BRITISH CHEMICAL ABSTRACTS
B.—APPLIED CHEMISTRY
JANUARY 18, 1929.
I.— GENERAL; PLA N T; MACHINERY.
U tilisa b le n atu ral en erg y . H. Bap.j o t (Compt.
rend., 1928, 187, 1048—1050).—I t is suggested th a t the w ater a t alm ost 0° beneath thick layers of ice in regions where the air tem perature is of the order of —40°
m ight be pum ped to the surface and its laten t heat used to boil a liquefied gas {e.g., ammonia) or, preferably, to remove by boiling a volatile non-aqueous hydrocarbon {e.g., propane) from an intim ate m ixture w ith water.
The fluid could then be used to work a turbine, frozen sea-water or brine providing an efficient and convenient condenser, since the hydrocarbon would be recoverable from the saline liquor produced by fusion. If the mechanical efficiency of the installation is assumed to be 4% , 1 m .3 of w ater would supply energy equal to th a t produced by the fall of the same q u an tity of water
through 1360 m. J. Gr a n t.
T ech n iq u e and eco n o m ics of m ech an ical d is p ersin g p r o c e sse s. F. He b l e r (Kolloid-Z., 1928, 46, 225—227).—An investigation into the efficiency of various types of colloid mill. The type selected for a given process m ust vary w ith the particular conditions.
E . S. He d g e s. T h e C ottrell-M oeller p r o cess [for p recipitation of d u st and m is ts fro m g a se s]. P . Ve r Ee c k e
(Bull. Fed. Ind. Chim. Belg., 1928, 7 , 389— 402 ; cf. B., 1928, 877).—In a particular case the du st deposited by a Cottrell plant working on pyrites burner gases in a sulphuric acid p lan t am ounted to 550 kg./24 hrs., or 1 '33% of the pyrites charged, w ith a current consumption of 0-2 kw. The high tem perature (560—570°) in such plants formerly created difficulty owing to the destruction of the insulation, b u t this has been overcome. A t a Norwegian works dusts other th an arsenic are precipi
tated a t above 300°, and the arsenic is then separated by treatm en t a t 220°. In plants working in conjunction w ith contact acid plants, th e precipitation of arsenic is so complete th a t the Marsh te s t gives a negative result.
Amongst other acid mists successfully treated by the Cot
trell process are those from acid copper sulphate solution, ammonium nitrate solution, and phosphoric acid. The exit gases from bleaching powder chambers have been treated by injection of lime and subsequent electrical precipitation, and nitric acid is recovered from the waste gases from cellulose nitration. Sulphur dioxide for use in the paper industry is first freed from iron which reduces the catalytic formation of sulphur trioxide, and then freed from the la tter by a further Cottrell precipitation w ith cooling and injection of water. Experim ents have been made w ith the electrodeposition of hydrochloric acid. The removal of dust from blast-furnace gases is a particularly desirable application where these dusts
are rich in alkalis. Carbon dust is successfully precipi
tated in German lignite briquetting plants, the risk of explosion being guarded against by autom atic cut-outs.
The electrodeposition of ta r is particularly suitable for lignite tar, producer ta r, and the like, as trouble with emulsification is avoided. The Cottrell process is capable of removing smoke particles from the gases from industrial furnaces, b u t in this case no economic return is received. C. Ir w i n.
See also A., Dec., 1345, C alculation of a n a ly ses (Lie s c h e). 1348, T u n g sten and zircon iu m oxide furnace (Co h n). T h erm o sta t (Cu f r). T h e rm o sta t for p o la rim etric w ork (Ra m b e r g and He u b e r g e r).
Pa t e n t s.
[P reventing heat lo s s from ] annealing and other furnaces, m u ffle s, etc. Bir m in g h a m El e c t r ic Fu r n a c e s, Lt d., and A. G. Lo b l e y (B .P . 300,293, 6.7.27).—
H eat-retaining flaps or shutters arranged within the charging and/or discharging doors, and/or between preheating and cooling chambers, are displaced by the working charges during movement through or from the furnace'. " .T. S. G. Th o m a s.
D ry in g or sm o u ld erin g of lo o se m a te ria l. 0.
Do b b e l s t e in(U.S.P. 1,690,444,6.11.28. Appl., 26.11.26.
Ger., 30.11.25).—The apparatus comprises a vertical, rotary, cylindrical drum operating w ithin a stationary jacket and sealed therefrom a t the lower end by means of a liquid. The drum is provided w ith annular heating chambers arranged one above a n o th e r; the m aterial to be treated is fed to the spaces between the heating chambers, and means are provided for heating the chambers and for autom atically charging the dryer.
A. R. Po w e l l. A pparatus for m ix in g d ry and liquid m a ter ia ls.
L. Tr u e (U.S.P. 1,691,535, 13.11.28. Appl., 23.2.28).—
Dry, powdered m aterial is mixed in a chamber provided with delivery nozzles for discharging liquid into different parts of the chamber from points above the material.
The liquid is drawn from a ta n k provided w ith means for heating the liquid and is forced to the nozzles by a
pump. W. J . Bo y d.
T rea tm en t of so lid m a te ria ls w ith liquid r ea g e n ts. J. E. Eg l e s o n, Assr. to Ge n. Chem. Co. (U.S.P. 1,690,363, 6.11.28. Appl., 7.3.27).—The solid m aterial is digested w ith the liquid reagent and the solid residue allowed to settle. The supernatant liquid is withdrawn on completion of settling, and the sludge is washed w ith a counter-current of w ater under such conditions th a t the sludge settles continuously and is continuously withdrawn. W. J. Bo y d.
B r itis h C h e m ic a l A b s tr a c ts —B ,
4 0 C t,. I I . — Fu e l ; Ga s ; Ta b ; Mi n e r a l Oi l s.
