Patent Application
20140090268
The present invention relates to a drying device suitable for drying a pumbable mixture. The drying device is more particularly suitable for drying manure and/or a digestate and/or an industrial effluent.
Diverse dryers are known in practice. Some of these dryers use horizontal transport of the mixture for drying, wherein dry air is blown over a mixture. Others of these known dryers use a substantially vertically provided conveyor belt or rollers with which the mixture is picked up, exposed to drying air and subsequently scraped from the belt or roller for further transport.
Such dryers known in practice have a number of drawbacks, including the relatively large amount of energy required for the drying process and in addition the inability to cope with relatively great variations occurring in many of the mixtures for drying. Such variations, for instance in mixtures comprising manure, are inherent to the natural origin of the mixtures.
The present invention has for its object to provide an improved drying device with which the above stated problems can be wholly or partially resolved.
The present invention provides for this purpose a drying device for drying a pumpable mixture, wherein the device comprises:
The mixture for drying is for instance slurry or digestate. The mixture can for instance also be an industrial effluent.
Providing a supply holder in which the mixture can be held enables a quantity of the mixture for drying to be introduced into the supply holder. A batchwise or non-continuous drying is hereby made possible in addition to a continuous drying. It is hereby possible to compensate for variations in the incoming mixture in relatively simple manner by returning the partially dried product to the supply holder. Only discharging the mixture after a fixed time period, and/or at a specifically obtained dry substance content of the mixture, achieves that incoming variations are reduced or wholly obviated.
In a currently preferred embodiment the carrier carries a part of the mixture out of the supply holder and exposes this entrained mixture to drying medium. The mixture is then returned to the supply holder.
By providing heating means in the supply holder the mixture can be heated in the drying device. Alternatively or additionally, heating means can be provided for the ingoing mixture, for instance by making use of a heat exchanger upstream of the inlet of the supply holder. Use can optionally be made here of an additional heating loop wherein mixture from the supply holder is pumped over a heat exchanger in order to be heated. Providing heating means has the surprising advantage that drying is improved by keeping warm and/or heating the mixture in the supply holder. This can be realized in that the energy necessary for the evaporation is available from the mixture and the energy in the drying air can likewise be utilized in effective manner. In the case of drying a manure the temperature of the mixture in the supply holder is perfectly held at about 40-70° C. It has been found that the most effective and efficient drying of the mixture is realized at this temperature. Such a heating is for instance realized by arranging in the supply holder a spiral through which hot water can flow.
In a currently preferred embodiment the drying device according to the invention is provided with a carrier embodied as a drivable endless carrier belt extending substantially in vertical direction. A lower outer end of such a carrier belt is preferably situated in the supply holder filled with the mixture. The carrier belt will hereby carry a part of the mixture upward, wherein the mixture is exposed to drying air as it is carried upward. The carrier belt is preferably provided for this purpose with links such that the mixture is entrained and carried upward.
In an advantageous preferred embodiment according to the present invention the drying device comprises an energy supply system for supplying energy to the drying medium and the heating means.
The drying medium, in particular drying air, is preheated by the energy supply system, energy preferably being supplied in the form of heat. Owing to this preheating more water is evaporated out of the mixture on the carrier. The energy supply system according to the invention preferably also supplies heat to the heating means in the supply holder. Heat is hereby supplied to the mixture present in the supply holder and not located on, at or in the carrier.
Surprisingly, it has been found that the additional supply of heat to the mixture in the supply holder results in a more effective drying. This is caused by the additionally supplied heat being wholly usable for the evaporation process.
The available energy, in particular available heat, is preferably distributed over the drying medium and the heating means by an energy distributor. If the available energy is available in the form of hot water from for instance a combined heat and power (CHP) unit, the available hot water can be distributed with a distributing valve over a heat exchanger intended for the purpose of heating the drying air and over the heating means in the supply holder. The distribution is preferably adapted to the process conditions, including for instance air temperature and air humidity. It has been found that supplying about 30-40% of the available energy to the heating means, and using 60-70% to heat the drying air results in the most effective drying during use. The available energy can originate here from a single process or from different sources.
