BRITISH CHEMICAL ABSTRACTS
B.—APPLIED CHEMISTRY
S E P T . 2, 1927.
I.— G E N E R A L ; PL A N T ; MACHINERY.
Pa t e n t s.
O vens for baking, drying, and other heating op eration s. T. & T. Vic a r s, Lt d., and E. M. Cr o s-
l a n d (E.P. 272,261, 1.2.26).— The goods are conveyed through the oven in tiers (e.g., on trays) which alternate with heat-radiating elements so th a t the goods are heated both above and below. The radiators are heated internally by burners which direct the heat either downwards or upwards as desired.
B. M. Ve n a b l e s. A pparatus for d rying m aterial in bulk, or in sta ck s. C. Tin k e r (E.P. 272,316 and 272,319, [a], 6.4.26, [b], 15.4.26).—H ot air is supplied through a duct passing underneath and up through a drying floor, and the bulk material is stacked around the air outlet.
In (a) a casing is erected so designed as to adm it the hot air a t different levels to the material. In (b) a liftable core is used to form an air shaft through the material as it is built up. B. M. Ve n a b l e s.
U tilisa tion of h eat in d rying d ru m s. C. Lu d w ig
(E.P. 267,543, 11.3.27. Conv., 11.3.26).—In a rotary dryer which is provided with spiral air outlets a t the dry end, the internal distributors for the material are continued right across the air outlet zone and the material is allowed to accumulate in a heap preparatory to discharge in a zone between air outlets and a baffle or end wall. B. M. Ve n a b l e s.
C ooling to w e r. R. A. Le w is (E.P. 272,325, 29.4.26).
—The tower comprises a casing with unobstructed interior and unobstructed large spaces beneath for entry of the air. Vertical sprays of the water to be cooled produce both the upward draught and the necessary surface of water. Horizontal sprays of water, which may be either hot water or water already cooled from the pond below, prevent cross-winds blowing m ist out of the air inlets. The tower may be constructed in sections comprising long bays joined a t their centres by short bays, so th a t no p art of the interior of the tower is far from an air inlet. B. M. Ve n a b l e s.
A bsorption refrigerating apparatus. J. 0.
Boving (E.P. 271,958, 5.3.26).—An absorption refri
gerator of the discontinuous type. B. M . V e n a b l e s . M ixing liquids for th e purpose of carrying out rea ctio n s and for producing d isp ersion sy ste m s.
J. R. Ge ig y A.-G. (E.P. 257,274, 18.8.26. Conv., 22.8.25).—Materials constituting the disperse phase are atomised by a je t of gas under pressure and the spray is passed through a sheet of the dispersion medium.
B. M. Ve n a b l e s.
Apparatus for purifying and otherw ise treating gases. W. H. Ta y l o r and C. Sh a w (E.P. 266,097, 2.1.26).—An apparatus for purifying air and other gases consists of a vaned drum rotated by the flow of the gas itself and having its curved surface made of wire mesh or perforated metal. The drum rotates hori
zontally and contacts with a liquid surface which seals the space below the drum and also maintains the per
forations in the drum wet. The gas stream to be cleaned is directed by vanes tangentially against the perforated plate and passes through the moist perforations.
S. Pe x t o n. Centrifugal m achine. M. L . Sa n s a r ic q ( E .P . 272,047, 21.6.26).—The apparatus comprises a number of baskets arranged round a hollow shaft and rotating as a group round the axis of the machine, each one in addition rotating round its own axis, being driven a t a variable speed by means of friction and bevel gearing and a second shaft within the hollow shaft.
B. M. Ve n a b l e s. Centrifugal extractors. H. J. Pa r k e r ( E .P . 272,368, 2.10.26).—In a centrifugal machine the bowl or basket is directly coupled to a motor beneath it.
The weight of the bowl, its contents, and the electrical rotor is taken by a thrust bearing between the bowl and the motor casing. The weight of the whole is taken by a stiff pneumatic diaphragm beneath the motor, so th a t the bowl can wobble under unbalanced load. An elec
trical brake is provided which is automatically pulled off just before the motor starts. B. M. Ve n a b l e s.
Centrifugal purifying and dehydrating apparatus.
Em pso n Ce n t r if u g a l s, Lt d., and S. Al e x a n d e r (E.P.
272,339, 11.6.26).—In a centrifugal machine as described in E.P. 224,935 (cf. B., 1925, 57) and provided with crater-shaped separating cones, a horizontal annular baffle is inserted in the annular space between the hollow shaft and the crater of the uppermost cone ; this baffle is stated to improve the separating action and cause the solid and viscid impurities to pass out continuously with the heavy wash liquid. The baffle may be adjustable.
B. M. Ve n a b l e s. F ilters and th e lik e. E. C. Ha t c h e r (E.P. 272,266, 2.3.26).—The filter medium comprises a spiral spring which m ay be more or less compressed to alter the size of the spaces between the coils. The spring is supported against lateral collapse by ribs on the outer casing and by a ribbed sleeve internally ; the latter may be rotated to act as scraper. An alternative construction comprises a filter medium in the form of a clock spring which may be n u re or less wound up. B. M. Ve n a b l e s.
639 a
B r itis h C hem ical A b s tra c ts —B .
640 C l. I I . — IT u e l ; G a s ; D k s t u u c t i v e D i s t i l l a t i o n ; M i s k r a l O ils .
Centrifugal filtering apparatus. A. W . Em pso n
(E.P. 271,916, 5.10.26).-—In a centrifugal apparatus in which the solids (or heavy liquid) are collected oil the outer wall of the rotating bowl and the lighter liquid passes inwards through an edge filter comprising a number of rings of paper compressed together, the filter is constructed of a long ribbon of paper, of small width compared with the radius of the filter and wound edgewise between two perforated cylinders acting as formers.
To alter the compactness of the filter while in use, the top is pressed down by an expansible pneumatic tube connected to a pump on the shaft of the machine.
