Search Images Maps Play YouTube News Gmail Drive More »
Sign in
Screen reader users: click this link for accessible mode. Accessible mode has the same essential features but works better with your reader.

Patents

  1. Advanced Patent Search
Publication numberUS2532792 A
Publication typeGrant
Publication dateDec 5, 1950
Filing dateApr 13, 1946
Priority dateApr 18, 1945
Also published asDE847279C
Publication numberUS 2532792 A, US 2532792A, US-A-2532792, US2532792 A, US2532792A
InventorsEdvin Svensjo Nils
Original AssigneeSeparator Ab
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Process for the centrifugal separation of sludge-containing liquids
US 2532792 A
Images(2)
Previous page
Next page
Description  (OCR text may contain errors)

Dec. 5, 1950. N E SVENSJO 2,532,792

PROCESS FOR fHEfCENTRIFUGAL. SEPARATION OF SLUDGE CONTAINING LIQUIDS Filed April 13, 11946v 2 Sheets-Sheet l FLOW REGULflTOR l i/070C541. 3

ilaw REGUtfiTOR 7 L 5 Dec. 5, 1950 N E svENsJo 2,532,792

PROCESS FOR THE CENTRIFUGAL SEPARATION OF SLUDGE CONTAINING LIQUIDS 2 Sheets-Sheet 2 Filed April 13, 1946 I/VVE/VI'UK A zZ; 41 3? 31/5875 named Dec. 5, 1950 PROCESS FOR THE CENTRIFUGAL SEPARA- TION OF SLUDGE-CONTAINING LIQUIDS Nils Edvin Svensjii, Nockeby, Sweden, assignor to Aktiebolaget Separator, Stockholm, Sweden, a corporation of Sweden Application April 13, 1946, Serial N0. 661,997 In Sweden April 18, 1945 2 Claims. (01. 233-14) This invention relates to a process for the centrifugal purification of sludge-containing liquids. The invention is particularly applicable to the removal of solid particles from a liquid in which they are in suspension, by means of a centrifugal separator of the type in which the bowl is provided at its periphery witi'isutletopenings through which the solid particles leave the bowl together with a certain quantity ofv carrier liquid.

The sludge-discharge openings should be large enough to allow solid particles to freely pass therethrough. However, if the content of solid particles is small, a concentrate very poor in sludge is discharged through the openings. This is usually undesirable, as, for example, if the liquid in the concentrate must be removed later on by evaporat on.

To avoid this excessive discharge of carrier liquid with the sludge, it has been proposed to return varying amounts of the concentrate into the bowl, whereby is obtained an arb trary increase in the sludge content of the concentrate in the bowl. However, the concentration must not be too high, since this causes the openings in the bowl to become clogged.

In practice it has been necessary to work at rather low concentrations, it being diflicult to judge at what sludge-content of the concentrate clogging takes place. As the sludge-content of the unseparated liquid often varies considerably and as a discharge opening or several of the discharge openings may be clogged by separate large particles which have entered the bowl, the maintenance of a desirable sludge content in the separator is diflicult. In practice it has been found necessary to work well below the maximum capacity of the separator.

I have found that a too high sludge content of the concentrate is not the sole cause of the clogging. The size and form of the particles are also contributory clogging factors.

I have found that viscosity is the determining factor influencing the danger of clogging.

- Viscosity is dependent on many factors, such as the sludge content, the temperature of the liquid to be separated and the size and form of the particles. By determining the vscosity of the sludge-containing concentrate, discharged from the bowl, and by regulating, in accordance with such viscosity determination, either the percentage of the discharged sludge-containing concentrate returned to the bowl, or, less preferably, the rate of feed of the mixture fed to the bowl, the viscos ty of the concentrate may be main. tained substantially constant.

The accompanying drawing shows an arrangement in which the above-mentioned method of regulation is employed. Fig. 1 shows diagrammatically the whole installation, whilst Fig. 2 is a detailed illustration. of one form of the regulating device. In the drawing, I designates the centrifugal separator bowl or locus of centrifugal force, 2 the feedpipe for the mixture to be separated, 3 the discharge-pipe for the separated liquid free from sludge and 4 the discharge pipe for the separated sludge-containing concentrate. Part of the concentrate is fed back to the bowlthrough the ppe 5 to increase the viscosity of the concentrate in the bowl. The remaining concentrate leaves the system via the outlet pipe 6.