A pparatus for the concentration of liq u id s.
Ze l l s t o f f-f a b r. Wa l d iio f, and A. Sc h n e id e r (G.P.
449,685, 6.5.25).—The hot gases after passing around the heating tubes in a tubular evaporator are led over the tops of the Field tubes, these being open. The liquid is conveyed into the Field tubes through rotatable inlet tubes provided with scrapers to remove deposits from the inner walls of the Field tubes. Scrapers are also provided for cleaning the surface of the heating tubes in contact w ith the h o t gases. L. A. Co l e s.
P erform in g [exoth erm ic] ch em ical reaction s [betw een g a se s]. C. W. Mo r t im e r (U.S.P. 1,691,903, 13.11.28. Appl., 17.4.23).—The vapour of a liquid kept a t the boil to regulate the tem perature of gases reacting in the presence of a catalyst is separated into two portions, one being used to h eat p a rt of the gases entering the reaction chamber and the other being condensed separately. L. A. Co l e s.
F riction m a teria l, p articu larly for u se for brake lin ers. Br i t. Thom son-Houston Co., Lt d., H. W . H.
Wa r r e n, and R. Ne w b o u n d (B.P. 300,309, 12.8.27).—
Layers of asbestos cloth and brass wire are coated w ith a solution of the condensation product of phthalic anhydride and glycerin modified w ith a plasticising agent, e.g., oleic acid ; after drying, the layers are heated and moulded under pressure. W . G. Ca r e y.
M anufacture of friction e lem en ts. I. J. No v a k, Assr. to Ra y b e st o s Co. (U.S.P. 1,692,136, 20.11.28.
Appl., 26.2.23. Renewed 22.12.27).—The element has an asbestos base containing as binder the solid residue from waste sulphite-pulp liquor. II. Ro y a l-Da w s o n.
Production of fir e -e x tin g u ish in g foam . R . Sc h n a b e l, and Ex c e l s io r Fe u e r l o s c h g e r a t e A.-G.
(B.P. 299,097, 22.7.27).—Foam-producing substances, such as saponin solution, are supersaturated w ith carbon dioxide, or other suitable gas under pressure, in closed vessels ; the foam is generated by releasing the pressure. Soluble or insoluble substances which assist the absorption or liberation of the gas (either chemically or catalytically) m ay be added to the liquid.
P. E . L, Fa r i n a. Producer or shaft furnace. J . W . Re b e r, Assr. to Wo o dall- Du ck ha m (1920), L td . (U.S.P. i , 692,572, 20.11.28. Appl., 25.1.27. U.K., 7.7.26).—See B.P.
262,668 ; B., 1927, 128.
U ltra -filter m em b ra n e. J. Du c l a u x (U.S.P.
1,693,890, 4.12.28. Appl., 30.8.23. Fr., 11.9.22).—
See B.P. 203,714 : B , 1924, 657.
M ech an ism for stirrin g the con ten ts of v e sse ls.
G. W. Cu ss o n s and G. Cu s s o n s, Lt d. (B.P. 301.159, 8.10.27).
II.— F U E L ; G A S; T A R ; MINERAL OILS.
A ir-d ry in g of Canadian lig n ite s, and the re- absorption of m o istu re b y the sa m e. J. H. H.
Nic o l l s (Canada Dept. Mines Fuel Invest., 1926, 51—-60).—'When samples of air-dried lignite were completely dried and then re-exposed to the air they never regained the original moisture content. This may have been caused by oxidation during drying.
Even when the samples were wetted and exposed to air
they did not retain as much moisture as the original samples. W ater was reabsorbed less rapidly and to a smaller extent the more severe and prolonged were the drying conditions. The gain in weight of a dried sample exposed to air was n o t wholly accounted for by moisture.
The moisture content of finely-divided lignites in air depended on its hum idity. Im provem ents in the standard air-drying apparatus (Rep. Sci. Ind. Res.
Council of Alberta, 1923, 39) are described. A. Ke y. P y r itic oxid ation w ith sp ecial referen ce to the R avine se a m . H. Ma c p h e r so n, N. Sim p k in, and S. V.
Wil d (Safety in Mines Res. Bd., 1928, Paper No. 47, 24 pp. ; cf. B., 1926, 1001).—Analyses were undertaken to determine the behaviour on oxidation, by exposure to air, of pyrites in sections of coal from the Ravine seam.
Underground observations of corresponding sections in the p it were made. The Ravine seam, consisting mainly of clarain, is covered by a low-grade m aterial, the “ Chitters.” E xam ination of the la tter and of a coal from a freshly exposed section of the seam showed th a t the larger the am ount of pyritic iron present the greater is the proportion of pyritic oxidation. The base of the
“ Chitters ” and the upper p a rt of the top coal showed the greatest pyritic oxidation. These parts of the seam are also those chiefly suspected of causing heating. Micro
scopical exam ination shows the distribution of pyrites as being irregular throughout the seam and occurring chiefly a t the base of the “ Chitters ” and the upper p a rt of the top coal. The content of oxidisable pyrites is small. Its oxidation causes disintegration of the coal and some self-heating. Analyses show the absence of any m aterial likely to cause catalytic oxidation a t any point. Photographs showing incrustations and atmospheric oxidation are appended. C. B. Ma r s o n.
N ature of sulphur in Canadian coal and coke.
J. H. H. Nicolls (Canada D ept. Mines Fuel Invest., 1926, 34—50).—Typical W estern Canadian coals were analysed for sulphate, pyritic, and organic sulphur.
