BRITISH CHEMICAL ABSTRACTS
B.—A P P L IE D C H E M IST R Y
NOV. 8, 1929.
L-GENERAL; PLANT; MACHINERY.
Extractor. J a l a d e .—See XX.
See also A., O ct., 1161. H igh-tem perature technique
( R u f f ) . 1162, Volum enom eter ( F r a n c i s a n d O x n a r d ) . Pa t e n t s.
F u rn ac e. M. A p p e l (U.S.F. 1,726,606,3.9.29. Appl..
28.10.21).—A reversing, regenerative, reverberatory furnace is provided with adjustable deflectors adjacent to the mouths of the gas and air ports.
B. M. V e n a b le s .
[Rotary] kiln. M. S. Price (U.S.P. 1,727,217, 3.9.29. Appl., 17.3.26).—The kiln is shaped as follows, working downwards from the outlet for gases: a rela
tively small and short cylindrical section, a quickly expanding conical part, a long slowly converging part, a cylindrical part. The rate of travel of the material in the slow taper which comprises the major part of the kiln is slower than in the final cylindrical part.
B. M. V e n a b l e s .
[V ertical] kiln. W. D. M o u n t and I. W a r n e r
(U.S.P. 1,725,763, 27.8.29. Appl., 4.4.21).—The kiln is supplied with gaseous fuel at an intermediate point and with air a t the bottom, the products of combustion being drawn off by suction at the top of the kiln proper, but below the feed hopper. The latter is of large capacity and discharges into the kiln by gravity without control.
The finished and cooled material is withdrawn at the bottom by continuous mechanical means, the rate of withdrawal determining the rate of feed.
B. M. V e n a b l e s .
D eterm ining the am ount of heat given off by a heating body. S ie m e n s & H a l s k e A.-O. (B.P.
'299,880, 29.10.28. Gcr., 3.11.27).—The difference in temperature between two points in a heat-conducting substance attached to the heating body is measured and integrated with respect to time. In the case of a domestic radiator, one end of a metallic rod is attached to the narrow face of the radiator at the top, the rod being insulated radially, but the free end is exposed to the atmosphere and may carry a surface having heat-emitting properties similar to those of the radiator.
Both junctions of a thermocouple are embedded in the rod, the hot junction being nearer the radiator than the cold junction; alternatively either two thermo
couples with a common cold junction or an electrical resistance thermometer may be used. The leads of the thermocouple are connected to an integrating device, e.g., an electrolytic counter. B. M. V e n a b l e s .
D rying apparatus. H. D. M i l e s , Assr. to B u f f a l o F o u n d r y & M a c h in e C o. (U.S.P. 1,726,751, 3.9.29.
Appl., 18.6.25} —A drying drum is supported (and
rotated) a t one end only, and the same support carries the means for supplying material to and removing it from the drum. A vacuum-tight casing enclosing the whole can then lie easily slipped on from the other
end. B . M. V e n a b l e s .
Centrifugal drying m achine. G . G r a u s s (B.P.
303,120, 28.12.28. Fr., 28.12.27).—A centrifugal machine with quickly detachable basket (as described in B.P.
212,551 ; B., 1924, 622) is made completely airtight so that it can be used with pressures and temperatures different from those of the atmosphere. The solid m atter may be collected in a filter bag which, when running, fits closely to the basket, but when stopped springs away because of whalebone insertions.
B. M. Ve n a b l e s.
F ire-extinguishing m edia. A. E. W h i t e . From
F y r - F y t e r Co. ( B .P . 318,302, 5.4.28).—Aqueous solu
tions for spraying on to fires comprise potassium, rubidium, or cæsium carbonate considerably in excess of th a t required to react with the acid added to liberate carbon dioxide for generating pressure, or, alternatively, the whole or a part of the excess carbonate may be replaced by other alkali salts with high fire-extinguishing properties, e.g., sodium lactate or nitrate, potassium lactate, formate, acetate, chloride, chlorate, etc. ; f.-p. depressants, e.g., glycol, and about 0-8—2% of a chromate to counteract the corrosive action of th«
carbonate, may also be added. L. A. C o l e s .
Pulverisers. W . A. W h i t e ( B .P . 318,375, 21. and 31.8.28).—An impact pulveriser has oppositely-rotating blade-carrying elements, and both the inlet and outlet for material are nearer the axis than is the pulverising zone, the ground material being withdrawn by a current of air produced by a fan in a separate compartment from the pulveriser. B . M. V e n a b l e s .
Single-zone pulverising apparatus. D. K.
B e a c h , Assr. to R i l e y S t o k e r C o r p . (U.S.P. 1,724,895, 20.8.29. Appl., 5.5.26).—In an impact pulveriser the inlet for material (and air) is at the periphery and the outlet a t the axis. B. M. V e n a b le s .
Rotary ham m er m ills and crushers. J. Y.
J o h n s o n . From P e n n s y l v a n i a C r u s h e r Co. (B .P .
317,208, 24.7.28).—In a mill of the type where the material is flung by rotating hammers against a crusher plate or plates, each plate is pivotted a t one end, and the other end is mechanically agitated to free it from adhering material. The crusher plate may be sub
divided and each section independently agitated.
B. M. Ve n a b l e s.
Fine-grinding m ills. H . J o h a n s o n and G. K ô p p e l
(B.P. 318,302, 4.9.28).—In a mill in which the material
B ritis h C h em ical A b s tr a c ts —B.
8 7 6 Cl. J . — Ge n b b a l; Pl a n t; Ma o h i n e b y.
{e.g., graphite for pencils) is fed to the grinding elements under pressure, the feed pump is of the screw-thread type, and a similar pump of about equal capacity is used to return the partly ground material back to the reservoir, the net amount of material delivered being regulated by controlling the delivery of the return pump. Both pumps are driven by the same shaft as is the grinding mill. B. M. V e n a b le s .
H igh-speed m ixer. R. M . G r e e n l e a f and 0 . L.
R o u t t , Assrs. to P l a s t o i d P r o d u c t s , I n c . ( U .S .P .
1,725,186, 20.8.29. Appl., 7.2.27).—A vertical shaft rotating at high speed carries horizontal arms from which the material is flung to the wall of the containing vessel and by which it is scraped from the wall.