B . M . Ve n a b l e s. Apparatus for spraying or ato m isin g liquids or for d issem inatin g g a ses. R. A. Le w is (E.P. 272,003, 20.4.26).—A device in which fluid is adm itted a t high velocity tangentially to a spiral-shaped chamber and exhausted in the form of spray either axially to the chamber or a t another part of the circumferencer is constructed with the lining of the spray chamber separable from the main body of the apparatus so th a t the spiral may be die cast or moulded in such materials as glass, bakelite, or aluminium-silicon alloy (which is electrolytically neutral to cast iro n )m a c h in in g is thus avoided or much simplified. B. M . V e n a b l e s .
P u l v e r i s e r . 0 . A. Kk k u t z b e e o (E.P. 272,111, 21.12.26. Conv., 5.11.26).—A pulveriser with air separation comprises a table which is rotated and on which bear grinding, rollers. Air is admitted with a whirling horizontal motion to the grinding zone, which also serves as a first precipitation chamber, and leaves with the ground material upwards through an annular chamber the inner wall of which is composed of adjustable yanes, causing the air to enter horizontally and whirling into another precipitation chamber from which the oversize material drops back to the grinding zone.
B. M . Ve n a b l e s. T um bling m ill. H. W. Tit g e n (E.P. 266,664, 8.7.26. Conv., 25.2.26).—The mill comprises a tapered shell within another shell with a reverse taper, both rotating together on a substantially horizontal axis.
THe goods to be cleaned and the abrasive pass through the inner shell from the small to the large end, a t which ptiiilt the goods pass out of the apparatus, but the abrasive drops through perforations into the outer shell alorlg which it returns to the feed end, where it is picked up by lifting vanes and returned to the inner shell for use
again. B. 31. Ve n a b l e s.
Separating substances such as solids and gases from liqu ids. Gil c h r is t & Co., Assees. of W. C.
Gr a h a m, H. S. Ru m s e y, and A. U. We t h e r b e e (E.P.
245,476, 5.1.26. Conv., 5.1.25).—See U.S.P. 1,602,014 ; B., 1927, 32.
T ubular h eat exchanger. H. Hil l ie r (E.P.
273,450, 26.5.26).
R e frig e ra tin g a p p a ra tu s . S i l i c a Ge l Co r p., Assees.
of E. B. M i l l e r a n d W. L. Ed el (E .P . 260,542 aiid 264,859, 2.4.3.26. C onv., 28.10.25).
Separating d u st or fum e from air and [dust- d ischarging device in] apparatus of the fabric tube filter type therefor. J. P. v a n Ge l d e r (E.P. 273,563, 22.11.26).
A dsorbent or catalytic m a sse s (E.P. 255,901).—
See VII.
I I - F U E L ; G A S ; DESTRUCTIVE DISTILLATION;
MINERAL OILS.
P rob lem s encountered in preparing coal for the m arket. F. S. Sinnatt (J.S.C.I., 1927,46,242—250 t).
—Various aspects of the relationship existing between the properties of coal seams and the preparation of commercial grades for the m arket are reviewed. The heterogeneous nature of coal seams is considered, and an attem pt made to indicate in general terms the effect this may have on the commercial grades obtained from seams. Sized coals obtained by screening run-of-mine coal exhibit differences not only in caking properties, bu t also in the am ount of ash present and the m.p.
of the ash of the coals. The absence of any uniform nomenclature to describe the commercial grades of coal is mentioned, and the necessity for an investigation of the sizes of coal most suited to particular coal seams is suggested. The effect of the size of the coal on the results obtained in the carbonisation of the coal, both in gas retorts and in low-temperature carbonisation, is discussed, and attention is drawn to the associated problem of the influence of the addition of inorganic m atter to coal on the mechanics of carbonisation and combustion. In connexion with blending, it is shown th a t if, for example, equal proportions of two seams are mixed together a t a colliery and the blend is then separated into commercial grades by screening, the grades will contain varying proportions of the two seams and will differ in properties, calorific value, etc. according as the séants are distinct in quality and yield varying proportions of the sized coals. The method of testing coals is examined briefly and ash characteristic curves prepared by the Henry tube and the method of specific gravity analysis are compared.
C om parison of p rocesses for cleaning coal.
W. R. Ch a p m a n and R. V. Wh ë e l e r (J.C.S.I., 1927, 46, 229—23S t).—A number of points are indicated with regard to which it is profitable to compare processes for thé cleaning of coal. The theoretical principles upon which eight types of cleaning processes depend are outlined, together with the limitations imposed on them by reason of the principles involved. All of these eight typical processes are compared with respect to seven conditions which, it is suggested, a coal-cleaning plant should be able to fulfil, viz. : (1) there m ust be differen
tiation between light and heavy middlings ; (2) there should be little mechanical stress on the coal particles ; (3) the particles should be in contact with water for a minimum time ; (4) fine adjustm ents should be reduced to a minimum ; (5) it should be possible to stop or start the plant rapidly, and efficient washing should obtain immediately on re-starting ; (6) there should be efficient operation with an irregular rate of feed and a feed varying in quality or size ; (7) there should be a minimum number of accessory appliances such as pumps, motors, elevators, conveyors, and screens. The processes con
sidered are the Draper, Baum, Rheolaveur, and Chance washers, the Deister-Overstrom concentrating table, the Wye and Spiral separators, and froth flotation.
B r itis h C hem ical A b s tr a c ts —B .
Cl. IL —Füel ; Gas ; Dksthuottvb Distillation ; Mineral Oils. 641
Cleaning of coal, w ith special reference to pneum atic separation. C. W. H . Ho l m e s (J.S.C.I., 1927, 46, 270—279 t).—The development of pneumatic as opposed to hydraulic classification is discussed, dealing more fully with development from the Sutton, Steele, and Steele pneumatic separator to the “ S.J.” and the
“ Wye ” type. The laws governing the separation of particles by virtue of the difference in their densities are discussed, and the advisability of applying the m athe
matics of hydraulic classification to pneumatic separation is questioned. The dry cleaning of coal by pneumatic separation is discussed in relation to the carbonisation industries. Notes are appended describing some of the methods adopted in recent investigations on the process of pneumatic separation which is being carried out by the Birtley Iron Company.
Froth flotation applied to a B aum [coal] w asher.
