US2190615A

US2190615A - Method for making and processing soap

Info

Publication number: US2190615A
Application number: US119168A
Authority: US
Inventors: Benjamin H Thurman
Original assignee: REFINING Inc
Current assignee: REFINING Inc
Priority date: 1937-01-05
Filing date: 1937-01-05
Publication date: 1940-02-13
Anticipated expiration: 1957-02-13

Description

Feb.13, 1940. HTHURMN 2,190,615

METHOD FOR MAKING AND PROCESSING- SOAP Original Fileddan. 5, 1937 2 Sheets-Sheet 1 Feb. 13, 1940.

B. H. THURMAN METHOD FOR MAKING AND PROCESSING SOAP 2 sneets-shee 2 Original Filed Jan. 5, 1937 THIHHIHwHhHhHHMHIM e INVENTORG M/NH. URMAN drToR/vm'.

o a w 6 6 m n V xgllill Patented Feb. 13,1940

, 2,190,615 METHOD FOR AND PROCESSING Benjamin H. Thurman, Bronxville, N; Y., assignor'to Refining, Ina, Reno, Nev a commation of Nevada Application January 5, 1937, Serial No. 119,168 Renewed October 3, 1939 llclalms.

(c1. gen-41a) One feature of the invention is the production, by presence of material amounts of glycerine,

of a friable soap as an intermediate or final product and which has new characteristics differentiating it from soaps now known. In producing this friable product substantially anhydrous soap is cooled from molten, plastic, or semiplastic condition, preferably while out of contact ,with the atmosphere or oxidizing agents, to form a solidified soap having incipient planes of fracture throughout. Upon extrusion this soap breaks up almost entirely into a powder or into small masses which are easily crushed into a fine powder. This friable soap has unexpected properties in that item be directly and uniformly hydrated by adding water thereto.

It will uniformly absorb water in considerable amount as distinct from ordinary drastically dried 'soap powders which will form a gel when such an amount of water is added and thus can- 'not be uniformly hydrated when water is added thereto. This friable soap, as well as a novel method and apparatus for producing same, is a part of'the present invention. 1

In the preferred mode-of operation the soap is produced continuously Itmay be dellvered from the apparatusin powder or fiake form and having the desired moisture content, or it may be continuously produced in the form of bars or cakes. In this connection the friable soap may be produced as an intermediate product, if desired, by cooling thesoap from molten, plastic,

or semi-plastic condition while it is substantially anhydrous, water being later added in controlled amount. This mode 'of operation is apart of 5 the present-invention, as well as the production of friable soap as an end product.

In forming the friable soap any suitable method can be used for forming amass of soap which is in molten, plastic or semi-plastic condition. The soap should be substantially anhydrous,

containing at most not more thana very few per cent of water. It is brought into this condition by application of heat, and extreme fluidity'immediately preceding cooling is not requisite.

5 The soap should be kept from theatmosphere while at the high temperatures necessary, thus preventing oxidization, discoloring, and other deleterious reactions. If the soap-making materials used areof such character as to form 50,.glycerine, this glycerine can be'advantageously removed in'whole or in part before cooling the mass, and a mass of molten, plastic, or semiplastic soap will usually contain no great proportion of glycerlne. Howeven'the friable nature of the product is apparently not destroyed if, this is desired in the finished soap.

The next step is to cool this soap from its molten, plastic, or semi-plastic condition in such manner that incipient planes of fracture extend 5 throughout the cooled mass, making it extremely friable. This cooling can best be accomplished during continuous movement of the soap, and it is important that the moisture content of the soap should not be greatly increased prior to 10 coohng, otherwise the friable nature of the soap be destroyed.

The resulting product will break up largely into soap powder if the stream of friable soap is extruded, and any remaining masses can be 15 readily broken up by application of small crush-. ing pressure.

The resulting powder, or the masses of friable soap' not I yet disintegrated into a powder, have the unexpected property of directly and uni- 20 formly absorbing moisture even though it is a drastically dried product. A desired amount of water may be added to a mass of the soap and I gentle mi ging will cause uniform hydration of the soap. U On the other hand, the water may 25 be supplied to the soap continuously as fast as produced, it a continuous process is utilized.

