text:
|Publication number
|Publication type
|Application number
|Publication date
|Oct 28, 1986
|Filing date
|Oct 7, 1983
|Priority date
|Oct 7, 1983
|Fee status
|Publication number
|Heinz O. Schumacher
|Original Assignee
|Schumacher Heinz O
|Export Citation
|BiBTeX, EndNote, RefMan
|Patent Citations (19), Non-Patent Citations (2), Referenced by (23), Classifications (26), Legal Events (4)
|External Links: USPTO, USPTO Assignment, Espacenet
The invention relates to a process and apparatus for gentle, energy-saving, and non-polluting desolventizing of heat-sensitive, flaky or granulated residue material, so-called meal, that is obtained in the extraction of natural substances, particularly seeds, by means of organic solvents, said meal being treated in a continuous process with steam or with a steam-containing fluid and being thereby freed of solvent.
By, the process and the apparatus adapted for carrying out said process in accordance with the present invention involve such processes by which the solvent shall be substantially, if not entirely, driven out of solvent-wet extraction residue. Such meals, besides containing up to 22% by weight and more moisture, may still contain 25% by weight and more, occasionally even up to 35% by weight, of solvent. These considerable quantities must be recovered not only on grounds of the economy of an extraction plant; there must also be obtained desolventized meals which allow safe shipment and further utilization without any hesitation or objection.
Addressed by the invention are particularly such solvent-wet meals as are obtained in the extraction of seed material, such as soybean, rape, sunflower seed, turnip seed, nut material, etc. in the oil and fat industry with the aid of preferably low-boiling point hydrocarbons. The solvents or extractants used for this are, inter alia, benzene, propane, butane, pentane, hexane or mixed solvents, such as mixtures of the above-mentioned hydrocarbons with alcohols, ketones or quite generally polar solvents etc.
The so-called miscella formed in the extraction of the above-mentioned raw materials with the respective suitable solvents and consisting of solvent and oils and fats dissolved thereby is separated from the residue (meal) and passed on for further processing (purification, distillation, driving off of solvents, etc.).
The residue of the extraction, i.e. the above-mentioned meals consisting of residue material, solvent and water, is treated in the desolventizing apparatus with a view to recovering the solvent and obtaining a low-solvent or solvent-free meal, as already indicated above.
Processes and apparatus suitable for this desolventizing have long been known in the and are offered by the respective industry as a under the terms toaster, desolventizer, drier or steamer in many, more or less efficient designs. The extraction residue is freed substantially from the adhering solvent by steam or steam-containing fluids, and the solvent is returned to the extraction apparatus in a mostly continuous operation.
The U.S. Pat. No. 2,585,793 discloses a so-called toaster designed particularly for extracted soybean flakes (soybean meal) wherein, in the upper region of a multistage or multi-compartment system, the desolventizing, and possibly also the drying, is effected by direct feeding-in of steam into the solvent-containing material.
A known desolventizer frequently used in the field of the industrial production of oils and fats, which is based on the principle of the counter-current action of steam and, if necessary, hot air on the solvent-wet meal and derives from development work of the applicant of the present invention, is described in "Fette-Seifen-Anstrichmittel", 78 (1976, pages 56-59.
This apparatus, which is also designated as "Desolventizer-Toaster-Drier-Cooler" (TTK), operates fully continuously, and in the desolventizing stage thereof, pure steam is used.
Therein, the solvent-wet material being continuously introduced through a sluice or valve is conducted in opposition to the steam in a closed, vessel of one-compartment or multi-compartment design and constantly moved or agitated on the bottom or bottoms downwardly defining the individual compartments by multiarm agitator elements secured on a central agitator shaft. After a predetermined time, the material will either get into the next following stage or be discharged from the apparatus through rotary valves or sluices. During this process, the treating medium, i.e., in the special case of desolventizing, the steam, is fed, through the compartment bottoms, which are in the form of double bottoms, and through the perforated upper bottom plate, into the compartment adjoining the latter. The steam for the desolventizing, or hot air for the subsequent drying (in a succeeding compartment), streams through the material being agitated on the perforated plate by the agitating elements and leaves the apparatus, together with the driven out solvent, as so-called vapors.
Multi-compartment devices or systems of this type in many cases serve also for simultaneous drying and cooling of the desolventized material, the desolventizing taking place in the uppermost or first compartment of the multistage system.
In the apparatus or device known from "Fette-Seifen-Anstrichmittel (loc.cit.), the solvent-wet material (meal) thus is desolventized by direct steam action through the perforated upper plates of the double bottoms. The meal having been desolventized--either with or without subsequent drying and cooling--leaves the plant in a continuous stream as a low-solvent or "solvent-free" material. Thereby, there are achieved extremely uniform retention times and uniform admission of steam or subjection to steam, results which have to be rated as especially significant advantages of the known apparatus.
An apparatus also operating with a perforated double-bottom is described in U.S. Pat. No. 2,776,894. However, in view of the general apparatus structure of this device, it is necessary for achieving a fairly satisfactory degree of desolventizing additionally to introduce direct steam into the material above the bottoms. This results in overheating, agglutination of material, and unusually high steam consumption.
DE-C 26 08 712 relates to an apparatus serving the same purpose wherein live steam is introduced into the vessel in a multi-compartment system through the lowermost steam distributor thereof being constructed as a perforated or sieve bottom and is caused to stream upwardly, through likewise perforated intermediate bottoms between the compartments, in opposition to the solvent-wet material throughout the entire height of the vessel. Additionally, each stage or compartment can itself be supplied with steam through further steam inlets, so as to prevent supersaturation of the upwardly streaming steam or condensation of said steam in the upper, cooler areas of the device. Also, the additional feeding in of steam into the individual compartments makes it possible to maintain or adjust a desired temperature profile within the entire system. The apparatus according to DE-C 26 08 712 already attains a relatively uniform distribution and admission of steam, which is due especially also to the throughgoing perforation of all the bottoms, and, thus, also of the bottoms between the compartments or stages. In this apparatus, the material is treated very gently, and the expulsion of solvent is brought to very low residual values at low steam consumption as well as improved general efficiency in regard to energy.
Another publication that must be considered as belonging to the state of the art is DE-C 11 33 969, which describes an apparatus having hollow bottoms centrically arranged about the centrically disposed vertical rotary shaft. The hollow bottoms fill or occupy only a portion, preferably only one half of the cross-section of the apparatus, so that steam can be admitted only to that portion of the bottoms. In this known apparatus, it is provided that the intermediate bottom assembly comprises a plate having upwardly open perforations through which additional steam can be fed in while the principal amount of steam comes directly into the individual compartments (stages) through laterally arranged connection pieces.
However, with all systems or apparatus of the described type that are known so far and which are equipped with simply perforated bottoms, it has been found that plain perforation bores result in the formation of so-called steam channels whereby uniform admission of steam to the material to be desolventized is permitted only conditionally, so that a considerable portion of the steam introduced streams through the material unused and, thus, leaves the plant unused. The attained degree of desolventization is extremely inadequate. Fairly usable, i.e. low-solvent, meals can be obtained only by considerable additional input of steam. However, the additional input of steam jeopardizes the economical operation of all these systems, especially as an increased input of energy is required also for the drive of the agitator means in order to overcome the resistance of the wet material in case of the material being subjected to large amounts of steam.
