Spiral Vibration Cooler for Continual Cooling of Biomass Pellets

: Cooling is an important process during the production of pellets (as post-treatment). The pellet cooling process signiﬁcantly impacts the quality of the pellets produced and the systematic use of energy. However, the cooling systems currently in use sometimes encounter technical problems, such as clogging of the perforated grids (sieves), the discharge hopper, or pellet degradation may occur. Therefore, a prototype of a new pellet cooling system using a vibrating feeder was tested. The aim of the study is to present a new variation of pellet cooling system using spiral vibration cooler as a possible solution next to a counterﬂow cooler. The presented system was tested (critically evaluated and discussed) in two design variants. The ﬁrst variant consists in cooling by chaotic movement of the pellets. The second is then in combination with the chaotic movement of the pellets together with the action of intense air ﬂow using specially placed air hoses. All tests involved pelletization of rapeseed straw. It was found that both cooling system variants could, realistically, be used. However, the variant with an intense air ﬂow was more energy-intensive, a factor which is, however, offset by the higher quality of the pellets. No negative impact of vibrations to pellets quality was occur. Studies provide insight into new usable technologies that do not reduce the efﬁciency of the process as a result of grate clogging.


Introduction
The entire technological process of pellet production consists of several consecutive, energy-intensive sub-operations (see Figure 1). The process of producing pellets from energetic plant species begins with the storage of raw material in the form of pressed bales of straw from, for example, oilseed rape (Brassica Napus), dogwood (Agrostis Gigantea), reed fescue (Festuca Arundinacea) and others. During storage, the raw material may contain large amounts of moisture [1]. The presence of moisture affects the densification of biomass. It allows the formation of interparticle bonds, lowers the glassification temperature of lignin, starch and gluten, affects the cooling phase and, last but not least, the calorific value of the final products [2][3][4]. This is followed by drying as the first pre-treatment process [5,6]. This step can be omitted in the event of suitable moisture content of the input energy plants and biomass waste (below 15%) [7]. This is followed by crushing to an optimal particle size distribution [8][9][10]. It is also important to check the moisture content of the material before it is entering the pelletizing press. It is necessary to identify the optimal moisture content for each alternative material. Several research papers have addressed this issue [4,11,12]. Once the necessary processing operations of the raw material have been performed, the pelletization process itself takes place in pelletizing presses [13][14][15][16][17]. During the pressing of the pellets, the temperature in the pressing matrix increases and can exceed 100 • C. The temperature of the pellets at the outlet of the pelletizing press can reach about 90 • C. After passing through the matrices, the hot pellets are very brittle and must be cooled to between 30 and 40 • C in a relatively short period of time at an ambient temperature approaching room temperature of 20 • C. Their moisture content and latent heat are reduced, which is a condition for making their further storage for a sufficient time possible. The risk of mold and bacteria growth increases with moisture content. The amount of water and heat released from the pellets is a function of the air flow during cooling, the mechanical and physical properties of the raw materials and the cooled pellets themselves [2]. During cooling, so-called maturation (pellet maturation) occurs, when the strength and hardness of the pellets, due to recrystallization of soluble components, increases with decreasing temperature [18]. An accompanying phenomenon is also the so-called elastic spring back [13]. As the temperature of some components of the material decreases, the viscosity increases; this has a positive effect on the structural integrity of the pellets [3]. Pellet degradation effects must be prevented during the cooling process, and a continuous flow of a considerable amount of material must be ensured.
In practice, the most commonly used coolers are counterflow air coolers, classified according to output. For example, the SKLB4 type Counterflow Pellet Cooler can cool 10 t·h −1 at a power input of 2.5 kW. However, this does not take into account the energy consumption for the production of compressed cooling air [19]. In most cases, the pellets enter the countercurrent cooler from above via a turnstile feeder (via rotary valve). The pellets are evenly distributed on the radiator grate. For this type of cooler, a large amount of cooling air must be continuously supplied. The production of a large amount of cooling air is a very energy-intensive process. A stream of cooling air passes through the grate into the layer of pellets cooling them. The air is further discharged into the environment via a filter unit. The cooling efficiency depends on the height of the layer of pellets lying on the grate and the extent of the size distribution of the pellets in the cooled layer [20,21].
The occurrence of a large amount of fine and dust-sized particles fills the air gaps in the cooled layer of pellets, thereby restricting the passage of cooling air. The air then seeks the path of least resistance and creates tunnels or ratholes in the pellet bed. The cooling of the pellets then takes place only in limited areas of the layer. The cooled pellets then fall through a grate onto a sieve separator, where small and dust-sized particles are separated and returned to the crushing process. A considerable amount of the pellets produced are broken or degraded after passing through a countercurrent air cooler and thus lose their optimal size and shape [2]. The counter flow cooler simulation model revealed that the cooling rate is influenced by the diameter of the pellets and the initial temperature of the pellets exiting the pelletizer. It is stated that the pellets with a diameter of 3.2 mm were cooled to a temperature of maximum +5 • C ambient temperature within 3.5 min, in contrast to the 6.4 mm pellets, which remained above +5 • C ambient air temperature after this time. In contrast, the initial humidity, the supply air temperature and the relative humidity did not affect the cooling rate of the pellets. The major cooling factor was the resting time of the pellets and their location in the bed [2].
Another type of cooling device used for cooling biomass and pellets is a horizontal belt cooler. The basic cooling principle of this type of cooler relies on the transport of pellets by means of a perforated drawing element (conveyor belt), on which a layer of pellets is carried. During transport, cold air is blown onto the pellets, which cools the hot pellets. The efficiency and duration of the cooling process can be regulated by the speed of movement or the length of the conveyor belt [22]. In both types of cooling mentioned above, the pellets are cooled by a stream of cooling air passing through a layer of pellets statically lying on a grate or on a conveyor belt. It follows that the pellets are always more cooled from the side from which a stream of cold air is applied to them. Thus, the individual pellets are unevenly cooled. After evaporation of water from the surface of the pellet, the pressure gradient and heat inside the pellet cause water to migrate from the pellet core to its outer layer. When the pellets are exposed to excessive air velocities in the cooler, the outer layer of the pellet dries faster. This creates more stress in the pellet causing cracks on the outer surface. Such pellets are more prone to permanent damage and abrasion. The transport of pellets is also negatively affected. It is obvious that the cooling process affects the quality of the produced pellets [23,24]. The quality of pellets is very important for some energy processes, e.g., torrefaction, combustion, etc.
In general, the production of pellets is only associated with the pressing of the pellets in a pelletizer. However, the above, briefly described technological process of pellet production shows that it is necessary to focus more on and optimize other sub-operations to reduce the overall energy intensity of the operation. This is directly related to the selling price of the final pellet product traveling to the end consumer. In this context, the experimental study focuses on the design of new, less energy-intensive technologies for cooling alternative pellets, which would help reduce the technical problems of current cooling systems while reducing overall costs. The conducted research is described in the current trend of designing machines producing and processing biomass into energy materials aimed at reducing energy consumption [25][26][27][28]. Therefore, a spiral vibratory feeder was designed to cool rapeseed straw pellets during their transport from the pellet press. The aim was to experimentally test two possible variants of a cooling system using vibrations-the chaotic movement of pellets by micro-pitch, and the use of air through air channels distributed along the trajectory of pellets on the vibrating conveyor. Based on the qualitative parameters of the pellets, transport speeds and thermal imaging measurements of both variants, the efficiencies of both designs were tested. An additional part of the research aims to determine the effect of vibrations on the properties of cooled pellets. How and whether vibrations can affect the internal structure of the pellets during the cooling process is assessed. Parameters such as mechanical durability of pellets (PDI), moisture resistance of pellets MRR and the quantity of degraded pellets after the cooling process were evaluated.