However, the method and apparatus is not limited to the production of this friable soap as an intermediate or final product and many 30 features are new regardless of this ,use. For instance, the system for removing the soap from the vacuum chamber and subsequently processing the soap is new, -as ,-is also the cooling system which permits attenuation of the soap to 5 facilitate removal of heat therefrom. So also,

the method of introducing the reaction products into the vacuum chamber is new, and the complete system'permits hydration and addition of builders or other material during continuous 40 movement of the soap.

Other new features forming a'part ofthe invention will be evident from the followin d scription.

One convenient and very satisfactory ap paratus for making and processing soap of this friable or non-friable character is disclosed in the attached drawings, in which:

Fig. 1 shows the complete apparatus, partially in-section.

Fig, 2 is a section of the conveyor system taken on the line 2-2 of Fig. 1.

Fig. 3 is a sectional view of one form of valve, being takenas indicated by the lines j H of E18. 2. 55

Fig. 4 is a view of one type of member extending into the conveyor for breaking up the soap stream, being taken as indicated by the line 4-4 of Fig. 2.

Fig. 5 is taken as indicated by the line 5-4 of Fig. 2 and shows one of the cooling grids.

Fig. 6 is a sectional view taken on the line H oi Fig. 1.

The materials used in the process include a saponiflable material which may be any material capable of being saponified to form soap,

for instance, various fats, glyceride-type oils, greases, etc. The saponifying material may be any material which will act with the saponiiiable material to form reaction products including soap and a vaporizable material, such, for instance, as glycerine or water, or both. Examples such saponifying materials are aqueous alkaline solutions of caustic soda, caustic potash, etc. In using he apparatus disclosed, these materials are respectively contained in tanks HI and II and may be therein heated to increase the fluidity or facilitate satisfactory mixing.

Proportioned quantities of these materials are mixed in any suitable way. In the continuous system shown, proportioned streams are with drawn by pumps i2 and i3 and delivered to a mixer i4 through closed conduits. The pumps may be inter-connected by a variable-speed means I80 to control the proportions. The mixer i 4 may be of any suitable type and mechanical mixers can be used, though a satisfactory mixture can be obtained by injecting one material into a stream oi the other as it flows through a chamber of the mixer I4. In the continuous system shown the pumps develop suflicient pressure to force the mixture through the heating zone.

This mixture moves through a pipe I5 to any suitable type of heater IS, the pipe I! being equipped with suitable devices i1 and il to indicate the pressure and temperature of the mixture. Various types of heaters can be used which provide a heating zone through which the mixture continuously flows. The type illustrated is particularly suited to a continuous process and includes a coil of pipe I! heated by a burner 20 or by any other heating means. A suitable thermostat may be used to control the amount of heat applied.

In the heating zone defined by the coil I! complete saponiflcation takes place under heat and pressure and the reaction products discharging through a pipe 22 comprise a mixture of soap," water, and glycerine'in the event that an aqueous alkaline solution was used as the saponifying material. In this pipe the water will be in the form of steam, and the glycerine will be either in liquid or vapor state in wholeor in part. The pipe 22 is equipped with a pressure gauge 23 and a thermometer 24.

These reaction products are continuously discharged into a separating chamber II through a valve 28 and a nozzle 21 which may be used to I throttle the flow if desired. However, in some instances no throttling action at this .point is necessary. The nozzle 21 is preferably so directed that the soap in the reaction products impinges against the walls of the chamber II and moves downward therealong as a thin stream. This nozzle may be tangentially directed if desired, in which event the soap may move downward in a curved path.

In the chamber II vapors of water or glycerine orbothseparateiromtheaoapandmovethrough smaller than the conveyor housing 49 so as a pipe 20 to a condenser system if it is desired to condense these vapors. If both water and glycerine vapors are present, it is possible to fractionally condense same by use of a glycerine condenser 3| and a water condenser 3 I. The condensed glycerine moves downward throughabarometric column 32 with its lower end submerged in glycerine in a tank 33, this barometric column being of sumcient height to balance the low pressure maintained in the chamber 25. The water vapors are condensed in the condenser SI and move through a barometric column 34 to a tank it A vacuum pump 3' is connected to the condenser II and maintains a low pressure in the chamber II by forcibly withdrawing the vapors therefrom.

or hot inert gas introduced into the chamber.