W. Gu id e r (J.S.C.I., 1927, 46, 238—242 t).—An investi
gation of the washing conditions in the Baum apparatus led to the conclusion th a t fine dirt had no adequate outlet from the washer, and froth flotation was introduced as a means by which the d irt could be discharged from the washer while the fine coal was recovered. The installation of the machine and its effects on the washer are exhaustively described and a detailed table of costs is given. The advantages and disadvantages of froth flotation plant are considered ; it is stated th a t the reduction of ash content in the slack is obtained a t the expense of an increase in moisture content.
F loat-and-sink testin g of sm a ll coal. J. L.
Tho m so nand C. N. Ke m p (J.S.C.I., 1927,46,206—209 t, 312—313t).—A semi-portable self-contained unit adapted for use in the control laboratory, or on the washing plant itself, is described. The capacity of the float-and-sink vessel may be such as to meet individual requirements, and the separation of the float and sink is facilitated by the special construction of the jig tube within the main container. The removal of each successive float is effected by means of the specially shaped scoop which is introduced after separation, between the float and the sink. The handling of the various solutions is obviated by the employment of compressed air (about 5 lb. per sq. in.) as the means of filling the container, which is emptied by gravitation after the separation of each float.
Although the unit is designed to carry out separations through a range of specific gravities, any individual solution is immediately available for a special test for any particular purpose.
R ecovery of a m m o n iu m thiocyanate in coking.
W. Glu u d and W. K lem pt (Z. angew. Chem., 1927. 40, 659—660).—The results of large-scale experiments on the removal of hydrocyanic acid from coke-oven gases by the thiocyanate process, in which the crude gases are passed through washers in which an aqueous sulphur suspension is circulated, are described. After twelve days, during which 2000—3000 cub. m. of crude gas were treated per hr., the solution attained a strength of 20% by weight of ammonium thiocyanate, the efficiency of extraction of hydrocyanic acid being 98% ; only one washer was employed. I t is possible to obtain much stronger solutions, bu t after a strength of 20%
has been exceeded the extraction is no longer quantita
tive. Suggestions are made for possible uses of the thiocyanate on a scale which would absorb the possible production from coke ovens in Germany, estimated a t 20,000 tons per annum. S. I. Le v y.
D eterm ination of th e quality of activated carbons.
Z. V y t o p i l (Z. Zuckerind. Czechoslov., 1927, 51, 511—-514).—In examining carbons as to their suitability for use in sugar manufacture, the author determines the water, ash, water-soluble m atter, reaction, and the weight of 1 litre of loosely-packed material. The decolorising power is determined by Sporry’s equal- effect method (cf. B., 1923, 369 a ) , the results being compared with Carboraffin or one of the Norit grades as standard. A 4% solution (by vol.) of beet molasses, or better the actual product to be treated in the refinery, is heated with the carbon a t 80—90° for 10—15 min. Other determinations which might be made are : adsorption of inorganic substances, alteration of pn during decolorisation, rate of filtration, and power of regeneration. I t is not possible to translate the figures obtained in the laboratory into practice, where a much better decolorising effect may be obtained when the method of filtration through a layer on the filtering surface is applied. J. P. O g i l v i e .
Value of low -tem perature tar as th e carburetting oil for w ater gas. K. Sh im o m u r a (J. Fuel Soc. Japan, 1927, 6, 50—51).—Experiments on an industrial scale have shown th a t low-temperature tar is as satisfactory for carburetting water-gas as the gas oil usually used for the purpose. Creosote oil, on the contrary, gave poor
results. A. B. Ma n n in g.
D eposit on an underground gas m ain. A.
Ma r s d e n (Gas J., 1927, 179, 219—221).—An 18-in. foul main laid 40 years ago and recently exposed had become covered externally by a crystalline deposit consisting essentially of anhydrous calcium acetate (93%) and containing some butyrate. The calcium had evidently been derived from the marl in which the main was laid, and it is suggested th a t the acetic and butyric acids have been produced by bacterial action on organic material conveyed by water percolating through the soil. H ot crude gas passed through the main, so th a t the tem perature of the adjacent soil would favour bacterial action. The main was not corroded.
A. B. Ma n n in g. P roduction of liquid fuels from coal. J. G. Kin g
(J.S.C.I., 1927, 46, 1 8 1 -1 8 6 t).—The three main lines along which the problem of oil production from coal is being attacked are described and the latest results reviewed. The effect of temperature of carbonisation on the constitution of low-temperature tar is illustrated by experiments carried out a t H.M. Fuel Research Station. There are indications th at 550—600° is a critical temperature so far as the tar is concerned when external heating is used. At 600° only 8-8% of the tar is saturated. On a large scale the yields of tar are not much greater than 16-5 gals, per ton of coal, and if 50 million tons of coal were carbonised only 150 million gals, of motor spirit and 550 million gals, of tars oils would be available—much less than the coun
try ’s requirements. The Bergius process offers tech
nically 100—130 gals, of oils per ton of coal or up to a 2
B r itis h C hem ical A b s tr a c ts —B .
6 4 2 C l . I I . — F i t e l ; G a s ; D i a x n c c n v * D i s t i l l a t i o * ; M j n h r a l O i l s .
60% by weight of suitable coals. The plant is described and yields are quoted. The catalytic production of alcohols and hydrocarbons from carbon monoxide is showing considerable promise for the future, bu t so far results are only experimental. The recent work of Fischer and Tropsch in producing petroleum-like hydro
carbons shows particular promise. The catalysts used and the nature of the end products are described.
Products of com bustion from coal gas flam es.
H . Da v ie s and II. Ha r t l e y (J.S.C.I., 1927, 46, 201—206 t).—The iodine pentoxide method was em
ployed to determine the carbon monoxide in diluted products of combustion. Simultaneously the air of the laboratory was also examined. Large volumes were employed and an accuracy of 1—2 parts per million was attained with the apparatus and procedure used.
Well-aerated and poorly-aerated Bunsen as well as luminous flames were investigated, and the results of 27 experiments are given. The experimental results indicate th a t traces of carbon monoxide escape from the combustion zone. On the assumption th a t only the air theoretically required for complete combustion actually enters into the combustion phenomena, it is calculated th a t the ratios of carbon monoxide to dioxide in undiluted products of combustion are respectively 0-00024, 0-00034, and 0-0001 for the three types of flames. These ratios correspond to 31, 44, and 13 parts per million of carbon monoxide in undiluted dry pro
ducts.