The carrier, preferably embodied as the described carrier belt, or alternatively as a blade wheel in another embodiment, is also provided in a currently preferred embodiment with openings such that drying medium, in particular drying air, can be carried through these openings. The medium flows here substantially perpendicularly through the carrier, preferably the carrier belt. This has the result that the drying air moves in a direction substantially perpendicularly of the plane formed by the carrier/carrier belt. This means that the drying air is carried through the carrier (conveyor) belt, and thereby through the mixture, instead of being carried over the mixture. The contact between the mixture and the drying air is hereby greatly increased and drying can take place in more effective manner. The air transport is for instance realized by blowing and/or suctioning air through the carrier belt. An effective process for concentrating the mixture is in this way realized.
In the case it is applied to manure, the device according to the present invention brings about a preferably batchwise concentration of manure which is performed in an effective and efficient manner, wearing variations in the incoming moisture content or dry substance content are also compensated relatively easily.
In an advantageous preferred embodiment according to the present invention the drying device comprises ventilation means for realizing underpressure on the inner side of the carrier belt.
An effective drying is realized by providing ventilation means embodied such that air from the outer side of the carrier belt is carried to the inner side by realizing an underpressure. Relatively dry air from the area surrounding the drying device is hereby drawn in and carried through the mixture in the opening in the carrier belt, after which the relatively moist air is discharged. This further simplifies evaporation and limits energy consumption.
In an advantageous preferred embodiment according to the present invention the supply holder is provided with a first compartment for the mixture and a second compartment for the heating means.
Providing the heating means separately of the mixture achieves that the heating means remain clean. This has the result that the transfer of energy in the form of heat from the heating means to the mixture is not impeded by for instance encrusted mixture. This further results in cleaning of the heating means being relatively simple. In a currently preferred embodiment the supply holder is provided with two compartments one above the other separated by a floor or separating wall. The upper compartment contains the mixture and the lower compartment contains the heating means, preferably making use of hot water. An agitating element and/or a pump is preferably provided here in the lower compartment for the purpose of distributing the heat in this compartment and providing for the best possible heat transfer from the second compartment to the first compartment with the mixture.
In an advantageous preferred embodiment the carrier belt is connected at a first outer end to a drive roller, with a second outer end being provided loosely in the supply holder during use.
Owing to the use of drive rollers a carrier belt can be moved relative to the supply holder. In this embodiment the second outer end is provided loosely in the supply holder. This has the result that a separate travelling roller or drive roller need be provided at the bottom. It has been found that a controlled movement of the carrier belt through the mixture of the supply holder can hereby nevertheless be realized. Surprisingly, it has further been found that a quantity of mixture can in this way be carried along even more effectively by the carrier belt. An additional mixing also occurs in the supply holder, since the carrier belt does not move continuously through the mixture in the same manner. This additional mixing further enhances entraining of the mixture. This increases the effectiveness.
An additional advantage of providing a second outer end loosely in the supply holder is that fewer components are therefore necessary. This results in a simpler device at lower cost, with less maintenance and less cleaning since fewer components are hereby present in the mixture.
In an advantageous preferred embodiment according to the present invention more than one carrier belt is provided and the drive rollers can be driven groupwise by a drive.
Providing a plurality of carrier belts achieves that a carrier belt is suspended as a kind of loop in the device, wherein one outer end is driven and the other outer end is preferably suspended loosely in the supply holder. A number of loops of carrier belts placed adjacently of each other in the device are preferably driven by a single drive. This has the result that the number of drives can remain limited. In a possible embodiment about 10-20 carrier belts are provided in a supply holder with a running length of 3 to 6 metres. The option of driving a group of carrier belts is further improved in that it is possible to dispense with a scraper, since the drying device is preferably used for the concentrating process carried out in batchwise manner.
In a further advantageous preferred embodiment according to the present invention the drying device further comprises one or more sprayers for wetting the carrier belt.
