BG98186A - Method for the regulation of the moisture content in tobacco - Google Patents

Abstract

A process for reordering tobacco, which results in no significant decrease in equilibrium tobacco CV or significant tobacco degradation, is provided. Tobacco to be reordered is contacted with an air stream having a relative humidity near the equilibrium conditions of the tobacco. As the ov content of the tobacco increases, the relative humidity of the air stream contacting the tobacco is increased to affect reordering of the tobacco. Also provided is a process for drying tobacco, which results in no significant change in equilibrium tobacco CV or significant tobacco degradation. Tobacco to be dried is contacted with an air stream having a relative humidity near or below the equilibrium conditions of the tobacco. As the OV content of the tobacco decreases, the relative humidity of the air stream contacting the tobacco is decreased to affect drying of the tobacco. It has been found that tobacco can be reordered or dried successfully in a continuous manner using a self-stacking spiral conveyor. <IMAGE>

Description

MUOD TO CONTROL THE MOISTURE CONTENT

IN ORGANIC SHUGERIALS

The invention relates to methods of re-humidification, i. increasing the moisture content and drying of tobacco or other hygroscopic organic materials such as pharmaceuticals and agricultural products including, but not limited to, fruits, vegetables, cereals, coffee and tea. In particular, the invention relates until the use of controlled humidity air to moisten or dry these materials.

The prior art has long been aware of the need to control the content of tobacco in various organic materials, including tobacco. For example, the moisture content of tobacco, which has been treated to produce a final product with a particular application, changes many times during processing. .Each technological step, ie..removal of stems, cutting, mixing of components, addition of aromatic ingredients, inflating and making cigarettes, requires some optimal levels of moisture content that must be controlled. IRA carefully to OE provide high quality tobacco and other hygroscopic organic materials.

- 2 • · · · • ::. ... · · ·

In addition, the way in which the moisture content of tobacco is altered can have a lasting effect on the physical, chemical and specific characteristics of the finished product. Therefore, the methods used to induce changes in the moisture content of the tobacco. tobacco or other organic materials are of great importance.

Re-moisturizing blown tobacco is a process with many requirements. Typically, tobacco obtained after blown has a moisture content of less than 6¾ and often less than 3 /. At such low moisture content, the tobacco is very breakable. the structure of the swollen tobacco undergoes degradation upon re-humidification, i.e., the full or partial return of the tobacco to its pre-swollen state. This water leads to a loss of resistance to the tobacco filling, which reduces the benefit of swelling.

Different means of re-humidifying blown tobacco have been used. The most common method is to subject the tobacco to water jet, usually while the tobacco is being processed in a rotating cylinder, another method is to use saturated steam as a re-humidifier. another method is to blow high humidity air through a moving bed of layered tobacco onto a conveyor, as shown in / I /.

None of the above methods is completely satisfactory for use in blown tobacco.Treatment of rolling tobacco in a rotating cylinder of water until the fragile blown tobacco is broken.Direct contact with water causes the structure of the blown tobacco to break. water to destroy the structure ia the swollen tobacco.While this may be partly due to the high temperatures in the vapor-saturated medium, the exposure of the swollen tobacco to any gas medium in which the condensation of water occurs, ca. o steam or highly humidified air may result in breakage.

.1the method by which these labors are avoided is to place the dry blown tobacco in a chamber. Containing air at the desired degree of humidity and bringing the tobacco to equilibrium condition in the chamber for a period of 24 hours to 48 hours. The air velocity through the chamber is kept very low, usually not greater than about 0.12? m / sec.This method has no or very small disturbances in the structure of the blown tobacco. However, the required duration of 24 to 48 hours limits the application of this method for laboratory purposes only.

Attempts were made to reduce the required duration of the method by increasing the air velocity. These attempts were unsuccessful due to the inability to duplicate maintaining the stability of the tobacco filling observed under slow equilibrium conditions in laboratory cells, the size of the conveyor, the required smoke. the transfer of tobacco in order to adapt to the duration of the process, the non-uniform moisture content of the tobacco product at the outlet of the conveyor, and the extent of the spread of fires in such devices and / 2 /.

The use of drying as a means of controlling the moisture content of tobacco processing is equally important with the use of re-humidification for this purpose. When tobacco is dried, physical and chemical changes can occur that affect the physical and specific qualities of the product. Therefore, the method of drying the tobacco is extremely important.

There are two types of drying devices commonly used in the tobacco industry: drum dryers and belt dryers. In some cases, pneumatic dryers are used.

The type of dryer depends on the drying conditions.

For example, belt dryers are usually used for tobacco in the form of strips / tapes /, while drum dryers are generally used for cut tobacco. Both types of oui4jj ': cf. for drying * · ._ »w. · Tobacco stems.

In the belt dryer, the tobacco is spread on a perforated strip and the air is directed either up or down through the strip and through the bed of layered tobacco.This type of dryer often results in uneven drying of the tobacco. This is due to the channels being blown into the bed. tobacco and canoes allow the drying air to surround the tobacco.

Most of the tumble dryers used in the tobacco industry are supplied with steam coils and can function as indirect or direct heat dryers depending on whether the heat is applied externally or internally to the oven casing containing the tobacco. be actuated either on the principle of joint action when the flows of tobacco and air are in one direction, or on the principle of counterflow * when the flows of tobacco and air are in opposite directions.Dryers should be controlled Carefully avoid to avoid excessive drying, which causes chemical changes and unnecessary damage from rotational motion. In addition, very dry drying may form on the outer bond of the tobacco, which impedes the passage of moisture from inside the tobacco. The formation of such a layer slows down the drying process and leads to uneven drying of the tobacco.

The use of a drum or belt dryer for tobacco drying can result in a heat treatment that can cause chemical and physical changes in the tobacco. Although not always undesirable, these changes are necessary to remove the water from the tobacco. tobacco applications The need to dry tobacco for a limited time determines the result of heat treatment at the drying stage, preventing the optimization of heat treatment separately from the process constraints imposed by drought-5- ..

• · · • · net. **

Embodiments of the present invention have the advantage that tobacco, or other suitable hygroscopic and agricultural products, including fruits, vegetables, cereals, coffee and tea, without being limited to them, can be re-moistened or dried without damage or with minor ones Furthermore, the present invention has the advantage that the re-wetting of the blown tobacco is carried out without the loss of the blown tobacco structures or with small ones and provides wiggle of tobacco or other suitable hygroscopic organic material almost at atmospheric pressure, for example, without the use of vacuum and at a selected temperature wherein the thermal treatment imparted can be controlled by vrelo the process to an extent unattainable in conventional processes for the drying of tobacco.