25 exerts its own partial pressure and facilitates removal of glycerine vapors from the soap if it is desired that the glycerine content of the finished soap be low. Sufficient heat is applied, either in the heater ii or in the chamber 25, or both, to insure that the soap reaches the bottom of the chamber 25 in molten, plastic, or semi-plastic condition.

A rotating scraper 45, suitably driven, moves the soap from the bottom wall of the chamber 25 into two troughs 41 extending transversely across this chamber and forming a part of the conveyor system. Each of these troughs can be heated or cooled as desired by circulation through jackets 48 extending therearound.

Extending as a continuation of each trough is a conveyor housing 4! of cylindrical shape, and a suitably driven soap-advancing screw It is pofltioned in each housing and extends into the corresponding trough 41. Each screw provides a shaft 5| driven by a gear 52, and provides a helical vane 53 of a diameter only very slightly to continuously force the soap into a chamber 55. I! desired, each screw 10 may be formed in flights, separated by spaces receiving members 50 which extend into the conveyor housing. To make each of the members 58 removable and adjustable, it may extend through a nipple 5B, being-carried by a cap 59 threaded to the nipple as shown in Fig. 4. break up the soap stream, and serve to mill or plod the soap during advancement. This construction thus provides conveyors B0 and SI for continuously removing the soap from the chamber II. In some instances a single conveyor is suiilcient.

.Each conveyor is preferably provided with a pipe '2 whichreturns to the chamber 25 any vapors which may separate from the soap while in the conveyor.

It is desirable to,cool the soap while in the conveyors Cl and I. A cooling medium may be circulated through a .jacket 63 surrounding each conveyor housing 4!. In addition, it is often desirable-to internally cool the annular stream or soap moving in each conveyor. In this-capecity, the shaft ll of each conveyor is hollow and a pipe 04 extends therein. vA cooling medium,

These members serveto such as water, may be forced into the pipe 84 and discharged into a space 05 surrounding a sleeve 08, this water returning through the annular space GI-around the pipe 84 inside the shaft 5|, being ultimately discharged through a head 88.

It is often desirable to make that end of the shaft 5| next the chamber 55 of larger diameter, to provide an enlargement or head 68. This decreases the available space for the soap and acts to compress same. In addition, it causes attenuation of the soap, thus facilitating cooling thereof.

The heat conductivity of the soap in such a soap stream is quite low and in many instances it is desirable to further cool the soap by moving this soap stream through one or more cooling grids: I and 7| which may extend through the chamber 55. Each of these cooling grids is formed of a plurality of pipes positioned close to each other so that the soap must move through the rather small spaces therebetween. Water or other cooling medium is circulated through these pipes,'for instance, by connecting these pipes to headers 13 such as shown in Fig. 5. By thus further attenuating the soap very eflicient cooling can be obtained.

The two soap streams discharged from the conveyors 60 and SI move into an intersecting conveyor 80, the chambers 55 opening on a passage formed in a conveyor housing 8I in which a screw 82 rotates. This screw is formed similarly to the screw 50, providing an enlarged head 83 and being hollow so that water or other cooling liquid can be circulated therethrough Whenintroduced into a pipe 84, this water being discharged through a pipe 85. The screw 82 is similarly formed in flights between which members corre-' sponding to the members 58 extend. The soap is thus milled and plodded during passage through the conveyor 80 and is further compressed by the enlarged head 83 before discharge into a chamber 86. The conveyor housing 8| is jacketed as indicated by the numeral 81 and a cooling medium is circulated through this jacket to further cool the soap. The screw 82 is turnedas by a gear 88 preferably at a faster rate than the screws 50, especially as it is desirable to make the conveyor housing 8| somewhat smaller indiameter than the conveyor housings 48. In addition, the heli-' cal vane forming a part of the screw 82 is preferably of smaller pitch near the conveyor 80 than throughout the remainder of its length, this smaller pitched portion being indicated by the numeral 89.