B. M. Ve n a b l e s.
Separation of dry m aterials. K . C. A p p l e y a r d ,
C. W. H . H o lm e s , I. L . B r a m w e l l , and B i r t l e y I r o n
Co., L t d . ( B .P . 317,802—4, 6.2.28).—These three patents refer to the arrangement of riffles on tables for the dry concentration of material such as coal.
B . M. Ve n a b l e s.
Production of dispersions of solids in liquids.
W . H . W iia tm o u g h (B.P. 317,981, 9.8.28).—A relatively coarse suspension is treated first in a high-speed mill (e.g., as described in B.P. 293,510 or 304,178; B., 1928, 658 ; 1929, 268) until only a small percentage of solid remains undispersed, and then in a roller mill having smooth reciprocating rollers. B. M. V e n a b l e s .
Centrifugal filter. C. G . H a w l e y , Assr. to C e n t r i f i x
C orp . (U.S.P. 1,725,712, 20.8.29. Appl., 4.5.25).—
The material enters downwardly through an expanding conduit within which is a conical baffle ; a t the base of the cone is situated a fluid-whirling element, and below th at an axial outlet and bulbous collecting pocket for heavy material. B. M. V e n a b l e s .
Clarifier. P. J. C h a p p e l l e (U.S.P. 1,725,618, 20.8.29. Appl., 1.8.27).—The apparatus comprises a number of concentrically arranged, basket-shaped elements provided with openings and engaging with one another by flanges at the upper ends. The side and bottom walls of the baskets are covered with a fibrous filtering material which is retained in position by means of the stiff lower walls of the baskets. The outer basket is adapted to revolve. A. R. P o w e l l .
Liquid sprayers. D o r m a n , L o n g & Co., L t d . , and M. R. K ir b y (B.P. 318,061, 28.11.28).—Compressed air is led through a tapered (converging) inlet nozzle which abuts against a diverging outlet nozzle ; on the abutting surface of the inlet nozzle radial grooves are formed through which the liquid is admitted from a pipe a t the side. B. M. V e n a b le s .
D istillation apparatus. M. K o n t e r (U.S.P 1,725,528, 20.8.29. Appl., 15.4.27).—The conduit lead
ing from the still to the condenser is bent downwards and up again. An opening is left a t the apex of the V thus formed and a jar is attached in a gas-tight manner for collection of products of distillation.
B. M. Ve n a b l e s.
Bubble still. C. F. B r a u n (U.S.P. 1,725,052,20.8.29.
Appl., 7.9.26).—In a bubble still the drain pipes from successive plates are in vertical alinement, but interposed is a device for mixing downwardly-flowing liquid and
rising vapour and projecting both in a turbulent manner into the liquid on the bubble plates.
B . M . Ve n a b l e s.
[Metal rings for] fractionation apparatus. R . H.
V a n S c h a a c k , j u n . (U.S.P. 1,725,429, 20.8.29. Appl., 8.9.27).—Each ring is formed, as a hollow cylinder with diametral partition, from one strip of sheet metal bent somewhat like a letter S closed up.
B . M. Ve n a b l e s.
Evaporators. H. L . G u y , and M e t r o p o l i t a n - V i c k e r s E l e c t r i c a l Co., L t d . (B.P. 317,772,19.5.28).—
The horizontal tubes of an evaporator are of oval cross- section, and have the long axis vertical, and are evenly spaced over the wetted cross-section of the containing vessel. To allow freer passage for rising bubbles of vapour the upper ranks of tubes may be of smaller horizontal dimensions, or some may be omitted.
B . M . Ve n a b l e s.
Vaporising apparatus. L . V . B a r n a b e (B.P.
318,123, 25.5.28).—The apparatus comprises a freely supported tube coil which is heated from an external source and to which the liquid to bo vaporised is supplied under pressure from a reservoir above. Between the vaporising coil and the reservoir is situated an auxiliary heating coil which is connected at both ends to the reservoir and serves to maintain the pressure therein by heating the liquid. B . M. V e n a b i.e s .
Purification of furnace and like gases. 0 . R a d u l - e s c u (B.P. 292,118, 2.5.28. Roum., 14.6.27. Addn. to B.P. 289,825; B., 1929, 839).—The device described in the original patent is preceded by a dry-cleaner for removal of coarser particles, comprising centrifugal discs rotating between annular baffles.
B . M . Ve n a b l e s.
Separation of dust from boiler flue ga ses. J. T.
B a r o n and J. B . C l a r k e (B.P. 318,082, 22.12.28).—
An uptake, with a cross-section not smaller than th at of the flue from the boiler, is provided with one set of steam jets above the junction with the flue, and with another set below the flue in a downward extension of the uptake which serves as a settling chamber.
B . M . Ve n a b l e s.
Refrigeration. E. B. M i l l e r , Assr. to S i l i c a G e l C o r p . (U.S.P. 1,729,081, 24.9.29. Appl., 3.8.29. U.K.
and Irish Free State, 25.10.24).—See B.P. 225,191;
B., 1925, 483.
Mill for hom ogenising, em ulsifying, etc. W . E p p e n b a c h (U.S.P. 1,728,178,17.9.29. Appl., 24.12.27).
—See B.P. 306,502 ; B., 1929, 497.
Preparing em ulsions of liquid or dissolved sub
stances. B. R e d l i c h (U.S.P. 1,729,185, 24.9.29. Appl., 18.10.27. Ger., 13.7.26).—See B.P. 302,761; B., 1929, 308.
Furnace w alls [com prising water-tubes and m etal blocks]. F u l l e r L e h i g h C o., Assees. of (a )
R. S h e l l e n b e r g e r , (b) E. G. B a i l e y (B.P. 292,959 and 294,876, 27.6.28. U .S ., [a ] 27.6.27, [b] 30.7.27).
Furnace w alls [com prising water-tubes and tiles]. A. P. T h u r s t o n . From F u l l e r L e h i g h Co.
(B.P. 318,695, 27.6.28).
Absorption refrigerating apparatus. E l e c t r o l u x , L t d . , Assees. of P l a t e n - M u n t e r s R e f r i g e r a t i n g
B ritis h C h em ica l A b s tr a c ts —B .
Cl. n . — Fu e l; Ga s; Ta b; Mi n e r a l Oi l s. 8 7 7
Sy s t e m Ak t ie b o l a g (B.P. 301,323, 26.11.28. S w e d .,
25.11.27).