Further, of importance is also the fact that simple perforations in the bottoms are continually clogged by meal particles lodged therein, particularly when an agitator sweeps over the bottom to agitate and turn round the material. The friction of the material on itself or in contact with the agitator elements and with the surface of the bottom results in a continuous comminution of the meal which favors the penetrating of the particles into the holes or perforations in the bottoms.
For this reason the bottoms according to DE-C 26 08 712 already have slightly rounded-off holes or perforations whereby the particles of material that have got into the holes are again ejected therefrom in the manner of a Venturi system. Moreover, by the rounding-off of the edges of the holes it is possible to largely diminish the danger of the formation of steam channels.
In the course of the further development of processes and apparatus for the technical desolventizing of extraction residues of the type referred to above, it has now been found that it is possible to totally meet the requirements of controlled and uniform distribution of steam in the material to be desolventized, of preventing the formation of steam channels (and, consequently, increased, unused, steam consumption), of preventing the cominution of material on the compartment bottoms, and overheating, and steam condensation, as well as preventing particles of material from entering into the perforations in the bottom, while achieving at the same time increased yield and efficiency in regard to material and energy (steam consumption, energy for driving the agitator shaft, throughput of material per unit of time, solvent content in the desolventized meal, degree of recovery of solvent, etc.), if--starting from an apparatus according to DE-C 26 08 712, or, alternatively, from the apparatus known from "Fette-Seifen-Anstrichmittel" (loc.cit.)--the following features are provided
(a) the bottom plates of a multistage or multi-compartment system are in the form of double bottoms capable of being heated by means of steam, the bores of the perforations in said double bottoms being formed by individual distance pieces or spacers each having a bore therethrough, the cross-section of the bores being such as to allow the passage of upwardly streaming steam or steam-containing fluid, but not the passage of the material being moved or agitated on the bottoms;
(b) the steam being used for desolventizing is present in superheated form at a temperature of at least 120° C. (248° F.) (normal pressure);
(c) at least 45%, but particularly all, i.e. 100%, of the superheated steam or of the steam-containing fluid is introduced through the lowermost compartment bottom;
(d) the temperature of the escaping vapors consisting of steam and solvent is about 64°-69° C. (147.2°-156.2° F.), particularly between 66° and 68° C. (150.8° and 154.4° F.).
The combination of the features underlying the process according to the invention obtains for the first time a desolventized material (meal) that contains practically no solvent (extractant) or the solvent content of which is so low that the limits of toxicity as well as the ranges of possible development of explosive compositions are not exceeded.
Moreover, there does no longer occur condensation of steam on the individual perforated plates downwardly defining the treatment stages or compartments, or also inside the material being desolventized, does not occur. This is so because the design of the perforated plate, the use of superheated steam, and the constantly recurring redistribution of the superheated steam upon its exit from the perforated plates results in a so-called stripping process which causes uniform carrying out or removal of solvent without any formation of channels, eliminates at once any local condensation of steam, keeps the solvent-wet or partially desolventized material on the upper bottoms in a uniform state of suspension, thereby also relieving the driving shaft of the agitator system and eventually making possible the attainment of a temperature of the escaping vapors which comes near to producing an optimal composition of the azeotrope H2 O vapor/hexane, for example.
If the condition according to the invention regarding the use of superheated steam is not met, that is, if by inadequate of the apparatus, by use of steam containing condensate, by enrichment of the steam in condensate from the moisture of the feedstock, by inadequate maintenance of temperature of the double bottoms etc. there is used, or produced in the process, a steam having condensed H2 O content, the advantages aimed at and improvements offered by the process according to the invention cannot be achieved.
Thus, saturated steam is not suitable for carrying out the process according to the invention. Even in case of using a saturated steam supplied from the steam boiler at a temperature of e.g. 180° C. (356° F.)/10 bar and expanded at entry into the desolventizer to 1 bar it is not possible to prevent the separation of condensate. In such a case, the stripping process on the double bottoms or in the material, which is necessary for smooth and complete desolventizing, is prevented or not fully achieved. The moisture in the material may also increase, the energy required for moving or agitating the material on the perforated bottoms as the degree of desolventizing decreases. To provide for compensation for the incomplete desolventizing, additional amounts of steam will be necessary, but such additional amounts of steam in turn jeopardize the economy of such processes, especially for throughputs of 1,000 metric tons of wet material per 24 hours.
Aside from these efficiency considersations, when using for the desolventizing of the solvent-wet material so-called saturated steam which is not absolutely dry, i.e. not superheated and, thus, contains condensate,--even in case of the use of very recently developed apparatus approximately in accordance with "Fette-Seifen-Anstrichmittel" (loc.cit.) or DE-C 26 08 712--there will still be measurable residual hexane: from 0.04 to 0.1% by weight (case of hexane-containing soy meal; from 0.1 to 0.2% by weight in case of hexane-wet rape meal.
Residual free hexane, or extracting agents similar thereto, in the desolventized material still cause considerable difficulties and problems, although these values already represent a considerable improvement over earlier extraction processes and systems. Difficulties due to the above-quoted residual portions of extracting agent in the desolventized meal arise particularly in loading and transportation on ships, in storage in silos or in packaging and transportation in paper bags and similar packings means. During this handling (packing or packaging, storage, transportation) the residual portions of solvent--particularly at higher than normal temperatures or under direct influence of the sun--are desorbed and react with the air contained in the surrounding and ambient atmosphere or also in the interstitial volumina of the meal to form explosive mixtures.
For example, the lower explosion limit of n-hexane (one of the most important extractants for e.g. soy flakes, rape, linseed, etc.) in air at 20° C. (68° F.) lies at 1.12% by volume. Furthermore, according to IHA (International Health Association) standards, in working with or handling hexane-containing materials, the maximum content of hexane in the air that must not be exceeded is 125 ppm. Hexane belongs in the group of anesthetics. Hexane contents in the air of merely 1% by volume may already be lethal. The values for comparable extractants, such as pentane, butane, heptane, mixtures of n-hexane and iso-hexane or mixtures of these or other hydrocarbons with one another, are similar.
The further reduction of these residual free hexane levels made possible by this present invention is very important. The large number of explosions and fires that have become known to have occurred in storehouses, silos, and on ships, particularly during shipment to more or less torrid zones emphasizes the importance of this desolventizing. The frequent occurance of such explosions and fires are a hazard that has not yet been mastered.
Moreover, the toxic properties of the solvents for the extraction of oil- and fat-containing vegetable material cannot be overrated in their importance for the political economy. The desolventized extraction residues (meals) of soya, rape, linseed, nut and kernel material, sunflower seed, corn, etc. are being used increasingly as feedstuff and, indeed, also as food for human consumption, especially in developing countries. The potentially disastrous effects of improper, i.e., incomplete desolventizing of such materals, underlines the importance of the invention.
With the the present invention, it is for the first time. Possible to obtain desolventized extraction residue (meal) that is practically free of solvent (extractant), or wherein the content of extractants that are toxic and react with air to form explosive mixtures is so low that the hazards or dangers indicated above are eliminated even in unfavorable working conditions.
Moreover, when the invention is used, the moisture content (water content) of the solvent-wet meal as introduced initially will hardly be changed, due to the stripping being achievable only with superheated steam that takes place at the exit from the specifically designed bores in the double bottoms, which assures that no steam condensation takes place. Furthermore, considerable amounts of desolventizing steam are saved, as mentioned before.
Specifically, in a known plant of the type belonging to the state of the art and using saturated steam or non-super-heated steam, considerable accumulation of water in the desolventized material was observed.