If desired, the soap may be delivered from the chamber into the atmosphere, being extruded through a valve 90, the subsequent portion of the equipment illustrated being disconnected.- This mode of operation can be utilized if the soap has been cooled to such an extent that exposure to the atmosphere will not result in deleterious .reactions, such as discoloring or spontaneous combustion. Depending upon operating conditions in the preceding\part of the'system, the soap thus pivoted at and adjusted by an arm 83 so as to extend partiallyacross the chamber". This valve acts in part as a vacuum seal, being preferably adjusted so that the available opening through which the soap discharges iscompletely filled by the soap stream. Thus, even ii. the chamber 25 is under a high vacuum, no air will move rearward through the conveyors to impair the vacuum in this chamber. In this connection, the soap stream in the conveyor 80 acts as a vac uum seal, and if the chamber 25 is maintained under high vacuum, pressure on the soap will progressively increase during flow through the conveyor system described.

In many instances it is preferable to continu the processing of the soap beyond the valve 90 for purposes of hydration, addition of builders or fillers, etc. Thus, the soap moving through the valve 80 may move directly into a conveyor I00, or may drop thereinto through a member IOI. This conveyor provides a screw I02 which may be rather loose fitting and which is rotated to further plod and advance the soap. If desired, various builders or fillers may be introduced into the soap at this time, for instance, by moving same under pressure through a pipe I03. Such material may bemoved along the pipe I03 and into the soap by use of a screw rotating in this pipe. Materials thus introduced into the conveyor I00 will be intimately mixed with the soap therein. The conveyor I00 builds up sufiicient pressure to extrude the soap through one or more orifices, preferably through a perforated plate I 04, into a housing I05.

The soap emerges from the openings of the perforated plate and drops as a powder or in small masses into a throat formed between rotating rolls I01 and I08 where any masses of soap are crushed and where the soap is further attenuated and compressed into a thin layer. These rolls are hollow to provide chambers I09 and a cooling medium is circulated through these chambers.

"This is an excellent way of further cooling the prolonged contact with the atmosphere.

It is often possible to use the rolls I 01 and I08 for hydrating the soap, especially if 'the soap is of such a nature that water can be directly added thereto to be uniformly absorbed thereby. In this connection, the entire-external length of the roll I01 may be wetted by water sprayed thereon or supplied through an elongated nozzle II 2 to form a layer or film of water along this external surface. Any excess water above .the desired quantity may be removed by a scraper II 3 extending along this external surface and adjusta ble in, radial position relative thereto. This scraper II3 may be mounted on one or more screws I I4, and nuts I I5 may be used to vary the distance between the wiping edge and the periphery of the roll I01 to form a film of water on the to further distribute the water uniformly.

The soap drops frombetween the rolls I01 and I08, or is scraped. therefrom by scrapers I I8, and

moves into a hopper I I8 which discharges into a throat formed by rolls I and I 2I which are also hollow so that a cooling medium can be circulated therethrough. If desired. further moisture can be applied at this point.

The soap drops from between the rolls I and i2 I, or is scraped therefrom by scrapers I25, and reaches a belt conveyor I which extends through a small opening of the housing I05 and conducts the soap to a hopper I28. The soap at this point may be in'powdered or flake form and if desired may be marketed as such. However, if it is desired to form the soap into a bar the hopper I26 may discharge into an extruding device which will compact the soap and extrude same through an orifice I28. A screw I29 rotating in a housing I30 may serve to compact the soap into a homogeneous mass, supplying sufflcient pressure to extrude the soap as a continuous stream through the orifice i28. This stream of soap may be cut into bars as desired.

In general, it can be said that this system can be operated to produce various diflerent forms and types of soap. Proper control of pressure and temperature conditions at various points in the system will largely control'in this regard, and the condition of the soap in the bottom of thechamber 25 is one important factor. Primarily, the temperature and pressure conditions in the coil [9 and in the chamber 25 control the character of this soap which is withdrawn from the lower end of the chamber 25.

It will be clear that the pressure in the coil l9 decreases progressively from the inlet end to the exit end due primarily to pipe friction retarding the flow. For instance, when using the throttling nozzle 21 the pressure in the pipe 22 may be in the neighborhood of 50 lbs. per sq. in. or even considerably more if desired, while the pressure in the pipe i5 may be much higher, often as high as 350 to 450 lbs. per sq. in. If no throttling action is desired the vacuum in the chamber 25 will carry back a considerable distance into the coil [9. Fromthe angle of temperature, it will be clear that this temperature increases progressively during flow through the coil l5.