The coking coals from the M ountain P ark and the two Crowsnest Pass areas and also the p artly coking coals from the Nanaimo area contained very little pyritic sulphur, b u t the two Saskatchewan coals analysed con
tained a considerable percentage of bo th pyritic and sulphate sulphur. Cokes made from the Maritime Provinces’ coals were analysed for sulphide, sulphate, free, and solid-solution sulphur. The coke made from the Springhill coal was the only one with a low enough sulphur content to be classed as a good metallurgical coke. The proportion of pyritic sulphur present in Maritime Provinces’ coals in a finely-divided condition was determ ined by means of “ float-and-sink ’’ separa
tions, as this p a rt of the sulphur m ay influence the liability to undergo spontaneous combustion.
W . H . Bl a c k b u r n. D eterm in ation of total sulphur in c o a l. 0 . Ha c k l
(Chem.-Ztg., 1928, 52, 933—934).—In view of the low results given by the Eschka m ethod, especially in the case of coals very rich in sulphur, due to (a) loss of sulphur during the heating up process and (b) incom plete oxidation, the following m ethod is suggested.
1 g. of finely-powdered coal, after drying a t 100°, is mixed in ail iron crucible w ith 8 g. of a. m ixture of equal
B r itis h C h e m ic a l A b s tr a c ts —B .
Op. II .—F u e l,; G a s; T a b ; J Iin k k a l O ils. 41
parts of sodium carbonate and potassium perm anganate, and the whole covered w ith a further 2-—3 g. of the m ixture. The crucible is very carefully heated to redness and m aintained there for ^ hr. A fter cooling, the crucible contents are extracted w ith 100—150 c.c. of hot water, containing a small am o u n t of sodium carbon
ate, until free from sulphate. The filtrate is then pre
cipitated with barium chloride after making slightly acid w ith hydrochloric acid. I n the case of coals very rich in sulphur only \ g. of coal is taken. F. J. De n t.
L aboratory m eth o d s o f te stin g the ash of solid fu els w ith regard to its ch em ica l a ctiv ity tow ard s refra cto rie s. N. G. Pa c u k o v (Izvestia Thermo-Tech.
In st., 1928, No. 5, 18—28).—A discussion of recent work on this subject, m ainly by the U.S. Bureau of Mines.
T. H. Po p e. R elative in fla m m a b ility and ex p lo sib ility of coal d u sts. T. N. Ma so n and R. V. Wh e e l e r (Safety in Mines Res. Bd., 1928, Paper No. 48, 13 pp.).—The results of experiments on a larger scale th an those de
scribed in Paper No. 33 (B., 1927, 434) are given. E xplo
sions were produced in a gallery 7 i ft. diam. and 720 ft.
long. The relative “ inflam m ability ” was measured by the mean speed of the flames over a given distance, and the relative “ explosibility ” by the maximum pressure developed. I t is shown th a t the orders of inflammability and explosibility are approxim ately the same and in close agreem ent w ith the order of inflamm
ability as determ ined for the same coals from the proportions of incombustible d u st required to suppress inflammation, as previously described (loc. ch.). The inflammability of a coal dust is directly proportional to its volatile m atte r content. Exceptions to this pro
portionality are coals containing a large am ount of resinous m atter, dusts of which arc more inflammable th an is indicated by their volatile m atter content. In general, volatile m atter determ inations serve as a useful guide to the degree of inflammability of a coal
dust. C. B. Ma r s o n.
Ign ition of firedam p b y the heat of im p a c t of ro c k s. M. J. Bu r g e s s and R . V. Wh e e l e r (Safety in Mines Res. B d ., 1928, Paper No. 46, 25 pp.).—Mixtures of m ethane and air could readily be ignited by the sparks or the heat produced when the edge of a block of rock was pressed against a revolving wheel of the same material. The heated area on the stationary rock appeared to be the direct cause of the ignition. The expenditure of energy required for ignition was com
paratively small. The conditions m ost likely to cause ignition in the mine would appear to be those occurring either when a large mass of rock falls some distance and glides along the sharp edge of another piece, or when a mass of falling roof causes two surfaces to grind against one another under great pressure. No marked differences were observed in the ease of ignition w ith different sandstones, b u t the quart.zitic types appeared to be the more dangerous. A. B . Ma n n i n g.
L ow -tem p eratu re carb on isation of B razilian co a ls. F . W . Fr e is e (Brennstoff-Chem., 1928, 9 , 385—387).—Results of carbonisation tests a t 450° are
r eco rd ed . A . Wi l s o n.
L ow -tem p eratu re carb on isation te sts on Cana
dian b itu m in o u s co a ls. R. A. Str on g (Canada Dept.
Mines Fuel Invest., 1926, 12—33).—The products of distillation of ten bitum inous coals of varying volatile m atter and ash content were collected and examined, carbonisation being carried out by heating 2 kg. of the crushed coal in an annular reto rt immersed in a lead bath at; 600°. The apparatus and m ethod Were described in a previous report (B., 1926, 697). For the coals examined, the yield of ta r (average = 1 3 -5 gals./ton) and gas (3000—4000 cub. ft./to n , calorific value 618—724 B.Th.U ./cub. ft.) was not sufficiently high to w arrant the adoption of low-temperature, in place of high-tempera- ture, carbonisation in view of the poorer handling properties of the cokes. The crude ta r oils contained 10—24% of ta r acids, and approx. 50% of the remainder was unsaturated and soluble in concentrated sulphuric acid. 1-1—2-7 gals./ton of light oil were obtained from the gas, and an average of 7 lb. of ammonium sulphate from the liquor. F. J. De n t.
P rod u ction of illu m in a tin g g a s from lig n ite.
