température de sortie de 45-160°C. Un procédé de production de biogaz à partir de déchets biodégradables et un appareil de traitement de déchets sont également décrits.
PCT/GB2014/050160 2013-01-21 2014-01-21 Appareil de traitement de déchets et production de biogaz WO2014111734A1 (fr)

Applications Claiming Priority (2)

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GB1301045.9 2013-01-21
GB201301045A GB201301045D0 (en) 2013-01-21 2013-01-21 Waste Processing Apparatus and Biogas Production

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004033920A1 (fr) 2002-10-11 2004-04-22 Pursuit Dynamics Plc Pompe a jet
US20090240088A1 (en) * 2007-05-02 2009-09-24 Marcus Brian Mayhall Fenton Biomass treatment process and system
US20120270275A1 (en) * 2004-07-29 2012-10-25 Marcus Brian Mayhall Fenton Systems and methods for treating biomass and calculating ethanol yield
WO2012175999A1 (fr) * 2011-06-22 2012-12-27 Pdx Technologies Ag Appareil et procédé de traitement de micro-organismes

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004033920A1 (fr) 2002-10-11 2004-04-22 Pursuit Dynamics Plc Pompe a jet
US7111975B2 (en) 2002-10-11 2006-09-26 Pursuit Dynamics Plc Apparatus and methods for moving a working fluid by contact with a transport fluid
US20120270275A1 (en) * 2004-07-29 2012-10-25 Marcus Brian Mayhall Fenton Systems and methods for treating biomass and calculating ethanol yield
US20090240088A1 (en) * 2007-05-02 2009-09-24 Marcus Brian Mayhall Fenton Biomass treatment process and system
WO2012175999A1 (fr) * 2011-06-22 2012-12-27 Pdx Technologies Ag Appareil et procédé de traitement de micro-organismes

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