It is a preferred embodiment of the invention to contact the tobacco with air that has a carefully controlled relative humidity above or below the equilibrium relative humidity of the organic material in contact with which changes in the moisture content of the tobacco or other suitable organic materials occur.

The relative humidity of the air is continuously increased or decreased accordingly during the maintenance of a controlled difference between the relative humidity of the air and the equilibrium relative humidity of the organic material with which it is in contact. · Careful continuous control of the relative humidity permits control of the degree of transfer of the humidity. moisture between the organic material and its environment, thus minimizing the structural changes in tobacco. Using relative humidity as the main The moisture transfer visibility allows independent control of heat treatment.This process can be continuous grinding to take place in series.

In addition, the process of cleaning the cylinder will cease using the rotating cylinders without any subsequent damage.

Describe embodiments of the present invention and preferred embodiments thereof, together with drawings having the following meaning:

Figure I is a diagram showing the relative humidity (£ H) in% relative to the moisture content of tobacco or 0V;

Figure 2 is a schematic drawing of a laboratory device for re-humidifying a hygroscopic organic material according to the invention by rapid linear change of the HV of the air;

Figure 3 is a partial sectional view of an exemplary continuous flow process apparatus of the invention;

Figure 3a is a cross-sectional view of a portion of the helical conveyor shown in Figure 3, which shows the airflow path relative to the trajectory of the hygroscopic organic material;

Figure 4 is a schematic drawing of an alternative device suitable for carrying out the process according to the invention on a continuous basis;

Figure 5 is a block diagram illustrating the application of the present invention to the process of wetting rea; and

Figure 6 shows the graphical relationship between the RH of the air in the vicinity of the tobacco relative to the time obtained during the re-humidification in the device of Figure 3.

The present invention relates to methods for regulating the moisture content of tobacco or other suitable hygroscopic organic materials such as pharmaceuticals and agricultural products, including, but not limited to, fruits, vegetables, cereals, coffee and tea, as long as they are reduced to minimum damage, changes in physical structure or thermal. In particular, the present invention relates to the use of controlled humidity air for re-humidifying or drying tobacco or other suitable hygroscopic organic material. The moisture content of the tobacco or other suitable hygroscopic organic material is increased or decreased by a gradual and continuous increase or decrease of the relative humidity of the air in contact with the tobacco or another suitable Thus, moisture transfer is controlled, enabling the other variables of the method, such as temperature, air velocity and air pressure, to be optimized individually.

Two commonly used methods for characterizing the physical structure of tobacco are the determination of the cylindrical volume / SI / and the specific volume /5V /. These measurements are especially valuable for achieving good results from the re-humidification of tobacco.

Cylindrical Wallpaper / SU /

Tobacco stuffing material weighing 20 grams if not swollen or 10 grams if swollen is placed in a cylindrical densitometer 6 cm in diameter, model K DD-60, designed by Heins. .Bo ^ waMt Company, Heins .Bo ^ v / aCcU QmiH, $ chacKen8u ^ a2 £ «e I5, Postfac {c 54 07 02, 2000 HamEuig 54Wesi ^ exmany.The tobacco mass is pressed with a piston weighing 2 kg and with a diameter 5.6 cm for 30 seconds. The resulting volume of compressed tobacco is counted and divided by the weight of the tobacco sample, resulting in a cylindrical volume (cylinder volume) in cm ^ / g. This experiment determines the apparent volume of a given tobacco filling weight. cylindrical volume.This experiment is carried out under standard ambient conditions, namely 23.39 ° C and 60% relative humidity (ES).

• · · · · ·. · ··: ·

Usually, despite some adverse effects, the tobacco sample is pretreated in this medium for 24-48 hours.

Specific volume / ^5V 7

The term specific volume is a unit for measuring the volume occupied by solids, i. E. tobacco, using the Archimedes law of displaced fluid.The specific volume of a body is determined by taking the inverse of its density.It is measured in cm3 / g. Suitable methods for making these measurements are mercury and helium. pycnometry that show good results.

When helium pycnometry is used, the weighed sample of tobacco, or as / i.e. in its original state /, dried at 100 ° C for 3 hours, or brought to equilibrium, was placed in a single cell of a Quantum Chromatopycnometer Model 2042-1 / manufactured by Quarviachxome CoipotaHow, 5 Aewa ^ Way, Syosset, Wew YotV. The cell is cleaned and loaded with pressurized helium * The volume of helium displaced by tobacco is compared with the volume of helium required to fill an empty test cell. Tobacco volumes are determined on the basis of the fundamental principles of the ideal gas law .In this app, despite some controversial opinions, spec cific volume of the tobacco is determined using the same tobacco sample used to determine the 0 /, ie. tobacco, dried for 3 hours in a circulating air oven at a controlled temperature of 10 ° C.

As used throughout the text, moisture content can be assumed to be equivalent to the volatile matter content / 01 //, whereas no more than about 0, 3X of the weight of the tobacco are volatile substances other than water. Determination of the volatile matter content is generally measuring the weight loss of tobacco after staying in a circulating air oven for 3 hours at a control of 3 …… .ί. ”. · “·” '* Liter temperature of 10 ° C. Lose '4Gt €? Giaof': Like * 'Percentage First: ... · ··· ·· ·· ·· Initial Weight is the content of volatile substances.

Screening refers to a method of measuring the distribution of individual pieces along the length of aa sample of sliced tobacco filling. This test is often used as an indicator of reducing the length of pieces during processing. Tobacco filling material weighing 150 + 20 g. is inflated, or 100 + 10 g. if inflated, placed in a vibrator. The vibrator contains a series of circular trellis tubs with a diameter of 0.48 cm / manufactured by W. $. Tu ^ er, Inc., a subsidiary of the A $ '1X standards. The usual dimensions of sieves for bathtubs are 6 mesh, 12 mesh, 20 mesh and 35 mesh. The vibrator stroke is about 2.54 cm to 1.27 cm and the speed is its tobacco is 350 + 5 rpm. The tobacco is stirred in the vibrator for 5 minutes, whereby the tobacco sample is divided into batches of different particle sizes. Each of these batches is weighed, resulting in a distribution of the tobacco sample

Sog & k & cop bminee ^ Ma Inc.

OCteevMviQ .i.lerrto'C.Ok 44060 / by particle size.