K. Sc h m id t (Gas- u. W asserfach, 1928, 71, 1153— 1161 ; cf. B., 1927, 691).—R etorts designed for carbonising lignite are discussed. The gas so obtained, after removing carbon dioxide and hydrogen sulphide, cannot be used directly for tow n supply because of its high calorific value and density. Methods to overcome this difficulty are : (a) by dilution with hydrogen, (b) by gasifying ta r in steam in a separate apparatus and mixing the gas obtained, after removing the carbon dioxide, w ith the original carbonisation gas, or (c) by the carbonisation of lignite in superheated steam. Processes based on the last-named idea are described. To avoid the initial outlay in adopting the above processes, experiments were made on the carbonisation of briquetted lignite in normal gas-works’ retorts. Lignite carbonised more rapidly th a n bitum inous coal, b u t, especially if the retorts were steamed, the ta r escaped w ithout decom
position, yielding a gas of low calorific value. Thus a mode of operation is suggested wherein a setting of retorts is divided into three groups ; steam, superheated in the first, is passed through the lignite, being carbonised in the second, and the gas produced is passed through hot coke in the th ird group to crack the ta r vapours and diminish the carbon dioxide content.
F. J. De n t. P roduction o f illu m in a tin g g a s from lig n ite . A. Sa n d e r (Gas- u. Wasserfach, 1928, 71, 1181—1185 ; cf. preceding abstract).—The carbon dioxide and hydrogen sulphide contents of the gas from lignite, carbonised by the low-temperature process of the Kohlen- veredlung A.-G., are reduced from 34 to 6-7% and from 3-9 to 0-08% , respectively, by washing with w ater under 13 atm . pressure a t 15°, while the net calorific value is increased from 5000 to 6200 kg.-cal./m .3 and a yield of 65% by vol. of the crude gas is obtained.
The cost of the purification process could be reduced by the form ation of sulphur as a by-product from the waste hydrogen sulphide. The hydrogen content of the purified gas could be raised and th a t of the m ethane and heavy hydrocarbons diminished, thereby facilitating its combustion in normal burners and decreasing its density
B r itis h C h em ica l A b s tr a c ts —B .
42 Cl. II.—Fu e l; Ga s; Ta b; Mineral Oils.
and calorific value, by the addition of (a) ordinary coal gas or (6) electrolytic hydrogen, or by subjecting p a rt of the gas to cracking by passage over coke a t 900—1000°, b u t dilution with water-gas is unsatisfactory. The high-pressure distribution over long distances of a tow n’s gas thus produced is discussed. A. Wil s o n.
F orm ation of products rich in su lp h u r b y the action of sulphur d ioxid e on carbon. F . Fisc h e r
and A. Pr a n s c h k e (Brennstoff-Chem., 1928, 9 , 361—
363).—By the passage of sulphur dioxide over semi- coke or over carbon (from carbon m onoxide; cf. B., 1928, 146) a t 500° or by carbonising filter paper or wood in a current of the gas a t the same tem perature, products were obtained containing up to 37 • 5% S, about 60% C, and <[1% H. A t the same tim e some free sulphur was deposited on the cooler parts of the tube. Although no means could be found of proving th a t the sulphur had combined chemically w ith the carbon, yet it could n ot be separated from the la tte r by extraction with solvents, so th a t the assumption of physical adsorption, a t least of the usual type, also failed to account for the formation of these products. A. B. Ma n n in g.
P eat b itu m en . G. St a d n ik o v and N. Tito v
(Brennstoff-Chem., 1928, 9 , 357—358).—Russian peats contain up to 24% of bitumen, extractable by means of a m ixture of benzene and alcohol. The bitum en consists of a m ixture of free acids, saponifiable esters, saturated and unsaturatcd compounds. By treatm ent with solvents it can be separated into two fractions, (a) yellow or brown crystalline waxes, soluble in light petroleum, and (6) black, non-crystalline resins, soluble in benzene b u t not in light petroleum. On heating the bitum en a t 180° some polymerisation of the resins takes place with the form ation of substances which are insoluble even in carbon disulpliide. Comparison of the results of the low-temperature carbonisation of the original peat, the bitum en, and the peat freed from bitum en shows th a t in carbonising the peat the decom
position of the bitum en and th a t of the residue proceed independently of each other. A. B. Ma n n i n g.
D ehydration of b itu m en em u lsio n from A lberta b itu m in ou s sa n d s. P . V. Ro s e w a r n e and G. P.
Co n n e l l (Canada D ept. Mines Fuel Invest., 1926, 96—103).—Small and large laboratory-scale experi
m ents made on a barrel sample of “ separated ” bitum en, containing 28% by wt. of w ater in the form of a stubborn emulsion and 4 -3% by wt. of mineral m atter, have been found satisfactory. The m ethod in each case con
sisted in causing the emulsion to flow on to a h o t surface in an enclosed space sufficiently large to allow the bitum en to foam w ithout overflowing. Initially, the hot surface was provided by the bottom of a heated pyrex glass flask in the small-scale experiments and by molten lead in the work on a larger scale, b u t after dehydration the liquid bitum en itself constituted the hot surface for the incoming wet m aterial. The apparatus employed for the interm ittently operated small-scale process and also for the large-scale work, either interm itten t or continuous in operation, is described, and data are given from typical runs when these processes were employed. The method of proced-
ure should prove suitable for the dehydration of oil—
w ater emulsions in general. A. Wil s o n. D eterm in ation of the p enetration of a sp h a lts.
E. Gr a e f e (Petroleum, 1928, 2 4 , 1599—1603).—
The design and application of a num ber of penetro
meters are described, and results obtained for asphalts of different classes are tabulated together w ith figures for other physical and chemical properties.
R . H . Gr i f f i t h. T h eo ry of the form ation of p e tr o le u m . I l l . C om p o sitio n of the lo w -tem p era tu re ta r fro m C hacha- reisk i boghead coal. G. St a d n ik o v and N. Pr o s- k u r n in a (Brennstoff-Chem., 1928, 9 , 358—361 ; cf. B., 1928, 700, 735, 882).—The ta r was steam -distilled, and from the non-volatile portion the “ asphaltenes ” (0-31% of the tar) and the paraffin wax (13-3% ) were separated. B oth portions were then freed from their acidic and basic constituents and were fractionated.