Evaporator units for [absorption] refrigerating apparatus. E l e c t r o l u x , L t d . From P la t e n - M u n - t e r s R e f r i g e r a t i n g S y s t e m A k t i e b o l a g (B.P. 319,050, 15.6.28 and 28.2.29).
[Autom atic conveyor] apparatus for filling solid articles [tablets, p ills, etc.] into receptacles.
I. G. F a r b e n in d . A.-G. (B.P. 299,017, 18.10.28. Ger., 19.10.27).
Distributing plate for gas w ashers and the like.
C. S t i l l (B.P. 318,812, 28.12.28).
II.—FUEL; GAS; TAR; MINERAL OILS.
Evaluation of gas coal. G. A. B r e n d e r a B r a n d i s
and H. J. A. d e G o e y (Het Gas, 1929, 4 9 , 91—103;
Chem. Zentr., 1929, i, 1771—1772).—“ Specific values,”
Q (calorific value of gas X volume/quantity of volat
ile substance, computed on the . dry material), a r e : cellulose 29-1, brown coal 34-2, bituminous coal 47-7—
84-3, anthracite 129-1. Curves illustrate the relation
ship of il to volatile matter, oxygen, water and carbon dioxide, oxygen content of coal, and to the ratio of oxygen to hydrogen. A. A. E l d r i d g e .
Rate of burning of individual particles of solid fuel. H. K. G r i f f i n , J. R. A d a m s, and D. F. S m ith
(Ind. Eng. Chem., 1929,21, 808—815).—The times taken for the complete combustion of particles of fuel when dropped down a vertical furnace maintained a t a definite temperature have been measured. The furnace was provided with a narrow, vertical, silica window through which the incandescent particles were photo
graphed on a film fixed to a rotating drum. The time of burning for particles of a gas coal (45—50-mesh) increased from 0-258 sec. at a furnace temperature of 720° to 0-578 sec. at 1000°. Similar figures were obtained for a semi-coke. Particles of activated char
coal required a considerably longer period to burn than particles of coal of the same size, but the rate of burning of the former showed much less variation with the tem
perature. Results obtained with a beehive coke were somewhat indefinite, due probably to difficulty of ignition, and to selective burning of the smaller par
ticles. The time of burning for all the fuels decreased with the particle size. Possible explanations of the negative temperature coefficient of the rate of burning
of coal and semi-coke particles are discussed.
A. B. M a n n in g .
Fire and explosion risk w ith acetylene. W.
R i m a r s k i (Z. angew. Chem., 1929, 4 2 , 933—936).—
An enquiry into the cause of the recent disaster at Borsigwalde, and into the conditions under which explosive decomposition may be initiated and propagated in acetylene. The findings of earlier workers on the effects of high temperature and pressure, and the ade
quacy of the normal safeguards, are confirmed.
S . I . Le v y.
D eterm ination of carbon dioxide in g ases containing acetylene. H. F r i e d r i c h (Chem.-Ztg., 1929, 53, 706—708).—Acetylene and carbon dioxide are appreciably soluble in caustic soda and fuming sulphuric
acid, respectively, so th a t the determination of either by absorption in these reagents is inaccurate. In an improved method the carbon dioxide is measured by removal with soda-lime, and then both acetylene and carbon dioxide are absorbed by treatm ent with fuming acid followed by caustic soda. The final traces of acetylene are removed by a solution of mercury cyanide containing a little alkali. R. H. G r i f f i t h .
D esign ing flash -d istillation equipm ent for petrol
eum refining. R. S. P ir o o m o v and N. E. L o o m is
(Chem. Met. Eng., 1929, 3 6 , 472—475).—The term
“ flash distillation ” is applied to any operation in which a mixture of hydrocarbons, after being heated above its initial b.p., is discharged into a zone where separation of vapours from residual liquid can occur.
Distillation takes place under conditions of substantial equilibrium between vapour and liquid in the separating zone. The equilibrium single-flash curve of a stock starts at a higher and ends a t a lower temperature than either the true b.p. or the Saybolt 10% distillation curves, crossing the last two somewhere in the lower- middle range. I t is possible to establish a simple relationship for the slopes and points of intersection of flash curves with the slopes and mean b.p. of the corre
sponding true b.p. or Saybolt 10% distillation curves.
This relation holds only for the distillation curve at 760 mm. If the true b.p. distillation of a stock is available, the point of intersection and the slope of the flash curve may be read off, and the straight line drawn to represent it will approximate very closely to the actual equilibrium curve at atmospheric pressure. Experi
mental results indicate th at the slope of the flash curve and the percentage off a t its intersection with the true b.p. curve are practically independent of pressure.
Consequently, to estimate the flash curve of a stock at any other pressure than 760 mm., the temperature at the intersection of the two curves a t 760 mm. must be extrapolated to the desired pressure by using the Cox chart (B., 1923, 699 a ) for the vapour pressure of hydro
carbons. Examples are given showing how steam con
sumption, and the temperatures a t the top and bottom of the bubble tower etc., can be obtained from these curves.
The bearing of these principles on the proper design of the overhead separating equipment and of the pipe- still itself is indicated. W . S. E. C l a r k e .
Recent developm ent in the art of cracking [of petroleum hydrocarbons] in the vapour phase.
C. R. W a g n e r (J. Inst. Petroleum Tech., 1929, 1 5 ,
484— 492).—A review of the scope and development of vapour-phase cracking, with especial reference to the Gyro process in which charging stock is pumped through heat economisers to an evaporator, and the vapours pass through a separator to remove entrained liquid and are mixed with superheated steam prior to passing through parallel convertor tubes fitted with catalytic cores. The plant is equipped with modern fractionating and gas-recovery plant. Carbon formation is reduced to a minimum and the non-condensible gas production, although double th a t made by liquid-phase processes, is produced at the expense of the fuel oil fraction and not by reduction of the yield of motor fuel. The distil
late contains 45—50% of defines and 40—45% of
B ritis h C h em ical A b s tr a c ts —B.
S I S C l . I I . — F u e l ; G a s ; T a b ; M i n e r a l O i l s .
aromatics, the balance being naphthenes; paraffins are almost wholly absent. Methods have been evolved for removing colour and odour from the motor spirit, whilst the gum-forming tendency is reduced by special treatment. By blending equal volumes of straight-run gasoline and vapour-phase cracked motor fuel, there is produced a motor fuel having an anti-knock rating of 40—50% of benzol. The finished motor fuel is richer in low-boiling fractions than ordinary gasoline, its sp. gr.
is greater by about 0-03 than th a t for a straight-run spirit of the same distillation range, whilst its f.p. is considerably below —73°. The fixed gas is a valuable material for synthetic chemical manufacture, its com
position varying little except in hydrogen sulphide content, which is dependent on the sulphur in the charging stock, the greater part being liberated in this
way. H. S. Ga r l ic k.