Laboratory tests have shown that re-humidifying the tobacco by exposing it to high humidity air leads to losses in the CV. It is clear that losses in the CV occur either during condensation processes or when moistened inside the bed of bloated tobacco.

Condensation processes occur when moist air comes in contact with tobacco, the temperature of which is below the humidity condensation temperature. Humidification can occur when there is a change in moisture inside the tobacco bed due to uneven exposure to moist air. a successful humidification re-humidification system must operate at a relatively low speed with good control of the relative humidity, air temperature, airflow and pressure here through the bed of tobacco.

- IO „v * ··· · ·······:

This is best achieved. by simply increasing the moisture content of the humid air passing through the tobacco in such a way that the tobacco is exposed to an air stream which is close to equilibrium with the tobacco.

1a, the ABC line is an isotherm of 23.89 ° C for a typical swollen light tobacco. This isotherm gives the relationship between 0 / of the tobacco and the QO of the air that surrounds it, at one equilibrium for a given temperature. that at BZ, 89 ° C and at € 0% RH, the swollen tobacco sample will have 0V with a value of about 11.7% at

The equilibrium state of DEF in FIG. 1 is a typical EN profile for tobacco that has been re-moistened according to the present invention. The ^ EF line represents an alternative profile of EN, which can also be considered satisfactory. The HF line represents a trajectory characteristic of the prior art such as laboratory re-humidification in an equilibrium chamber at very low air speeds. The line represents the application of this invention for tobacco drying.

Figure 1 shows that the re-humidification of 0V tobacco is about 6.5%, where it could be in equilibrium with air with an Eri of about 30%, to a value of 0 / about II, 7%, where it would could be in equilibrium with air with an EN of about 60% would have to be met by exposing tobacco to air whose humidity rises from about 40% RH in small increments over a period of time until the EE reaches a value of about 60% , which is preferable to direct exposure to air with RH of 60%.

When under these slowly changing conditions, the mass flow between the air flow and the tobacco is relatively slow because the driving force is small, while maintaining the structure of the blown tobacco. Re-moisturizing the blown tobacco without loss in CV can also be achieved by exposing the tobacco to air, the moisture content of which is increased by about 40% EN in small increments ,, ·· · ·······

- Vols. · :::

* · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · until it reaches a value of RH = 62; This reduces the total time required to complete the re-humidification process without significant changes in the structure of the blown tobacco. Therefore, the two lines DEF and GjEF of Figure 1 represent effective embodiments of the invention when performed re-humidification of tobacco.

It is apparent from FIG. 1 that close to equilibrium states between the air flow and the tobacco are illustrated by the linear segment EF and the ABCLe line, it becomes clear that at a value of 0 / under 7 / the difference between the relative humidity of the air at equilibrium with the tobacco and the relative humidity of the humid air stream used for re-humidification may be very high without adversely affecting the stability of the tobacco fill. It will also be clear that at values of 0V of about 7.5? up to about 11.5%, the relative humidity of the humidified air stream used for re-humidification may be from about 2% to about 3% above the relative humidity of the tobacco in equilibrium, with the greatest deviation from equilibrium, corresponding to lower DU values without adversely affecting the stability of the tobacco filling.

When the present invention is used for tobacco drying, no tobacco CV losses are observed. This is even noticeable when the relative humidity of the drying air stream is substantially below the relative humidity of the tobacco, i. E. .the relative humidity of the drying air stream is under equilibrium conditions for tobacco. Therefore, it is clear that the line IJ of Fig. 1 illustrates only one of the many possible trajectories that can be used in the drying of tobacco according to consisting invention.

- 12 «· · · · · · · · · · · · · · · · · · · · · ·

The present invention aims to * * flow as a 'serial' or 'continuous' process. When forgiveness as a serial process of re-humidification, the relative humidity of the air flow. increases for some time to provide a continuous increase in the moisture content of the tobacco.This can be done in an artificial climate chamber like the one shown in Figure 2. The tobacco to be re-moistened is put on layers to form a bed about & cm thick, in sieves with a sieve on the bottom, atre in an environmental chamber so that a stream of controlled humidity air may pass through the tobacco in a direction nadolu.Razmerite the chambers are of 0.560 m ³ to about 2.265 m ^ / produced by Paxameiet ^ enetartion and Coiifcotlnc., 1104 Oid 14S 70, Mast, in £ acA Mountain,

N.C. 28711 / .They have been used in a large number of studies. Chambers with artificial climate are equipped with microprocessors, which allow to control the rapid change in linear law of the state of humid air in the chamber. Attempts have been made to dry the tobacco with humidity. from starting values of 0U from 2% to ending values of 0V from II, 5% by infinitesimal increments of RH from initial values from 30% to 52% to final values from 59% to

65% for 30-90 minutes. Air velocities from about 0.254 m / s to about 1.016 m / s are used. DN and temperature measurements are controlled with a TkuiacLe% 4A-I model tool / manufactured by TPcms1g Science Sohr ., 623Woming, SE, A ^ ujwe'Qjue, New Mexico 87123 /. The air velocity is measured with a model 8525 heat-anemometer, model 8525 / manufactured by A-poch 1p54th ^ Co., 7555 λ.λίπά & ΐ AVe, Slcolte, 60066 /.Experiences in which the relative humidity changes linearly from a starting value of 52% RII to a final value of 62% RH for 40 minutes result in re-moistened tobacco with full o preserving SU when compared to similar tobacco reordered in an environmentally controlled room with air that is maintained with 60% RH at 23,89 ° C and which passes through

-'13 • Tobacco at low speed in prolonged .. at 24 hC.DZ / changeover is thus successful at a humid air velocity of about 1,016 m / s and at temperatures from 23.8i) ° C to 32.22 ° 3. Swollen tobacco, re-humidified in this way, shows minimal CV losses compared to swollen tobacco, re-humidified in a properly maintained artificial climate.

The present invention can be accomplished as a continuous process most successfully in a scayid / a self-priming helical conveyor, such as that shown in ;, ig.Z.This device is a specially modified model 3'лен 42 of a spiral ^ riser designed by? ^ oscan (^ a VoodlProcess Sy ^ ie ^ ^s AZ by 'lefci ^ o ^ .Sweden. The dry tobacco, which will be re-humidified, enters the device 10 on the conveyor 13, passes through XO in the form of a spiral from bottom to top of device 14, as shown, and exits outlet P after re-humidification. The humidified air is purged downward through the tobacco from the humidified air port 15 to the bottom of the spiral device 14, where it exits through the outlet port 16, the flow of air being opposite to the flow of tobacco <, i.e., most of the humidified air flow is from the upper a portion of the conveyor down through the layers of tobacco as the tobacco moves upwards, following the conveyor spirals. A small amount of moist air follows the spiral path of the conveyor from top to bottom in the opposite direction to the direction of movement of the conveyor. This device repeats to it For sake of efficiency degree, the increase is not Yaa RH, obtained in the device shown in _L ig.2.