Hexane-wet soya meal entering the desolventizing apparatus with a water content of 15% by weight, when treated with saturated steam, had a water content of 22% by weight at the exit from the desolventizing process. Although this water content does not much impair the quality of the desolventized meal as the material will later be subjected to drying, yet the water contained in the issuing desolventized material was introduced by condensation of the desolventizing steam, so that considerable unused steam consumption, corresponding to the difference of input and output values, has to be noted.
The consequence again is either higher expenditure of steam or higher expenditure of energy for the subsequent drying (e.g. by means of hot air).
Finally, apart from the additional expenditure required by desolventizing apparatus using the use of saturated steam for the driving out of condensate or for maintaining an original water content in the desolventized material, considerable amounts of steam are also saved by the process according to the invention also due to the higher theoretical heat content of superheated steam. This is illustrated by the following comparison: A soya residue material having been deoiled and, hence, subjected to extraction with a solvent, in the present case hexane, (hexane-wet soya meal), contains, on the average, about 15% by weight water and between 30 and 35% by weight hexane. This means that with a charge of 1,500 kg. of hexane-wet meal, approximately 500 kg. hexane must be driven out in the desolventizing.
The meal is fed to the desolventizer at an average temperature of about 60° C. (140° F.) (from the extraction after separation of the oil-containing miscella) and is treated with steam at about 105° C. (221° F.). The amount of heat required for 1,000 kg. hexane-free meal--1000×0.5 (spec. heat)×(105-60)=45° C.--is approx. 22.500 kcal. Further, 500 kg. hexane must be vaporized. 500×85 (heat of vaporization)=approx. 42.500 kcal. Thus, theoretically, the total heat required for the desolventizing of 1,500 kg. hexane-wet meal with about 33% by weight hexane is approx. 65.000 kcal. When taking into account the usual energy losses due to the prevailing operating conditions (about 8%), a heat input value close to the practice is 70,000 kcal.
When using saturated steam (heat content 640 kcal/kg.), this requires 109.4 kg. steam. When using superheated steam (heat content 695 kcal/kg.), 100.6 kg. are sufficient, the saving consequently being 8.8 kg. steam per 1,000 kg. desolventized meal.
With present-day large-scale plants with throughputs of the order of over 1 million metric tons of hexane-wet meal, e.g. soya meal, per year, this means over 8,000 metric tons of steam.
The apparatus according to the invention particularly suited for carrying out the new process will be described by reference to FIGS. 1-5, of which
FIG. 1 shows the general structure of an apparatus according to the invention schematically, omitting all construction and control elements that are self-evident and not decisive for the invention itself;
FIG. 2 shows the distance pieces or spacers used for forming the double bottoms and having bores or apertures, with indication of usual dimensions;
FIG. 3 shows a plurality of spacers arranged side-by-side and their distance relation to one another;
FIGS. 4a and 5a-b show further possibilities of constructing the spacers;
FIG. 6 shows a schematic multistage or multi-component system with temperature measuring points according to Table I of the specification; and
FIG. 7 shows the content of steam in the escaping vapors as a function of the temperature of the vapors.
The significance of FIGS. 6 and 7 will be further discussed later, following the discussion and description of the apparatus according to the invention.
According to FIG. 1, the apparatus consists of the particularly cylindrical reaction vessel (1) with a centrally inserted drive shaft (2) for effecting horizontal movement of a number of agitator arms (5) corresponding to the number of treatment stages (A,B,C,D . . . ). The showing of the drive for the agitator shaft (2) or the exact indication of the mounting and support thereof etc. in the reaction vessel (1) has been omitted as such construction elements are self-evident to the man of ordinary skill in the art. This applies also--and this is said here on principle--to all other auxiliary means of apparatus construction, such as valves, piping, elements for measuring and control, accessory units, such as heat exchangers, dosing or metering means, charging and discharging elements, cyclones, condensate separators etc.
The agitator arms (5) move over and at a slight distance from the bottoms (3) of the treatment stages (compartments) and, respectively, the lowermost bottom (4) which serves exclusively for distributing the steam. By the motion of the agitator arms (5) slightly above the bottoms (3, 4), the solvent-wet material (from the extraction; NS), which is brought in through suitable dosing or metering means (sluice or valve, bucket wheel, worm etc.) by the connecting piece (19), is kept in mixing motion.
By the motion of the agitator arms (5), the material, e.g. hexane-wet residue of the extraction of soy flakes or of an oil- and fat-containing material of other origin, gets to suitable discharge means (7), e.g. rotary valves of the type described in "Fette-Seifen-Anstrichmittel" (loc.cit.) and through the latter into the compartment disposed thereunder, that means, from (A) to (B), to (C), etc., until leaving the apparatus through the lowest connecting piece (8) (TS).
At the same time, superheated steam (UD) is introduced into the apparatus through connecting piece (6), namely, underneath the lowest bottom (4) into the steam distributing chamber ("E").
Instead of pure superheated steam, there may also be used a steam-containing fluid, such as nitrogen, air, inert gas etc., but, preferably, pure superheated steam is used.
The superheated steam having entered the chamber (E) gets--in the direction of the arrows as shown--through the perforations of the lowermost bottom (4) into the compartment (D) disposed thereover, etc., streams--in uniform distribution and with the superheating being maintained--through the material to be desolventized being moved or agitated on the respective bottom and leaves the plant as vapors (D+H) through the connecting piece (20).
The bottoms closing the treatment stages (A,B,C,D . . . ) are in the form of double bottoms adapted to have steam (6') admitted thereto, so that it is possible to adjust and control the temperature of the steam or, respectively, the vapors as well as the temperature of the material, as required or desired in the individual treatment stages (A,B,C,D . . . ).
Of special importance for the achieving of complete, or practically complete, desolventizing of the solvent-wet material (NS) without condensation of steam or without increase in the moisture content in the desolventized material, at considerably improved thermal efficiency and energy efficiency--as is aimed at and solved by the invention--is the maintenance of the superheated state of the steam throughout the entire system, but especially in the region of the bottoms closing the stages or compartments, in the region of the steam chamber (E), etc., which is achieved only by absolute insulation of the apparatus, by the provision of steamheated jackets (26), as for the steam chamber (E), but also for the entire apparatus--not shown--or other heating facilities (steam inlet connection 16). The perforations or apertures in the double bottoms (3) are formed by individual bored distance pieces or spacers (12) the construction of which will be explained in detail in the following.
As is shown by FIGS. 2 and 3, the double bottom (3), and, if necessary, also the lowest bottom (4) serving to distribute the steam, each consist of two bottom plates (10,11) enclosing a steam space (13) therebetween. This steam space is supplied with live steam (6' in FIG. 1 ). According to the invention, so-called spacers or distance pieces (12) are inserted into the holes formed in the plates (10,11) by bores, the plates (10, 11) being connected with each other and held by said spacers (12). The connection is made in known manner by welding, so that thereby a steam-tight closure or seal is provided between the steam space (13) and the holes in the plates. The spacers (12) themselves also have bores (14) therethrough; said bores preferably have the configuration according to FIGS. 2 and 3, that means, they taper conically from the lower end--at the lower plate (11) of the double bottom (3)--to the top end--at the upper plate (10) of the double bottom. This preferred configuration is of advantage whenever the process steam coming from the lowermost steam distributing plate (bottom 4) (6") is to be used also as drying steam for material containing water in a special measure, i.e. material having besides the usual hexane content of approx. 25 to 35% by weight a higher than normal moisture content. By the form of the spacers according to FIGS. 2 and 3 the steam when issuing from the bores (14) is imparted additional tension, which results in a pronounced bubble action of the steam and consequent optimal whirling motion of the material being desolventized, but without formation of channels. The form of the spacers as shown in FIGS. 2 and 3 has proved especially successful also for the formation of the lowermost bottom (4), which, after all, serves only to distribute the steam.