Materials and Methods
Pellets were produced from Odeon oilseed rape straw, which is produced as waste during the harvesting of oilseed rape seeds. It is a bred variety supplied by the seed company Oseva Pro. Oilseed rape is cultivated mainly to achieve higher yield, resistance and vitality of the variety.
At present, according to statistics from the Ministry of Agriculture in the Czech Republic, rapeseed is grown on an area of about 400,000 hectares of land [29]. It has a growing season of 300-350 days. After this, it is harvested, and what remains is the so-called rapeseed straw, which is biological rapeseed waste and which retains energy potential for further use. Therefore, it is important to address the possibilities of processing this type of bio waste.
Rapeseed straw was ground to a uniform particle size distribution using a Green Energy 9FQ 50 hammer mill, Green Energy Machinery Ltd., Uherský Brod, Czech Republic, (engine output 11 kW, mill capacity 800-1200 kg·h −1 ). It was also homogenized in a mixer called Alba Re 22, ALTESE Ltd., Hořovice, Czech Republic. This is a universal device for homogenizing mixtures of different compositions and materials. During homogenization, water was gradually added by spraying. The moisture level of the mixture was adjusted to 14%.
Rapeseed straw was pelleted in AMANDUS KAHL 14-175 (AMANDUS Ltd., Reinbek, Germany) laboratory rotary pelletizer with a flat matrix and 3 kW motor [30]. The flat matrix consists of a horizontal disk with holes with a diameter of 6 mm. A pair of rotating rollers pushes the raw material into the holes of the flat die, thus compacting and forming the final shape of the pellets. To illustrate, Figure 2 shows crushed rapeseed straw and the pellets produced. The hot pellets coming out of the pelletizing press are fed directly to the inlet of the spiral vibrating trough. A spiral vibrating feeder was used to cool oilseed rape straw pellets. The cooling itself takes place during the transport of the pellets on the spiral trough of the vibrating feeder. The vibrating spiral trough causes the pellets to move upwards in a spiral due to micro-motions. The heat from the hot pellets is dissipated to the environment. The cooling efficiency of the hot pellets depends on the setting of the operating conditions of the spiral vibrating feeder and its construction. With a pair of vibromotors running, the vibrating unit produces a motion that consists of the amplitude of a rectilinear oscillating displacement (A z , m) in the direction of the Z axis and an oscillating angular rotation (ϕ', • ) around the Z axis (see Figure 3). Combining these two movements creates oscillations in the shape of a partial helix. The excitation force (F E , N) is perpendicular to the axis of the vibromotors and acts in the direction of the angle of rotation of the vibromotors (β, • ) to the horizontal plane. The excitation force of vibromotors can be determined as the product of the square of the angular velocity of the vibromotor (ω v , s −1 ), the mass of the rotating eccentric weight (W w , kg) and the radius of the center of gravity of the eccentric weight (R, m) from the vibrator axis (see Equation (1)). Figure 3 shows the location of a pair of vibromotors on a vibrating structure and the purpose of oscillation of the individual movements. Cooling during transport of pellets using micro vibrations is ensured by constant chaotic movement of individual pellets on a vibrating spiral trough. This allows the passage of air into the space between the individual pellets. In addition to the primary cooling, the pellets are transported to the desired height or space, where other sub-operations, such as dosing or packaging, can continue. The bottom of the spiral trough can be replaced in some sections with a perforated plate, through which dust and fines can fall and which can then be dispatched back to the beginning of the pelletization process. This can even replace another sieve operation. Figure 4 shows a process for the production and subsequent cooling of pellets by means of a spiral vibrating feeder. Two variants of the construction of the spiral trough of the vibrating feeder were tested in pellet cooling experiments. The first design variant is a spiral trough of rectangular cross-section with dimensions of 60 × 25 mm (see Figure 5a). The length of the spiral path of the trough on the middle diameter (D T = 210 mm) is 5.9 m, and the transport height H is 0.5 m. The second variant of the construction consists of a basic spiral trough and a distribution of air hoses with holes. The air hose is located on the middle diameter of the spiral trough (D T = 210 mm). The openings in the air hoses allow cooling air to flow into the chute space. In this way, a more efficient entry of cooling air is ensured, which also penetrates the internal spaces between the individual pellets, and at the same time, the