The fractions, which contained 3-5—6% of oxygen and consisted largely of u n saturated compounds, yielded, on oxidation by potassium perm anganate, products which consisted principally of monobasic acids of the aliphatic series. The hypothesis previously p u t forward, th a t the boghead coals consist of the polymerised fats, waxes, and fa tty acids of algae, is thus further confirmed.
A. B. Ma n n i n g. A n im al and v eg eta b le fa ts a s parent su b sta n ces of the in active co n stitu en ts o f p etr o leu m . M . A.
Ra k u s in (Petroleum, 1928, 2 4 , 1519—1520).—The work of Zelinski and Lavrovski on the form ation of paraffin hydrocarbons by the action of alum inium chloride on oleic, palm itic, and stearic acids is summarised (cf. A.,
1928, 731). A. B. Ma n n i n g.
Canadian sh ale o il, and b itu m en from b itu m in o u s sa n d s, a s so u rces of g a so lin e and fuel o il b y p r e s su re crack in g. R . E . Gil m o r e, P . V . Ro s e w a r n e, and A. A. Sw in n e r t o n(Canada D ept. Mines Fuel Invest., 1926, 121—132).—Shale oil (d 0-896, b.p. range 65—
362°), obtained by the destructive distillation of New Brunswick oil shale, was subm itted, after “ topping ’,’
by ordinary distillation to remove the “ blending n ap h th a,” to cracking tests a t different pressures by the Dubbs residuum and non-residuum processes. Lower gasoline yields w ith higher yields of b etter quality residue oils were given by the former process, whilst the results from the la tte r were in close agreem ent w ith those obtained when the same crude shale oil underw ent pressure-cracking by the Cross process. Bitum en, obtained from A lberta bitum inous sands and containing 28-8% of w ater and 4% of m ineral m atter by w t., was dehydrated and “ to p p e d ” and the product (d 1-061) was distilled in a fire still. The resulting gas oil (equiva
lent to 67 • 3% of the dehydrated and “ topped ” bitum en) was then cracked a t 468° and under 700 lb. pressure by the Cross process. The yields of gasoline and fuel oil, from bo th “ topping ” and cracking, am ounted to over 80% by vol. of the crude shale oil and to about 60% by vol. of the bitum en (water-free basis), whilst gasoline yields of 60—65% of the shale oil, approx.
equivalent to 18—20 Im p. gals./ton (2000 lb.) of shale retorted, and of nearly 40% of the bitum en were obtained.
B r it is h C h e m ic a l A b s tr a c ts —B .
Cl. I I . — Fu e l ; Gas ; Ta r ; Mi n e r a l: Oi l s. 43
Other products were a good quality coke and an uncon
densed gas of high calorific value. A fter refining, the gasoline, from both shale oil and bitum en, was of good q u a lity ; th a t from bitum en also possessed excellent anti-detonating properties. A. Wil s o n.
P ritch ard p ro ce ss for d istilla tio n of o il sh a le.
R. E. Gilm or e and A. A. Sw in n e r t o n (Canada Dept.
Mines Fuel Invest., 1926, 106—120).—This process, prim arily designed for the distillation of wood (cf.
B.P. 18,576 of 1914 ; B., 1915, 949), employs recircula
tion of uncondensed gases through the charge to facilitate the removal of decomposition products. L aboratory distillation of New Brunswick shale gave an oil yield of 35 gals./ton (2000 lb.). In th e large-scale tests on charges of 1500 lb., oil commenced to distil a t 400°, and the tem perature exceeded 430° only tow ards the end of the process. The yield of oil in the first two tests was 21 gals./ton, the low value being ascribed to cracking of ta r fog reintroduced into the retort, producing gaseous hydrocarbons. The oil yield in the th ird te st was increased to 29 gals./ton by reducing th e rate of circu
lation, by fitting more efficient condensers and scrubbers, and preventing the ingoing gas from coming into contact w ith the sides of the retort. The quality of the oil was n o t superior to the product of ordinary distillation processes. The q u an tity of heat required to preheat the circulating gases was excessive. A. Ke y.
D eton ation of m o to r fu e ls. N. A. Bu t k o v (Izvestia Thermo-Tech. In st.,1928, No. 1,9—10).—The oxi disability of «-heptane, toluene, and Grozny aviation petrol was determ ined b y heating 1 g. of the liquid in a 500 c.c.
bomb charged w ith oxygen under 3 atm . pressure in a b ath a t 230° for a definite tim e (1,2, or 3 hrs.), the bomb being afterw ards allowed to cool and the percentages of carbon monoxide and dioxide in the gas determined.
The results obtained showT th a t the tendency of a m otor fuel to knocking is conditioned b y its slight resistance to oxidation. The oxidisability of Ji-heptane is retarded by addition of 2% of (3-naphthylamine and, to a greater extent, by 2% of aniline, and aviation petrol containing 30% of toluene is considerably less oxidisable th an the petrol alone. The above te st is suggested as a means of obtaining an indication of the knocking properties
of m otor fuels. T. II. Po p e.
C ap illarity of lu b ricatin g o ils . N. A. Bu t k o v
(Izvestia Thermo-Tech. In st., 1928, No. 5, 29— 31).—
The theory of the action of lubricating oils is discussed, and the values of the lim iting angle for various oils are calculated from m easurem ents of the surface tension and the force of adhesion. Purification of " nigrol ” and of a transform er oil by treatm en t w ith sulphuric acid removes valuable lubricating substances. The value of the limiting angle for medicinal oil is appreciably dim in
ished by small adm ixtures of vegetable oils.