Further favorable developments of the spacers (12) which consider the process conditions given in each case, particularly the material used, are shown by FIGS. 4a, 4b, 4d as well as 5a and 5b.
According to FIG. 4a, the spacers are rounded off at both ends, forming double-cone openings or passages (14) for the superheated steam. While the effect of the rounding off of the edges, whereby, for example, particles of material that have got into the bore (14) are thrown out by the steam tension increased in (25), can be achieved also by a unilateral cone formation (24) only, the additional rounding off also of the lower edge results in a considerably improved streaming in of the stream into the bore as a possible turbulence at the entry of the steam into the bore is counteracted.
In the construction of the spacers (12) according to FIG. 4b, the lower cone passes over into a cylindrical or even square or rectangular offset opening (27), while the radius of the upper cone (26) is somewhat reduced compared to that of (24) according to FIG. 4a. It is understood that the radius of the rounded portion or curvature according to FIG. 4b may also be equal to, or greater than, that of the rounded portion or curvature according to FIG. 4a. The bore (14), according to FIG. 4c, may also be of a form conically enlarging (29) from the bottom to the top and then ending also with a rounded-off edge (28).
The formation of the bore (14) shown in FIG. 4d is in the manner of a Venturi tube with the edges (30) being rounded off corresponding to FIG. 4c but the rounding-off of the lower edge (31) showing a reduced radius that falls into the boundary zone of the plane of the lower plate (11) of the bottom (see FIG. 2).
In the simplest case, according to FIGS. 5a, and 5b, spacers are also possible in the form of tubular pieces the lower cylindrical ends of which extend slightly beyond (32) the lowermost plate boundary and into the next following treatment stage or compartment (B,C,D . . . ). According to experience, this extension (32) may be about 0.5-2.0 times the thickness of the plate (11). A special formation of such spacers may again include a conical configuration (14') in the upper plate (10) of the bottom, whereby the effect of the spacers according to FIGS. 2 and 3, in connection with the extended end (32), is still further enhanced.
It is understood that each of the above-described forms of the spacers or types of bores (14,14') has a quite specific effect which serves to increase or maintain the tension of the steam at the exit from the bores, prevents the formation of channels in the material being desolventized, counteracts steam condensation, favors the stripping effect, prevents congestion of the bores by particles of material and ensures uniform action of the steam on the material being desolventized. Thereby, considerable amounts of steam are saved and the consumption of electric energy, e.g. for driving the agitator elements, is reduced.
In practice, such double bottoms (3) or (4) according to [hereby FIGS. 2-5 have proved satisfactory in which--not excluding] usual technical deviations or specific dimensions or proportions--the lower plate (11) has a thickness
d=approx. 8 to 15 mm, the upper plate (10) a thickness
b=approx. 14-22 mm, and the distance between said plates
c=approx. 12-30 mm.
The external diameter (a) of the spacers (12) generally is in the range between 25 and 75 mm.
The distance (e) between the individual spacers (12)--see FIG. 3--may be equal, smaller or greater than the external cylindrical diameter (a) of the spacers themselves. Generally, however, the distance (e) is equal to or greater than the external cylindrical diameter of the spacers. Especially satisfactory has been found a distance
e=80 mm with a diameter of a=e.g. 50 mm.
In case of spacers (12) that are not circular cylindrical or oval, but square, rectangular or polygonal the conditions in regard to dimensions and sizes are similar.
In case of conical bores (14) according to FIGS. 2 and 3 with an upwardly tapering cone, the inclination of the inner surfaces of the cone is such that the ratio of the two taper bore areas (f):(g) is at about 2.0-1.5.
This aperture ratio has proved to be favorable e.g. in the desolventizing of hexane-wet soya meal with superheated steam especially when the diameter of the bore in the region of the lower bottom plate (11) does not exceed the value of approx. 25 mm.
With a large apparatus of the construction defined above by reference to FIG. 1, with three treatment stages (A,B,C) each closed downwardly by a steam-heated double bottom (3), wherein the overall useful height of the apparatus is approx. 5,500 mm and the internal diameter is approx. 3,000 mm, the double bottoms (3) have between 60 and 140 spacers (12) per m2 of bottom area, so that the bores (14) constitute a cross-sectional proportion of approx. 3-30% of the total bottom area.
In such a plant it is possible to desolventize in continuous operation approx. 480 metric tons (480×103 kg.) per 24 hrs. of hexane-wet soya meal having a hexane content of up to 33% by weight.
The desolventized meal has a residual hexane content of <<0.01% by weight in case of the use of superheated steam of 205° C. (401° F.) and a residual hexane content of <0.01% by weight in case of the use of superheated steam of 125° C. (257° F.).
Such values cannot be realized when using steam other than superheated steam, not even with the specially designed double bottoms (special bores) according to the above-described apparatus.
If the desolventizing steam used is not superheated, the hexane content in the meal in case of the use of steam of 130° C. (266° F.) is still in the region of 0.06% and in case of the use of steam of 160° C. (320° F.) in the region of 0.03%.
Conversely, in case of the use of a simply perforated bottom system, i.e. a system not having the specific bores of the present invention and thus having only circular or similarly formed steam outlet openings, it is not possible to achieve the surprisingly low residual hexane contents in spite of the use of superheated steam.
The reason is to be seen in the fact that only the combination of the bottom construction with superheated, absolutely dry steam that is introduced into the desolventizing apparatus at as high a temperature as possible will result in a practically solvent-free meal.
The desolventizing apparatus shown quite generally in FIG. 1 can--without leaving the scope of the invention--still be technically refined in many respects. Thus, to complete the plant, there may be provided below the double bottoms (3) connections for the introduction of additional live steam, i.e. connections directly leading into the respective steam space of one of the treatment stages (A,B,C,D . . . ); that additional steam is of course also superheated. This steam serves to assist the superheated steam (UD) introduced into the steam chamber (E) at (6) according to FIG. 1, e.g. in case of solvent-wet material having a high water content, in case of meal difficult to desolventize or also in case of relativley low temperatures of the superheated steam, e.g. in the absence of suitable means for intensive superheating.
To the same effect such additional steam may also be introduced by way of the agitator shaft (2) or by way of the agitator elements (5), although such a measure is only of minor importance in the scope of the present invention.
Of special importance for the process according to the invention is also the adjusting of a relatively narrow range of temperature of the vapors consisting of steam and solvent above the topmost process stage, i.e. above the freshly introduced solvent-wet material.
In this connection, the temperature gradient, in all, from the steam inlet at (6) into the distributing chamber (E) up to the vapor outlet at (20), is also a factor of decisive importance.
First of all, the requirement has to be fulfilled that--independent of the number of the treatment stages (A,B,C,D . . . )--the steam below the lowermost bottom plate (4) should itself have an optimal temperature. On priniciple, no temperature limits are give for the superheated steam, so that steam temperatures of over 120° C. (248° F.) are already quite useful. However, for reasons of economy, for optimal utilization especially oflarge-scale plants, it is advisable, as far as possible, to use temperatures not lower than 130° C. (266° F.), so that a certain distance from the condensation temperature (100° C./1 bar) is given already at the steam inlet. Preferably, one works with steam inlet temperatures of over 150° C. (302° F.) or, better, over 180° C. (356° F.) and sometimes also up to 220° C. (428° F.).
