Method and installation for drying fluids to give powders after spraying

Abstract: A method for drying fluid (1) concentrates, after spraying, to give a powder, which concentrates, as drying progresses, display a so-called critical moisture content point in which method the fluid to be dried is sprayed in a hot first drying gas (2) of which the inlet temperature and the amount of the first drying gas are so chosen that the product (1) to be dried acquires a moisture content which is approximately equal to the critical moisture content point after which, by means of a second, freshly supplied drying gas (5), the drying of the product is continued to the equilibrium point, the sprayed product being collected after a certain time on a porous screen element, and the drying gas being completely or substantially drawn through the screen element and transported to a gas outlet, while the drying product forms a porous layer and the exhausted first drying gas is mixed with an amount of added second drying gas in a mixing layer, close above the permeable product layer on the screen element, in which mixing layer the two drying gases and the product are subject to a virtually complete mixing.

Description: The invention relates to a method for the preparation of powders, in which the starting material in the form of fluid concentrate is, in some way or other, sprayed in a first step in a hot first drying gas and is dried by the spray-dry principle, to give particles having a moisture content corresponding to the critical moisture content, which particles are further dried in a second step, using a second and cooler drying gas in accordance with the flow-through principle, to give the moisture content corresponding to the equilibrium moisture content, after which the product can be post-dried in a possible third step, using a third drying gas, to give the desired final moisture content. The term powders comprises products which, during conventional drying, after spraying, are subject to product and quality losses, which can be influenced by the product temperature and the rate of drying during the drying path. The concepts constant rate, falling rate and equilibrium rate as the three phases in the drying of particles are explained in more detail hereinafter. The invention also relates to an installation for carrying out the method. The following methods and installations are frequently encountered in the current state of the art: A. Two-phase drying, in which the sprayed product is dried using a hot first drying gas to approximately the equilibrium moisture content and is then post-dried using a second drying gas, in, for example, a fluidised bed, as in US-A-3 956 521 (NL-A-7 413 829). The sprayed product dries in a spray chamber, in which the drying particles touch neither one another nor the walls and have reached the equilibrium moisture content after about 23 seconds, after which they leave the drying chamber and are post-dried, either via the cyclones or directly in a post-drying installation, such as, for example, a fluidised bed, to the desired final moisture content. In this two-phase drying, about 19 kg of drying gas are used per kg of solvent to be evaporated. The first drying gas thus serves for product drying in both the constant rate phase and the falling rate phase, only the falling rate phase being determining for the inlet/outlet temperature combination of the entire drying path through the constant rate phase and the falling rate phase. Disadvantages of this method are: The powder product quality is not optimum because the optimum (slow) drying rate is not complied with in the falling rate phase and the product temperature is also unnecessarily high in this phase, as a result of which losses in quality occur, such as solubility, colouring power, emulsifying action, crushing volume, etc. The energy consumption is high, because it is necessary to work with large amounts of fairly cold drying gas in connection with the quality requirements, which can only be influenced in the falling rate phase, while the building size demands a fairly large driving force between outlet drying gas residual moisture/product equilibrium moisture content, so that the outlet drying gas has only a low residual moisture at a high outlet gas temperature, which combination is very far removed from an equilibrium condition desired from an energy standpoint. B. Modified two-phase drier in accordance with DE-A-1729439, in which a first drying gas serves for evaporation in the constant rate and the falling rate phase and a second drying gas ensures fluid evaporation in the equilibrium phase. The particular method, introduced for reasons of energy saving, is that some of the drying does not take place in the spraying chamber but the product is collected with a residual moisture content of about 13% on a screen belt, on which the product remains and forms a porous layer permeable to the drying gas, while all or the bulk of the drying gas is drawn through this porous layer and the screen belt and removed. The porous layer is further dried by the drying air passing through, in accordance with the flow-through principle, to a moisture content corresponding to the equilibrium moisture content and is transported by means of the screen belt to a subsequent drying chamber for post-drying to the desired final moisture content. By applying this method, the spray chamber can be made smaller and less first drying gas can suffice, which drying gas is also cooled, as a result of the long residence time of the product in the porous layer, to a lower outlet gas temperature and a higher residual moisture. The drying gas required is about 14 kg per kg of evaporation. The residence time in the drying chamber above the porous layer is about 14 seconds. The disadvantages