Fuel for internal-com bustion en gines. (Si r) F. L.
Na t h a n (J.S.C.I., 1927, 46, 211—220 t).—The world’s petrol position is discussed and the conclusion is drawn th a t petrol will continue for a long time to come the principal liquid fuel, b u t th a t it will probably be supple
mented in due course by a liquid fuel from shale. The possibilities of producing alternative liquid fuels within the Empire are considered, such fuels being benzol and tetralin, both coal distillation by-products, and alcohol from vegetable materials rich in starch, and from the cellulose of plants—a process for this is described.
Other sources of alcohol referred to are sulphite waste liquors, ethylene from coal and coke-oven gas, and carbide. The production of liquid fuels by the low- temperature carbonisation and the hydrogenation of coal, as 'well as their synthetic production from carbon monoxide and hydrogen, is briefly described. Gaseous fuels, mainly coal gas and producer gas, are also re
ferred to.
Separation of the com ponents of petroleum . V.
E dge filtration. I. Isolation of w axes from un
topped crude oil w ithout p yro ly sis. P. F. Go rd o n
and A. C. Ma r s h a l l (J.S.C.I., 1927,46, 304—306 t).— The effect of filtering untopped crude Persian oil through a laboratory model of the Hele-Shaw stream-line filter under varying conditions of temperature and of pack and oil pressure was examined. Black, viscous, asphaltic material can be separated a t ordinary temperature ; the yield is increased by decrease of temperature. By cooling the crude oil in ice and salt and receiving the filtrate a t 11—12° quantities of this residue (d22 about 0-899) varying, according to pack and oil pressure, from 1-6 g. to 12-4 g. were removed from 100 c.c. of
crude oil (d about 0-839). Up to about 60% of white wax could be isolated from these residues. The waxes had different forms, e.g., amorphous brittle masses ; amorphous clouds; amorphous flakes; granular c lu sters; long needles; fibrous flocks, and lustrous fibrous flakes. They had m.p. varying from 67-5° to 76°. One series of filtrates separated into two well- defined layers on cooling—the lower viscous and rich in asphalt, the upper mobile and volatile. Clusters of crystalline wax separated from the upper layer during slow low-temperature evaporation. The physical condi
tion of waxes in crude oil is discussed.
D etection of coal tar and coal tar d istilla tes in petroleum asphalt and natural asp halt. (Miss) J. C. M. Sa u e r b ie r (Chem. Weekblad, 1927, 24, 348—
350).—Coal-tar products may be detected by means of Graefe’s reaction, which'gives better results if diazotised sulphanilic acid is used in place of diazobenzene chloride.
The material is boiled with sodium hydroxide solution, the whole filtered when cold, and the test carried out with the filtrate. The proposal of Marcusson to dis
tinguish between coal tar itself and its distillates in admixture with an asphalt by means of the solubility of the latter in light petroleum is found to give no tru st
worthy results. S. I. Le v y.
V olatility and carbonisation of oils for cylinder lubrication. J. W. Do n a l d so n (J.S.C.I., 1927, 46, 324—327 t).—Examination of three mineral oils—light, medium, and heavy—used for cylinder lubrication and tested under varying conditions of temperature (350—
550° F.), varying periods of time (15—60 min.), and over varying surface areas (0-5—2-0 sq. in.), indicated th a t volatilisation was proportional to the varying times and areas. The character of the residues was determined by the tem perature and showed th a t the light-bodied oil did not carbonise till most of the oil had volatilised and only a small deposit remained, whilst the heavy
bodied oil volatilised slowly, even a t high temperatures, and left a large deposit.
C orrosion in p etroleum distillation plant. II.
M. Fr e u n d (Chem.-Ztg., 1927, 51, 528; cf. B., 1919, 808 a).—The corrosion of the iron valves and condensing columns of the apparatus used in distilling crude petro
leum with steam may be due to two causes—the presence of chlorides in the emulsified water in the oil and the production of a large volume of carbon dioxide by partial oxidation of the unsaturated hydrocarbons in the oil.
The latter is due to entrapm ent of air in the steam used or to leakage of air into the apparatus. Thus, in the distillation of crude benzine from Boryslav petroleum a t 400°, the uncondensed gases contained as much as 2-5% of carbon dioxide and the issuing water from the apparatus contained 4 kg. of iron per 100 m.3 of oil distilled, partly as chloride and partly as ferrous hydrogen carbonate. To avoid these troubles addition of lime or dilute alkali solution is recommended, together with the use of air-free water in the boilers. A. R. Po w e l l.
B urning of m in eral oils in w ick-fed la m p s.
J . K e w l e y and J . S. Jackson (J . Inst. Petrol. Tech., 1927,13, 364—397).—The essential features of a good oil include no loss of illuminating power during use and no formation of deposits on the glass. The impurities
B r itis h C hem ical A b s tr a c ts —B .
C l . I I .— F u e l ; G a s ; D e s t r u c t i v e D i s t i l l a t i o n ; M i n e r a l O i l s . 043
likely to occur in kerosenes are sulphur compounds, including sodium sulphonates. The formation of bloom on lamp glasses is caused by sulphur compounds in the kerosene and also by fog or ammonia in the atmosphere.
A new chimney accumulates bloom more easily than an old one. Bloom was found to contain organic sulphur acids, ammonium and sodium sulphates, with traces of potassium and calcium. The cooler the chimney the greater is the deposition of bloom, other things being equal. The brighter the flame shortly after lighting the lamp the better is the kerosene for burning purposes.