Fig. 3a, which is a cross-section of a portion of the helical conveyor 14 of Fig. 3 shows the paths of the air stream 20 and 22 relative to the path of the tobacco bed 21. As can be seen from Fig. 3a, the air flow moves from the top of the conveyor to its lower part / 20 and 22 / .The flow of tobacco is from the lower part of the con- 14 ·· **. ·· ·· · *. * Fan and is shown in Fig. For the two ^ Wash to the right * 'yul ^ vo.next

.. .......

The main part of the air stream 20, which is in the reverse direction of the tobacco path, is directed through the layers of the tobacco bed 21 and comes into contact with the tobacco bed immediately below it, until one a small portion of the air stream 22 passes over the tobacco bed 21 in a direction opposite to the tobacco direction.This portion of the air stream 22 may later pass through the tobacco bed

21.

One condition for the successful implementation of the invention, in the case of re-humidification, is a steady increase in the tobacco's relative exaggeration of 0U of tobacco. air humidity means in contact with the conveyor carrying the tobacco.When the tobacco is fed at the bottom of the conveyor and the humidified air at the top of the conveyor, the total flow of air and tobacco This is the principle of countercurrent. This provides a natural continuous CN gradient in the air in contact with the

L.

tobacco because air is progressively dehydrated as it moves down the rows of tobacco when re-humidified.

With appropriate and careful selection of conveyor belt speeds, airspeed and non-tobacco flow rates, and control of inlet air temperature and air quality, conditions such as those used in series laboratory re-humidification experiments can be approximated on a continuous basis. For humidification of approximately 55.95 kg / h from 3% 0V, the strip is blown, providing a duration of about 40 minutes to about min and air at a temperature of about 23.89 ° C to about 35 ° C with relative humidity at the entry from Fr. olo $ 61 to about $ 64 at an air flow of about 28.32 mVmmh to about 70.8 m ^ / min using tobacco; speed- 15 on a modified model CCP 42 spiral.-device ia a completely satisfactory re-humidification is ensured. of CV or damage to tobacco that can be logged relative without significant measurement.

humidity during model 29-03 KDetprea ^ t ^ is 2sou9et / manufactured by RusHalc InsHuwewh Co. by E. Gj-TeevtKick, ΚΙ / are mounted in the device during the re-humidification of the tobacco.

These devices show a steady increase in relative humidity and air with initial RH readings from about 35% to about 45% at the bottom of the spiral conveyor where the tobacco is driest, to about 62% at the top of the conveyor where the tobacco is most wetter.

Figure 6 represents a typical RH curve over time, with values obtained with a Rugate device. It gives the RH values of the air in close proximity to the tobacco bed in%. The tobacco, with an initial value of 0V of about 3%, enters the spiral conveyor for humidification and comes in contact with the air with RH about 43% / t.A. Fig. 6 / .4Figure 6 shows how with the passage of the tobacco through the re-humidification coil, 8H of the air in the immediate vicinity of the tobacco increases from about 43% to about 62% at the outlet of the device / b. 6 / .When exiting the spiral device, the tobacco has a value of 0V of about 11% .The value of R H of the air entering the re-humidification device was controlled to obtain re-humidified tobacco without significant CV loss.

other means of providing an increase in RH of the air, such as that of FIG. 4, can also be used to carry out the invention on a continuous basis. As shown in FIG. 4, the tobacco enters the device through the inlet 40 of the conveyor 43 and exits. through the outlet 41. Air with a steadily increasing relative humidity tobacco 42 in a plurality of linear laws in a linear law a source can be provided

Pa

- 16 is blown up by the bed of the zones 44 to multiply the effect of increasing the device of Fig. 2. The effect of magnification is realized by moving air from the unity of a serpentine trajectory on the right. to the left in Figure 4, as the air flow in the reverse direction of the tobacco movement.

In this way the air "leaving a zone" will become the inlet air for the next zone on the left.

Whole tobacco tobacco leaves, cut tobacco, puffed or non-puffed tobacco or selected parts of tobacco such as stems or reconstituted tobacco may be processed for the permeation and process of the present invention. The method may be from the above mentioned types of tobacco.

For the special case, apply to anyone or everyone with or without aromatic additives.

of tobacco drying, undisturbed cut tobacco can be dried for a long time at ambient temperature from the air flow opposite the tobacco flow through a modified self-priming spiral conveyor starting from a moisture content of about 21% 0V to about 15 % 0V at a distance of approximately I hour. In this case, the air top of the device at a temperature of about 29.44 ° C 58% pH and exits at a temperature of about 25 ° C and about 68% RH.

Drying is performed with little or no heat treatment of the tobacco.

enters in and around

Accordingly, the method of the present invention can be used to dry tobacco at a temperature substantially higher than the ambient temperature, i. E. tobacco at a temperature of about 93.33 ° C to I2I, II ° C.When tobacco is dried in this temperature range, the temperatures of the drying air are adjusted to provide suitable conditions for the process of the present invention.

- 17 Similar to the re-'Hewl & jus $ v4not tobacco, it becomes clear ··· * ·· * * · ·· that drying is most successful in a minimum amount of time by adjusting the final moisture content in the air lower from what is necessary to achieve the desired final level of moisture content in tobacco, thereby increasing the moisture gradient for air-tobacco and, accordingly, the driving force for carrying out the drying process. Unlike the re-humidification process, the final moisture content of the air stream can be maintained at a level much lower than that which would be in equilibrium with the tobacco at the desired 0V value after drying.

Experiment Μ I

To demonstrate the advantage of re-humidifying dry, rationed tobacco by slow dosing of water and adding it to it compared to re-humidifying in a jet cylinder, 20 g of a sample of tobacco stuffing is placed in a hermetically sealed drying cabinet. liquid carbon dioxide and expanded in an expansion column at 287.78 ° C. The 0V value of the blown tobacco filler is 3.4%. It is estimated that approximately 1.89 g of water will be needed to increase 0Y of the sample to II, 5% .This amount of water is placed in a small glass with a rubber stopper through which a glass tube with an inside diameter of 0.32 cm was passed. The flask was also sealed tightly in the oven. After ten days all the water was swallowed by the tobacco.Then the tobacco was analyzed and set as one. is a value of 0V of about II, 5%. The term ^{, d} as used herein, refers to tobacco before being equilibrated in an air-conditioned chamber with air maintained at 60% RH and 23,89 ° C, passing through it at low speed for 24 to 48 hours.This process of bringing to equilibrium state hoeing is typically used to bring tobacco to a standard state before CV, SV and sieve measurements.