of this method are: The product must be dried in the spray drier section to far into the falling rate phase, since the input moisture content in the post-drying compartment must be so low that the fresh drying air does not give rise to case hardening. The maximum moisture content must be approximately the moisture content associated with the equilibrium moisture content. Since the product is dried with a single type of drying gas in the constant rate and falling rate phase, while the residence time of the product in the falling rate phase is very long, the product must be deposited on the porous layer with a moisture content at which no further denaturing can occur. As a result, the product must be dried in the spray-dry section to far into the falling rate phase. There is thus a residual energy advantage because, due to a longer residence time, a better equilibrium can be found between the residual moisture content of the waste air and the moisture content of the product. However, this advantage which arises and is caused by the long residence time is offset by the restrictions on the inlet temperature of the drying gas. On grounds of product quality, the wet-ball temperature (= the minimum product temperature) must also be sufficiently low to prevent denaturing during the very long residence time in the flow-through section during the remainder of the falling rate phase. The wet-ball temperature is a function of the inlet drying gas temperature. Thus, on these grounds also, a restricted inlet drying gas temperature can be chosen. In practice, the inlet drying gas temperature is found to be equal to or somewhat lower than the inlet drying gas temperature for a two-phase drier. C. Three-phase drying, in accordance with US-A-4,362,273, in which, for reasons of product quality, two types of gas are admitted into the drying tower for drying the product to approximately the equilibrium moisture content (and optionally a third gas for post-drying). The two gases admitted into the drying tower are: A hot drying gas essentially for evaporation in the constant rate phase. A cold drying gas, fed into the drying tower at the top and mixed with the drying gas after the constant rate phase drying with which the drying in the quality-determining falling rate phase tees place. The advantage of this method is a very good product quality. Disadvantages are an appreciably greater energy consumption and larger dimensions of the spray chamber, determined by a residence time of > 23 seconds and the requirement of, in total, about 25 kg of drying gas per kg of moisture to be evaporated. Given the fact that the abovementioned methods belong to the current state of the art, it can be stated that it is still the case that an optimum powder quality cannot be achieved other than with significant expenditure on energy costs and with the use of large spray chambers. The object of the present invention is to improve drying fluid concentrates. This object is achieved by providing a method according to claim 1 and an installation according to claim 9. By application of the new method it has been found to be possible to substantially improve this situation, by achieving an optimum product quality with a substantially reduced energy consumption and also reducing the space requirements for the drying. With the new method, the evaporation process is divided into at least two parts: a spray-drying for the constant rate phase using a hot first drying gas entirely suited for drying in this first phase only, a flow-through drying for the falling rate phase, using a second drying gas, which can be arbitrarily chosen and is entirely suited for drying in this second phase, (and, if appropriate, a post-drying using a fresh drying gas suited for the equilibrium phase drying). A particular feature in this new method is the strict division of tasks of the three drying gases, which are made up independently of one another, and the use of large amounts of cooler, second drying gas as a constituent of the drying gas for the second phase. The effect of large amounts of cool drying gas was surprising to experts and accepted as established only after a number of measurements. In drying practice the admission of a cool gas during drying has always been avoided in order to prevent energy loss. In the new method, spray-drying of the concentrate during the constant rate phase is carried out by means of a hot first drying gas which, at the end of said phase, has a very high residual moisture content and cannot dry the product further. The partially dried product is now collected on a screen, which is permeable to gas and on which the product forms a porous layer permeable to a drying gas, the drying gas flowing through this layer and flowing via the screen to the outlet (outlets). The layer through which the gas flows is further dried, in flow-through drying, to equilibrium. For drying at the correct rate and at an adequately low product temperature in this flow-through section, a second drying gas is used which is composed of the exhausted first drying gas and a freshly added drying gas, the inlet temperature and the amount of which determine the desired product temperature, which is determined by the wet-ball temperature of the mixed drying gas and the initial residual moisture content of the drying gas. The effects on the product quality are very favourable. As a consequence of the application of drying at a low product temperature, specifically in the falling rate phase, and the relatively very long time which is available for drying in the flow-through section, a significant gain in quality is achieved for the majority of products, there also being a large energy advantage, and it being possible both to set a desired product temperature and a desired low drying speed. In