removal of warm air from the trough space is ensured. The location of the air hoses and the direction of the flowing cooling air are shown in Figure 5b. The first part of the experimental study deals with the influence of setting operating parameters on the efficiency of transport of pellets made from rapeseed straw on a spiral vibrating feeder. The plan for the experimental tests was created to set the revolutions of the vibromotors n = 1800 rpm in combination with various settings of the oscillation amplitude of the spiral trough A z . The amplitude of the A z was adjusted by eccentric weight adjustment of each of the vibromotors to 60 • , 90 • and 120 • (see Table 1). The pellets were cooled in two basic design variants. The first instance involved direct cooling on the spiral trough of the vibrating feeder. In this case, the pellets are transported and spontaneously cooled at the same time. This is passive air cooling, which uses natural air circulation. The second setting was with the distribution of air hoses along the entire trajectory of the spiral trough. The pellets are cooled by flowing air from the hoses and at the same time transported to the packaging line, to the hopper, etc. This design uses active air cooling, when forced air circulation is created. Both variants were tested three times.
In both design variants, the pellet cooling process was always monitored by the FLIR-E60 thermal imager. The ambient temperature was 17 • C during measurement. A final operational setting of the oscillation amplitude was used for all tests A z120 • = 0.48 mm.
The pellets were subjected to analyses based mainly on standardized quality standards for determining the properties and quality of the produced pellets. These were particle and bulk density of pellets [31][32][33], mechanical durability of pellets [34] and size of pellets.
The moisture content of all samples (input material of rapeseed, homogenized, pellets) was measured according to the standard ISO 18134-2:2017 [35]. Moisture reduction ratio MRR 1 -ratio of reduction of moisture content of rapeseed (moisture reduction ratio) (MRR 1 , %) is defined according to Equation (2), where M B is the moisture content of the produced pellets, and M S is the moisture content of the input sample of rapeseed straw.
Moisture reduction ratio MRR 2 -the moisture loss ratio of the pellets is analogously defined by Equation (3), where (M A , %) is the moisture content of the pellets after the cooling process on the spiral vibrating feeder and (M B , %) is the moisture of the pellets before the cooling process, i.e., the moisture of the pellets produced.
Particle density of pellets was determined on the Mettler Toledo JEW-DNY-43 tester, Mettler-Toledo Ltd., Prague, Czech Republic. Bulk density was determined according to the standard [32]. The values correspond to the average value from 5 measurements.
The pellets were subjected to a mechanical durability test on a Holmen NHP 100 tester, TEKPRO Ltd., Norfolk, UK. The tester works on the principle of circulation of 100.0 ± 0.5 g of pellets in a chamber where the pellets hit each other and the surrounding walls. The pellets durability index is expressed as the percentage weight loss of the test sample before and after the test process. The pellets circulated in the device for 60 s. The sample was sieved on a 3.15 mm sieve and then weighed. The test is repeated 5 times with various pellets and the average PDI value is calculated.
The size of the produced pellets was assessed mainly with respect to their possible degradation during the cooling process on a spiral vibrating feeder. In this analysis, the degree of influence of vibrations on the degradation of pellets was assessed. The pellets size was determined before entering the cooler and at its exit. A batch of approximately 150 pellets was used for determination of pellet size distribution before and after cooling process. Inlet and outlet of cooler were visually monitored. Record was used for pellet size determination. Outcoming pellets were arranged side by side, and the size was validated with a caliper [36].
High-speed camera-Olympus I-SPEED 2, iX Cameras Ltd., Rochford, UK. was used to measure the amplitude of movement of the vibrating spiral trough. The Olympus i-Speed 2 is a compact, mobile, autonomous color camera suitable for recording very fast and short-term, transient or random processes. The FLIR-E60 thermal camera, Teledyne FLIR Ltd., Wilsonville, OR, USA was used to monitor the temperature changes of the pellets during the cooling process on a spiral vibrating feeder. Thermal camera was used for determining of pellets temperature in time during the experiment. The FLIR-E60 has an IR sensor resolution of 320 × 240 points, a 25 • lens field of view, manual focus and temperature measurement range from −20 • C to +650 • C. Temperature sensitivity of camera is 0.05 • C.

