Patent Application
20070029264
The present invention relates to a process and an apparatus for processing biological waste materials, which may be based on plant or animal waste products, to provide energy in useful forms such as electricity or hydrocarbon fuel.
The use of anaerobic digestion to produce a biogas from biological waste materials is known, but the resulting gas mixture, which primarily consists of methane and a significant proportion of carbon dioxide, has been perceived as suitable only for combustion to generate heat or electricity. For example JP 2002-336898 A (Ebara) describes a process for treating sludge from a waste water treatment, in which the sludge is treated with ultrasound and then subjected to methane fermentation, so that cells are broken down, and the decomposition rate in the fermentation stage is increased. Similarly, DE 196 15 551 A (Ingan GmbH) describes a multistage anaerobic treatment for a wide range of waste biomass materials, using ultrasound to disrupt cells, and digestion to generate methane; this may also entail warming the waste material and adjusting its pH. The present invention involves the appreciation that biogas may be used as a flexible feedstock so that energy may be provided in a variety of ways.
According to the present invention there is provided a process for treating biological waste materials, the process comprising the steps of:
Adjusting the proportion of steam to methane enables the output of the process to be adjusted according to market conditions. Thus the process preferably includes at least one of the additional steps:
It will be appreciated that the biogas may contain sulphurous compounds, and it may therefore be desirable to subject the biogas to desulphurisation before it is fed to the catalytic reformer unit.
The invention also provides apparatus for performing the said process.
The invention will now be further and more particularly described by way of example only, and with reference to the accompanying drawings in which;
Referring to
Preferably the ultrasonic transducers 14 are attached to the wall of the tube 12 in an array extending both circumferentially and longitudinally, each transducer being connected to a signal generator so that each transducer radiates no more than 3 W/cm2, the transducers being sufficiently close together and the number of transducers being sufficiently high that the power dissipation within the vessel is between 25 and 150 W/litre. The values of power given here are those of the electrical power delivered to the transducers, as this is relatively easy to determine. Such an irradiation vessel is described in WO 00/35579. It is desirable to ensure no focusing of the ultrasound occurs, and this may be achieved by energising groups of adjacent transducers in succession. Where the vessel is cylindrical it is particularly preferable to avoid energising diametrically opposite transducers at the same time. The non-focusing can also be achieved by energising adjacent transducers, or adjacent groups of transducers, at different frequencies; and in particular to vary the frequency at which each transducer or group of transducers is energized over a limited range, for example between 19.5 kHz and 20.5 kHz.
The biogas is fed to a compact catalytic reformer 20 in which it flows through a reaction channel 21 kept at an elevated temperature that may for example be 800° C. The first stage involves steam reforming, in which methane reacts with water vapour, that is to say the reaction:
H2O+CH4→CO+3 H2
This reaction is endothermic, and may be catalysed by a rhodium or platinum/rhodium catalyst in the reaction channel 21. The heat required to cause this reaction may be provided by combustion in an adjacent channel 22 of an inflammable gas such as methane or hydrogen, which is exothermic and may be catalysed by a palladium/platinum catalyst. In both cases the catalyst is preferably on a stabilised-alumina support which forms a coating typically less than 100 microns thick on a metal substrate. Both these reactions may take place at atmospheric pressure, although alternatively the reforming reaction might take place at an elevated pressure. The heat generated by the combustion would be conducted through the metal sheet separating the adjacent channels. The steam reforming reaction can be encouraged by adding steam to the biogas stream before it is supplied to the reaction channel 21.
If no steam is added the biogas will undergo the dry reforming reaction:
CO2+CH4→2 CO+2 H2
The proportion of methane that undergoes dry reforming can be enhanced by cooling the biogas stream 18 to condense and remove water vapour. Hence by adjusting the proportion of water added at the inlet to the reaction channel 21, the ratio of hydrogen to carbon monoxide in the resulting synthesis gas stream 24 can be adjusted between about 2:1 to 1:1.