addition, the space requirement for the spray chamber is substantially smaller; this is now determined by the maximum residence time of the product in the spray chamber of 5 seconds and a first drying gas amount of about 6.5 kg per kg of drier capacity. Backgrounds to the drying process. The drying of a sprayed particle proceeds in three phases, as shown in Fig. 1. A constant rate phase, in which the rate of evaporation is not linked to the moisture content of the particle but only to the drying power of the drying gas, essentially determined by the difference in vapour pressure of the drying air and that in the particle, which latter is dependent on the particle temperature. The falling rate phase, in which the rate of evaporation is subject to limits and is lower the lower the moisture content of the particle, passing into the equilibrium phase, in which the particle is free from non-bound moisture and goes to an equilibrium moisture content determined by the vapour pressure of the surrounding gas. The transition point between the falling rate phase and the equilibrium is the equilibrium point; this point is interpreted somewhat more broadly in the description of the new drying method. The transition point between constant rate and falling rate is the critical moisture content point, abbreviated as CMP. This point also is interpreted somewhat more broadly in the description of the new drying method. The moisture contents at CMP and equilibrium point are product-specific. Concluding remarks By means of a product temperature which can be chosen to be low and a drying rate in the falling rate which can be chosen to be low, optimum product quality can be achieved without concessions in respect of energy consumption. The new method is very suitable for the use of low-calorie heat, for example for the application of the total energy principle to the waste air fan drive. An extremely low energy consumption also results if the new method and installation are used in an environment where sufficient low-calorie waste heat is available at about 50° C for use as pre-heating for the first drying air in spraying and as a heat source for the second and third drying gases to be added. (In this context we are thinking of an evaporator/drier combination process in which water of condensation and/or condensate is used for heating the air for the drier). Another advantage of the new method and installation results from the very high residual moisture content of the outlet gas, as a result of which (partial) condensation with a view to the separation of substances, such as solvents and/or odours, from the outlet gas is possible in a simple manner and no cyclones are needed, but a simple wet scrubber can suffice to meet the most stringent environmental requirements relating to the outlet gases. Finally, it must be regarded as striking that the new method and installation lead to very much smaller dimensions of the building, the reductions in volume being very much larger than 50% compared with installations in accordance with the current state of the art. For example: Powder tower for the production of 500 kg of skimmed milk powder per hour: Single-phase drying Cylinder diameter 6 metres Cylinder height 6 metres Cone height 6 metres Building size 15 x 10 x 16 metres high, i.e. 2,400 m 3 New drier: Ground area is 3 x 2 metres Height 4 metres Building size 10 x 5 x 6 metres high, i.e. 300 m 3 Description of the new installation Fig. 2 is an example of the construction of an installation for the new method. First step: spray-drying The fluid (1) to be dried is sprayed in some way or other into a hot jet of drying gas (2) in a spray-drier section (3). The sprayed particles and the drying gas move in virtually the same direction (co-current drier). The spray-drier section passes at A-A' into a mixing region for two types of drying gas. At this transition location, the following conditions of drying product and drying gas prevail: (before mixing starts). The solids content of the product is approximately equal to the content, for example 60%, at the CMP. The vapour pressure in the drying gas has become virtually the same as the surface vapour pressure of the particle, so that the drying gas has a very high residual moisture content and a low dry-ball temperature. In order to maintain these conditions, the inlet temperature of this drying gas (2) is controlled in accordance with the amount of fluid to be evaporated which is added. The amount of drying gas (2) is in principle kept at a constant value by means of the adjustable, but constant, capacity of the feed fan(s). The inlet temperature is controlled as a function of the residual moisture content of the exhausted first drying gas. Second step: flow-through drying A fairly large amount of fresh drying gas (4) is drawn into the mixing region (A-A'/B-B') vertically or virtually vertically to the direction of flow of drying gas (2) and product when passing through the first phase. This can be effected from several directions. Partly as a result of the fairly high speed of this incoming dry gas, a complete or virtually complete mixing with the exhausted drying gas from the first phase occurs. This mixing takes place mainly in the air mixing layer between A-A' and B-B'. The amount of drying gas (4) is so chosen that, after mixing with drying gas (2), a specific desired wet-ball temperature results, a larger amount of drying gas (4) leading to a lower wet-ball temperature. The drying power of the said drying gas also depends on its relative humidity. By adjusting the temperature of the drying gas (4) freshly introduced, this relative humidity of the mixing gas is brought to the desired value. The drying gas produced by mixing is then drawn through perforation D-D', the product, which remains behind, forming a