Results and Discussion
The section with the results was divided into three consecutive parts. The first part of the research was focused on monitoring the operating conditions of a spiral vibrating feeder designed for subsequent cooling of pellets. The second part was focused on a separate process of cooling pellets, and the analysis of pellets was performed from the point of view of controlling the influence of vibrations on the mechanical properties of pellets in the third part.

Optimizing Pellet Transport on a Spiral Vibrating Feeder
The monitored magnitudes of the vibration amplitude of the spiral trough are given in Table 1. The values given in Table 1 were obtained using a high-speed Olympus I-SPEED 2 camera and tracking software. The principle of amplitude measurement by tracing is shown in Figure 6.  For the subsequent transport and at the same time the process of cooling the pellets on the spiral vibrating feeder, the operating setting of the oscillation amplitude Az 120 • = 0.48 mm was chosen. At this setting, the transport of the pellets in the spiral trough had the longest duration. This parameter is essential for this type of cooling process, because the pellets are cooled individually, having been arranged side by side by the vibrations. The vibrations also increase the efficiency of the cooling process. Due to the vibrations of the spiral vibrating feeder, the pellets slowly change their position over time and gradually cool down. All pellets move at single layer on the spiral trough. Therefore, combination of parameters (length and width of trough, amplitude, frequency) gives a different mass flow and duration of the passage. Different needs can be met in this way.