According to the invention, the viscosity of the sludge concentrate discharged through pipe 4 is determined, and the quantity of concentrate led back to the bowl through pipe 5 is varied in accordance with any departure of the determined viscosity from a desired viscosity. That is, if said determined viscosity is above standard, the percentage of the discharged concentrate that is returned to the bowl is reduced. If said determined viscosity is below standard, the percentage of the discharged concentrate that is returned to the bowl is increased. The effect is to maintain the viscosity of the discharged concentrate at a substantially constant value.

The drawing discloses means whereby the above descr bed operation may be eflected automatically. Interposed in the pipe 4 is a continuous flow viscosimeter 1, which operates through a connection Ia to control a quantity-regulating device 8 in the pipe 6. If, for instance, the viscosity as measured by the viscosimeter rises above a predetermined value, the device 8 is actuated from the viscosimeter to increase the liquid flow through the pipe 6 and so to reduce the flow through the pipe 5 until theviscosity is reduced to the desired value. The predetermined viscosity should be as high as is possible consistent with avoidance of clogging of the sludge discharge openings.

The quantity of sludge in the concentrate may vary and also the temperature and the form and size of the particles, but the concentrate should always have as high a content of solid particles as is consistent with the maintenance of a free dscharge from the bowl.

It is important that the quantity-regulating device 8 should control the liquid-flow through the pipe 6. If one of the openings in the bowl should get clogged by a large particle, thus re- (lim ng the total flow through the pipe 4, the return-flow through the pipe I will be reduced immediately, whereby a temporary increase of the concentration in the bowl is prevented. The quantity regulator 8 is so designed that its capacity is not influenced in a substantial degree by the quantity of liquid flowing out through the openings per unit of time. It may comprise, for example, as shown in Fig. 2, a gear-pump II, or other type of pump, whose speed is regulated by the viscosimeter 1. Such a viscosimeter may consist of a rotatably supported drum l2, connected to the pipe 4 by a flexible inlet I3 and a flexible outlet it. Thus the concentrate discharged from the separator l flows through the drum. In the drum there is enclosed a rotatable element ll, which is driven at a constant speed by an electric motor IS. The rotary motion of the drum i2 is, by means of two gears l1 and II, transmitted to the movable contact-arm l 9 of a variable rheostat. A small or great part of the resistance of the rheostat can be switched in the circuit of an electric'motor 2|, which drives the pump I l. A spring 22 tends to maintain a certain part of the resistance 20 in the circuit. The torsion moment transmitted from the rotating element ii to the drum l2 by the intermediary of the flowing concentrate, counteracts this tendency of the spring.

The concentrate flowing through the drum i2 will transmit a torsion moment to the drum from the constant speed rotating element IS, the magnitude of the transmitted torsion moment depending upon the viscosity of the concentrate in the drum. Thus, when the viscosity increases, a reater torsion moment will be transmitted to the drum l2 so ,that the latter, operating through the gearing l'l-l8, will act against the spring 22 and cut out additional resistance 20 of the rheostat. As a result, the motor 2| will drive pump II at a higher speed and thereby reduce the rate of flow of concentrate through the return pipe 5 to the centrifuge. Conversely, when the viscosity of the concentrate decreases, the torsion moment transmitted from rotating element ii to the drum i 2 will decrease and allow the spring 22 to cut in additional resistance 20 of the rheostat. The speed of the pump II will then decrease and cause an increase in the rate of flow of concentrate through return line 5 to the centrifuge.

The viscosimeter may be made to control a quantity-regulating device in the pipe 2, but this arrangement is not as desirable as the control of the flow from pipe 6, since the separator would not then operate at its highest separating capacity.

An arrangement according to the above may comprise a photocell 9, in the purified liquid discharge pipe 3, controlling a quantity-regulating device Ill in the feed-pipe 2 in such a way that the feed to the separator is so regulated that a predetermined degree of purity in the liquid is insured. The separator may be operated at capacity and at the same time badly separated liquid is prevented from passing from the system if some opening in the bowl is clogged.