T. II. Po p e. U tilisa tio n of m a rin e -a n im a l o ils in [internal- c om b u stion ] m o to r s. H. Ma r c e l e t (Chim. et Ind., 1928, 20, 829—836).—The following constants were determ ined for a large num ber of whale, seal, and fish oils : calorific value, tem perature of inflam m ability and com bustibility, d, and viscosities a t various tem peratures.
Considerable variations occurred in the calorific values
found, some oils, especially those containing squalene, approaching gas oil in value. The lowest ignition point observed was 175°, the m ajority being above 200°.
Viscosities a t 25° were very variable, b u t a t 50° were usually below 4° Engler. I t is considered th a t on the whole the figures indicate greater suitability for Diesel engines th a n with vegetable oils. Trials in Diesel motors showed only m inor difficulties due to the rath er high viscosities of the oils. I t is concluded th a t there is a prospect of these oils being economically used for such purposes in certain French colonies. C. Ir w i n.
[M ech an ism of] co m b u stio n in in tern al-com b u s- tio n m o to r s . A. Gr e b e l(Chim. et Ind., 1928,20,813—
818).—I t is pointed out th a t the combustion of hydro
carbons is essentially a chemical problem, and physical calculations based on the assum ption th a t combustion is complete to carbon dioxide and w ater vapour are inaccurate. The gas m ixture in the cylinder is not homogeneous, and its composition does not correspond with chemical equilibrium. The evidence of combustion by stages (to aldehydes, acids, carbon monoxide, etc.) in the presence of insufficient oxygen is summarised.
The beneficial effects of the presence of gases of combus
tion (carbon dioxide and w ater vapour) in promoting ignition or rath er precombustion are explained by hypo
thetical equations. Methyl alcohol, unlike hydrocar
bons, cannot undergo precombustion, being decom
posed under cylinder conditions directly into carbon monoxide and hydrogen. The speed of revolution of the engine is necessarily lim ited by th a t of flame propagation. A carburettor is referred to in which the heat of exhaust gases is used to effect precom
bustion with prim ary air and catalysts. The simple composition of the resultant explosive m ixture is an advantage in engine design. C. Ir w i n.
See also A ., Dec., 1317, C harcoal a s an ad sorb en t ( Du b i n i n). A d sorp tive p ow er of certain ad sorb en ts (Al e k s e e v s k i). 1331, G aseou s ex p lo sio n ra tes at con stan t p ressu r e (St e v e n s). P rop agation of fla m e in g a seo u s m ix tu r e s ( Pa y m a n). G aseou s e x p lo sio n s (Hu n n and Br o w n). 1336, P o iso n in g of iron c a ta ly st in d e co m p o sitio n of carbon m o n o x id e (Wa t a n a b e). 1341, C rystallin e carbon w ith high a d sorp tive p ow er (I Io e m a n n) .
U tilisa b le n atu ral en erg y . Ba r j o t.—See I . P u rification of p h en o ls. Br u c k n e r. N aphthene- su lp h on ic a c id s, v o n Pil a t and Da w id s o n.—See III.
Pa t e n t s.
T reatin g and fo rm in g a rtificia l fu el. H. E.
We t h e r b e e, Assr. to R. F . Gr a n t and H . M. Ha n n a
(U.S.P. 1,687,815, 16.10.28. Appl., 13.4.26).—The finely-divided fuel, before being coalesced, is subjected, in a moistened condition, to the action of a filming carrier and a binding m aterial, in such a way th a t the la tter is evenly applied to the fuel particles.
A . B . Ma n n i n g. T rea tm en t [d e-w aterin g] of p eat. F. Gin s b a c h, Assr. to H . Ho r s t (U.S.P. 1,686,807, 9.10.28. Appl., 23.4.27. Luxembourg, 30.4.26).—Raw p eat is de
watered in stages by mixing and compressing it with
B r itis h C h em ica l A b s tr a c ts —JB.
44 Cl. II .— Fu f.l; Ga s; Ta r; Mi n e r a l Oi l s.
p eat partially dehydrated by -compression, and then mixing the product with dry peat and again compressing.
W. G . Ca r e y. D istilla tio n of so lid fu els. M. Ku l zin sk i (B.P.
278,740, 7.10.27. Esthonia, 7.10.26).—The fuel is con
veyed in a layer through a furnace wherein a gaseous heating medium is circulated in such a way th a t it passes transversely through the layer of fuel, and then, together w ith the products of distillation, is reheated by any suitable means and recirculated. A t the same tim e a general movement of the vapours and gases is m aintained along the furnace, and a t a suitable point they are drawn off and passed to a condensing system.
A. B. Ma n n i n g. D ry d istilla tio n of s h a le s, brow n coal, etc.
Pa t e n t a k t ie b o l a g e t Gr o n d a l- Ra m e n (B.P. 278,694, 24.9.27. Swed., 7.10.26).—An apparatus for the distil
lation of highly bitum inous shales etc. consists of a tunnel oven containing a series of travelling perforated grates which can be charged with a layer of the m aterial.
Below the grates lie the heating elements formed of vertical tubes heated by the combustion gases from suitably placed fireplaces. The oven is divided into several chambers by partitions which end a little above the upper edge of the grate and a little below the lower edge of the heating elements ; a t the top of these chambers are fans which draw the distillation gases through the m aterial on the grate, pass them down to the heating elements through channels in the oven walls, and so recirculate the heated gases through the m aterial.
In order to m aintain sufficient steam within the oven to prevent sticking of the material, p a rt of the gas escap
ing from the distilling chamber m ay be returned thereto after the removal of the bulk of its oil, b u t none of its steam, by cooling i t to 100°. A. B. Ma n n i n g.
H eating of fin ely-p u lverised coal. Tr e n t Pr o c e ss Co r p., Assees. of W. E. Tr e n t (B.P. 291,062, 12.9.27.