Cooling on a Spiral Trough (Variant A)
The spontaneous cooling of the pellets during their transport in the spiral vibratory feeder is shown in Figure 8 from the perspective of thermal imaging measurements. Figure 8a shows the entry of hot pellets into the spiral vibratory feeder and Figure 8b shows the output from the spiral vibratory feeder. In this case, measuring the temperature during the transport of the pellets is essential not only to determine the efficiency of the cooling process but also a prerequisite for evaluating the tested designs. As can be seen from Figure 8a, the temperature of the pellets at the outlet of the pelletizing press was more than 91 • C. Temperature is one of the process parameters influencing pelletization. It can, of course, vary due to other parameters, such as the mechanical-physical properties of the input mixture, the geometry of the pelletizing press or the frequency of rotation of the pelletizing rollers. However, in the case of energy grass pellets, lignin acts as a natural binder in the temperature range of 75-120 • C (so-called glass transition temperature) and causes sufficient strength of the produced pellets [37]. For example, in wheat straw, the glass transition temperature is between 53-63 • C, but a pressing temperature above 100 • C is still recommended [38]. It can be seen from the thermo-images that the pellets did not exceed 100 • C. During transport in the spiral trough, the pellets were continuously cooled to a temperature of on average 31 • C (see Figure 8b). In the tested design-cooling on a spiral trough-it is a temperature drop of 60 • C on average in 308 s.

Cooling on the Spiral Trough with a Distribution of Air Hoses (Variant B)
During the transport and cooling of the pellets on the spiral trough with a distribution of air hoses, i.e., in the second design variant, temperature changes were also monitored using thermal imaging (see Figure 9). During the tests, the rotation of the individual pellets was observed not only by vibrations caused by transport but also by the air flow from the air ducts. This should support the exchange of thermal energy and make it easier. Hot pellets were able to cool continuously from the mean value of original 91 • C to a final 22 • C in a period of 322 s. This represents a temperature difference of 69 • C.

Cooling of Pellets on Free Surface (Variant C)
To compare the effects of vibrations on the pellet cooling process, three simple experiments were performed, in which samples of pellets coming from the pelletizing press were spread on a steel contact surface and allowed to cool spontaneously in an ambient temperature environment of 17 • C. These experiments were carried out in addition to, for example, laboratory conditions. Experiments show a comparison of the free cooling rate of pellets with the proposed system. The spiral vibrator pellet cooler described can be moved relatively easily and used for different types of pelleting presses. Figure 10 shows thermal images acquired during the spontaneous cooling of pellets. The hot pellets cooled on their own from an average original 90 • C to an average final 24 • C over a period of 1057 s. That is a temperature difference of 66 • C. From the above-mentioned tested designs of pellet cooling (variants A and B) and spontaneous cooling of loose pellets (variant C), it is possible to observe differences in the cooling time of the pellets to a temperature suitable for their further processing. The use of vibrations to cool the pellets during transport has proven effective. The vibrations cause a slight rotation of the pellets; the pellets are spread side by side facilitating the exchange of thermal energy more easily than in a bed of pellets, as is the case in a countercurrent cooler. Using micro-vibration in a helix pattern, the pellets constantly move irregularly on the transport path, thus allowing cooler ambient air to enter the spaces between the pellets and at the same time to draw off the heated air. In addition, this positive effect can be amplified by the flow of cold air by means of distributed air hoses along the entire transport route (variant B). This method proved effective in the overall evaluation. Figure 11 shows the cooling curves of the design variants used (A, B) and the comparative spontaneous cooling of the pellets C.