porous layer B-B'/D-D' permeable to the drying air. Under the influence of the mixed drying gas in the entire region A-A'/D-D' the product cools to the new wet-ball temperature and moisture is released into the drying gas, as a result of which this gas thus becomes more moist and its temperature is lowered. In this way, the further drying takes place until the product has reached the solids content of the equilibrium phase and the falling rate has gone to completion. Third step: equilibrium drying: The product which has passed through the flow-through drying of the second phase can now be post-dried in another flow-through drying section. Here a fresh drying gas (6) with a high drying power is again added. This drying gas has a low residual moisture content and a temperature of 20-70° C. In this third drying phase the product assumes the dry-ball temperature of the drying gas used here. (The waste gas (6) from this drying can be used directly as admix gas for the second phase; the moisture uptake in the third phase is low, so that the temperature of the gas is still high enough and the moisture content low enough to be used as part of the dry gas to be admixed for the abovementioned second phase). The optional product cooling after the third phase has gone to completion can also take place in a flow-through section. In this case also, the waste gas (8), which is warmed by the cooled product, can usefully be used as a constituent of the amount of drying gas (4) to be admixed for the second phase. The exhausted gas from the first, the second and, insofar as desired, also the third cooling phase is drawn off below the perforation via so-called waste air compartments (7a, 7b, 7c), connected to a central suction unit. Mutual distribution of the amounts of drying gas drawn off per compartment can be effected simply by means of (manually adjustable) channel resistances per compartment. This is important for the adjustment, which may be necessary, of the mixing process of the drying gas types (2) and (4) above the porous layer. In the case of process control of the new installation it is important that once a mixing ratio between the amounts of first drying gas (2) and added second drying gas (4) has been chosen, this ratio is maintained. Assuming a fixed amount of hot drying gas (2), it is necessary only to adjust to a constant amount of total gas to be removed and to maintain this value automatically by means of the discharge valve(s). The temperature control of the total amount of drying gas (4) to be admixed takes place via measurement of the temperature on entering the mixing layer and adding the desired amount of heat to the drying gas (4). In this operation exhausted drying gas which may have originated from the abovementioned third drying phase and/or the cooling is carried over, with the heat absorbed therein, so that the fresh gas (5) still required to make up to the total amount of drying gas (4) is provided with the thermal energy which is still lacking. By measuring the wet-ball temperature of the gas in the waste air compartments below the flow-through drying sections and using the measured value for adjustment of the temperature of the drying gas (4) to be admixed, the drying process can be controlled automatically in the flow-through drier section. The spray-drying section can be controlled automatically by the abovementioned modifications of the inlet air temperature in accordance with the changes which occur in the amount of fluid supplied, which is to be evaporated, by measuring the residual moisture content of the exhausted drying gas (2) close to the gas mixing layer. Tests A series of tests were carried out in a test drier constructed specifically for this purpose. The drying chamber has a height of 1.80 metres above the perforated drum and is also 1 x 1 metre in the horizontal plane. The drum has a diameter of 1.5 metres. The size of the perforations was found not to be very critical and can be very many times greater than the particle diameter without any problems and without particles passing through. The drying gas for the mixture for the flow-through section for the falling rate phase was supplied at (4) and the side opposite hereto. The post-drying took place using tertiary drying air which flowed from below through the perforated drum and the porous layer. The tertiary air was then mixed with the secondary air at (4), while this mixture was further mixed with primary air in layer AA'/BB'. Test 1 Test 2 Skimmed milk concentrate 45% 47% Inlet temperature of primary air 226°C 400°C Amount of primary air 800 kg 800 kg Dry-ball temperature of primary off-gas 49°C 52°C Relative humidity 100% 100% Product solids content above mixing layer 59% 61% Inlet temperature of secondary drying air 8°C 10°C Relative humidity 20% 75% Product solids content after 1st flow-through 91% 89% Waste air temperature 7a 28°C 25°C Waste air temperature 7b 36°C 29°C Waste air temperature 7c 32°C 27°C Total waste air 13,200 kg 18,000 kg Dry-ball temperature of tertiary drying air 50°C 55°C Final moisture content of product 3.2% 3.4% Nozzle pressure 35 bar 50 bar s.i. ADMI < 0.1% < 0.1% Crushing volume 730 745 Specks soluble cold none none Characteristic features are: The very low nozzle pressure and thus a large particle does not influence the s.i., the crushing volume and the cold solubility. The high inlet temperature (400°C) does not influence the powder quality. The crushing volume is exceptionally high. The good permeability of the porous layer. 110 mm difference in pressure for a 12 cm product layer. This is lower than when a fluidised bed is used for virtually dry powder. The high xt over the spray section 400-52° C. The low temperature of the secondary air is striking. Drying after mixing cannot be explained by a Mollier diagram.