These temperature gradients are just as much a function of the remaining process conditions and qualities of material as is the amount of steam used--which, generally, must be adjusted for each material--or the amount of steam introduced below the lowest bottom.
Generally, all of the superheated steam, i.e. up to 100% of the amount of superheated steam required--no matter [form whether such steam is in the form of pure steam or in the of a mixture of steam with a suitable fluid--is introduced directly into the steam chamber (E). This is always the case if the number of stage or compartments (A,B,C,D . . . ) is of the order according to FIG. 1 or less. In case of more than four stages, however, it is advisable to introduce the bulk of the steam again into the steam chamber, that means, into the lowermoster chamber or compartment below the steam distributing bottom (4), and a partial amount, i.e. the quantitive balance to make up 100%, into the spaces in the higher compartments below the respective stage closure bottoms (3) where the escaping vapors collect. The utmost limit for the distribution of the steam among the lowest stage or steam chamber on the one hand and the vapor spaces on the other hand is at about 45%, that means, irrespective of the number of stages or compartments, at least 45% of the total amount of live steam in superheated form that is required must be introduced below the steam distributing bottom (4).
The superheated steam generally is supplied by the steam boiler of the mill and is available at an average pressure of 10 bar. On entering the steam chamber (E) the steam expands to 1 bar, as it is only in rare cases that desolventizing is performed under overpressure conditions. If no superheated steam is available from the steam boiler of the mill, the necessary degree of superheating can be adjusted also by interposition of a superheater before the entry of the steam into the steam chamber (E). Suitable superheaters are well-known so that they need not be described here.
The stripping effect repeatedly referred to hereinbefore can be realized only with superheated steam being absolutely free of condensate, and only thus can the desired azeotrope steam/solvent be maintained in its ideal composition with a narrow temperature range of the vapors without substantial alteration of the water content in the desolventized material.
In continuous operation of a multistage or multi-compartment system according to FIG. 1 there will result throughout the height of the plant temperature diagrams which are specific for the process according to the invention and which reflect the ideal desolventizing conditions aimed at. This will be shown on the basis of Table I by reference to FIG. 6.
In this connection, Table I shows the effective temperatures established in continuous operation of a large-scale technical plant which appear in a plant comprising four treatment stages or compartments (A,B,C,D according to FIGS. 1 and 6) in the desolventizing of hexane-wet soy meal as well as of hexane-wet rape material.
TABLE I______________________________________ Temperature in °C. at the Measuring Point Soy Meal Rape Meal 33% Hexane 30-32% HexaneMeasuring Point approx. 15% H2 O approx. 9-10% H2 O______________________________________T1 (steam 180 180chamber E)T2 (in the material 115-116 120-122of stage D)T3 (vapor space 115-116 120-121of D)T4 (in the material 112-114 118-120of C)T5 (vapor space 112-115 118-119of C)T6 (in the material 112-114 115-116of B)T7 (in the material 64-66 67-68of A)T8 (vapor outlet) 66-68 66-68Hexane Content: <<0.01% <0.01%______________________________________
As is shown by Table I, there are maintained temperatures in the individual process stages up to and including stage (B)--measuring point T6 in the material of stage (B)--which, at 112° C. (233.6° F.) and 115° C. (221° F.) respectively, are considerably above the temperature of condensation of steam. As late as in the region of the freshly introduced hexane-wet material, i.e. in the material of stage (A)--measuring point T7 --does there appear a marked drop in temperature, which, however, is not caused by condensed steam but results from the formation of the azeotrope steam/hexane.
A comparative experiment showed that in case of the use of wet steam, under identical technical conditions, i.e. even with the use of an apparatus according to the invention, temperatures only slightly over 100° C. (=212° F.) (103°-105° C.) (=217.4°-221° F.) were measured already in the region of measuring point T2. The temperature at measuring point T4 was 98° C. (208.4° F.) for soy meal, 99° C. (210.2° F.) for rape. The temperature at measuring point T6 was 80° C. (176° F.) for soya, 81° C. (177.8° F.) for rape. On the other hand, the vapors had to be maintained at over 70° C. (158° F.) by considerable additional steam in order to arrive at a desolventized material, which, however, still had a residual hexane content of 0.06% by weight (soya) or 0.03% by weight (rape) respectively.
As has been stated hereinbefore, in case of the use of steam other than superheated steam, the amount of steam required is many times that required in the case of superheated steam as otherwise it is not possible to counter the condensation of steam. This, however, means at the same time an additional load on the driving shaft for the agitator as the material itself remains in a state of increased water content which impedes the rotary motion of the agitator elements.
On principle, it is pointed out here that when superheated steam is used in an apparatus not showing a design of the compartment bottoms according to the invention, as is known e.g. from "Fette-Seifen-Anstrichmittel" (loc.cit.), the extremely low residual hexane contents according to the invention, the narrow temperature range of the steam-hexane vapors in connection with great economy (amount of steam, energy for agitator driving shaft, etc.) cannot nearly be achieved.
With regard to the saving in steam by the process according to the invention the following reflection should be noted which supplements the heat balance made up hereinbefore. By this reflection, the significance of superheated steam for the desolventizing of solvent-wet material once more comes to the fore.
As is well-known, the paraffin hydrocarbons Cn H2n+2, by C4 through C9, which alone are of importance in technical extraction processes of the oil and fat industry, form, in connection with steam, more or less distinct azeotropes which are alone responsible for an optimal steam/solvent ratio in the vapors in desolventizing. The commercial hexanes which have boiling points only little higher than 60° C. (140° F.) (normal pressure) (boiling point of n-hexane: 69° C. (156.2° F.); iso-hexane: 60° C. (140° F.); benzine containing over 50% n-hexane: 62°-64° C. (143.6°-147.2° F.) will, for reasons of azeotrope formation, carry corresponding proportions of steam, as entrainer, out of the desolventizing system.
As the content of steam in the vapors of desolventization present in azeotrope form is a function of the temperature of the vapors, the maintaining of a particular temperature of the vapors is of decisive importance for optimal utilization of the steam with a view to the formation of the azeotrope.
Table II, in connection with FIG. 7, shows the quantity of steam absorbed, or entrained as azeotrope, by one kilogram of hexane, plotted against the temperature of the vapors.
TABLE II______________________________________Temperature of Vapors °C. Kilograms of Steam per(T8 in FIG. 6; D + H) one kg. of Hexane______________________________________60 0.50065 0.07566 0.08067 0.08568 0.09070 0.10075 0.13580 0.20085 over 0.300______________________________________
It follows from the values of Table II that in any case the temperature of the vapors (D+H in FIG. 6) must be kept as low as possible.
At a temperature of the vapors of not more than 70° C. (158° F.), the solvent, i.e. in this particular case hexane, already entrains 0.1 kg. steam per kg. of hexane, this amount of steam being carried out of the plant unused. At a temperature of the vapors of 80° C. (176° F.), the amount of steam leaving the plant unused already is 0.2 kg per kg. hexane, and at 85° C. (185° F.) 0.3 kg.
When using superheated steam of as high a temperature as possible (see Table I; 180° C., superheated), it will not be difficult to adjust a temperature of the vapors (T8 or D+H) of 66°-68° C. (150.8°-154.4° F.) even in case of large-scale operation involving a throughput of material of more than 2500 metric tons per 24 hrs. The steam entrained by the expelled hexane unused is reduced to a minimum of approx. 90 g/kg. hexane (temperature of vapors 68° C. (154.4° F.)).