Flam e characteristics of “ pinking ” and “ non
pinking ” fuels. II. G. B. M a x w e l l and R. V.
W h e e l e r (J. Inst. Petroleum Tech., 1929,15, 408—415).
—Former research (B.,1928,511) has been continued with slightly modified apparatus. Increase in temperature of pentane-air mixtures slightly widened the range in which pinking occurred, and with benzene-air mixtures a narrow range giving faintly audible explosions was found.
Previous observations, th at the addition of benzene, the combustion of which is continuous throughout the explosion, to pentane reduces the likelihood of a pinking explosion by reducing the amount of chemical energy available to maintain a shock-wave when the initial wave is arrested, were confirmed. Addition of “ pro
knocks,” e.g., ethyl ether and amyl nitrite, reduces the amount of afterglow in the wake of the flame and gives a correspondingly more intense glow a t the moment of pinking. When carbon dioxide and steam were added to pentane-air mixtures it was found that, with the former, the range of mixtures giving pinking explosions was narrowed, and, with the latter, the spread of the flame and its luminosity were progressively decreased with increase in amount of water vapour added, the audibility of the pinking was greatly reduced, and the afterglow nearly eliminated. With carbon disulphide-air mixtures combustion was continuous and long-continued behind the flame front. No mixture of hydrogen and air was found which gave a pinking explosion similar to th at with pentane-air mixtures. Two conditions were established under which a pinking explosion may occur in a closed vessel: (1) the shape and size of the vessel, the nature and strength of the mixture, and the magni
tude and rate of heat liberation in the burning gases must be such th a t a stationary wave could be set up in the column of gases before the initial flame has travelled throughout the vessel: (2) the nature of the fuel and its concentration must be such th a t there is sufficient residual energy available to maintain a shock-wave when the flame, accelerated by the stationary wave, is arrested by the wall of the vessel. Anti-knocks render the combustion continuous behind the flame fronts.
Turbulence tends to prevent the formation of a stationary wave and accelerates the combustion in the wake of the
flame. H. S. G a r l i c k .
M easurement of detonation in internal-com bus-
tion engines. R. 0. K in g and EL Moss (Engineering, 1929, 128, 219—221, 272—274).—The tendency of a fuel to detonate is usually determined by one of the following methods : (1) The running conditions of any available engine are set to produce continuous detona
tion, the amount of the latter occurring in a given time being measured. The relative anti-knock values of fuels are thereby obtained by their measured amounts of detonation under carefully standardised conditions;
it is usual to determine the benzol or dope addition required to make an inferior fuel equal in performance to some fuel, provisionally adopted as a standard. (2) Some factor in engine running such as ignition timing is varied by being set a t a value to avoid detonation with the fuel under test, and is then gradually altered until continuous detonation is just audible ; the ignition timing to produce detonation is determined for the standard fuel, and the relative anti-knock values of inferior fuels may then be obtained in terms of the dope or benzol additions required to bring about the same ignition timing, with audible detonation, as the standard fuel. (3) The relative fuel values are obtained in terms of the highest useful compression ratio (H.U.C.R.), which is made a variable and is the controlling factor used to produce detonation ; it is obtained by running trials with the Ricardo variable-compression engine; the anti-knock value of a fuel can then be expressed in terms of the compression ratio with which detonation is just appreciable. The two fuels selected for examina
tion by methods (1) and (3) described above were a straight-run California spirit, highly resistant to detona
tion, and a straight-run naphtha possessing less resist
ance to detonation than any fuels in general use. An addition of 8 c.c. of “ ethyl fluid ” per gal. was required to make the naphtha equal to the undoped California spirit, but if 2 c.c. of ethyl fluid per gal. were added to the spirit the naphtha required 17 c.c. per gal. for equality.
The H.U.C.R. approached a maximum value for the larger additions of dope, but it would be impossible to use enough dope to enable the engine to run a t full power a t the ideal compression ratio of 8 : 1, even if the dope were added to superior fuels. The rate a t which metallic dope can be supplied to an engine is a t present limited by considerations of cleanliness, and 8 c.c. per gal. is the maximum th at can be used. On this basis a poor fuel could be used a t a compression ratio of 5-5 instead of 4-5, but a good fuel such as the California spirit could be used a t nearly 7 instead of 5 • 5.
C. B MARSON.
M easurem ent of detonation in in te rn a l-com bus
tion engines. F. B. T h o l e (Engineering, 1929, 128, 386).—The use of the bouncing-pin test for detonation, which is described, is particularly suitable with a special Armstrong engine on account of the cylinder design, but the method cannot be applied indiscriminately to any engine. The accuracy of measurement is always greater than th a t attainable by the audibility test, but the two give results in good agreement. The experi
ments of King and MossT(preceding abstract) are re
viewed, and suggestions are made as to an improved procedure for testing blended and doped fuels, which involves standardisation with chemically pure liquids of known values. R. H. G r i f f i t h .
B ritish C h em ica l A b s tr a c ts —B.
Cl. I I . — F u e l ; G a s ; T a r ; M i n e r a l O i l s . 8 7 9
Determ ination of paraffin hydrocarbons in motor fuels by sulphonation. G. K u h n (Chem.- Ztg., 1929, 53, 701—702).—The methods of Heilingotter (B., 1928, 512) and of Pritzker and Jungkunz (B., 1923, 483 a ) for the determination of benzine in benzine- benzene mixtures are considered unsatisfactory. The author’s method is to use 1 pt. of fuel to 2 pts. of acid, as in Pritzker and Jungkunz’s method, and fuming sulphuric acid containing 4-8% S03 (free). The sul
phonation is carried out in a 150-c.c. flask fused to a burette 60 cm. long and reading to ^ c.c. The opening of the burette can be closed by means of a ground glass stopper. The initial substances consisted of pure benzene (d15 O'8833) and normal benzine (d15 0-7005), and in each experiment 10 c.c. of benzine- benzenc and 20 c.c. of fuming sulphuric acid were used. Results so obtained for benzine-benzene mix
tures containing up to 30% of benzine are greater than those given by the Pritzker-Jungkunz method.