Satisfactory results were obtained with a Weber photo
meter, whereby a straight-line relationship was observed between height of flame ju st on the point of smoking, and candle power of th a t flame. The liquid extracted by liquid sulphur dioxide from Borneo kerosene pro
vided a typical aromatic kerosene ; typical paraffinoid and naphthenic kerosenes were also obtained. I t was then found th a t for kerosenes of similar boiling ranges the initial illuminating power is determined by the chemical composition. The higher the boiling range the less is the illuminating power. Viscosities and capillari
ties of kerosenes were examined in order to investigate the tendency of some kerosenes to give a steadily diminishing flame ; in general those with a high viscosity possessed a high capillarity. The tendency of the wick to char appears to be connected with the viscosity and the chemical composition of the oil. I t was found th at the lighter fractions of the kerosene did. not burn first during tests, bu t th a t the oil burnt as a whole. The chief cause of diminishing flame size in domestic lamps is the fall in oil level in the reservoir. W. N. Ho y t e.
B urning tests of kerosene. W. H. Th o m as(J. Inst.
Petrol. Tech., 1927, 13, 402—409).—In the author’s tests 900 c.c. of oil are fed to a special lamp and burnt by means of a flat 'nick f in. wide, the test continuing without attention to the lamp after the first hour, for 24 hours. Flame dimensions are adjusted to 1 in. height, 1 in. wide. The fall in candle power is observed together with oil consumption, am ount and type of film on the glass, and condition of the wick. The normal consumption is 27 c.c. per hour. The lamp gives between 5 and 6-5 candle power.
W. N. Ho y t e.
“ B ergin isation ” and an in vestigation of hydro
carbon m ixtu res. I. H . I. Wa t e r m a n and J . N. J . Pe r q u in (J. Inst. Petrol. Tech., 1927, 13, 413— 423).—
Tests on a large number of hydrocarbons showed th a t the refractive indices give more accurate information on the purity of the substance than does the dispersivity;
the latter constant is, however, of use in identifying the class of hydrocarbon. Bromine values and mol. wt.
determinations in many cases gave useful information.
In an attem pt to crack paraffin wax in the vapour phase the vapours were raised to 450° for 4 seconds. No decomposition was observed. F urther experiments in which paraffin wax was heated with aluminium chloride a t 200° and then 250° gave yields of 1 3 ‘9% and 11 -2%
of gasoline respectively. W . N. Ho y t e. S olu b ility of ox ygen , carbon d ioxid e, and nitro
gen in m in eral o il ; transfer of carbon dioxide from oil to air. L. S. Ku b ie (J. Biol. Chem., 1927,72, 545—
548).—1 c.c. of a heavy paraffin oil dissolved 0-841 c.c.
of carbon dioxide a t 24—25°, 0-134 c.c. of oxygen at 28°, and 0-071 c.c. of nitrogen a t 22—22-5°, a t atmos
pheric pressure. A saturated solution of carbon dioxide in the oil, when exposed to the air, lost carbon dioxide rapidly from the upper layers, but very slowly from the
lower. C. R. Ha r in g t o n.
D evelopm ent of d esign of by-product coke oven.
R. A. Mo t t (Fuel, 1927, 6, 373—380).
A m m on iu m chloride from gas liquor. Ad o l p iu.
—See VII.
A m m onium sulphate plant. Er n s tand Ed w a r d s.
—See VII.
A dsorption of activated carbons. Sp e n g l e r and La n d t, also Tr a u b e.— S ee XVII.
Pa ten ts.
P rocess and apparatus for testin g sam p les of coal b y d istillation . R. Ge i p e r t (E.P. 268,718, 23.9.26. Conv., 31.3.26. Addn. to E.P. 267,082 ; B., 1927, 516).—To prevent the undue expansion of coal during distillation in the test apparatus, a rod having an enlarged end extends through a gas-tight joint into the distilling chamber and rests on the coal blocks. These blocks are grooved and perforated to facilitate the pass
age of the gases evolved. A. C. Mo n k h o u s e. Coke oven. C. St il l (E.P. 260,974, 20.10.26.
Conv., 5.11.25).—The products of distillation from a coke oven are withdrawn through slats, arranged like a Venetian blind, into a hollow space in the door of the oven, and thence to a passage below the sole of the oven.
A. C. Mo n k h o u s e. D istillation of solid fuel in coke ovens. C. St il l
( E .P . 266,584, 15.6.26).—In a coke oven, the distillation products are drawn through a perforated oven sole into a heat-insulated flue. The gas off-take may consist of a channel running longitudinally and centrally beneath the sole of the oven, openings in the channel being arranged to register with corresponding grated openings in the sole, or, alternatively, it may consist of a box-like compart
ment extending the whole width of the oven and con
taining two hollow-cast members which support the perforated oven sole. In the latter case, the distillation products are cooled by passing steam through the members in the gas off-take, which steam may then be passed into the crown of the oven. The rich distillation products from the central uncarbonised portions of the charge are drawn off continuously without contacting with the hot crown of the oven. S. Pe x t o n.
Lo w-tem pera tu re distillation retort. A. V.
Ab b o t t (E.P. 266,193, 26.6.26).—The retort consists of four co-axial truncated cones revolving in a combustion chamber. In the annular spaces between the two outer
most and between the two innermost casings are her
metically-sealed steel flasks containing a fusible metal, e.g., lead. The centre annulus contains the coal under
going distillation. Coal is fed into the distillation chamber where it is forced by inclined ribs to travel in a circular and longitudinal direction along the outer heat
ing wall until, a t a certain position in the rotation, it is caused to fall on to the inner heating wall, which is also provided with guiding ribs so staggered in relation to the
B r itis h C hem ical A b s tr a c ts—B.
0 4 4 Cl. I L — Fu e l ; Ga s; Db s t i i u o t i v k Di s t i l l a t i o n; Mi n b b a l Oi l s.
others th a t the progress of the coal is retarded. The carbonised fuel falls over an inclined apron which re
volves with the retort and projects into the gas-collecting chamber. A condensing coil is built into this chamber and ta r condensed on its surface is drained away.
S. Pe x t o n. D istilla tion of solid carbonaceous su bstan ces.
T. M. Da v id so n (E.P. 273,389, 30.3.26).—Carbonaceous substances, such as coal, are carbonised in- a vertical retort with a taper of about 1 in 12, and such th a t on periodically discharging part of the coke a t the base, the remainder of the charge is lowered as a coherent mass, leaving an interstitial space between the retort wall and the charge, into which a fresh charge of the sub
stance is introduced. The fresh charge is thus heated in a thin layer from both sides, heat transmission and carbonisation being thereby rapidly effected.