On the other hand, if a larger proportion of water vapour is added then some of the carbon monoxide will undergo the water gas shift reaction, which increases the proportion of hydrogen still further:
CO+H2O→CO2+H2
One option is then to supply the synthesis gas 24 to a fuel cell 26 in which the hydrogen gas reacts indirectly with oxygen from the air to generate electricity and to produce water. In this case reformer 20 should be operated to maximise the proportion of hydrogen in the synthesis gas stream 24. For some types of fuel cell 26, for example a solid oxide cell, the hydrogen/carbon monoxide mixture may be supplied directly to the fuel cell. Alternatively the hydrogen gas may be separated from the other gases using a membrane separation unit 28, for example using a platinum or palladium membrane, or a palladium/copper membrane, so as to generate pure hydrogen gas for use in the fuel cell 26. In this case the fuel cell may be a proton exchange membrane cell. The resulting tail gas, consisting primarily of carbon monoxide, is preferably supplied to the combustion channel 22.
The other option is to subject the synthesis gas 24 to a Fischer-Tropsch synthesis to generate a longer chain hydrocarbon, that is to say a reaction of the type:
n CO+2n H2→(CH2)n+n H2O
which is an exothermic reaction, occurring at an elevated temperature, typically between 190 and 300° C., for example 210° C., and an elevated pressure typically between 2 MPa and 4 MPa, for example 2.5 MPa, in the presence of a catalyst such as cobalt, with a platinum or ruthenium promoter. In this case the synthesis gas stream 24 is compressed by a pump 30 and then supplied to a compact catalytic reactor 32, to flow through reaction channels 33 adjacent to heat exchange channels 34. The exact nature of the organic compounds formed by the reaction depends on the temperature, the pressure, the residence time and the catalyst, as well as the ratio of carbon monoxide to hydrogen. The heat given out by this synthesis reaction may be used to provide at least part of the heat required by the steam/methane reforming reaction, for example a heat transfer fluid may be used to transfer the heat from the reactor 32 and used to preheat at least one of the streams supplied to the reforming reactor 20. The preferred catalyst for the Fischer-Tropsch synthesis comprises a coating of lanthanum-stabilised gamma-alumina with about 10-40% cobalt (by weight compared to the alumina), and with a ruthenium/platinum promoter which is less than 10% the weight of the cobalt, and with a basicity promoter such as gadolinium oxide which may be less than 5% the weight of the cobalt.
The gas stream emerging from 30 Fischer-Tropsch reactor 32 will contain hydrocarbons of a range of different molecular weights, and also water vapour. These may be condensed to provide the desired high molecular weight hydrocarbons as an output stream 36. The low molecular weight tail gases (consisting primarily of hydrogen, methane and ethane) are supplied to the combustion channel 22 of the reforming reactor 20. The water that also condenses may be separated from the hydrocarbons and may be returned to the digester 16.
If the biogas stream 18 contains any sulphur-containing compounds it is preferably desulphurised before reaching the reforming reactor 20. This may involve a liquid scrubbing absorption, for example using an aqueous solution of a chelated ferric salt. This converts the ferric salt to the ferrous form; the solution can be recirculated through an air scrubber to regenerate the ferric salt and to form a precipitate of sulphur. Alternatively, it may use a desulphurisation technique that requires elevated temperatures, for example a solid state absorption process.
A benefit of subjecting the waste stream 11 to intense ultrasound is that the bio-availability of plant cellulose is increased by disrupting lignin layers, so that the rate of digestion in the digester 16 is increased and that the waste stream may contain significant proportions of woody material containing lignin. The process is particularly suited to treating wet organic materials, as no drying is required and indeed in some cases no water will need to be added. The ultrasound enhances the rate of digestion so that the retention time in the digester 16 is reduced and consequently a smaller digester 16 can be used to treat a given quantity of waste material.
It will be appreciated that both the fuel cell 26 and the digester 16 also generate heat. This heat may itself be useful, for example for community heating.
The plant 10 shown in
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/GB04/02491 | 6/15/2004 | WO | 11/22/2005 |