The differences between the two increase when the benzine content is above 30%, rise to a maximum at 50% of benzine, and then gradually decrease with greater amounts. I t is possible to ascertain the benzine content from the sulphonation residues of fuels of any composition with an accuracy of about 2 % ; greater accuracy is obtained by using increased quantities of
reagents. W. S. E. C l a r k e .
Determ ination of arom atic hydrocarbons in gasolines pi-oduced by straight distillation. M. D.
T i l i t s c h e e v and A. I. D u m s k a y a [D u m sk i] (J. Inst.
Petroleum Tech., 1929, 15, 465—483).—The aniline and nitrobenzene critical solution temperature as well as the densitometric and refractometric methods were critically examined, and attem pts made to determine the variation of the experimental constant, k, in the equation x = Jed, where x is the percentage of aromatic hydrocarbons by wt., and d is the difference between the gasoline constants before and after separation of the aromatics. Artificial mixtures of benzene, toluene, xylene, and cymene were made with pure paraffin and naphthene hydrocarbons, and with petroleum fractions, and the basic constants, i.e., the critical solution tem
peratures in aniline and nitrobenzene, the sp. gr., and the refractive index, were determined both for the petroleum fractions (or hydrocarbons) freed from arom
atics and for their respective artificial mixtures with aromatic hydrocarbons. For different solutions con
taining the same aromatic hydrocarbon in the same concentration, k is a function of the constants of the non-aromatic portion of the fraction. Values of k are plotted against the values of one or other of the constants of the non-aromatic portion of the fraction [e.g., the aniline point) to obtain a curve showing the functional]^ dependence of£?£. Similar curves were obtained in connexion with other methods. I t was found, in general, th at the simplest and quickest method is the refractometric, in which very small quantities of each fraction suffice, and the results are accurate to
± 0-3% . Where greater accuracy is required, the densitometric method is little inferior to the others for fractions boiling below 150°, but above this temperature the aniline and nitrobenzene methods are preferable, Bince these are less affected by the varying composition
of the aromatic hydrocarbons in this range. The nitrobenzene method possesses the advantages of lower critical solution temperature, and hence more rapid determination, smaller fluctuations of nitrobenzene coefficients due to variation of chemical composition of the non-aromatic portion, and greater stability of the nitrobenzene. H. S. G a r l i c k .
Determ ination of unsaturated hydrocarbons in benzine w ith brom ine. J. Z d a r s k y (Chem. Obzor, 1929, 3, 165—168, 205—210 ; Chem. Zentr., 1929, i, 1772).—Bromine values differ according to the method employed for their determination. Even when the conditions are constant, only relative values can be
obtained. A. A. E l d r i d g e .
See also A., Oct., 1168, Destructive d istilla
tion of lignin from corn cobs ( P h i l l i p s ) . Lignin colouring m atters (P o d b r e z n ik ) .
Pa t e n t s.
Apparatus for carbonising coal and the like.
F. C. G r e e n e and I. F. L a u c k s , Assrs. to O ld B e n C o a l
C orp . (U.S.P. 1,723,932, 6.8.29. Appl., 24.10.25).—
Preheated coal is discharged into the bottom of a vertical screw-retort comprising a tubular casing, which is sus
pended from its upper end and contains a screw-con- veyer, the width of each thread of which is one third of the space between adjacent threads. The casing tapers slightly downwards, and is free to expand into an enlargement at the bottom, provided with a steam
outlet. F. G. C l a r k e .
Treatm ent of coking coal and the like with sm oke and dust from reduction furnaces. P. L. J.
M ig u e t (B.P. 292,931, 25.6.28. Fr., 25.6.27).—The fine dust from furnaces of the reduction type, other than blast furnaces, which is collected, e.g., by electro
static precipitation, is utilised by its incorporation in the coke used for the reduction, by mixing it with the fines of the coking coal before compressing and placing the latter in the coke oven. A. B. M a n n in g .
H ydrogenating and treating carbonaceous m a terials. M. H o f s a s s (U.S.P. 1,711,499, 7.5.29. Appl., 30.11.26. Ger., 2.12.25).—Carbonaceous material is hydrogenated under pressure in presence of anthracene or a homologue above the decomposition temperature of hydrogenated anthracene. Anthracene etc. may be re
covered by fractional distillation of a part of the pro
duct. R . B r ig h t m a n .
Recovery [from hydrogenated coal products] of organic substances which are volatilisable at an elevated tem perature and apparatus therefor.
J . Y. J o h n s o n . From I. G. F a r b e n t n d . A.-G. (B.P.
317,506, 30.4.28).—The mixture of oleaginous liquors and solid m atter obtained by destructive hydrogenation of coal etc. is fed in a thin stream on to a revolving vertical cylinder or cone down the surface of which it flows. The cone is heated by burner gases either from the outside or through a chimney within the cone, the gases passing in the latter case down the inside of the cone and up over the outer surface. The volatile pro
ducts are carried off by the heating gases, and the solid residue is removed by suitably placed scrapers.
C. Ho l l in s.
B ritis h C h em ical A b s tr a c ts —B .
8 8 0 Cl. I I . — Fu e l ; Ga s ; Ta r ; Mi n e r a l Oi l s.
Activation of carbon. J. C. M o r r e l l (U.S.P.
1,713,347 and 1,712,930, 14.5.29. Appl., [a ] 19.5.23,
[b] 4.3.26).—(a ) Carbon is treated with an aqueous solution of a halogen {e.g., chlorine), (b) in presence of a neutralising agent, e.g., a metallic carbonate or hydrogen carbonate, selective for hydrochloric acid and not hypochlorous acid. R. B r ig h t m a n .
Carburetted w ater-gas apparatus. R. M. S e a r l e
(U.S.P. 1,726,317, 27.8.29. Appl., 23.7.24).—The com
bined carburetter and dust catcher comprises a vertical cylindrical shell having a spray device depending from the centre of the roof. The water-gas enters by a tangential inlet, and the carburetted gas passes to a superheater through a vertical outlet pipe, the mouth of which is immediately below the spray.
F . 6. C l a r k e .
Manufacture of w ater-gas. J . Y. J o h n s o n . From I. G. F a r b e n in d . A.-G. (B.P. 318,016, 17.9.28. Addn.
to B.P. 214,544 ; B., 1924, 549).—The process described in the main patent is modified by the provision of a heat accumulator above the fuel bed in the producer.