These conditions of temperature and pressure in the coil is should be so regulated as to give complete saponification therein. In addition, all of the water, and all or at least a part of the glycerine, should be vaporized in the coil 19 if the friable soap product is to be produced. If the flow of reaction products is throttled, as by the nozzle 21 or the valve 26, some or all of the remaining unvaporized glycerine will flash into vapor at the lower pressure existing in the chamber 25. Such a vacuum condition in this chamber is very desirable in that it reduces the boiling point of the glycerine and permits the soap to be withdrawn from the chamber in substantially glycerine-free condition if desired. The presence of steam in the chamber 25 will further lower the boiling point of the glycerine due to the law of partial pressures.

The friable nature of the soap results from cooling same from a molten, plastic, or semiplastic condition. Such. a condition can sometimes be brought about by utilizing suflicient heat in thecoil l9 and without addin additional heat in the chamber 25 but it has been very d s able to utilize a heating medium in the Jacket 40 especially when starting up the apparatus and preferably throughout continuous operation thereof. Application oi. heat to this chamber will decrease the necessary temperature in the coil 39 and will insure that the soap withdrawn from thelowerendofthischamberwillbeln molten, plastic, or semi-plastic condition.

It will thus be apparent that no definite range of temperatures and pressures in the coil I! can be named, for these will vary with the temperature and pressure in the chamber 25 and also with the particular saponiflable material utilized. Further, no definite temperatures can be set forth as necessary for maintaining the soap in molten, plastic, or semi-plastic condition, for these temperatures will vary with different soaps. In general, however, it can be said that soaps made from cottonseed oil should be at a temperature above about 455 F., and soaps made from palm oil or tallow should usually be at a temperature above 518 F. if such soaps are to be in molten condition. Somewhat lower temperatures are permissible if the soap is to be in plastic or semiplastic condition.

'The temperature of the reaction products in the pipe 22 may be above these values, for some cooling of the soap takes place in the chamber 25 unless a large amount of heat is added at this time. Some cooling is not detrimental, for it has been found that the soap when once molten can be cooled somewhat without changing it from molten, plastic, or semi-plastic condition. In fact, molten soap can be reduced to a temperature somewhat below that necessary to bring it into molten condition and yet be quite fluid. If no large amount of heat is added in the chamber 25, best operating temperatures in the pipe 22 will often be above 500 F. if the soap is to be in molten, plastic, or semi-plastic condition in the bottom of this chamber. With many saponifiable materials, best results have been obtained when temperatures in the pipe 22 were as high as 570 F. or even higher, when no large amount of heat was added to the chamber 25.

The preferred mode of operation is to use coil temperatures sumciently high that the soap reaching the side walls of the chamber 25 will be quite fluid so as to readily move downward there along. This facilitates separation of vapors from the soap due to the fact that this soap moves downward as a relatively thin layer, thus exposing a large surface to the low-pressure in the chamber 25. This feature of flowing the soap along the walls of the chamber 25 also prolongs the time necessary for the soap to reach the bottom of this chamber and thus gives additional time for vapors to separate. The tendency for this downward-flowing soap to somewhat cool can be attributed to loss of heat by radiation, or to vaporization of glycerine during this downward movement. However, even if no large amount of heat is added to the chamber 25, this cooling usually does not exceed F., and can be made much smaller or even eliminated, if sufflcient heat is added to this chamber. Application of sumcient heat to the chamber 25'may even slightly increase the temperature of the soap.

"The controlling factor is that the soap in the 2 cooling is preferable. with the system shown 7 it is possible tov cool the soap in a short time, usually between four and twenty minutes, depending upon the length of the conveyors and the amount of soap moving through the system. While slower cooling can sometimes be used, it has been found that rapid cooling is preferable in that it assists in forming the incipient planes of fracture throughout the soap which results in its friable nature. Attenuation of the soap prior to or during cooling will greatly facilitate rapid cooling, and the internal and external cooling of the soap streams in the conveyors, in conjunction with the cooling grids 10 and II will be found very effective for this purpose. In addition, cooling on rolls is even more effective in this regard.