Providing the device with one or more sprayers, which are preferably provided in the immediate vicinity of the side edges of the carrier belt, achieves that particularly the side edges of the carrier belt can be cleaned, preferably periodically. Caking on these side edges is hereby countered and the effective drying surface area is retained.
In a further advantageous preferred embodiment according to the present invention the drying device further comprises a belt dryer operatively connected to the supply holder.
By combining the drying device, having a substantially vertically moving carrier belt with which a concentrating process is carried out, with a horizontal belt dryer the mixture is further dried following the preferably batchwise concentration. A further drying can be realized in effective manner by applying such an additional belt dryer. This belt dryer is preferably positioned horizontally here, and the drying air is carried over the mixture. Such a horizontal belt dryer is per se known.
The combination of such a horizontally disposed belt dryer and the substantially vertically disposed concentrator makes it possible to provide further ventilation means for carrying drying medium over the drying belt and through the carrier belt. By first conditioning and carrying the same drying medium, for instance in the form of drying air, over the substantially horizontally disposed drying belt and subsequently guiding it through the carrier belt of the concentrator, preferably by suctioning as described above, the conditioned drying air is utilized in effective manner. The overall drying is hereby carried out more effectively.
In an application of the drying device according to the invention in the drying of manure, a mixture is carried into the supply holder for the concentrating process and there concentrated or dried to a dry substance content of preferably about 16% ds. The mixture is then transferred to the substantially horizontally disposed belt dryer and further dried to a dry substance percentage of about 70-90%. The mixture from the concentrating process can in this way still be transported in effective manner, for instance using a pump, to the belt dryer and, after the process on the belt dryer, can then be transferred, for instance with a pneumatic transport, for the purpose of further transport, processing or storage.
A distributor is preferably provided at the belt for the purpose of placing a so-called thin fraction on the belt. A larger amount of moisture can effectively be removed from the mixture in this way and a further drying realized. In a currently preferred embodiment such a distributor is embodied as a so-called disc distributor.
The invention also relates to a method for drying a mixture, comprising of providing a drying device as described above, supplying and discharging the mixture and drying mixture.
Such a method provides the same effects and advantages as described for the drying device. Use is preferably made here of the distribution of available energy, in particular the distribution of available heat. This available energy or heat is in practice often available from other process steps or other processes, so that the drying can be performed in energy-efficient manner. In a first drying step a mixture is preferably also dried batchwise with the carrier belt. This first drying step does in fact come down to concentration of the mixture. The temperature of the mixture in the first drying step in the supply holder is preferably about 30-70° C., more preferably 35-50° C. and most preferably about 40° C. This is realized by preferably providing heating means in the supply holder. The dry substance content of the mixture following the first drying step preferably amounts to about 8-16% and more preferably about 14%. The mixture can hereby still be pumped after the first drying step. Following the first drying step the mixture is preferably also further dried in a second drying step with a belt dryer. Following the second drying step the dry substance content of the mixture preferably amounts to about 70-90%.
In a currently preferred embodiment a pressing of the mixture is performed between the first and second drying steps. Such a pressing is for instance realized by using a screw press or a centrifuge in the transport conduit between the supply holder with the substantially vertically disposed carrier belt and the substantially horizontally disposed drying belt. The pressed part of the mixture, i.e. the part with the highest dry substance content, is preferably carried to the horizontal drying belt for the second drying step, and the wet part of the mixture is fed back to the supply holder in order to be further concentrated once again. Alternatively or additionally, a part of the mixture dried in the second drying step can be mixed, optionally with an additional mixer, with for instance digestate and/or the mixture dried in the first drying step, and subsequently fed back to the horizontal belt dryer. The supplied mixture is thus dealt with in effective manner in the above stated ways and residual flows are limited.