U.S., 25.10.26).—Coal, sufficiently finely pulverised th a t it flows like a liquid, is preheated a t 300—350° and passed into a carbonising reto rt in which it travels down through narrow vertical pipes, up between them, down again through an annular space surrounding the pipes, and finally up to an outlet in the side of the retort. Under these conditions the exothermic re
action which is initiated by the preheating produces sufficient heat to complete the carbonisation of the powdered coal. The volatile products of carbonisation are discharged through outlets near the top of the
retort. A. B. Ma n n i n g.
R etorts for the d istilla tio n of solid carbonaceous su b sta n ces. Lo w-Te m p e r a t o h e Ca r b o n is a t io n, Lt d., and C. H. Pa r k e r (B.P. 299,795, 27.4.27).—A retort Setting, specially applicable to vertical retorts of oblong cross-section, comprises two parallel series of retorts and combustion chambers w ith a series of recuperator chambers lying between them. The heating gases pass from the combustion chambers, down through the corresponding recuperator chambers, and thence to the chimney. The recuperators, which are used for pre
heating the air for combustion, are formed by sets of vertical pipes connected in series. A. B. Ma n n i n g.
A pparatus for d istillin g com b u stib le m a teria ls.
O. Hu b m a n n, Assr. to Me t a l l b a n ku. Me t a l l u r g is c h e Ge s. A.-G. (U.S.P. 1,690,934— 5, 6.11.28. Appl., [a] 12.7.26, [b] 7.12.26. Ger., [a] 23.10.24, [b] 18.12.25).—
(a) The m aterial is fed into a shaft-like still, in which it is distilled in a current of hot gases introduced centrally about mid-way down the shaft. Below the inlet for the heating gases is a second inlet for cooling gases.
Gas outlets arc providecl near the top of the shaft and also in the side walls a t about the level of the cooling gas inlets, (b) High-ash, solid, carbonaceous m aterial is passed continuously down through a re to rt in which it passes successively through a distillation zone, a reaction zone, and a residue-cooling zone. Gases free from oxygen are introduced into the cooling zone, and gases containing oxygen into the reaction zone. The hot gases issuing from both these zones are mixed and passed through the distillation zone, thereby effecting carbonisa
tion of the charge. A. B. Ma n n i n g. R egen erative channel oven. H . Ko p p e r s, Assr. to Ko p p e r s De v e l o p m e n t Co r p. (U.S.P. 1,687,774,16.10.28.
Appl., 6.7.21. Renewed 25.6.27. Ger., 13.9.18).—
The heating channels, which lie parallel to o.ie another, are divided by a partition, and the oven is so arranged th a t the preheated fuel enters one channel s .lie outlet end and flows counter-current to the m aterial being heated ; the burning fuel then flows round the partition and passes along the second channel in the direction of movement of th e m aterial being heated therein, finally passing from the outlet of th a t channel to the outflowing
regenerators. A. B. Ma n n i n g.
R egen erative coke oven. G. 0 . Wo l t e r s (U.S.P.
1,690,805, 6.11.28. Appl., 10.9.26. Ger., 14.3.25).—
A coke oven w ith vertical flues communicating w ith each other a t their upper ends is provided w ith prim ary air passages connecting the regenerators beneath the coking chambers w ith the bottom s of the flues, and also has secondary air inlet passages passing vertically up between the regenerators and through alternate partitions sep arat
ing the flues, w ith outlets to the combustion chambers a t the upper ends of the partitions. A. B. Ma n n i n g.
P rod u ction of coke. Ch e m. Te c h n. Ge s.m.b.H ., Assees. of S. St e r n b e r g (B.P. 288,264, 19.3.28. Ger., 6.4.27).—A semi-coke is produced by the low-tempera- ture carbonisation of a fuel to which has been added a flux which, although not interacting w ith the ash of the fuel during carbonisation, does so a t th e higher tem peratures reached during the combustion of the coke, producing an ash or clinker of a desired character. The flux added is preferably one which also favourably affects the yield and composition of the tar.
A. B. Ma n n i n g. Coke and its production. U r b a n a C o k e C o r p ., Assees. of S. W. Pa r e and T. E. L a y n g (B .P . 290,575, 14.5.28. U.S., 12.5.27. Cf. Chapman, B ., 1926, 905).—
The crushed coal is passed from a hopper into an inclined rotating drum, m ounted w ithin a heating chamber, its tem perature being thereby raised to a point (about 300°) just- below th a t a t which it becomes plastic. The coal undergoes a preliminary drying in the hopper, in which are pipes traversed by hot waste gases. The preheated coal is discharged from the ro tatin g drum into a travelling car which, in turn, feeds a. b atte ry of vertical retorts.
B r itis h C h e m ic a l A b s tr a c ts —B .
Cl. II.—F u n t,; Gas ; Tab ; Mi n b b a l Oi l s. 45
The latter, each of which is constructed of a single piece of metal, are circular in cross-section and slightly tapered ; they arc heated by gas flames and are m ain
tained a t 700—800°. The exothermic reactions which commcnce immediately after the coal is dropped into the retorts produce a rapid rise of tem perature through
p u t the charge, the coking process being "completed in a few hours. The coke produced is as strong as by-product coke, b u t possesses smaller pores and a much lower ignition tem perature ; its volatile content is approx. 4% , and it forms a smokeless fuel suitable for domestic and other purposes. If desired, the preheating apparatus m ay be used in conjunction w ith an ordinary by-product oven in which the carbonisation is completed.
A . B. Ma n n i n g. A ctivatin g or rev iv ify in g carb on aceou s m a te r ia l.