A. B. Ma n n in g. D istillation of coal [of h igh sulphur content].
R . G. Gr is w o l d, Assr. to Do h e r t y Re s e a r c h Co.
(U.S.P. 1,635,667, 12.7.27. Appl., 29.4.22).—The coal is heated by direct heat transfer from a hot gas of low calorific value in such a way as to produce coke and a rich gas of high sulphur content. P a rt of the coke is burnt and the hot gaseous products are used to heat the remainder to incandescence, steam being then passed through the latter to generate the gas of low calorific value used for heating a fresh charge. The rich gas is purified and passed through the remaining incandescent coke, the sulphur content of which is thereby further reduced. A. B. Ma n n in g.
D estructive hydrogenation of coal, tar, m ineral o ils, and th e lik e. I . G. Ea r b e n in d. A.-G. ( E .P . 254,713, 28.6.26. Conv., 2.7.25).—Gases containing hydrocarbons and their derivatives prepared by the hydrogenation of carbonaceous substances are further treated with oxygen or gases richer in oxygen th an air in the presence of catalysts, e.g., nickel precipitated on magnesia, iron alloys, molten iron. The hydrocarbons are converted into carbon monoxide and hydrogen, water vapour and/or carbon dioxide being added, if required, for the conversion. Hydrocarbons such as ethane etc. may be separated from the initial gases by cooling or by adsorbents. A. C. Mo n k h o u s e.
Vertical retort for the extraction of oil from bitum inous solid fuels such as sh ale, coal, peat, and the lik e. G. Me n e l l (E.P. 272,766, 20.11.26).—
The retort consists of a vertical, flattened, narrow shaft with sloping plates arranged alternately on opposite sides of the retort wall to give a zig-zag course to the fuel. The retort is divided into two chambers by a rotary valve, the quantity of material discharged being controlled by similar valves on the charging and dis
charging ends. The products of distillation are with
drawn from each chamber through outlets which slope upwards from beneath the plates. The retort is heated externally, or internally by superheated steam or gas adm itted through pipes beneath the sloping plates.
A. C. Mo n k h o u s e. Apparatus for th e d istillation of fuel, roastin g ores, and lik e heatin g purposes. J. Pl a s s m a n n
(E.P. 254,697, 17.6.26. Conv., 30.6.25; cf. E.P.
240,800 ; B., 1926, 228).—The annular heating chambers or cells are built up from segments of refractory material.
The adjacent superposed segments are offset in relation to each other and are so shaped th a t the gases follow a zig-zag path round the apparatus. There is a central heating-gas and mixing shaft in the upper part of which is a heat-equalising accumulator. The apparatus may be worked a t a tem perature high enough for the produc
tion of metallurgical coke. R. A. A. Ta y l o r. Low -tem perature carbonisation of coals etc.
K. M. Sim p s o n (E.P. 273,935, 22.9.26).—A series of receptacles is affixed to an endless carrier. While they are passed in the direction in which they are inverted, they traverse a zone in which they are heated sufficiently to carbonise a charge of finely divided carbonaceous material, which is fed into them when they pass round into the upright position and on through a distilling zone. They are re-inverted a t the discharge end for the carbonised material, and necessary steps are taken to recover the distilled products. R. A. A. Ta y l o r.
Manufacture of illu m in ating and industrial g ases.
H . Nie l s e n and B. La in g (E.P. 272,822, 1.11.26).—A rotating inclined producer is used for the manufacture of water-gas. Gas and air for combustion are admitted a t one end and, after combustion, pass through chequer brickwork in channels surrounding the producer.
When the requisite temperature is attained, steam, preheated at. 1000° or above, is adm itted in reverse direction through the chequer brickwork and passes through the semi-coke in the producer. The resulting gases are withdrawn from the fuel inlet end of the producer, their sensible heat being further utilised in retorts. The heating value of the gases may be increased by passage through heated chequer brickwork for the purpose of cracking the tarry vapours.
A. C. Mo n k h o u s e. Manufacture of gas. H u m p h r e y s & G l a s g o w , L t d . , and J . C. S t e l f o x (E.P. 266,108, 20.1.26).—In the manufacture of gas by the complete gasification of coal in a single generator, the mixed coal gas and water-gas produced is of low calorific value. I t is proposed to limit the quantity of water-gas by withdrawing part of the coke from the carbonising zone and thus make a high-grade gas together with some coke. In a recess, built round the generator a t a level above the blast off
take, is mounted a rotary Ting carrying doors h in g e d on a vertical axis. As the ring rotates in one direction the doors engage in and extract p art of the well-carbonised periphery of the charge, which is diverted into suitable chambers ready for discharge. When the direction of rotation is reversed the hinged doors close and dis
engage from the coke, extraction thereby ceasing. The quality of gas made can be varied by adjusting the proportion of coke discharged w ithout resorting to
carburetting. S. P e x t o n .
T reatm en t of [fuel] ga ses w ith liqu ids. E. L. Pe a s e
(E.P. 273,103, 7.7.26).—A suspension of calcium sulphate is used to wash the gas, when, with ammonia and carbon dioxide present, ammonium sulphate aud calcium carbonate are formed. The spent liquor is then heated a t a higher tem perature (80—90°) and preferably at a reduced pressure. The reaction is reversed and the
B r itis h C hem ical A b s tr a c ts —B .
Cl. H I . — Taiła n d Ta b Pk o d d o t s. 645
ammonia and calcium sulphate are regenerated, the former being absorbed by a suitable acid agent.
R . A. A. Taylor. Purification of g as. Hu m p h r e y s & Gl a sg o w, Lt d. From E. J. Br a d y (E.P. 266,586, 18.6.26).—
Gas to be purified is passed upwards through a vessel of gradually increasing cross-section against a cloud of finely-divided purifying agent (e.g., hydrated iron oxide) which gravitates down the vessel. The velocities of the gas and of the purifying agent progressively decrease, but their relative velocities at various stages are fairly
constant. S. Pe x t o n.
R educing to carbon m onoxide the carbon dioxide content of g a ses. F. M. W i b e r g (E.P. 266,729,23.2.27.