At the end of the blow period steam is passed down
wards through the heat accumulator and fuel bed in succession. The steam may be preheated by passing through the hollow bars of the grate and through a heat accumulator in the dust separator before entering the producer. A good water-gas can thus be obtained from a brown-coal semi-coke with relatively low temperatures in the fuel bed. A. B. M a n n in g .
Suction gas generator for distilling and gasifying inferior fuel and its operation. F. A. G. D a n i e l
and J. V a n V l a a r d i n g e n (B.P. 318,013, 14.9.28).—
The distilling shaft of the generator and the feeding hopper are coned, becoming wider in the direction of their bases. The hopper has no valve and projects some distance into the interior of the shaft, leaving a small annular space for the gases to pass. A cylindrical wall is mounted outside the conical wall of the shaft, the intervening space containing water over which the entering air supply is drawn. The air and steam supplies are so adjusted th at the highest temperature 25—30 cm.
above the grate of the generator varies from 300° to 400°.
A. B . M a n n in g .
Apparatus for producing synthetic hydrocarbons and alcohols [from natural gas]. H. A. W e b s t e r ,
Assr. to E. T. S c h u l e r (U.S.P. 1,711,913,7.5.29. Appl., 1.10.26).—Natural gas, e.g., methane, mixed with steam is injected at 400 lb./in.2 into a retort initially at 1260°, and the mixture of carbon monoxide and “ nascent ” hydrogen is passed at 325—475° through a catalysis chamber containing, e.g., iron calcined with potash.
The resultant mixture of alcohol and hydrocarbon vapours passes through a relief valve to cooling coil and receiver. Alternate use of a similar retort in parallel with the first and connected with the same catalyst chamber gives a continuous process. R. B r ig h t m a n .
Effecting chem ical reactions in [hydrocarbon]
gases by m eans of electrical discharges. P. H.
H u l l , and I m p e r i a l C hem . I n d u s t r i e s , L t d . (B.P.
317,558, 31.5.28).—Hydrocarbon gases are fed turbu- lently (at 800—900 ft./sec.) into the zone of electrical
discharge of a high-tension arc. and, after treatment, are led rapidly away from th a t zone to a surrounding chamber, whence they re-enter the zone of electrical discharge and pass through a hollow electrode.
J. S . G. T h o m a s.
Effecting chem ical reactions in [hydrocarbon]
gases by m eans of electrical discharges. P . H . H u l l , and I m p e r i a l C hem . I n d u s t r i e s , L t d . (B.P.
317,920, 31.5.28).—Acetylene is produced (a) by treating hydrocarbon gases with high-tension electric arcs while passing between the opposing rims of two co-axial tubes, the gas passing in through one tube and out through the o th e r; or (b) by creating an electric discharge between a hollow conducting tube, having its mouth shaped convergingly in the direction of gas flow, and an opposing rod electrode, and causing the gas to enter the discharge and travel along the hollow tube at high velocity, thereby sucking the electric discharge into the hollow tube. The electrodes are made of or tipped with carbon. H . S . G a r l i c k .
Oxidation of hydrocarbons. G. E g l o f f and J. C. M o r r e l l , Assrs. to U n i v e r s a l O i l P r o d u c t s Co.
(U.S.P. 1,710,155, 23.4.29. Appl., 20.7.22).—Hydro
carbon vapours are mixed with oxidising gases under pressure and subjected to a high-potential electrical discharge in presence of a catalyst. R. B r ig h t m a n .
D istillation of tar. B a r r e t t C o ., Assees. of S. P.
M i l l e r (B.P. 289,832, 21.4.28. U.S., 3.5.27).—The hot gases from part of a coke-oven battery are subjected to regulated cooling, and are then cleaned by electrical precipitation before they are passed to the condensing system. The tar which is separated in the electrical precipitator, either alone or together with the tar which separates in the collector main, is distilled by being brought into intimate contact with the hot gases from other coke ovens (cf. B.P. 282,367 ; B., 1929, 507).
The enriched gases from the latter are also cleaned by electrical precipitation before passing to the condensing system. The gases from both treatm ents are combined for the subsequent recovery of ammonia therefrom.
A. B . M a n n in g .
D istillation of [tar] oil. B a r r e t t C o., Assees. of
S . P . M i l l e r ( B .P . 287,900, 19.3.28. U .S ., 29.3.27 ; cf. B ., 1929, 633).—Tar oils are brought into intimate contact with hot coke-oven gases, e.g., by spraying them into the uptake pipes and collector main, in sufficient quantity to cool and scrub the gases and supply an excess of undistilled oil to dissolve the separated tar constituents and flush them from the main. The vapours, free from pitch, pass to a suitable oondensing system. The temperature of the gases in the collector main may be regulated in part by the addition of a spray of water or ammonia liquor.
A. B . M a n n in g .
Production of lubricating oils and phenols from coal tar. A. W e i n d e l , Assr. to Z e c h e M . S t i n n e s
(U .S .P . 1,726,638, 3.9.29. Appl., 12.12.24. Ger.,
27.12.23).—Primary ta r is distilled to about 240° and benzine is added to the residue in order to precipitate asphaltic substances. After separation of these the benzine isvdistilled?ofi and the lubricating oil material remaining is taken up in a solvent which is also miscible
B ritis h C h em ical A b s tr a c ts —B .
Cl. EC.— F u e l ; G a s ; T a b ; M i n e r a l O i l s . S8I
■with w a te r; by then adding water to the mixture the oil separates out and the phenols remain in solution.
A. B . M a n n in g .
Apparatus for distilling m ineral oil. A. E. P e w , j u n ., and H. T h o m a s , Assrs. to S u n O i l Co. (U.S.P.
1,714,812, 28.5.29. Appl., 29.5.26).—The oil is vaporised by rapidly flowing in a thin stream in heat exchange with a mercury-vapour condensing chamber. Vapours pass out to a condenser and receivers, the unvaporised oil passing on to successive similar vaporising units in which the mercury vapour is maintained at progressively higher temperatures and pressures. R. B r ig h t m a n .
Apparatus for distilling [cracking] oil. A.