Claims: Method for drying fluid concentrates, after spraying, to give a powder, which concentrates, as drying progresses, display a so-called critical moisture content point CMP, this being a solids content above which "case hardening" or cornification occurs if drying is too rapid, and which concentrates, during drying at certain solids contents of the concentrates, are subject to denaturing, this denaturing being the greater the higher the temperature which then arises and the longer the residence time in the region, in which method the fluid to be dried is sprayed in a hot first drying gas and dried until a specific average solids contents has been reached in a first drying step, after which, by means of a second, freshly supplied drying gas, and after mixing with the first drying gas, the drying of the product is continued in a second drying step, in which the drying is continued to the equilibrium point, a solids content above which the product is not subject to case hardening and denaturing, after which, in an optional third drying step, the drying of the powder to the final moisture content can take place using a third freshly supplied drying gas, and in which method the sprayed product, which first travels a path which is on average virtually vertical, under the influence of drying gas and gravity, is collected after a certain time on a porous screen element, the drying gas, which at that time surrounds the product, being completely or substantially drawn through the screen element and transported to a gas outlet, while the drying product forms a porous layer during this operation, which porous layer is further dried by the gas passing the porous layer and the screen element, the porous layer being moved, by moving the porous screen element, to outside the flowed-through section and, finally, being separated from the screen element and removed, wherein it is ensured that: a) the inlet temperature and the amount of the first drying gas are so chosen that the product to be dried acquires, as a result of drying with said first drying gas, a moisture content which is approximately equal to the critical moisture content point CMP, the inlet temperature of the first drying gas being chosen between 125°C and 750°C, b) the inlet temperature and the amount of the first drying gas are adapted only for the drying of the product to virtually the CMP and are not adapted for drying the product at moisture contents lower than the CMP, c) the exhausted first drying gas is mixed with an amount of second drying gas which is at most 30 times larger than the amount of first drying gas in a mixing layer, close above the porous layer on the screen element, in which mixing layer the two drying gases and the product are subject to a virtually complete mixing, d) the wet-ball temperature of the mixed drying gas, formed by the first and the second added drying gas, is adjusted to the drying requirements for the product having moisture contents lower than the CMP, by means of such an amount of the second added drying gas that the wet-ball temperature of the mixed drying gas is at least 3°C and at most 100°C lower than the wet-ball temperature of the first drying gas, e) the drying of the product from spraying to a solids content corresponding to the equilibrium point takes place in two adjacent drying sections which pass one into the other and are integrated to a whole, said drying sections being a spray-drying section and a flow-through drying section, using two drying gases specially adapted to the drying requirements of the product in each of the sections, the spray-drying section serving for drying the product to the CMP and the flow-through section for drying the product between CMP and equilibrium point, the mixing layer forming part of the flow-through section, f) the first drying gas consists of air, inert gas or superheated steam, and g) the second drying gas consists of air, inert gas or superheated steam. Method according to Claim 1, for the preparation, with a reduced energy consumption, of powders from liquid concentrates, characterised in that the reduced energy consumption is generated in that, in the first drying step, spray drying is used with a drying gas suitable for this purpose and with which the product is dried to virtually the CMP, while in the second drying step flow-through drying is used with a second drying gas suitable for this purpose, the drying gas for the first step not being suitable for drying in the second step, while the outlet gas conditions are determined by the flow-through drying process in the second step. Method according to Claim 1, for the preparation of powders, which are not denatured or are barely denatured, from fluid concentrates, characterised in that the low degree of denaturing results from the fact that, in the first drying step, spray-drying is used with a drying gas suitable for this purpose, with which the product is dried to virtually the CMP, while in the second drying step flow-through drying takes place with a second drying gas suitable for this