The photocell 9, of course, will respond to changes in the light transmitting ability of the purified liquid discharging through pipe I, and operates through a suitable connection 9a to control the flow regulator I, so that the rate of feed through pipe 2 is reduced when the content of sludge particles in the purified liquid (pipe 8) increases, and vice versa. It will be apparent that if, at a given throughput rate for the separator, the viscosity of the sludge becomes $00 4 high,thelimitoi'theseparatingabilityofflie separator may be exceeded, whereby part of the sludge from the separator will accompany the liquid component flowing through discharge pipe 2. Accordingly, under this condition, not only will the viscosity of the outfiowing sludge in pipe 4 increase, but also the light transmitting ability of the liquid component (pipe 2) will decrease, as seen" by photocell 8, due to such intermixing of sludge with the liquid component. The arrangement of the photocell and flow regulator II is illustrated only schematically, as such arrangements per se are well known in the art. As an example of a conventional arrangement, the pipe I may have a transparent section located between a light source and the photo-sensitive element, so

that the light must pass through the transparent section (and the liquid flowing in it) to reach the photo-sensitive element. The electric'current changes in the latter, which are generally amplified, may be used to actuate a servomotor operating through connection so to control the flow regulator it, which may be a valve or a variable speed pump.

A method such as described will separate a concentrate with a varying sludge content, which, however, is at all moments as high in sludge content as possible when either the separator is operating with a free fiow through the bowl or is partially clogged. A partial clogging of the discharge effects only a reduction of the capacity, but does not increase the viscosity of the concentrate or involve any'deterioration in quality of the separated liquid. Alternatively, the feed need not normally be as low as when the risk of a partial clogging has to be considered.

What I claimand desire to protect by Letters Patent is:

1. In an apparatus for continuously purifying a sludge-containing liquid, comprising a centrifuge having a separating chamber with an outlet for discharging liquid bearing a concentration of separated sludge and also having an outlet lor discharging the purified separated liquid, a discharge pipe connected to said first outlet, and a return pipe leading from said first pipe for returning to the centrifuge part of said liquid bearing the sludge concentrate, the combination of a viscosimeter connected to the discharge pipe at a location between said first outlet and said return pipe, flow regulating means in the discharge pipe and located beyond the return pipe with respect to said first outlet, and an operative connection between the viscosimeter and saidv regulating means for operating the regulating means in accordance with variations in the indications of the viscosimeter, whereby the rate of return of sludge concentrate to the centrifuge is varied.

2. In the process of separating solids from a mixture of solids and liquid, by continuously feeding the mixture into a locus of centrifugal force to separate the same into a purified liquid and a sludge-containing concentrate, continuou.

1y discharging said separated liquid and concenin reasing the rate or flow at said region in recentrate discharge, and decreasing the rate of flow at said region in response to a decrease in the viscosity of the concentrate discharge, whereby the viscosity of the concentrate discharge is maintained approximately constant, and in which said changes in the rate of flow at said region of the concentrate discharge stream are effected in response to variations in the viscosity as determined at a part of said last stream between said locus and the point of withdrawal of the return concentrate.

NILS EDVIN svENsJ6.

REFERENCES CITED The following references are of record in the file of this patent:

Number Number 6 UNITED STATES PATENTS Name Date Ericsson Feb. 9, 1909 Sharples July 3, 1917 MacKaye Oct. 2, 1923 John Dec. 26, 1939 Hagy Jan. 25, 1944 Cram Jan. 1, 1946 FOREIGN PATENTS Country Date Great Britain Oct. 17, 1929 Great Britain May 8, 1935 Germany July 5, 1939 Sweden Sept. 8; 1942