* ··· ··

Then, a standard equilibrium chiller / drizzle subjected to re-humidification in a drying cabinet has a C V value of about 9.5 cm ³ / g and an SV of about 2.9 cm ³ / g at a value of 0 / about 11.6%.

For comparison, when a second sample of the same tobacco is placed directly inside the equilibrium chamber and re-moistened by up to

steady state under standard conditions, after equilibration 0V is about 11.3%, SU is about 9.4 cm ³ / g and SV is about

2.7 cm ^{3 /} yr. A third sample of the swollen tobacco filling is re-moistened in a jet cylinder to one value as 0V of about II, 5%. After reaching the equilibrium state, this sample has a CV of about 8.5 cm. ³ / g and S / about 1.9 cm ³ / g at an equilibrium value of 0V about 11.6%.

As can be seen from the data in Table I, the tobacco sample re-humidified in a drying chamber by slow addition of water showed a significant improvement in the equilibrium values of CV and 3 /, compared with the results of the sample re-moistened in a Lazy sample cylinder also shows a slight improvement in the values of

CV and SV .compared with the corresponding sample values «placed and processed directly into the equilibrium chamber.

TABLE I

Existing situation as it is

In equilibrium

0W SV / cm ³ / g / 0W SU / cm ³ / g / ^5U cm ³ / g Extension 3.4 3.0 II, 3 9,4 2.7 column Jet Cylinder II, 5 1.8 11.6 3.5 1.9 Dryer 11.5 2.7 11.6 '9.5 2.9 A second was held series of attempts like has been used climatic

a chamber for re-humidifying an inflated tobacco pad. A PC camera / Ratchet Gjanetali oi and Control / was used for this purpose. This k »- 19 ·· ·······. The measure is equipped with a microprocessor Μ'ίρτόΜϊτΧ) '20 D0? Apart from the P8C buss * ······ * * which allows to control the linear growth of the standard <

howling inside the camera

Experiment M 2

A sample, weighing approximately 1559 g of light tobacco, impregnated with liquid carbon dioxide and swollen at the uel "similar to those described in Experiment 1, is placed with a bed thickness of about 5 cm inside the vein. The bath" which has solid walls and a sieve at the bottom is placed inside an air conditioning chamber. The sample is re-humidified for one hour using air with a temperature of about 23.89¾ and an initial RH of about 36%, which increases to a final value of about 60%.

The air movement is down through the bed of tobacco at a speed of about 0.228 m / s. This experiment is then repeated at intervals of 3 hours, 6 hours and 12 hours. The results presented in Table 2 show that for periods of increase up to about 6 hours, the rewetting rate affects the values of CV and SV for tobacco under these experimental conditions. The lower the rewetting rate, the higher the CV and SV values are observed. Moreover, re-humidification according to the present invention! results in a CV of at least about 1 cm ^ / g greater and an SV of at least about 0.2 cm ³ / g greater than the values observed for tobacco treated in a jet cylinder. However, it should be noted that a significant proportion of this peh is achieved by a linear increase within one hour.

TABLE 2

Sample Existing position Balanced in an air-conditioning chamber

mm /% / SV / ohm ^ / g / 0V /% / With V / CIT / g / Expansion Column 3.10 3.06 11,33 9.71 Jet Cylinder 11.51 1.61 11,37 8.61 Increase I hour 10.83 1.85 11,38 9.72 Increase 3 h 11,44 1.88 11,36 9.81 Increase 6 h 11,45 1.90 11.30 9.88 Increase in 42-hr- 44.44 44,2-7 θ'δθ

- 20 Experiment ff 3. · '··: ·:::'

A laboratory study was conducted on the effect of the re-humidification rate and temperature on the CV and SV values for tobacco. 7 series of experiments were performed such as called tobacco impregnated with carbon dioxide and expanded in a expansion column at 287.78 °. C. Swollen tobacco is re-moistened by the following methods:

(I) By equilibration for 24 hours in an air-conditioning chamber at 60% RII and 23,89 ° C by air movement through the tobacco at a speed of about 0,127 m / sec;

(2) By spraying with water to increase 0V to about 7.5%, then equilibration at 60% EC and 23.89 ° C for 24 hours as in / I /;

/ 3 / By spraying with water to increase 0V to about 7.5% and then finally re-wetting in a jet cylinder:

(4) By spraying with water to about 7,5% 0V and then using moist air with an increase from initial RH of about 46% to final OH of about 60%; and / 5 / By a linear increase in humid air from about 46% EN to about 60% EN.

Re-humidification with humid air is carried out inside a P9C air-conditioning chamber equipped with a microprocessor to control the magnification for selected intervals. The conditions under which it performs the treatment are the following:

/ I / Zoom intervals: 30.60 and 90 minutes;

(2) Air temperature: 23.89 ° C and 35 ° C;

/ H / Air speed: up through the tobacco bed - approx

0.228 m / s sometimes down the tobacco bed - about 0.39 m / s / 4 / Thickness of the tobacco bed: 5 cm.

· '* ·· ^·:: · ·· :. '·

The tobacco used for stabbing * methods * of re-humidification, except for the treatment in a jet cylinder, is collected at the outlet of the expansion column after inflating and sealed in double plastic bags before re-humidification.

As a result, the tobacco is cooled by 93.33 ° C, ie. the temperature of the tobacco in the expansion column to ambient temperature before re-humidification. When re-humidification is performed by linearly increasing at about 35 ° C, the tobacco, while still in the plastic bags, is pre-heated to a temperature sufficient to avoid condensation on contact with humid air before being exposed to rapid magnification conditions. Data for these experiments are given in Tables Z - Ze.