purpose, the drying in the flow-through drier extending over a longer period and thus can take place at a lower temperature and a higher moisture content of the drying air, while the drying gas for the first step is not suitable for drying in the second step. Method according to Claim 1, for the preparation of crystallised powders from fluid concentrates, characterised in that the increased degree of crystallization results from the fact that, in the first step, spray-drying takes place with a drying gas suitable for this purpose, with which the product is dried to virtually the CMP, while in the second step flow-through drying takes place with a second drying gas suitable for this purpose, as a result of which drying in the second step takes place at a low temperature and a high moisture content of the drying air and over a longer period, while the drying gas for the first step is not suitable for drying in the second step. Method according to Claim 1, for the preparation of powders having a low fines content, characterised in that the fines content is low because, in the first drying step, spray-drying takes place with a drying gas suitable for this purpose, with which the product is dried to a moisture content virtually identical to the CMP, while in the second drying step flow-through drying takes place with a drying gas suitable for this purpose and suitable for drying the product at a slow rate at a lower temperature, while the first drying gas is not suitable for drying in the second step. Method according to Claim 1, for the preparation of powders from fluid concentrates, with the aim of forming agglomerates, characterised in that the addition of substances to be agglomerated takes place substantially together with the addition of the second drying gas in the second drying step, where flow-through drying takes place with a drying gas suitable for this purpose, while the concentrate to be sprayed is dried, in the first drying step, in a spray-drying installation with a first drying gas suitable for this purpose, with which the product is dried to virtually the CMP, while the first drying gas is not suitable for drying in the second step. Method according to Claim 1, for the preparation of powders having a high crushing volume from fluid concentrates, characterised in that the high crushing volume results from the fact that, in the first drying step, spray-drying takes place with a drying gas suitable for this purpose, with which the product is dried to a moisture content virtually identical to the CMP, while in the second drying step flow-through drying takes place with a drying gas suitable for this purpose, by which means the drying in the second step is greatly moderated and, consequently, hardly any vacuoles can form in the product, as a result of which a high crushing volume is obtained for the prepared powder. Method according to Claim 1, for the preparation of powders from concentrates, in which method condensable gases, originating from the fluid concentrate, must be completely or partially recovered from the outlet gas, characterised in that the outlet gas, consisting of a composition of exhausted drying gases from the first drying step, the second drying step, the optional third drying step for post-drying and a cooling step for product cooling, by use in the second drying step is cooled to a low temperature and has a high moisture content, as a result of which it can be cooled simply and inexpensively to below the dew point, after which the substances to be recovered can be obtained from the condensate. Installation for carrying out the method according to claims 1 to 8, characterised in that the installation comprises a spray-drying section (3) for spraying fluid concentrates, the installation further comprising: a) a first inlet (2) for the first drying gas, the spray drying section and the first inlet being arranged such that the sprayed fluid concentrates travel a path which is on the average virtually vertical; b) a flow-through drying section which forms an integrated whole with the spray-drying section, in which the two sections pass into one another, the flow-through section being placed in the vertical path of fluid travel; c) a second inlet (5) for introducing the second drying gas into the flow-through drying section; d) a curved or plane porous screen element provided below the second inlet and in the flow-through section for collecting the sprayed product, the screen element being movable out of the flow-through section and the upper surface of the screen element being parallel to the direction of flow of the gas introduced by the second inlet; e) a gas outlet for removing the used first and second drying gases drawn through the screen element and placed vertically below the flow-through section, in line with the spray drying section; and f) a wet scrubber for purifying the gases removed by the gas outlet.

Inventors: SLOB WOUTER, SLOB, WOUTER
Applicants: ROTACOM IND BV, ROTACOM INDUSTRIES B.V.
Application year: 1991
Main classification: B01D1
IPC codes: B01D1, A23C1