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US911652 *Mar 23, 1906Feb 9, 1909Separator AbCentrifugal machine.
US1232104 *May 6, 1916Jul 3, 1917Philip T SharplesProcess of and apparatus for separating solids from liquids.
US1469522 *Sep 27, 1921Oct 2, 1923Mackaye JamesCentrifugal separating apparatus
US2184598 *Apr 27, 1937Dec 26, 1939 G jahn
US2339991 *Nov 13, 1941Jan 25, 1944Hagy Ernest AViscosity measuring apparatus
US2392026 *Oct 14, 1944Jan 1, 1946Manitowoe Shipbuilding CompanyConsistency regulator
DE677969C *Feb 2, 1938Jul 5, 1939Bergedorfer Eisenwerk AgVorrichtung zum Entoelen von Niederschlagwasser durch Schleudern
GB307933A * Title not available
GB428188A * Title not available
SE105479A * Title not available
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US2817439 *Nov 10, 1954Dec 24, 1957Skb Schuchtermann & Kremer BauAdjusting the viscosity of heavy-material suspensions in the dressing of ores
US2955753 *May 3, 1957Oct 11, 1960American Machine & MetalsControl apparatus
US3126337 *Oct 11, 1960Mar 24, 1964 System for separating and classifying solids
US3189268 *Dec 17, 1962Jun 15, 1965AbDevice for determining the position of the interface between two separated components in a centrifugal separator
US3239137 *May 16, 1963Mar 8, 1966Separator AbMethod of discharging sludge from self-opening centrifuges
US3250218 *Nov 9, 1961May 10, 1966Socony Mobil Oil Co IncBlending apparatus
US3261546 *Oct 29, 1962Jul 19, 1966Pfaudler Permutit IncMethod for clarifying fats and oils
US3408000 *Aug 16, 1966Oct 29, 1968Alfa Laval AbDetermination of sludge level in sludge centrifuge
US3443691 *Nov 22, 1966May 13, 1969Alfa Laval AbApparatus for continuous control of the concentration of a substance in a flowing liquid
US3532264 *Oct 15, 1968Oct 6, 1970Bird Machine CoCentrifugal separation apparatus
US3595470 *Oct 28, 1968Jul 27, 1971Pennwalt CorpControl apparatus for centrifuge
US4344560 *Oct 20, 1980Aug 17, 1982Asahi Kasei Kogyo Kabushiki KaishaContainer, apparatus and method for separating platelets
US4475897 *Jul 18, 1983Oct 9, 1984Westfalia Separator AgMethod of and apparatus for optimizing the clarified phase and concentration of solids in a continuous solids-discharge centrifuge
US4525155 *Apr 11, 1984Jun 25, 1985Alfa-Laval Marine And Powering Engineering AbCentrifugal separator and method of operating the same
US4761157 *May 18, 1983Aug 2, 1988Pennwalt CorporationFor the continuous separation of a mixture of solids and liquids
US4784634 *Mar 16, 1987Nov 15, 1988Krauss-Maffei A.G.Sludge dewatering centrifuge for separating liquid and solid components
US4805659 *Mar 31, 1987Feb 21, 1989Westfalia Separator AgFor regulating flow
US5199938 *Oct 31, 1991Apr 6, 1993Westfalia Separator AgCentrifuge drum for concentrating suspended solids
US5277691 *Nov 6, 1992Jan 11, 1994Eastman Kodak CompanyVacuum degassing process
US5282780 *Feb 14, 1992Feb 1, 1994Kloeckner-Humboldt-Deutz AgApparatus for separating solids/liquids mixtures with a slurry bypass
US5300014 *Oct 16, 1992Apr 5, 1994Dorr-Oliver CorporationUnderflow control for nozzle centrifuges
US8702576 *Mar 16, 2011Apr 22, 2014Alfa Laval Corporate AbDevice and method for monitoring and adjusting the radial position of an interface layer in a nozzle centrifuge
US20130065744 *Mar 16, 2011Mar 14, 2013Per KarlssonDevice and method for monitoring and adjusting the radial position of an interface layer in a nozzle centrifuge
DE3228074A1 *Jul 28, 1982Feb 2, 1984Westfalia Separator AgVerfahren und vorrichtung zur optimierung der geklaerten phase und der feststoffkonzentration bei einer zentrifuge mit kontinuierlichem feststoffaustrag
DE3608664A1 *Mar 14, 1986Sep 17, 1987Krauss Maffei AgVollmantelzentrifuge
DE3612063C1 *Apr 10, 1986Sep 26, 1991Westfalia Separator AgVorrichtung zur Regulierung des Konzentratablaufes einer Zentrifuge
WO1994008722A1 *Aug 26, 1993Apr 28, 1994Dorr Oliver IncConstant underflow control for nozzle centrifuges
Classifications
U.S. Classification494/1, 494/37, 137/93, 494/35, 137/92, 73/54.1
International ClassificationB04B11/02, B04B1/12, B04B11/00, B04B1/00
Cooperative ClassificationB04B1/12, B04B11/02
European ClassificationB04B11/02, B04B1/12