Conversely, when using steam that is not superheated, it will be necessary to provide for temperatures of the vapors of over 70° C. (158° F.) or, due to the considerable additional amounts of steam, even over 80° C. (176° F.), to achieve as high a degree of desolventization as possible. However, a result of such high temperatures of the vapors is that, according to Table II, the amount of steam leaving the plant unused will be 100 g. steam per kg hexane in case of vapors at 70° C. (158° F.) and as much as 200 g. steam per kg. hexane in case of vapors at 80° C. (176° F.), that means, the additional steam input required merely due to "loss" is, in case of vapors at 80° C. (176° F.), already more than twice the steam input required for vapors of 66°-68° C. (150.8°-154.4° F.). The latter, however, can be achieved only with superheated steam.
Finally, on principle, it is pointed out that in FIGS. 1-5, particularly in FIG. 1, the apparatus according to the invention is shown only schematically. The auxiliary elements well-known to anyone skilled in the art such as temperature measuring points, steam inlet and outlet means, insulations, walkways etc. are not shown. Sight glasses (23) have been included in the drawing as representative of the accessories. The short feed pipe (6") serves to feed in heating steam for the bottom (4) above the steam chamber (E).
|Cited Patent
|Filing date
|Publication date
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|Oct 9, 1906
|Wilman W Mcelroy
|Drying apparatus.
|Nov 10, 1950
|Feb 12, 1952
|Central Soya Co
|Soybean treating process
|Aug 22, 1949
|Jan 19, 1954
|Vernon F Parry
|Method of drying solids in a fluidized bed
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|Jan 8, 1957
|Central Soya Co
|Meal-treating process and apparatus
|Sep 2, 1955
|Sep 17, 1957
|French Oil Mill Machinery
|Desol ventizer
|Feb 14, 1955
|Nov 24, 1959
|Phillips Petroleum Co
|Heat exchanger which forms the sole fluid distribution means in a catalyst regenerator
|Aug 31, 1959
|Mar 24, 1964
|Method of desolventizing and toasting soybean meal
|Nov 17, 1980
|Mar 8, 1983
|Bunge Corporation
|Method and apparatus for desolventizing residual solids after oil extraction therefrom
|Feb 27, 1981
|Apr 19, 1983
|Roberts Elliott D
|Dehydrator apparatus with unidirectional air flow control means
|Jul 20, 1982
|Mar 12, 1985
|Schumacher Heinz O
|Apparatus for the treatment of flaky or granulated material with gases or vapors in a continuous countercurrent process
|May 2, 1955
|Sep 3, 1959
|Eugen Georg Stich
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|Mar 25, 1965
|Fawkham Dev Ltd
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|Charbonnages De France
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|Oct 26, 1972
|Exxon Research Engineering Co
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|Aug 9, 1973
|Peters Ag Claudius
|Boden fuer wirbelschichtreaktoren
|Title not available
|Title not available
|Title not available
|Title not available
|"Der Desolventizer-Toaster-Trockner-Kuhler (TTK), ein neues Verfahren bei der Verarbeitung von Olsaaten", Von H. Schumacher, pp. 56-59, 1/1976, Fette-Seifen-Anstrichmittel.
|Der Desolventizer Toaster Trockner Kuhler (TTK), ein neues Verfahren bei der Verarbeitung von Olsaaten , Von H. Schumacher, pp. 56 59, 1/1976, Fette Seifen Anstrichmittel.
|Citing Patent
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|Nov 30, 1988
|Mar 27, 1990
|Sullivan James B
|Shock-absorbing innersole
|Jul 5, 1990
|May 12, 1992
|Francois Laurenty
|Drying process and tower for products in grain form
|Dec 18, 1992
|Aug 17, 1993
|Lundar Electric Ind. Co., Ltd.
|Vegetable dehydrator
|Jan 12, 1994
|Jun 13, 1995
|American Harvest, Inc.
|Food dehydrator
|Nov 20, 1991
|Mar 5, 1996
|Beckman Instruments, Inc.
|Laboratory workstation using thermal vaporization control
|Nov 20, 1991
|Sep 3, 1996
|Beckman Instruments, Inc.
|Heated cover device
|May 22, 1997
|Aug 4, 1998
|Jeffrey S. Brooks, Inc.
|Nov 11, 1998
|Nov 30, 1999
|The French Oil Mill Machinery Company
|Mar 5, 1999
|Jul 11, 2000
|The Metal Ware Corporation
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|Jan 21, 1999
|Aug 7, 2001
|Frazier, Barnes Research Llc
|Identity preserved oilseed mill
|May 15, 2001
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|Sep 20, 2002
|Feb 14, 2006
|Crown Iron Works Company
|Two stage apparatus for desolventizing food grain meal
|May 8, 2012
|Steve Hoffman
|Permeable non-stick cooking surface
|Aug 24, 2010
|Jul 14, 2015
|Steve Hoffman
|Process and device for forming a low adhesion cooking surface
|Sep 20, 2002
|Apr 17, 2003
|Crown Iron Works Company
|Two stage apparatus for desolventizing food grain meal
|Mar 3, 2008
|Sep 4, 2008
|Steve Hoffman
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|Feb 28, 2008
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|Desmet Ballestra North America, Inc.
|Meal dryer/cooler
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|Jun 24, 2010
|Kemper Timothy G
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|Jun 2, 2014
|Aug 13, 2014
|Device for vertically evaporating residual solvents in eucommia ulmoides husks
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|Jan 6, 2016
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|Nov 18, 1998
|May 26, 1999
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|U.S. Classification
|34/380, 99/483, 426/465, 34/173
|International Classification
|Cooperative Classification
|European Classification
|Apr 7, 1987
|Certificate of correction
|Dec 20, 1989
|Fee payment
Year of fee payment: 4
|Apr 18, 1994
|Fee payment
Year of fee payment: 8
|Feb 13, 1998
|Fee payment
Year of fee payment: 12


text:
Chattanooga Property Shop, Keller Williams Realty's newest group, features two lead agents, Diane Patty and Lisa Brown who combine experience and knowledge of the Chattanooga and north Georgia that only comes from being locals. Also included are Buyer Dedicated Specialist, Carmen Patty and Executive Assistant and Technological Guru, Tanya Swann.
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Today, 91 percent of all shoppers use the internet in their home search. Chattanooga Property Shop utilizes social media, internet marketing and their own website (www.Chattanoogapropertyshop.com). Local and relocation clients are dedicated readers of the company's weekly blog (blog.chattanoogahomessale.com) featuring not only real estate news and reviews but all things Chattanooga.