C'onv., 27.2.26).—A charge of carbonaceous material is partially burnt by means of air and the gas containing carbon dioxide, adm itted simultaneously or alternately ; further quantities of carbon dioxide are reduced by contact with a fresh portion of the charge heated electri
cally. The method may be utilised by alternating the processes of passing air through one and generating water-gas in the other of a pair of water-gas producers, and then passing the mixed gases through a chamber containing electrically-heated carbonaceous material.
R. A. A. Ta y l o r. M anufacture of m otor fuel. I . G. Fa r b e n in d. A.-G. ( E .P . 251,969, 27.4,26. Conv., 8.5.25).—To minimise “ knocking ” without substantially reducing the calorific power of the fuel, anhydrous methyl alcohol, either alone or mixed with higher alcohols or ketones, is added to gasoline. S. Pe x t o x.
Production of liquid hydrocarbons and other organic substances from heavy organic m aterials.
G. Pa t a r t (E.P. 249,519, 15.3.26. Conv., 21.3.25).—
The liquids or gases resulting from high-pressure syn
theses, e.g., the manufacture of methyl alcohol, are utilised a t their respective pressures and temperatures for the treatm ent of carbonaceous solids or liquids, e.g., coal, peat, heavy petroleum oil, in suitably designed digesters. Distillation or hydrogenation takes place and the products are recovered. Catalysts may be used in the digesters and the gas mixtures required in the initial operation prepared from the residue of the products by incomplete carbonisation. A. C. Mo n k iio u s e.
Purification of hydrocarbons. I . G . Fa r b e n in d. A.-G. (E.P. 255,905, 26.7.26. Conv., 27.7.25).—High- boiling hydrocarbon oils are treated with mixtures of methyl alcohol and low-boiling aromatic or naphthenic hydrocarbons. The impurities in the raw material are dissolved and the purified oil, not being miscible with the washing material, can be separated.
R. A. A. Ta y l o r. Converting h igh -b oilin g hydrocarbons, w hich have been freed from th e su bstan ces soluble in liquid sulphurous acid, into low -b oilin g hydro
carbons b y m ean s of alum iniu m chloride. Al l g e m. Ge s. f u r Ch e m. In d. (E.P. 273,999, 11.3.27. C o n v ., 17.9.26. A d d n . to E.P. 272,433, B., 1927, 595).—T h e r e s id u a l o ils, b e fo re th e re n e w e d t r e a t m e n t w ith a lu m in iu m c h lo r id e , a r e t r e a t e d w ith c o n c e n t r a te d s u lp h u ric a c id in s te a d o f w ith s u l p h u r d io x id e .
R. A. A. Ta y l o r.
Refining m ineral oils and/or their d istillates.
Bu r m a h Oil Co., Lt d. From J. P. Fr a s e r (E.P.
273,351, 25.1. and 21.9.26).—Mineral oils, or their distillates, are refined by extraction with phenol, or a mixture of phenol and cresylic acid, containing 5—15%
of water. The oil is separated and washed with a solution of caustic alkali, from which any phenol is subsequently recovered by acidification. A part of the mineral oil dissolved in the phenol is recovered by partial dilution of the latter with water and separation of the oily layer so produced. The phenol and dissolved substances are then separated by agitating the mixture with a large volume of water a t a temperature between 90° and 100°, or, in refining low-boiling fractions, by distilling to 120°. A. B . Ma n n in g.
Cracking of petroleum oils and carburetting o f w ater-gas. Pet r o l e u m Ch e m ic a l Co r p., and E. P, St e v e n s o n ( E .P . 273,781,24.3.26).—A vaporous distillate from petroleum is cracked in a tubular r e to r t; the gaseous product is stripped by condensation of heavier residues and motor spirit and by removal of hydro
carbons of three or more carbon atoms, especially the unsaturated hydrocarbons liable to form gummy deposits.
The remaining rich gas is mixed with a lean gas, e.g., water-gas. The production of defines is promoted by inhibiting any exothermicity in the cracking process.
The heating may be arranged in zones according to the temperature in the preceding zone. The define fractions and spirits in an oil are developed by cracking the vapours which distil off only up to 400°, the non-volatile residue being removed. Before the residual gas is used for carburetting it may be further stripped by refrigeration or oil-scrubbing. Before or after mixing with the lean gas, any remaining condensible con
stituents may be fixed by heating the gas to a tempera
ture higher than the cracking temperature.
R. A. A. Ta y l o r. G as-testing apparatus w ith pressure gau ges, m ore p articu larly flu e-gas testers. Sie m e n s &
Ha l s k eA.-G. ( E .P . 262,092,16.11.26. C o n v ., 27.11.25).
Ferric su lp h ate (E.P. 273,883).—See VII.
E lectrical purification of gases (G.P. 439,693).—
See XI.
III.— TA R AND TA R PRODUCTS.
Variation of H utchinson con sisten cy of tars with tem p eratu re. H. M. Sp ie r s (J.S .C .I., 1927, 46, 329—330 t ; cf. B., 1927, 38.)—The criticisms by Mallison and Soltau (B., 1927,517) are met by calculations made from the results quoted by these authors. The mathematical relationship previously proposed is shown to hold good over intervals of temperature as large as 10° C. I t is pointed out, however, th a t one or more transition points’ m ay occur where sudden changes in the value of the constant are encountered due to alterations in the physical nature of the tar possibly caused by crystallisation of naphthalene, deposition of waxy m atter, or change in the state of aggregation of the dispersed colloids.
A sp h a lt-lik e substances in coal tar. G. Seb o r
(Petroleum, 1927, 23, 890—897).—The methods used for determining “ asphalt ” in mineral oils give widely
B ritish C hem ical A b s tr a c ts —B.
6 4 6 Cl. I V . — D y e s t u f f s a n d I n t e r m e d i a t e s .
different results when applied to a coke-oven tar. From a consideration of the behaviour of the tar on admixture with different solvents the following procedure is recom
mended for separating the “ asphalt ” from the residual oil and determining the content of each : 1 g. of ta r is dissolved in 10 c.c. of carbon disulphide a t the ordinary temperature and 100 c.c. of methyl alcohol are added.