By way of example, the system can be used to produce the friable and directly hydratable soap mentioned above by operating under the following temperatures and pressures given. With a, saponifiable material comprising 70% tallow and 30% cocoanut oil, and with a solution of 31 B. caustic solution as a saponifying material, pressures in the pipe I5 have been used between 350 and 450 lbs. per sq. in. with a coil I9 composed of pipe .of A" internal diameter and about 550 ft. long. These pressures will be different with coils of different length and internal diameter. The pressure. in the pipe 22 may be about 50 lbs. per sq. in. though this is not critical, and the temperature therein in this example may be from 560 to 570 F. The reaction products will be discharged through the nozzle 21 against the walls of the chamber 25, the soap under these conditions being sufficiently molten to run down these walls. Due to expansion and radiation losses, the temperature of the soap in the bottom of the chamber 25 will be in the neighborhood of 500 F. or somewhat higher, the temperature in the Jacket 40 being about 536 F. A vacuum of 27-28 inches of mercury in the chamber 25 will permit removal of substantially all of the glycerine in this example. This soap is cooled in the conveyors 60, 'BI and to produce a friable soap.

Very satisfactory results can be obtained by able water can be added to this powder and by 7 any simple mixing operation it will be uniformly absorbed to produce a soap powder hydrated to the desired. extent. The amount of hydration thus possible varies with different soaps, but

with most soaps 8 to 20% or more water can the soap while in the conveyors to such. an

extent that it canbe discharged into the atmosphere from the valve 90. By way of example, it can continue its movement by moving through the conveyor I00, being further cooled on the rolls I01 and I08, and vbeing hydratci at this point. The soap will drop in flake r powdered form from the rolls I01 and III! and can be used in this form, or it can be .urfi-er cooled on the rolls 20 and. i2l, and adCT'o al water can be added at this point, if :1 Si d. The soap is then withdrawn by the belt conveyor I25 and is ready for use. If bar soap is desired, this product can be moved through the-extrusion device I30, being extruded as a bar through the orifice I28. This bar can be cut up to form cakes.

The hydratable character of this soap is not changed, by adding various fillers or builders in the conveyor IIlII. Further, the presence of some glycerine does not ,in itself defeat this hydratable characteristic, though best results have been obtained when substantially all of the glycerine has been removed.

The system herein disclosed can be used to continuously make other types of soap of a non-friable nature. For instance, if lower tern-*- peratures are used in the coil It, the soap can be collected in powdered or granular form in the chamber 25 and withdrawn by the conveyor system shown. So also, if the absolute pressure in the chamber 25 is higher this type of soap may be collected in the chamber 25 even with the coil temperatures mentioned above. Such powdered or granular soap may still contain all or a portion of the glycerine if desired, and all or a portion of the water may be allowed to remain therein under proper conditions of temperature and pressure in the system. As before, this type of soap will be continuously with drawn by the conveyors 60, 6:3, and to, being cooled therein. If cooled to a sufficient degree, this soap can be discharged into the atmosphere through the valve in the form of a temporarily adhering mass of soap particles. Alternatively, the soap, can be delivered from the valve 90 to the conveyor I00, and fillers or builders may be there added. This soap may thus be conditioned in a continuous process so that when it is discharged through the perforated plate I04, it is in condition for use.

If powdered or granular soap is withdrawn from the chamber 25, this soap may be hydrated by adding moisture thereto during flow through the conveyor system. For instance, water or steam may be supplied through pipe 200 into the conveyors 60 and 6 I or through a pipe 20I to the conveyor 80. Further, water may be introduced into the conveyor I00 through a pipe 202 to hydrate the soap. Such a method of hydration by directly introducing the water into one or more of the conveyors is to be avoided if the friable and uniformly hydratable soap is to be produced. However, this method of hydration can be successfully used with other types of soap. If used, it is sometimes preferable to introduce the water while the soap is still at such temperature that the water will be vaporized, thus more uniformly distributing the water.

The hydrated soap resulting from this mode of operation may be used as delivered from the perforated plate I04, or may be compressed into bars in an extruding device. extruded through the perforated plate I04 may be compressed between the rolls shown to form flakes which may be used in this form or compressed into a bar if desired. In this instance the soap reaching the rolls will already be hydrated and So also,.the soap thus to the soap.

If.a powdered soap is to be collected in the chamber 25, one or more baffles may be provided in the upper end so that the vapors move through a tortuous path. This will tend to separate any minute particles which might tend to be carried upward with the vapors. Such bailies are usually not necessary if the process is so operated as to produce molten, plastic, or semi-plastic soap in the chamber 25. Regardless of whether the soap is withdrawn from the chamber 25 in molten, plastic, semi-plastic or powdered condition, the conveyor system will continuously withdraw this soap without impairing any vacuum which exists in thischamber, for the soap and the valve 80 will act to seal this chamber from the atmosphere.