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Diane Patty: 504-5006
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May 26, 2016
May 25, 2016
May 23, 2016
On the heels of the grand opening for the St. Jude Dream Home, Realtor Jeremy Callahan announced via video that he will donate $500 to St. Jude Children's Research Hospital for each new family ... (click for more)
The Tennessee Housing Development Agency is getting back in the business of visiting and monitoring federally subsidized apartment developments, and properties in Memphis will be the agency's ... (click for more)
Not all homebuyers in Chattanooga and surrounding areas are looking for a house with a massive floor plan – and a massive price tag. In fact, a variety of lifestyle changes motivate many home ... (click for more)
On the heels of the grand opening for the St. Jude Dream Home, Realtor Jeremy Callahan announced via video that he will donate $500 to St. Jude Children's Research Hospital for each new family he helps buy or sell real estate between now and August 31. "My goal is to donate at least $10,000 to St. Jude, and all that would take is 20 new families jumping on board," ... (click for more)
The Tennessee Housing Development Agency is getting back in the business of visiting and monitoring federally subsidized apartment developments, and properties in Memphis will be the agency's top priority. Starting in July, THDA will resume on-site Management and Occupancy Reviews (MORs) at multifamily properties in Tennessee that participate in the federal government's ... (click for more)
The Hamilton County Department of Education Interim Superintendent Dr. Kirk Kelly announced Thursday several new principal and central office appointments. "Strong school leadership is essential to student success. Great school leaders are the key to ensuring there is an excellent teacher in every classroom. We are confident that these principals will provide ... (click for more)
The Cleveland City School board unanimously voted Thursday afternoon to offer the job of director of Schools to Dr. Russell Dyer. Dr. Dyer currently serves as the Chief of Staff of Schools in Collierville, Tn. If Dr. Dyer accepts the school board's contract, he will be paid $132,500 a year. Dr. Dyer's selection comes a few months after the last director of schools, ... (click for more)
It is interesting that Chief Fletcher would deem the handling of the Mayor's encounter as typical or normal. Is the Chief asking the public to believe that all misdemeanor domestic violence arrests include a 4-hour taped interrogation, and delayed reporting after a visit to the Chief's house. Of course, we believe that Chief Fletcher. April Eidson * * * I ... (click for more)
On this, the week of commencement, junior high graduations, and achievement at every level is displayed, we stand with hope and wonder as the next wave of promising Americans gives our nation the reason we pray for our next tomorrow. On Monday, as Vice President Joe Biden addressed 950 cadets who would become 2nd Lieutenants by the end of the day at the United States Military ... (click for more)

subset: commoncrawl


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Submit Best Offer: The item up for offer is a VERY RARE & Original CharlesCobelleOIL ON CANVAS Painting with incredible detail of his most desired, iconic image, scenes from Monaco. Cobelleis forever famous for the creativity, passion, beauty and many other ideals that his images reflect. But of all the paintingsCobellehas done, and the stunning masterpieces he has created, the image that is most desired of all his artworks are of his native land, France. Cobelle's talents are truly amazing, with quick and light strokes of a paintbrush he can still create such immaculate detail throughout this piece. It is very rare to find such an important painting with such great color and expressionistic detail painted byCobelle. Additionally,Cobellehas added his signature in the lower right corner. This tribute to expressionism whereCobelleallows the viewer to further develop the detail through one's own eye is a serene break from controlled realism. It allots us a sneak peek at, and, a greater understanding, ofCobelle's vision, values and desires. This ORIGINAL Oil Painting titled, "Port Hercule- Monte Carlo" looks absolutely spectacular in person with the tasteful, custom frame enhancing this stunning piece. This painting is being sold for well under retail with the Submit Best Offer option. So make your OFFERS today and you do not want to miss out on this item before it is in Alsace-Lorraine, France, and becoming a U.S. citizen in the late 1920s, CharlesCobelle,whose birth name was Carl Edelman, began his career in Paris after earning Bachelor and Master's Degrees at the University of Munich. Later he studied at the L'Ecole des Beaux Arts in Paris and with Marc Chagall. At Menton on the Riviera, he apprenticed with Raoul Dufy.In the United States where he lived in Brookfield and Fairfield, Connecticut, he continued to create mixed-media paintings, and also did mural work for commercial establishments such as Neiman Marcus Company in Dallas, Texas; The Desert Inn in Las Vegas, Nevada; and the Teheran Restaurant in New York City.His work is in the collection of the Hartford Atheneum, the Mark Hopkins Hotel in San Francisco, and the private collection of Howard Hughes.
Submit Best Offer, ALL OFFERS WILL BE CONSIDERED.CharlesCobelles's Paintings have sold for very high prices at major sale houses, and in Galleries around the world. However, this is your chance to own an originalCobelleat far less than retail prices command. The artwork listed here is a VERY RARE, Original, Oil Painting, on Canvas with intricate detail, titled, "Port Hercule, Monte Carlo", that depicts the energy from on the cities most famous tributary. This painting was signed in the lower right when it was completed and it has since remained in excellent condition. It is incredible to look it and thus will be a perfect addition to any home, office or vacation dwelling.Once again, this authentic and original artwork by Cobellecontains a wonderful rendition of a French Scene along the Seine, a most famous and desirable subject.The artwork is guaranteed authentic, and, comes with a gallery COA. This pieceis being offeredfor salewith the submit best offer option so make your OFFER NOW before someone else seizes the opportunity.This painting is a versatile size measuresapproximately 20"x 24", and, is elaborately placed in a custom wood, gold finished frame. The framed dimensions are approx. 28" X 32". This piece looks even better in person and surely will bring a wealth of warmth, enjoyment and intrigue to the buyer for many years to come! Cobelles art has been exhibited in major museums around the world, and his works of art are to be found in some of the most prestigious public and private collections worldwide. Please e-mail if you have any further questions. This item will be professionally packaged to ship domestically or Internationally. Submit your best OFFER NOW!!
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Rare Original Charles Cobelle Painting Signed Oil On Canvas Monte Carlo Monaco:
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text: Google opening 'digital garage' to help businesses in Leeds Technology 13 March 15 by James Temperton The six-month workshop will be held in Leeds Dock near the Royal Armouries MuseumShutterstock Google is opening a pop-up workshop in Leeds in a bid to help local businesses improve their digital skills. The Digital Garage project will see Google give advice on how companies can use the internet to reach more customers and grow faster.The six-month trial in Leeds will open on 30 March and include a digital "tune-up" service for small businesses. Aspiring entrepreneurs are also encouraged to attend events organised by local partners and book one-to-one mentoring sessions on digital business skills.As part of the project Google is investing in computer science and coding training for around 25,000 teachers. Working in partnership with Code Club Pro, Computing at Schools and Raspberry Pi, it will run workshops and events for teachers in local schools alongside online training resources. Raspberry Pi computers will also be donated to local schools. Don't miss BBC announces Micro Bit computer Google plans to expand the project to four other UK cities, although it hasn't announced where it will go next. Business owners and teachers in the Leeds area can register for workshops and other events being run at the pop-up by visiting digitalgarage.withgoogle.com. Latest on wired.co.uk


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Re-Framing Creativity
For a long time psychologists, educators and parents alike have assumed that imaginative play was most useful for learning when set in as realistic a situation as possible. However, is "real" always better than "imaginative" when it comes to the learning landscape?
Many have a fear that learning about, or at the very least not clearly distinguishing between, fantasy and reality can lead to misunderstandings and misconceptions. This assumption underestimates the importance and value of the childhood and nature design principle of "Imagination and Fantasy" as termed by David Sobel, director of Teacher Certification Programs in the Department of Education and director of the Center for Place-based Education at Antioch University New England. Read the rest of this entry »


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The Maturity Institute (MI) comprises a global network of leaders, practitioners and academics striving to build vibrant, healthy and sustainably successful organizations. Our aim is to build understanding and encourage the practice of effective Human Governance; an approach that not only reconciles the goals of societal and organizational value but makes them mutually inclusive. MI undertakes research, organizes educational events and provides professional development to help organizations better govern and manage human capital to release its full potential in the pursuit of never-ending improvements in societal value.