TABLE For

Sample Existing position Steady state

0V /% / SV / cm ^ / g / 0 / /% / CV / cm ³ / g / X Column Extension Output 3,43 3.02 11,31 9.04 $ Through a nebulizer 8.06 2.14 11,68 8.66 With Through atomizer and 11.53 1.81 11.59 8.59 and cylinder £ Through a nebulizer and 11,27 1.87 11.51 9.01

increased for 90 min / 46% RH to 60% RH, 23,89 ° C /

H Through a nebulizer and 10,961.98 subjected to an increase of 90 min / 46% RH to 60% RH, 23,89 ° C / I Sample I, held for 15 min at

60% RH and 23.89 ° C, 11,541.95

Through a nebulizer and 10,372,38 subjected to an increase of 60 min / 46% RH to 62% RH, 35 ° C /

X Sample J. held for 15 min at

62% RI and 35 ° C 11,172.26

II.36 9,48

11.56 9.40

11,23 9,85

11.22 9.88

- 22 - ·· · · • · · · · · · · _ l l · • · · · · TABLE 3b · ”··’. • · · · · • · · · · • · · · • · · · · • • Sample Existing Equilibrium position state 0V /: 7 SV / _cm 3 / _g / OV /% / CV / cm ³ /! / X Column Extension Output 3,01 2,53 11,34 9.23 $ Through a nebulizer 7.51 2.13 11,39 8.87 With Through atomizer and 11,86 1,69 11,64 8.07 cylinder F Through a nebulizer and 10.55 1.64 11,45 8.86

increased for 60 min / 46% RH to 60% EN, 23,89 ° C /

Sample F. held for 15 min

at 60% RH and 23.89 ° C 11.56 1.64 11,42 8.61 H Through a nebulizer and 10.28 1.97 11,27 8.99 increased 30 min / 46% RII to 60% RH, 23.8 ° C / I Sample H, held for 15 min at 60% CP and 23.39 ° C And, 73 1.82 N, 25 8.61

TABLE Zs

Sample Existing Equilibrium position state 0V /% / SV / cm ³ / g / 0V /% / CV / cm ³ / g / A Output column extension 1.81 2.78 11,37 9.23 £ Increase 60 min 10.91 1.36 11,47 8.86 / 46% RII to 60% RH, 35 ° C / With Increase of 60 min 10,63 2.02 11,28 9,20 / 46% RH to 60% OH, $ 23 ° C / D Increase 90 min 10.84 1.99 11,45 8.90 / 46% CI to 60% RH, 3 5 ° C / B Through a nebulizer 5.39 2.37 11,25 8.71 F Through a nebulizer and 10.80 I.8I 11,27 8.39 directly at 60% RH, 35 ° C for 30 min 3 Through a nebulizer and 10.66 1.85 11.23 8.65

increase 60 min / 46% OH to 60% RH, 35 ° C / 'W

- 23 • · · · · ·

Continuation from table '^ * • · · · ····· · ·

n Through a nebulizer and 10.76 magnification 90 min / 46% pH to 60% RP, 35 ° C / 1.82 11,24 3.62 I Through a nebulizer and 10.65 Magnification 60 min / 46% PH to 60% PH. 23.89 ° C / 1.90 11,23 8.75 J Through a nebulizer and 10.57 magnification 90 min / 46% RP to 60% RP, 23,89 ° C / 1.87 11,38 8.74 to Through a nebulizer and 10.73 directly at 60% RH, 23.89 ° C for 30 min 1.87 11,22 8.64 U Through a nebulizer and a 10.98 cylinder 1.60 II, 39 8.28

Sample

Steady state

TABLE 3d

Existing position

0V /% / SV / si3 / g / 0V /% / Cv / cm ^ / g / ΤΙ Output column extension 2.83 3.01 T2 Directly at 60% RP, 11,92 9.46 23.89 ° C over 30 min 11.24 2.27 11,77 9.08 TK Increase 90 min P, 08 2.24 / 46% RP to 60% RH, 23,39 ° C / 11, ¾ 9.29 T4 Increase 90 min 9.77 2.39 / 30% RH to 60% RH, 23,89 ° C / 11,85 9.43 ^ 1 Through a nebulizer 4.78 2.32 11,66 8.98 $ 2 Through a nebulizer IP, Yu 2.G9 directly at 60% pH, 23.89 ° C for 30 min 11,64 8.89 $ 3 Through the atomizer 10.34 2.25 and an increase of 20 min / 46% RP to 60% PH, 23,89 ° C / 11,27 9.05 $ 4 Through the atomizer 10.56 2.22 11,73 9.03

and increasing 60 min / 461 RH to 601 RH. 23, I9 ° C / * · * <· · · ·

Continued from ^: t®table'Sa ......

φ5 Through a nebulizer and 9.74 2.29 14.67 9.19 increase 30 min / 46% Eft to eH 3H, 23.89 ° C /

C Through atomizer and cylinder 10.48 1, X '11.81 8.80

Note: Table Ze is after the text section.

The data presented in Tables ³ to ³ show that the results are about 0.5 cm ³ / g to about I cm ^ / g in CV n from about 0.3 cm ³ / g to about 0.4 cm ° / g in SV can be achieved by re-humidifying chilled tobacco / i.e. tobacco at about 23.39 ° C to 35 ° C / s parameters aa increase in linear law compared to re-humidification in a jet cylinder of hot tobacco exiting the expansion column.Direct re-humidification of tobacco exiting the expander column, is preferable to processing in two steps, namely, pulverizing the tobacco to increase the OUD by about 7% and then re-moistening. There is no significant difference in the values of CV or SV of tobacco re-moistened by linear law increase such as used ca humid air with an initial RH of about 46% as compared to tobacco reordered by air having an RH of about 30%, or at those levels for tobacco reordered over a period of 60 minutes or 90 minutes.

It is observed that the tobacco can be re-moistened either by moving the air down through the tobacco bed at speeds of about 175 ft / min or 0.339 m / s to 235 ft / min or 1.194 m / s or by moving the air up through the tobacco bed at a speed of up to 45 ft / min or 0.228 m / s without significant differences in values of aa C V or 5V. In addition, it is observed that as a result of re-humidification, an increase in linear law results in equivalent or better linear law. QV and W values compared to tobacco, moistened by direct inserting it into the condenser 60a kN and 23, B9 ° C after leaving the expansion column. Finally, it is found that the atomization with water increases the values of 0 / up to about $ 7.5, followed by an increase in linear humidity parameters, resulting in better CV and SV values compared to atomization followed by final re-wetting in a jet cylinder.

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- 28 Experiment I 4:: ·· ·· :. :

.........

Tests were conducted to determine the effect of air flow and air velocity on drift, channel formation, and tobacco compaction. Two air-conditioning chambers were used.

