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    • 1. 发明专利
    • DE1088891B
    • 1960-09-15
    • DED0014156
    • 1953-01-22
    • DORR CO
    • WAL GERRIT JAN VAN DER
    • B04C5/02B04C5/04B04C5/081B04C5/28
    • 724,656. Centrifugal separators. DORR CO. Jan. 21, 1953 [Jan. 25, 1952], No. 1762/53. Class 23. A multiple hydrocyclone comprises a cylindrical or rectangular rubber block 1, Fig. 1, having a hole 2, at least one ring-like series of bores 3 and sealing lips 4, 5. Each bore has a rubber cover 9, Fig. 3, which has a feed channel 14, a vortex finder 12 and an interrupted cylindrical wall 10 for locating the cover in a like groove disposed in the block 1. The covers 9, together with perforated inlet and outlet plates 23, 22 and the block 1 are clamped between a housing 18 and a cover 24. The housing 18 has inlet and outlet pipes 19, 32 and the cover 24 has an outlet pipe 33. The cover may be modified as shown in Fig. 6, the diameter of a recess 48 therein corresponding to that of the cylindrical bore 6 in the block 1 whereby the length of the said bore 6 can be correspondingly reduced. Two such hydrocyclones may be arranged in series.
    • 7. 发明专利
    • FR1113895A
    • 1956-04-05
    • FR1113895D
    • 1954-10-26
    • DORR CO
    • C02F3/28C12M1/107
    • 766,933. Treating sewage. DORR-OLIVER, Inc. [formerly DORR CO.]. Oct. 14, 1954 [Oct. 27, 1953], No. 29612/54. Class 111. Highly-concentrated sludge which may be produced by the method and apparatus of Specification 745,295 is fed continuously or at short intervals (e.g. from ¢ hour to 2 hours) at 70, Fig. 4, to a digestion tank 49 fitted with stirrers 65, sludge draw-off 55, re-circulating pump 57 and heater (not shown). Fig. 1 (not shown )is substantially the same as Fig. 6 of the above Specification, the main modifications being the omission of the pipe 49 for return of digester supernatant to the inflow pipe to the plant, and the addition of a sludge transfer pump in combination with a time-clock device in the digester inflow pipe. Fig. 2 (not shown) is identical with Fig. 2 of the above Specification. The concentration of sludge fed to the digester is preferably high enough to eliminate the need for dewatering of the digested sludge. The digestion process is such that no supernatant is produced. Fig. 3 exhibits the relationship C2 between gas generated in the digestion tank as a percentage of the total gas available (ordinates) and digestion tank volume per capita in cubic feet (abscissae). The range of the latter within which the invention is practised is indicated at R2. The corresponding relationship C1 and range R1 for conventional sludge digestion processes are also shown. The variables in the expression for " Digester Index " shown on Fig. 3 are defined as follows : "g" is the amount, in cubic feet per day, of the available gas in the digested sludge discharged ; " V " is the volume, in cubic feet, of the digester ; " G " is the amount, in cubic feet per day, of the gas produced by the digester ; " Q " is the amount, in cubic feet per day, of raw sludge introduced into the digester. Assuming a fixed value for the Digester Index of 40 per cent for conventional digestion and of 120 per cent for high rate digestion, "g" is calculated, for a range of abscissa values, as a fractional multiple of G. In evaluating the equivalent ordinates, 100 (1-g/(g+G)), the variable G cancels. To attain a maximum Digester Index the digester must be operated so as to produce a maximum of gas and lose a minimum (g) in the sludge discharged while receiving the maximum sludge input into the minimum digester volume.
    • 10. 发明专利
    • Contacting solids with gases
    • GB729571A
    • 1955-05-11
    • GB1898952
    • 1952-07-28
    • DORR CO
    • DALTON BENJAMIN SKINNER
    • B01J8/18B01J8/44
    • In apparatus for reacting fluidized finely divided solids with gases, the apertured plate which supports the solids, and through which the gas is introduced, is provided with units which prevent the solids from passing down through the plate when the flow of gas stops; each unit comprises horizontal apertures leading into the bed of fluidized solid from a vertical aperture and includes a horizontal shield arranged so that the piled solids in defluidized condition do not reach to the vertical aperture. In Fig. 2 vertical pipes 233 have horizontal apertures 235 and shield plates 234. In alternative constructions, Fig. 3, horizontal gas passages 335 lead from the top of vertical passages 333; and Fig. 4, horizontal passages 435 are provided in a thickened part of the walls of vertical members 433. In Figs. 3 and 4, the relation between dimensions l and d is such that solids cannot reach the vertical passages.