After 2 hrs. the clear liquid is decanted through a filter and the residue washed with methyl alcohol until the filtrate is colourless. The residue in the flask and on the filter is dissolved in benzene, transferred to a basin, and after evaporation of the benzene weighed.
The properties of both the asphalt and the residual oil have been fully investigated. The asphalt content of a number of coke-oven tars varied from 16-5 to 24-5% . A m arled increase in the value was observed on heating the tar to 200°. The method can be applied to other types of tar, pitches, etc. A. B. Ma n n in g.
L ow -tem perature tar for carburetting w ater- g a s. Sh im o jiu r a.—See II.
Coal tar etc. in asp halt. Sa u e r b ie k.—See II.
Pa t e n t s.
D istillation of coal tar, tar o ils, and sim ila r liqu ids. A. Me ir o (E.P. 267,074, 15.6.26. Conv.,
■2.3.26).—After a preliminary dehydration, ta r is fed into a still where it is kept in constant agitation by stirrers. The distillation is carried out under pressure and the products pass into a series of dephlegmators, the final gas after purification being returned to the still. The flue gases from the still pass through flues to the dephlegmators, each of which is independently controlled. The liquid fractions condensed pass to coolers and receivers. A. C. Mo n k h o u s e.
Separation of w ater from m ixtu res of steam and vapours of benzene, toluene, and like hydrocarbons.
C. C o o p e r, D. M. He n s h a w, and W. C. H o l j i e s & C o., L t d . (E.P. 273,224, 16.12.25).—Mixtures of the vapours of water, benzene, toluene, etc., and in particular the mixed vapours arising from the steam-distillation of the wash oil used in the recovery of benzene from coal gas, are freed from water by treatm ent with a suitable absorbing liquid, e.g., a concentrated solution of calcium chloride. The vapours are brought into contact with the absorbing solution in a column in which the solution runs counter-current to the vapours ; the latent heat of condensation developed in the column is utilised for the re-concentration of the absorbing solution.
A. B. Ma n n in g. E xtraction of cry sta ls from anthracene, naph
thalene, and th e lik e d istillates of coal tar. A.
Me ir o (E.P. 255,429, 15.6.26. Conv., 15.7.25).—
Naphthalene, anthracene, etc. are separated from the distillate by mixing with the fraction a solvent of b.p.
below 100°, e.g., petrol, benzol, light petroleum, carbon disulphide, etc. The mixture is cooled in heat-insulated vessels and, after crystallisation, is passed through a filter a t the bottom of the vessel, compressed air being used to separate further oil and solvent from the crystals.
After washing with water they are removed and dried.
The solvent is recovered from the filtrate by distillation.
A. C. Mo n k h o u s e.
Furnace for heatin g tar and th e like. R. and A. B Ma c in t o s h (E.P. 273,890, 24.6.26).
H ydrogenation of tar (E.P. 254,713).—See II.
H ydrocarbons (E.P. 255,905).—See II.
IV .— DYESTUFFS AND INTERMEDIATES.
S y n th e sis of isoviolan th ron e (fsodibenzanthrone).
C. Ma r s c h a l k (Bull. Soc. chim., 1927, [iv], 41, 706—709).—Oxidation of dibenzoylperylene with m an
ganic sulphate or manganese dioxide in sulphuric acid solution a t — 10° to — 15° in presence of boric acid affords isoviolanthrone, which, by treatm ent with chlorine in nitrobenzene solution a t 60°, yields a chlorinated isoviolanthrone affording dyeings which are brighter and 50% stronger than those of Brilliant Indanthrene Violet RR. Oxidation a t room tem perature affords a hydroxylated v at dye forming a bluish- violet paste which dyes cotton in olive shades, turning blue with acids. Metliylation of this product with methyl sulphate in nitrobenzene in presence of sodium carbonate gives a bluish-green v a t dye dyeing cotton in blue shades fast to chlorine and washing. Substituted woviolanthrones can be similarly prepared from the corresponding diketoperylenes. R. Br ig h t m a n.
A zoic colou rs. Hi g g in s.—See VI.
Pa t e n t s.
Preparation of azo d y es. I. G. Fa r b e n in d. A.-G.
( F .P . 609,136, 12.1.26. Conv., 13.1.25).—Diaryl sul- phones which contain in separate nuclei a primary amino-group and an o-hydroxy-carboxylic acid grouping are diazotised and coupled with coupling components to give after-chrome dyes for wool, which also yield chrome printings on cotton fast to soap and chlorine.
After-chroming does not appreciably change the direct shade on wool. 4-Amino-4'-hydroxy-2 : 3'-dicarboxy- diphenyl sulphone, prepared by reducing the condensation product from 5-sulphinosalicylic acid and 2-cliloro-5- nitrobenzoic acid, is diazotised and coupled with [3-naphthol-S-suIphonic acid for an orange-yellow. 2- Amino-4'-hydroxy-3'-carboxy-4-sulphodiphenyl sulphone, obtained by reduction of the condensation product of 5-sulphinosalicylic acid with 4-chloro-3-nitrobenzene- sulphonic acid, is diazotised and coupled with 2-methylindole (yellow), 4-nitro-?»-phenylenediamine (reddish-yellow), ji-naphthol (orange), 4-methoxy-m- toluidine, further diazotised and coupled with salicylic acid (reddish-brown), H-acid and further coupled with 2 : 4'-diazodiphenylazosalicylic acid (green), y-acid
(bluish-red). C. Ho l l in s.
M anufacture of preparations of diazo sa lts for d yein g and printing. I. G. Fa r b e n in d. A.-G., Assees.
o f Ch e m. Fa b r. Gr i e s h e i m- El e k t r o n (E .P . 246,181, 19.1.26. C o n v ., 19.1.25).—Aryldiazonium neutral 1 : 5-naphthalenedisulphonates made from non-sulphon- ated arylamines are relatively stable, crystallise well from their aqueous solutions, are sufficiently soluble in water (often more soluble in presence of disodium 2 7-naphthalenedisulphonate or benzenesulplionate), and give clear shades when coupled on the fibre with, e.g., 2 : 3-hydroxynaphthoic arylamides. The presence of negative groups in the arylamine is advantageous,