The system disclosed has wide utility in making various types of soap from various'ingredients,

and the present invention has novelty in the process, the apparatus, and the friable soap product produced.

I'he term friable as employed in the product claim hereof is intended to define a soap product which can be reduced to a powder by such slight pressure as is produced by rubbing a portion of said soap between the thumb and iinser.

I claim as my invention:

1. A method of making soap, which includes the steps of: forming a mass of substantially anhydrous soap in a molten, plastic, or semi-plastic condition; removing a stream of said soap from said mass, cooling said stream of said soap while in substantially anhydrous condition and while in a space confined from the atmosphere to form a friable soap which is directly and substantially uniformly hydratable by adding moisture thereto; continuously breaking up said friable soap as fast as produced; and adding moisture to the brokenup soap in controlled amount to hydrate same.

2. A method of making soap, which includes the steps of: forming a mass of substantially anhydrous soap in a molten, plastic, or semi-plastic condition; and forming a friable soap therefrom which will substantially uniformly absorb water by removing a stream of said soap from said mass, coolingsaid stream of said soap from its molten, plastic, or semi-plastic condition while in said substantially anhydrous condition in a space confined from the atmosphere and then further cooling said soap on cooling rolls.

3. A method of making soap which includes the steps of: forming a mass of substantially anhydrous soap in a molten, plastic or semi-plastic condition; removing a stream of said soap from said mass, and cooling said stream of soap while in substantially anhydrous condition and while in a space confined from the atmosphere to form a friable soap which is directly and substantially uniformly hydratable by adding moisture thereto and continuously moving and attenuating said soap during'said cooling.

4. A method of making soap which includes the steps of: forming a mass of substantially anhydrous soap in a molten, plastic or semi-plastic condition; removing a stream of said soap from said mass, and cooling said stream of soap while in substantially anhydrous oondition'and while in 2,190,015 rolls need not serve this function of adding water a space confined from the atmosphere to form a friable soap which is directly and substantially uniformly hydratable by adding moisture thereto and maintaining a vacuum during at least a portion of said cooling.

5. A method of making subdivided soap from a mass of substantially anhydrous soap in molten, plastic, or semi-plastic condition, which method includes the steps of: withdrawing a stream of soap from said mass; continuously cooling said soap moving in said stream while still substantially anhydrous to form a friable mass capable of uniformly absorbing moisture when added thereto: reducing the resulting friable soap to subdivided form; and adding moisture to the subdivided soap in controlled amount to hydrate same.

6. A method as defined in claim 5 including the step of adding a material such as a soap builder or filler to the cooled soap stream before said moisture is added.

7. A method of continuously making soap, which includes the steps of: continuously heating a mixture of a saponifiable material and a saponifying material to form reaction products including soap. and vapor; continuously introducing said reaction products into a separating chamber maintained under vacuum; continuously removing vapor from said chamber to leave therein substantially anhydrous soap in molten, plastic, or semi-plastic condition; continuously withdrawing a stream of this soap from said chamber and cooling same while still substantially anhydrous and from its molten, plastic, or semi-plastic condition to form a mass of friable soap which will directly and uniformly absorb water; continuously subdividing the stream of soap; and hydrating the subdivided soap.

8. A method of continuously making soap, which includes the steps of: continuously heating a mixture of a saponifiable material and a saponifying material to form reaction products including a soap and vapor; continuously introducing said reaction products into a separating chamber maintained under vacuum by impinging said reaction products against a wall of said chamber, the soap flowing down said wall and reaching the lower end of said chamber in substantially anhydrous molten, plastic, or semiplastic condition; continuously removing vapor from said chamber; continuously moving a stream of the molten, plastic, or semi-plastic substantially anhydrous soap from said chamber in such a manner as not to impair the vacuum therein; and cooling this stream of soap before exposure to the atmosphere to form friable soap which will substantially uniformly absorb water.

9. A method as defined in claim 8 in which heat is applied to said chamber.

10. A method as defined in claim 8 in which heat is applied to said chamber by introducing a hot medium thereinto which is withdrawn with I said vapors.