Further advantages, features and details of the invention are elucidated on the basis of preferred embodiments thereof, wherein reference is made to the accompanying drawings, in which:
A farm building 2 (
Situated on the other side of belt dryer 10 in the shown embodiment are two concentrators 26. Concentrators 26 comprise a supply holder 28 with a number of carrier belts 30 arranged as loops. A number of fans 32 are provided at the top of farm building 2. Farm building 2 is further provided with a buffer 34, a screw press 36 and a central control 38.
The air drawn in via inlet 4 (
Energy E (
Concentrator 26 (
The lower outer end 56 of belt 30 is situated as a free loop in mixture M during use. In the shown embodiment holder 28 is provided with a first compartment 58 for mixture M and a second compartment 60 for heating medium, for instance hot water. The water is heated for instance using a heating spiral through which hot water flows. A small agitating gear (not shown) is preferably provided in second compartment 60 for optimum mixing of hot water. Compartments 58, 60 are separated by separating floor 62.
In an experiment the drying device according to the invention in the form of a concentrator was compared to a conventional device in respect of drying performance and energy consumption.
Air preheated by radiators using hot water, usually of about 80 to 90° C., coming from cooling water of motors of CHP units and/or the exhaust gases of CHP units, or even normal warm outside air is blown into a conventional concentrator with vertical drying belts. In order to bring the water in the slurry in the concentrator from for instance 7% ds to for instance 14% ds, wherein 50% of the liquid (water) is therefore evaporated, a considerable quantity of warm dry air is necessary.
Use is made in the experiment of a CHP unit with an electrical power of 1,000 kW and hot water which, as a result of the cooling of the CHP unit and of the exhaust gases, likewise has a thermal power of about 1,000 kW (or 1,000 kWh/h). The hot water going to the radiator then has a heat content or heat capacity of 1,000 kWh/h. About 50,000 to 100,000 m3 of air per hour can hereby be brought to 70° C. (in the summer at high outdoor temperatures about 100,000 m3 air/hour and in the winter at low outdoor temperatures about 50,000 m3 air/hour). In the present concentrator about 5 grams of water is evaporated per cubic metre of drying air passing through the concentrator with a humidity of 5-10%, wherein the outgoing drying air has a moisture content of 30-70%. With large quantities, and so at greater air speeds, and therefore short contact time with the digestate or the slurry on the drying belts of the concentrator, this is more like 30 to 40%; or, about 0.5 kg water is in practice evaporated per kWh heat. Under the most ideal conditions, at low airspeeds and so in the winter with relatively few cubic metres of air, a slightly higher evaporation can barely be realized.
It has further been found that following a period of concentration in the conventional concentrator the air humidity usually falls to 30% to 50% because the slurry or the digestate cools very quickly in the concentrator, in the case of digestate from for instance 40° C. to 10° C. This is because heat is extracted from the medium (e.g. digestate) due to the evaporation.
It can be stated in conclusion that, if in a conventional concentrator an average of 0.6 litre to 0.7 litre water is evaporated per kWh heat with the concentrator alone, this is a reasonable result.
With the concentrator according to the invention the available heat is distributed over the radiators through which the air passes, which air is heated, and for the purpose of heating the digestate in the supply holder of the concentrator with the heating means.
Due to the heating of the digestate in the supply holder in the concentrator using heating spirals in the concentrator or in a tray with water under the supply holder of the concentrator the digestate remains at a more or less constant temperature, for instance at about 25 to 40° C. during the whole drying process. For instance 400 to 300 kWh/h thermal heat then goes to the concentrator and 600 to 700 kWh/h to the radiators (and so to the drying air).
The result is that in this way the air humidity of the air downstream of the concentrator is usually about 80% to 100% and that an evaporation of 1 litre of water per kWh heat is achievable. The overall evaporation efficiency of the concentrator according to the invention is hereby considerably better than the further comparable conventional concentrator.
The installation 64 (
The present invention is by no means limited to the above described embodiments thereof. The rights sought are defined by the following claims, within the scope of which many modifications can be envisaged.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2006610 | Apr 2011 | NL | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/NL12/00027 | 4/16/2012 | WO | 00 | 12/20/2013 |