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The fate of former assistant Penn State football coach Jerry Sandusky will be decided in a Centre County courtroom and News 8 will be there. Follow live updates from our team in court, access investigation documents and review a timeline of events in our extended coverage section.
SpaceX landed one of its rockets on an offshore platform Friday, the third time in two months the private space exploration firm has made a successful landing at sea.
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Zinc prices touched a two-week high on Friday and copper also gained as investors bought futures to square positions, though analysts said metals may resume their downward trend next week.
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'Bones' Final Season Is Pushed to Midseason. Find Out the Replacement
- 11:07 AM, May 21
Tyra Banks Greets Fans and Signs Copies of Her Book Modelland
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Another Three to Present the Oscars
Compiling a great list of this year's Academy Awards presenters, telecast producer Laura Ziskin announced yesterday, February 19, that Tobey Maguire, Anne Hathaway, and Jack Black have also been picked up to perform the task at the event which is held for the seventy-ninth time.
Honoring best achievements in filmmaking of 2006, the 79th annual Academy Awards will take place at the Kodak Theatre at Hollywood & Highland Center on Sunday, February 25 and be aired live by ABC at 5 p.m. PST (8 p.m. EST), beginning with a half-hour red carpet arrivals segment, "The Road to the Oscars."
Maguire, a native of Santa Monica, California, next can be seen on the big screen reprising his role as the title character in highly anticipated superhero flick "Spider-Man 3" while Hathaway and Black in "Becoming Jane" and "Margot at the Wedding", respectively, both being slated to open in theaters this year.
More Tobey Maguire News
- 'DWTS' Pro Peta Murgatroyd and Maksim Chmerkovskiy Expecting First Child, but Something Upset Them
- Ben Affleck Gives Jennifer Garner 11-Carat Diamond Ahead of Their Anniversary - Is It True?
- Iggy Azalea Teases Collaboration With Zedd After Pushing Back Her Album's Release
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- Yikes! Kendall and Kylie Jenner Reportedly in 'Bizarre Love Triangle' With Scott Disick
- New 'Luke Cage' Set Photos Reveal Villain Diamondback
- Tom Hanks and Rita Wilson's Marriage Reportedly Crumbles. Here's the Truth
- Prince Hated the Idea of Appearing in a Music Video With Madonna


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Budgeting and knowing where your money is going is all well and good, but how do you use this knowledge to reach the goal of being debt free?
Is online insurance cheaper?
Buying your short-term insurance online and not through a traditional broker, may not end up being cheaper, and there may be...Continue Reading...
The right questions to ask your financial adviser
Craig Gradidge explains why "Where should I invest?" is the wrong question to ask your financial adviser.Continue Reading...
New unit trusts on the block
Four new unit trusts have been launched for longer-term investors with investment horizons of five or more years.Continue Reading...
Are gold coins a good investment?
Many South Africans bought gold coins in 2011, when the gold price was at nearly US$2 000 per ounce. Was it a good investment?Continue Reading...
Welcome to Maya on Money.
This site is a collection of articles written by finance journalist Maya Fisher-French as well as other contributors. The aim of Maya on Money is to help you with those day-to-day money decisions related to South African finance matters. Articles cover all those areas that you need in order to manage your money effectively such as budgeting, saving, investing, banking and insurance. Feel free to engage with us and post your questions on the Forum.
With interest rates rising and the economy slowing, is now the time to make the biggest investment of your life?
When you become a parent, you are faced with the reality that you have to form a value system within which you will raise your children
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Where's the best place to put extra money for retirement if you already have a company pension fund?
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The Tides of Mind: Uncovering the Spectrum of ConsciousnessA "rock star" (New York Times) of the computing world provides a radical new work on the meaning of human consciousness. The holy grail of psychologists and scientists for nearly a century has been to understand and replicate both human thought and the human mind. In fact, it's what attracted the now-legendary computer scientist and AI authority David Gelernter to the discipline in the first place
Mirror Worlds: or the Day Software Puts the Universe in a Shoebox...How It Will Happen and What It Will MeanTechnology doesnt flow smoothly; its the big surprises that matter, and Yale computer expert David Gelernter sees one such giant leap right on the horizon. Todays small scale software programs are about to be joined by vast public software works that will revolutionize computing and transform society as a whole. One such vast program is the Mirror World. Imagine looking at your computer screen and
Americanism:The Fourth Great Western ReligionWhat does it mean to "believe" in America? Why do we always speak of our country as having a mission or purpose that is higher than other nations?Modern liberals have invested a great deal in the notion that America was founded as a secular state, with religion relegated to the private sphere. David Gelernter argues that America is not secular at all, but a powerful religious idea—indeed, a
How Imperial Academia Dismantled Our Culture (and Ushered In the Obamacrats)America-Lite (where we all live) is just like America, only turned into an amusement park or a video game or a supersized Pinkberry, where the past and future are blank and there is only a big NOW. How did we come to expect no virtue and so much cynicism from our culture, our leaders—and each other?In this refreshingly judgmental book, David Gelernter connects the historical dots to reveal a
Computerizing the Poetry of Human ThoughtA leading mind in the world of artificial intelligence answers the provocative question: "Can we introduce emotion into the computer?"Can we introduce emotion into the computer? David Gelernter, one of the leading lights in artificial intelligence today, begins The Muse in the Machine with this provocative question. In providing an answer, he not only points to a future revolution in computers,
$16.79How is consciousness possible? What biological purpose does it serve? And why do we value it so highly? In Soul Dust, the psychologist Nicholas Humphrey, a leading figure in consciousness research, proposes a startling new theory. Consciousness, he argues, is nothing less than a magical-mystery show that we stage for ourselves inside our own heads. This self-made show lights up the world for us
A History of Fear and Loathing on the Populist RightFrom "Birthers" who claim that Barack Obama was not born in the United States to counter-jihadists who believe that the Constitution is in imminent danger of being replaced with Sharia law, conspiratorial beliefs have become an increasingly common feature of our public discourse. In this deeply researched, fascinating exploration of the ideas and rhetoric that have animated extreme, mostly right
How Queer Man Is, How Queer Language Is, and What One Has to Do with the OtherProfound and passionate essays from one of America's greatest literary voicesBefore winning the National Book Award for fiction in 1962, Walker Percy was an established scholar of science, philosophy, and language. Presented here are his strongest essays in those subjects, offering what he called a "theory of man for a new age." Ambitious yet readable, The Message in the Bottle encapsulates the
Evolution and the Birth of ConsciousnessHow does the water of the brain yield the wine of conscious experience? What is the link between bodily activity and our inner feeling of what it's like to be our selves? The problem of qualia — the so-called "hard problem" of consciousness — has intrigued philosophers for generations and remains the greatest challenge to contemporary science. In this path-breaking book, Nicholas Humphrey examines
Quicklet On Freud's Dream Psychology (CliffsNotes-like Book Summaries)ABOUT THE BOOK If you've ever woken at dawn (or, ahem, 3am) to scribble wildly in a dream journal, convinced that you've just written the world's most heartbreaking poem or unlocked the secret of perpetual motion, you know how powerfully real your night visions can seem. If by lunchtime that day, however, you realize what you've written is not only drivel but completely incomprehensible, you are
$40.49This reader brings together a selection of seminal papers by Christopher Bollas. Essays such as "The Fascist State of Mind," "The Structure of Evil," and "The Functions of History" have established his position as one of the most significant cultural critics of our time. Also included are examples of his psychoanalytical writings, such as "The Transformational Object" and "Psychic Genera," that