S c h w a r z (U.S.P. 1,713,149, 14.5.29. Appl., 6.11.25).—
The oil is heated in a still with a movable cover carrying hollow heating tubes which dip into the oil and through which hot gases are passed out of direct contact with th e oil. Carbon from the cracking process deposits on the heating elements and is periodically removed.
The still may be provided with a sleeve to promote circulation of the oil. Vapours from the still pass to a condenser or receiver, or a number of such stills may be connected in series, reflux condensate from the first stills being heated and cracked in successive units.
R. B r ig h t m a n .
Apparatus for cracking [petroleum] oil. A.
S c h w a r z , Assr. to C o a l & O i l P r o d u c t s C orp . (U.S.P.
1,714,454, 21.5.29. Appl., 20.5.25).—Petroleum oil, e.g., pressure-still tar, is sprayed into the top of a gas producer on to the relatively cool bed, e.g., at 430°, whale superheated steam at 315° and a small amount of air are admitted to the incandescent bed. Waste-heat gases escape from the top of the producer and oil vapours etc. pass out to a settling box and fractionating tower, vapours from which are condensed. Condensate from the upper part of the fractionating tower may be returned to the base of the tower or again injected with fresh oil. An alternative process, in which the waste gases from the producer are used to heat oil pumped to the injector is described. R. B r ig h t m a n .
Prevention of substantial corrosion in hydro
carbon oil-treating [cracking] apparatus. J. C.
M o r r e l l and H . P . B e n n e r , Assrs. to U n i v e r s a l O i l P r o d u c t s C o. (U.S.P. 1,715,095, 28.5.29. Appl., 3.9.25).
—Ammonia solution is injected into the pipe conducting vapours from the dephlegmator to the cooling coil.
R. B r ig h t m a n .
Cooling the heating coils of an oil cracking apparatus. G. E g l o f f and H. P . B e n n e r , Assrs. to
U n i v e r s a l O i l P r o d u c t s Co. (U.S.P. 1,725,067, 20.8.29.
Appl., 14.1.25).—In the type of cracking apparatus in which oil is continuously supplied to a heating coil, where it is raised to cracking temperature, and thence delivered to a chamber, provision is made for cooling the coil by discontinuing the application of heat, ceasing the delivery of oil from the coil to the chamber, and cyclically circulating cool oil from a bulk supply.
H . S . Ga r l ic k.
Oil cracking. M. J. T r u m b le (U.S.P. 1,724,982, 20.8.29. Appl., 10.12.25).—Successive portions of a revolving member pass through a heat-receiving zone, where direct flame contact occurs, and then through
an oil-receiving and vapour-evolving zone where oil is delivered on to the heated portion and the evolved vapours are conducted therefrom. H . S. G a r l i c k .
Cracking of oil. J. C. B l a c k (U.S.P. 1,715,980, 4.6.29. Appl., 20.10.26).—Petroleum oil, e.g., fuel oil, is heated at 425° in a primary coil and maintained at 425° for 20—25 min. in a secondary cracking coil under, e.g., 500 lb./in.2, whence the oil passes after heat exchange with incoming oil to atmospheric pressure at 290° to an evaporator and bubble tower. Gasoline and other light petroleum vapours after scrubbing with fresh oil are condensed, whilst the phlegms pass to a cooler and receiver as gas oil, or may be injected after passing through the heat exchangers into fresh oil in the primary or secondary heating coil. Alter
natively, the oil passing from the primary to the secondary coils may be cooled to 25—50° by the injection of cold
oil. R. B r ig h t m a n .
Converting heavy com bustible oils into light com bustible o ils. P. L. H a h n (B.P. 289,482, 27.4.28.
Ger., 30.4.27. Addn. to B.P. 235,625 ; B., 1925, 661).—
The preliminary vaporisation of the oil to be treated is efiected by passing it through a bath of molten metal provided with a circulating conduit which is heated to reheat the molten metal. Further, the vapours are mixed with superheated steam only, or the con
stituents thereof, a t 350—600° to eSect the necessary chemical changes. H . S. G a r l i c k .
Conversion [cracking] of petroleum oils. \V. M.
C r o s s , Assr. to G a s o l i n e P r o d u c t s Co., I n c . (U.S.P.
1,717,007, 11.6.29. Appl., 14.10.22).—The hydro
carbon oil is raised to cracking temperature in heating coils under high pressure and passed a t 370—510° and under 400—900 lb./in.2 for mid-continent gas oil into an insulated conversion chamber, into which air or other combustion-supporting gas is injected to agitate the oil and maintain a temperature above th at attained in the heating coils. The converted oil is drawn off and cooled under pressure and the carbon separated
by settling. R. B r ig h t m a n .
Distillation [cracking] of [heavy petroleum ] oil.
A. E . M i l l e r , Assr. to S i n c l a i r R e f i n i n g Co. (U.S.P.
1,714,097, 21.5.29. Appl., 11.6.27).—Heavy petroleum oil is topped, e.g., by heating in successive sliell-stills with gravity flow so th a t vapours leave the dephlegmators at 205° and 230°, and the topped oil is pumped to the bottom of a vertical still beneath a relatively deep bed of fuller’s earth at 300—340°. The earth is supported by screens to prevent contact with the hot still bottom, and vents are provided to avoid gas or vapour pockets beneath the screen. Vapours from the still pass to a reflux tower and are condensed, whilst the reflux is re
turned for re-use. R . B r ig h t m a n .
Treatm ent [cracking] of m ineral oils. H . B lu m e n - b e r g , j u n . (U.S.P. 1,713,252, 14.5.29. Appl., 24.10.27).
:—Dehydrated mineral oil is treated with 2—10% of dry hypochlorite (e.g., of aluminium) and cracked at 110—345° for 1—2 hrs. Hypochlorite of iron or copper is preferred with oils of high sulphur content.
R. B r ig h t m a n .
Pyrogenetic cracking process [for m ineral oils],
R . W . H a n n a , Assr. to S t a n d a r d O i l Co. o f C a l i f o r n i a
b
B r itis h C h em ical A b s tr a c ts —B .
882 Cl. I I ,— Fu e l ; Ga s ; Ta r ; • Mi n e r a l Oi l s.
(U.S.P. 1,724,476, 13.8.29. Appl., 15.10.27).—Vapour evolved by heating the oil under pressure is separated from the liquid, and vapour and oil, subjected to separate pressures, re-combine in such manner th a t the tem perature of the oil is raised to the temperature of de
composition. The oil is then passed into a reaction
zone. J. S. 6. T h o m a s.