Mechanical Properties of Pellets
During the tests, samples of pellets were taken from various areas from different process points-after exiting the pelletizing press, prior to entry into the cooling device (input), after cooling in design variant of cooling system A (A output ), after cooling in the design variant B (B output ) after cooling in the comparative spontaneous cooling of the pellets C (C output ).
Bulk density was determined for all samples. One of the reasons for pelletization is the increase in bulk density due to the simplified processing, transport and storage of residual biomass [7,39]. Moreover, in the case of pelletization of rapeseed straw, as expected, there was an increase in bulk density. The values are given in Table 2. All samples of pellets showed average bulk density values of 605-625 kg·m −3 , i.e., higher than the normative lower limit. It is clear that with decreasing moisture content, pellet bulk density also decreases. The specific gravity of the pellets can provide information on the burning efficiency of the pellets as well as information on their mechanical durability. Figure 12 shows a comparison of the mechanical durability of pellets (PDI) for individual design variants of the cooling methods used (variants A and B) and the reference variant (variant C). All produced pellets were normatively compliant with PDI (PDI > 97.5% for class A herbaceous biomass pellets). The influence of the cooling method used is seen in variant B, when the PDI values reached a more significant increase in a relatively short time. No negative impact of vibrations to PDI value was occur. During cooling, pellet firmness generally increases. This requires, among other things, certain deformation energy stored as a result of the palletization process. Prior to combustion, the pellets go through various transport and storage steps. They are often transported by pneumatically. They are subject to various loads and mechanical processes, leading to their abrasion, degradation and an increase in the proportion of fine dust. Pellet fragments can cause operational problems, such as system failure when draining pellet hoppers. Of course, the risk of dust explosion also increases and, during the combustion of degrading pellets, the increase in particulate emissions also increases [40]. Therefore, from the point of view of degradation of pellets, their size was assessed during the cooling process on a spiral vibrating feeder, for both construction design variants A and B.
The size of the produced pellets is assessed mainly from the point of view of possible degradation of the pellets during the cooling process on a spiral vibrating feeder. The particle size distribution results are shown in Figure 13. A batch of approximately 150 pellets was used for determination of pellet size distribution before and after cooling process. The results show that no size degradation of the pellets occurs during the cooling process (see Figure 13). This method of cooling can contribute to minimizing the operational problems caused by the degradation resulting from the usual transport of the pellets. Vibration cooling is the so-called "two steps in one", where they are also effectively cooled during the transport of the pellets. This innovative solution contributes to the trouble-free technology of producing alternative pellets.
The moisture reduction ratio MRR 2 value can define the maximum humidity of the pellets entering the cooling system for the desired and suitable outlet moisture content of the pellets after the cooling process. MRR 2 is an alternative to MRR 1 , which indicates the maximum moisture of the feedstock for the desired and suitable output moisture of the pellets for a given pellet press. In comparison with the literature data, we are in close agreement in the case of MRR 1 with respect to the various tested materials. This ratio was 28% for vines, 16% for spruce sawdust and 59% for cork [41]. The MRR 1 value for rapeseed straw is 23%.
The average value of the MRR 2 moisture loss ratio for variant A, cooling on a spiral trough, was 40.3% and for variant B, cooling on a spiral trough with air hose distribution, was 34.7%. These ratios allow a practical estimation of the targeted moisture content of rapeseed straw pellets both for the MRR 1 pelletization process and for the cooling process and their transport (MRR 2 ).

Conclusions
A new system of cooling pellets on a spiral vibrating feeder was built in two design variants and practically tested. Both variants included the innovation "two steps in one", where both the transport of pellets and their cooling take place in one step. Vibrational motion was used, where by means of helical micro vibrations, the pellets moved irregularly on the transport route, thus allowing cooler ambient air to enter the inter particle spaces and at the same time remove the heated air. In the first experimental part, the optimal operating conditions of the spiral vibrating feeder were determined. The optimal oscillation frequency of 30 Hz and the oscillation amplitude A z120 • = 0.48 mm proved to be the most suitable for transporting and at the same time cooling the pellets on a spiral vibrating feeder. In the second experimental part, both variants of the structural arrangement of the spiral trough were tested. The first variant consists in cooling by chaotic movement of the pellets. The second then combines the chaotic movement of the pellets with the action of an intense air flow, using specially placed air hoses. Both variants were compared based on temperature changes, qualitative parameters of cooled pellets, degradation of pellets and moisture reduction ratio. The results confirmed that the use of both design variants is suitable for cooling pellets. No negative impact of vibrations to pellets size or PDI occurred. Pellets have sufficient mechanical durability after the cooling process. After the cooling process at the outlet of the spiral vibrating feeder, the pellets can be dosed directly into the prepared containers or packed. Variant B showed better results than variant A in terms of cooling efficiency, degradation and durability. Both design variants A and B were also compared with the cooling variant of bulk pellets. A summary of the advantages and disadvantages of the individual variants together with the countercurrent cooler are given in Table 3. The paper presents a new variation of pellet cooling system which can be chosen for transport during cooling in biomass pellets production systems as a different solution against counterflow cooler.

Conflicts of Interest:
The authors declare no conflict of interest.

Nomenclature/Abbreviations
A Z Z direction amplitude (m) A Z120 • Z direction amplitude for vibration motors inclination of 120 • (m) D T trough diameter (m) F E excitation force (N) H height (m) l 0 average pellet length before cooling process (m) l 1 average pellet length after cooling process (m)