The actual movement of air in both chambers is approximately 14.16 m / min. The air moves upwards through the bed of tobacco in one chamber and down through the bed of tobacco in the other chamber. cm are placed in bathtubs 5 ”x 5 3/4, which are open at the top and with a sieve at the bottom.

* The bathtubs had solid walls of 10.16 cm in height. These tubs were placed on shelves inside the air conditioning chamber. The air was forced through the samples by covering the unoccupied area of the shelves with cardboard and all gaps were sealed with tape. the change in the number of sample containers the air passes through. The tobacco used for these experiments is impregnated with carbon dioxide and is swollen at 287.78 ° C. The tobacco to be re-moistened goes through the first stage, which is a water spray e about 8% 0V just after the blowout. The conditions inside the chambers are controlled and during opiates their values are about 23.89 ° C and about 60% CN.Two anemometers are used to measure the air velocity, namely: a scapula anemometer / ah! you. model fsa 6000, Tfcedeek, magtawl / and heat / Λοτ InW'Uiw ^ Cojnpany.Skokae, model 8525 /. These instruments shall be positioned directly above or below the air movement sample up or down, respectively.

When the air is moving upwards, a slight rise in the tobacco is observed at the moment when the air passes at an average speed of about 26 ft / min or 0.13 m / s. Then small air channels are formed and the tobacco settles down. this air flow through the tobacco bed is very uneven / about 22 feet / min or 0.11 m / s to about 45 feet / min or 0.23 m / s

- 29 average velocity around p ^ 3 / k / se ^ -C. Increasing the velocity increases the formation of a channel * .which are visible, and at a value * above 0.23 m / s a significant blowing of the upper layer is observed. of tobacco, followed by substantial groove formation in the bed of tobacco.

When the air moves down, it is observed for some time

tobacco compaction and the corresponding reduction in air velocity through the beds of tobacco. This is shown in Table 4. At an initial velocity of about 192 ft / min or 0.975 i / s, the compaction of the bed of tobacco is about 28% and as a result the air velocity through the bed decreases to about 141 ft / min or 0.716 m / s. At an initial air velocity of about 0.716 m / sec or less, tobacco compaction is about 50% of that observed at an initial velocity of 0.975 m / s and the air flow through the tobacco bed is very slow.

TABLE 4 «a, bed ..... on, ..... speed

..... dre ^ deglowo

Air velocity / ft / min /

Thickness of Bed / Bands /

home extreme change% home extreme change% 192 141 27 2 1.45 28 161 144 11 2 1.65 18 141 1O3 6 2 1,70 15 104 98 6 2 1.80 10 43 41 5 2 1.90 5 Note: 100 ft / min “0.508 m / s 1 inch = 2.54 cm Voz the basis of above experience · it is determined that the swollen tv * can be preferably re-humidified by increasing n <

linear law under the following conditions:

- 30 ·· ·· • · ·. ::: ./: ·.

/ a / Time: About 60 minutes to reach / 30 flint. '• · · · · · *

L / W: from an initial value of about 30 / - 45 / to an end value of about 60% - 64%;

/ c / Temperature: from about 75 ° F to about 95 ° F or from 23.89 ° C to 35 ° C;

/ d / Airflow velocity: up to 45 ft / min or 0.23 m / s down to 235 ft / min or 1.19 m / sec.

ISHMYAO ..... 5

A mixture of light tobacco and tobaccoWag8-eu impregnated with carbon dioxide according to the method described in (3), in an amount of approximately 55.95 kg / h and blown as described above, is passed through a cooling conveyor to reduce its temperature from 92.33 ° C to 29.44 ° C before being fed to a self-priming spiral conveyor of ossapf, model QCP 42. The flow of tobacco through the spiral device is from the bottom to the top. The air flow is from the top of the device downwards, t .f. This device provides re-humidification of the tobacco with a linear increase as a result of prolonged dehydration and the air from the tobacco. The incoming tobacco is 3 / 0V and the tobacco at the end of the treatment is 11% 0 /. the feed value of the feed material is about 10.53 cm / g, while the equilibrium value ia the CV of the re-moistened material is about 10.46 cm ^ / g without a significant loss of tobacco resistance during the process, i. no statistically significant loss of stability as determined by the standard analysis and variant process. In addition, no measurable reduction in the size of the tobacco particles, as determined by the smet analysis, was observed during re-wetting.

- 31 Excipients Μ 6 .-.:.: 7-.:.-- ^-

A series of experiments were carried out using tobacco in different forms and coplfee swollen at different temperatures. In these experiments, the tobacco was re-moisturized according to the method of the present invention. In each batch approximately 55.95 kg / h of tobacco based on the re-moistened tobacco mass is subjected to re-humidification in a self-inflated spiral device of Experiment 5. The air entering the device is at a temperature of 29.44 ° C and a relative RH of about 62%. The air exiting the device is usually at a temperature of from 32,22 ° C to 35 ° C and relative humidity FH from 40% to 45%. As shown in Table 5, the tobacco subjected to re-humidification according to the method of the present invention does not show a significant loss of stability.

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Experiment and 7 .. · ...........

Approximately 74.6 kg / h light tobacco with 0V approx

21.6% is fed to a modified self-filling device described in Experiment 5, which acts as a drying device

The flow of tobacco through the spiral drying device is from the bottom to the top. The air flow is from the top of the device down to the bottom, ie. The tobacco is successfully dried to about 12.2% 0V for about 60 minutes using air with an inlet temperature of about 35 ° C and an inlet relative humidity of about 35%. 33 ° C and about 62% relative humidity. The inlet and outlet tobacco is cooled to 23.33 ° C. This temperature indicates that the tobacco is not subjected to heat treatment. There is no change in the equilibrium value of the tobacco CV as a result of the drying. to minimize heat treatment. Similar drying results would be achieved using a high temperature controlled heat treatment.

From the described preferred embodiments and the present invention, it will be apparent to those skilled in the art that various changes can be made in the form and details without departing from the spirit and scope of the invention.