Converting heavy m ineral oils into lower-boiling products. W. G. L e a m o x (B.P. 317,868, 14.3.28).—
Mineral oil to be cracked passes through a pipe still where it is raised to a temperature below th a t of cracking but sufficient to vaporise a substantial portion, leaving the high-boiling portions, including the tarry con
stituents. The vapours are discharged into a dephlegm- ator, and the separated vapours are rapidly super
heated, to avoid extensive cracking, to 530—550° while travelling a t high velocity in a stream of relatively small diameter. The superheated vapours are delivered to a heat-insulated cracking chamber containing a mass of inert, refractory, porous, absorptive contact material, and maintained there sufficiently long for cracking to be effected wholly by the continued superheat, the cracked vapours then passing to a condenser. The fixed gases from the condenser pass to a flow-meter and to means sensitive to differential gas pressure for automatically regulating either the supply of fuel to the furnace or the rate a t which the oil to be cracked is fed into the system. H. S. G a r l i c k .
Manufacture of low -boiling and gaseous hydro
carbons from those of higher b.p. J . Y . J o h n s o n .
From I. G. F a r b e n in d . A.-G. (B.P. 318,270, 27.4.28).—
Olefines, diolefines, and butadienes are obtained from tars, mineral and vegetable oils, bituminous coals, etc., which, maintained in a vapour or finely-divided state, are subjected to high-temperature electrical discharges at temperatures not exceeding 700—800°.
C. B. Marsox. T herm al decom position of hydrocarbons.
E l e c t r o M e t a l l u r g i c a l C o., Assees. of S. M. N o r w o o d
(B.P. 298,556, 19.6.28. U.S., 11.10.27).—Hydrocarbons are passed a t cracking temperatures through a tubular member consisting of an alloy containing 15—40% Cr, 2—15% Ni, 0- 7—3-0% Si, 0-7—3-0% M n, and not more than 1-0% C, the balance being principally iron.
H . S. G a r l i c k .
Catalytic cracking of hydrocarbons. G . E g l o f f , A ssr. t o U n i v e r s a l O i l P r o d u c t s C o. ( U .S .P . 1,722,042, 23.7.29. Appl., 7.1.21. Renewed 12.5.27).—Oil is passed continuously through a cracking zone of high tempera
ture and superatmospheric pressure into an expansion chamber where vaporisation occurs and the pressure is reduced though still maintained above atmospheric.
The vapours are led through a catalytic bed consisting of a relatively thin layer of a metallic oxide supported in the vapour space of the expansion chamber before passing to a condenser for collection as pressure dis
tillate. H. S . G a r l i c k .
Treatm ent [cracking] of hydrocarbons. G.
E g l o f f , Assr. to U x i v e r s a i , O i l P r o d u c t s Co. (U.S.P.
1.722.043.23.7.29. Appl., 14.11.21. Renewed 14.9.28).—
Portions of unvaporised oil are continuously withdrawn from a supply of oil subjected to cracking conditions of
temperature and pressure, diluted with an oil of lower sp. gr., passed through a bed of filtering material, and the cleansed oil is injected into the lower portion of the bulk supply of oil being cracked. H. S . G a r l i c k .
Cracking of hydrocarbons. E. W . Is o m , Assr. to
S i n c l a i r R e f i n i n g Co. (U.S.P. 1,711,351, 30.4.29.
Appl., 21.7.27).—Hydrocarbon oils are cracked by passing the oil vapours from the heating conduit (540—
650°) successively through digesting drums (510—650°), scrubbing tower (260—290°), reflux tower (180—230°), and fractionating tower (150—190°), vapours from the fractionating tower passing to the usual condenser, receiver, and gas separator, direct or after treatm ent with absorbent earth or clay. R . B r ig h t m a n .
Conversion [cracking] of hydrocarbons. W. M.
C o lo n y , Assr. to P e t r o l e u m C o n v e r s i o n C o r p . (U.S.P.
1,715,341, 28.5.29. A ppl, . 3.1.27).—Hydrocarbon oil vapours are passed into a conversion chamber a t 390—
425° fitted with chequer work, together with steam and hydrocarbon gases etc. from a regenerative hot-blast stove at, e.g., 815—980°, the tem perature of the hot gases being regulated by previous admixture with cold gas, e.g., stripped gas from the final receiver. Vapours from the converter, after heat exchange with feed oil, are condensed, the uncondensed vapours being then stripped in an absorber and the gas finally recycled through the blast stove, a part being used to cool the hot gas feed to the converter. R . B r ig h t m a n .
Conversion of hydrocarbons. L. J . W a l s h , Assr.
to S t a n d a r d O i l D e v e i ,6f m b n t Co. (U.S.P. 1,725,434, 20.8.29. Appl., 28.11.23).—Hydrocarbon material leav
ing the heating coils enters a reaction drum where tarry material is allowed to separate during conversion and is withdrawn from near the bottom. Vapours are w ith
drawn from near the top of the drum, and both streams are combined and conveyed to a region of reduced
pressure. H. S . G a r l i c k .
T reatm ent [cracking] of hydrocarbon co m pounds. A. B a l m e r . From P e t r o l e u m C o n v e r s i o n C o r p . (B.P. 317,508, 11.5.28).—The process of B.P.
207,276 (B ., 1924, 84) for the treatm ent of petroleum oils so as to produce motor fuels of lower mol. wt. and b.p., is modified by the following improvements : (1) A stream of heat-carrier gas of uniform temperature is produced by mixing hot gas from regenerative furnaces with a regulated supply of relatively cold gas. (2) The oil is vaporised and the vapour mixed with the hot carrier gas to bring about the conversion reaction.
(3) The heat in the products of the reaction chamber is used to raise the tem perature of the carrier gases prior to their admission to the heating element employed and to raise the temperature of the incoming oil. (4) The products of the reaction are scrubbed with a high- boiling oil to remove carbon before passing to the recti
fying and condensing columns. (5) Advantage of the scrubbing step is taken to top the oil used as scrubbing medium, and the vapours are added to the products of the process. H. S . G a r l i c k .
Preparation of hydrocarbon products. F. A.
H o w a r d , Assr. to S t a n d a r d O i l D e v e l o p m e n t Co.
(U.S.P. 1,727,303, 3.9.29. Appl., 25.4.24).—A fraction having a relatively high b.p. is condensed out of vaporous