L. Wic k e n d e nand S. A. W . Ok e l l(B.P. 300,146, 5.7.27).
—The m aterial is . fed continuously into an electric furnace in which it is heated a t 800—900°. The upper electrode of the furnace is adjustable in position, whilst the lower, which is rotatable, is hollow and perforated, and so designed th a t a current of gas or steam can be passed through it into the furnace. The treated m aterial is caoiLi! »jover into a separator and passes thence to a ro tary electric furnace, in which it is subjected to further treatm en t a t about 400° in a current of air or other oxidising gas. A. B. Ma n n i n g.
D estru ctiv e h yd rogen ation of carbonaceous m a te r ia ls. J . Y. Jo h n s o n. From I. G. Fa r b e n i n d. A.-G. (B.P. 300,703, 11.8.27. Cf. te.P. 276,001 ; B., 1929, 8).—A catalyst for use in the hydrogenation of carbonaceous m aterials a t elevated tem peratures and under high pressures contains up to 10% of a m ixture of copper and zinc or cadmium, the rem ainder consisting of boron, aluminium, silicon, vanadium , etc., or their compounds. The hydrogenating gas is used in large excess and preferably in a circulatory system.
A . B. Ma n n i n g. M anufacture of liquid and oth er hydrocarbons and d eriv a tiv es thereof b y th e d estru ctiv e h y d ro gen ation of carbonaceous m a te r ia ls. I. G. Fa r b e n i n d. A.-G. (B.P. 275,663, 8.8.27. Ger., 7.8.26).—The
process is carried ou t a t elevated tem peratures and under pressures of a t least 50 atm ., in the presence of catalysts composed of m etals of the fifth periodic group, or their compounds, together w ith magnesium or its compounds.
A. B. Ma n n i n g. T rea tm en t of b itu m in o u s m a te r ia ls [from the b erg in isa tio n of co a l]. Soc:. In t e r n a t, d e s Com b u s t ib l e s Liq u id e s (F.P. 623,184, 15.10.26. Ger., 8.5. and 11.6.26).—The crude viscous distillate is treated w ith benzene or light petroleum and w ith a small qu an tity of a m ineral acid, whereby th e resinous m atter is coagulated and m ay be separated by filtration. The remaining oils are then separated byfractional distillation or by chemical treatm en t. A. R . Po w e l l.
T r ea tm en t of fu e l-a ir m ix tu r e s for in tern al- co m b u stio n e n g in es. J . Gr i v i n s (B.P. 281,702, 2.12.27. L atvia, 4.12.26).— The fuel-air m ixtures are passed through a centrifugal separator which throws the insufficiently atomised fuel particles into an annular cham ber heated by the exhaust gases. A fter evapora-
tion therein the fuel is re-mixed with the remainder of the fuel-air m ixture. The whole is then mixed thoroughly w ith cold secondary air, cooled in this way until the fuel begins to condense, and then adm itted to the cylinders. A. B. Ma n n i n g.
G as-p rod u cin g ap p aratu s. W . L. S h e p a r d , Assr.
to E. A. Be a l s (U.S.P. 1,689,159, 23.10.28. AppL, 11.6.25).— A gas-generating chamber, arranged for the partial combustion of fuel therein, is fed from a hopper imm ediately above it. A hollow, vertical shaft to which worm-gearing is attached can be rotated w ithin the hopper, the lower end of which can be closed or opened by means of a valve attached to and operated by a stem passing down through the hollow shaft.
A . B. Ma n n i n g. M anufacture of fuel g a s . A. H. Wh it e (U.S.P.
1,689,940, 30.10.28. AppL, 14.1.20).—A gas of calorific value above 200 B.Th.U ./cub. ft. is made by blowing a charge of solid fuel in a generator w ith a gaseous m ixture containing steam and oxygen in such proportions th a t the fuel bed is continuously m aintained a t a suitable te m p e ra tu re ; a t the same tim e enriching materials are introduced into th e hot gases and are allowed to interact with them , out of contact w ith metallic'surfaces, a t tem peratures which fall slowly, so th a t the separation of free carbon from the enriching hydrocarbon is
avoided. A. B. Ma n n i n g.
M anufacture of g a s of high calorific valu e.
R . Dr a w e (F.P. 622,305, 30.9.26).— Bituminous coal is p artly coked in a container above the ordinary gas producer, and the coke is then treated with air and steam in the producer proper. A. R . Po w e l l.
R ecovery of benzene and hydrocarbons from coke-oven g a s . Soc. An o n. Me t a l l u r g. d e Sa m b r e e td e Mo s e l l e, and Ge s. f. Lin d e’s Eis m a s c h in e nA.-G.
(F.P. 623,568, 19.10.26. Ger., 4.8.26).—The gas is compressed and cooled to remove benzene, water, and naphthalene, and the purified gas is then cooled further on the counter-currcnt principle by means of expanded gas which has already been purified, whereby the remaining easily condensible hydrocarbons are deposited.
A . R. Po w e l l. P rod u ction of m ix tu r e s of h yd rogen and carbon m o n o x id e. J . Y. Jo h n s o n. From I. G. Fa r b e n i n d. A.-G. (B.P. 300,328, 24.8.27).—Vaporised hydrocarbons, or gases containing hydrocarbons {e.g., coal gas), are b u rn t with ju st sufficient oxygen a t tem peratures above 1000° (preferably 1250— 1500°) to convert all the carbon into carbon monoxide. The gas is first given an eddying motion by tangential passage into the lower p a rt of a chamber, whence it expands through an annular passage in to the combustion chamber where the oxygen, as such or in adm ixture with air, is introduced under pressure through a series of water- cooled nozzles. The hydrocarbons are all converted into carbon monoxide and a small q u an tity of carbon dioxide ; no carbon is deposited. The admission of oxygen is regulated so as to produce th e required tem perature of combustion ; w ater vapour should be
excluded. P- E. L . Fa r i n a.
Isolation of pure h yd rogen from g a seo u s m ix tu res. J . Y. Jo h n so n. F r o m I. G. Fa r b e n i n d. A.-G.