Claims (33)

I. Method for increasing the moisture content of organic material (characterized in that it comprises the following steps: (a) contacting the organic material with an air stream having a relative humidity close to the equilibrium conditions of the organic material, and / c) increasing the relative humidity of the air stream in contact with the organic material to increase the moisture content in the organic material in such a way that the relative humidity of the air stream in contact with the organic material is maintained close to the equilibrium conditions of the organic material until the desired content of the organic material is reached Aga in the organic material. Method according to claim I, characterized in that the CV value of the organic material at equilibrium after step (c) is not significantly less than the CV value of the organic material at equilibrium before step (a). 3. A method for increasing the moisture content of an organic material, comprising the following steps: (a) forming a bed of organic material by superimposing organic material on a conveyor, / c / contacting the organic material with an airflow directed along a trajectory opposite to the trajectory of the bed of organic material, and / c / transferring a portion from the moisture content of the air stream to the organic material in such a way that the relative humidity of the air stream in contact with the organic material is maintained close to the equilibrium conditions of the organic material, by which the air flow decreases it is dehydrated and the organic material is progressively moistened as the air becomes dehydrated. . ·. ··. . ··· ·: *. ·. _β ·. their flow changes in the direction of rotating the organic material until the desired moisture content of the organic material is reached. Method according to claim 3, characterized in that the CV value of the organic material at equilibrium after step (c) is not significantly lower than the GV value of the organic material at equilibrium before step (c). Method according to any one of claims I to 4, characterized in that the temperature of the organic material is lower than 38 ° ΰ / 100 ° / / before it enters contact with the air stream. Method according to any one of Claims I to 5, characterized in that, before the contact of the organic material with the air stream, the organic material has an initial moisture content of from about 1.5% to about 13%. A method according to claim 6, characterized in that before the step of contacting the organic material with the air stream, the organic material has an initial moisture content of about 1.5% to about 6%. A method according to claim 3, characterized in that the desired moisture content of the organic material after step (c) is from about 11% to about 13%. Method according to any one of the preceding claims, characterized in that the air flow contacting the organic material has a relative humidity of about 30% to about 64% at a temperature of about 2I ° C / 70 ° F / to about 49 ° C / I20 ° F /. Method according to any one of the preceding claims, characterized in that the air flow temperature is selected in order to provide the desired thermal treatment of the organic material, while the relative humidity of the air stream is selected in order to provide re-humidification. - 36 from • ·· · · ::: ··· 11. The method according to each of the Lrayish preteashes, characterized by ............. smelling of the organic material being tobacco. A method according to claim II, wherein the tobacco is swollen. Method according to claim II, characterized in that the tobacco is selected from the group consisting of: puffed or non-puffed tobacco, whole tobacco leaves, shredded tobacco, tobacco stems, reconstituted tobacco or any combination thereof. 14. A method of reducing the moisture content of an organic material, comprising the following steps: (a) contacting the organic material with an air stream having a relative humidity close to or lower than the equilibrium conditions of the organic material, and (c) reducing the relative humidity of the air stream contacting the organic material, since the moisture content of the the organic material is reduced in such a way that the relative humidity of the air flow in contact with the organic material is maintained at or below the equilibrium conditions of the organic material until the desired vessel is reached moisture retention in the organic material. A method according to claim 14, characterized in that the value of the CV of the organic material at equilibrium after step (c) is not significantly lower than the value of SU of the organic material in equilibrium before step (a). 16. A method of reducing the moisture content of an organic material, comprising the steps of: (a) forming a bed of organic material by depositing the organic material on a conveyor, / c / contacting the organic material with air flowing in a direction opposite to the direction of the bed of organic material, and • · - 37 / s / we pass in part _; of the organic material to the air stream in such a way that the relative humidity of the air stream in contact with the organic material is maintained near or below the equilibrium conditions of the organic material, by which the organic material is progressively dehydrated. and the airflow is progressively moisturized as the airflow passes in a direction opposite to the direction of movement of the bed of organic material until the desired moisture content of the organic mat is reached. Rial. 17. The method of claim 16, wherein the steady-state value of the organic material after step (c) is not significantly lower than the value of the steady-state organic material before step (c). Method according to any one of claims 14 to 17, further comprising the step of preheating the organic material at a temperature of from about 38 ° C / I00 ° F / to about I2I ° C / 250 ° F / before stage / a /. A method according to any one of claims 14 to 18, characterized in that the organic material temperature is lower than I2I ° C / 250 ° F / prior to the stage of contact with the air stream. 20. The method of claim 19, wherein the temperature of the organic material is lower than 38 ° C / 100 ° F / prior to the step of contacting it with the air stream. A method according to any one of claims 14 to 20, characterized in that, before the contact of the organic material with the air stream, the moisture content of the organic material is from about II% to about 40 ^z . A method according to any one of claims 14 to 21, characterized in that the air flow in contact with the organic material has a relative humidity of about 20% to about 60% at a temperature of about 21 ° C. 120 F /. QQ - * ··· ♦ · ·· ...... • ::: *:: · * · ·. 23. A method according to any one of H ^ MbTb'ot / H.-AO 22, characterized in that the temperature and air flow are selected in such a way as to provide the desired heat treatment. A method according to any one of claims 14 to 22, characterized in that the air flow temperature is selected so that substantially no heat treatment is carried out. A method according to any one of claims 14 to 24, characterized in that the air flow temperature is from about 24 ° C (75 ° F) to about 121 ° C (250 ° D). A method according to any one of claims 14 to 25, characterized in that the organic material is tobacco. Method according to claim 26, characterized in. that the tobacco was cut. The method of claim 26, wherein the tobacco is selected from the group consisting of: puffed or non-puffed tobacco. sings tobacco leaves, cut tobacco, tobacco stems, recovered tobacco, or any combination of them. A method according to any one of the preceding claims, characterized in that the step of contacting the organic material with the air stream is carried out in a continuous manner using a helical conveyor in which the air flow passes in a direction opposite to the direction of movement of the air. the flow of organic material. A method according to any of the preceding claims, characterized in that the step of contacting the organic material with the air stream is carried out in a continuous manner using a linear conveyor. 31. The method of claim 30, wherein the linear conveyor is designed to provide multiple zones of increase in relative humidity. -39'4. ··. . · 32. A method according to any one of nptfterfilM, characterized in that the step of contacting the organic material with the air stream is carried out using an air stream at a speed of about 0.23 m / sec / 45 feet / min / to about 1.22 m / sec / 240 ft / min /. A method according to any one of the preceding claims, characterized in that the step of contacting the organic material with the air stream is carried out by directing the air flow either down or up through the bed of organic material or by directing the air flow together downwards. and up through the bed of organic material. A method according to any one of claims I to 10 or to 14 to 25, characterized in that the organic material is hygroscopic organic material. Method according to claim 29, characterized in that the hygroscopic organic material is selected from the group consisting of: fruits, vegetables, cereals, coffee, tea, pharmaceuticals and any combination thereof. A method according to claim 29, characterized in that the helical conveyor comprises an ordering device having multiple floors, and the air flow passes through that device sequentially through the floors.