BRITISH CHEMICAL ABSTRACTS
B.—A PPLIED CHEM ISTRY
SEPT. 13, 1929.
I.— GENERAL; PLANT; MACHINERY.
R apid d eterm in ation of d ust in air. L . C. McNa ir
and J. F . Hir s t (J.S.C.I., 1929,48,127 t).—The method depends on the retention of the dust in sugar and the subsequent measurem ent in a centrifuge tube.
R eg isterin g m a n o m eter for perm anent control.
R. Gu il l e r y (Rev. Mtt.', 1929, 2 6 , 329—333).—The apparatus is described with reference to photographs and scale plans, w ith full details for which the original must be consulted. A. R. Po w e l l.
Pa t e n t s.
A pparatus for continuous ch em ica l, h eat, or other trea tm en t of m a teria ls. E. Hay w ard (B.P.
314,916, 5.3.28).—In the autoclave with worm conveyor for solid m aterials described in B.P. 295,975 (B., 1928, 814) the worm is n o t provided with a through shaft, but is divided into sections w ith dog-clutch teeth, the sections resting on the bottom of the autoclave tube and driving each other. Only one stuffing box need be provided for the short driving shaft a t one end. Slide valves are described for regulating the admission and outlet of m aterial. B. M. Ve n a b l e s.
O perating in d u strial furnaces and furnaces adapted th ereto. R . Wa r s it z (B.P. 292,146, 14.6.28.
Ger., 15.6.27).—A reverberatory or similar furnace is heated largely by radiation from a mass of gas-freed solid fuel a t one side of the hearth, and streams of air and/or gas are forced through the solid fuel from several directions to m aintain a central zone opposite the work chamber a t a white heat, the solid fuel acting as a surface-combustion agent and also as a combustible.
Above the w hite-hot zone the preheating and removal of volatile m atter take place ; below it th e fuel is con
sumed by the lowermost supply of air, preferably w ith formation of carbon monoxide. After passing over the goods th e gases leave through another mass of solid fuel which also radiates heat to the work chamber and causes th e form ation of water-gas from any w ater vapour present in the products of combustion. The water-gas is reburnt by another supply of air imm ediately after leaving the mass of fuel, and the heat produced utilised in a regenerator or recuperator.
B . M. Ve n a b l e s. P reven tin g form ation of d ep o sits on heat- exch an ge apparatus ex p o sed to hot g a s e s . La b o r-
a t o ir ed e Pe r f e c t. Th e r m iq u e s, Assees. of P . E. J . J.
Co u tu r a u d (B .P . 284,218, 24.1.28. Fr., 24.1.27).—
The fire side of the tubes etc. is painted w ith a m ixture of graphite and a fire-resisting heat-conductive binder such as a soluble silicate. B . M. Ve n a b l e s.
L in in gs for fu rn aces, k iln s, and the lik e. S.
Tr a v is, a n d Ca llo w Roc k Lim e Co., Lt d. (B.P. 314,772, 701
27.3.28).—In a shaft furnace the lining above and below th e zone where com paratively rapid destruction of bricks takes place is in a single thick layer of bricks or blocks, b u t the destructive zone has a double layer, to enable the inner one to be renewed w ithout collapse of the other zones. Sight-holes arc formed in the outer layer in order to determine the condition of the inner
layer. B . M. Ve n a b i.e s.
C ooling d ru m s. W. O. Sch r o d er (B.P. 290,976, 9.5.28. Ger., 21,5.27).—The drum is double-walled, th e cooling agent flowing in the annular space, which is provided w ith obstacles such as chain links, rods w ith collars, vanes, strips, etc. to cause the medium to become agitated w ithout m aterially increasing the resistance to its flow. The inner and outer walls of the drum m ay also have relative rotation w ith the same object.
B . M. Ve n a b l e s. D ryin g apparatus. A. W. F. Ca p p s (B.P. 314,907, 5. and 9.1.28).—The air or other drying medium first passes over the m aterial to be dried (preferably counter- current) in a com partm ent on one side of a heat exchanger and then returns on the other side of the heat exchanger so th a t moisture abstracted from the m aterial is con
densed on the return pass and gives up its laten t h eat to the air in the drying com partm ent. The air is heated initially to sta rt the drying, and also continuously, preferably between the two passes, to make up for losses.
B . M. Ve n a b l e s. D ryer. P. T. Lin d h a r d, Assr. to F. L . Sh id t h & Co.
(U.S.P. 1,718,243, 25.6.29. Appl., 26.1.28).—The m aterial passes downwards through the annular spaces left between two series of superposed conical baffles, the outer series being inverted and truncated. Means are provided to adjust one series vertically w ith respect to the other, and to give them relative m ovem ent horizontally. The drying medium passes through th e m aterial as it works downwards. B . M. Ve n a b l e s.
D ry in g ch am b ers w ith h eatin g floor. Soc. An o n. DE COMJIENTRY, FoURCHAMBAULT & DECAZEVILLE (B.P.
296,440,25.8.28. Fr., 1.9.27).—The combustion cham ber and flues are below th e floor of the drying chamber.
The flues (not less th an two) are arranged sym m etrically about th e longer axis of the chamber and the gas passes from them into the chamber.
B . M. Ve n a b l e s. M anufacture o f fin ely -d istrib u ted or c o llo id a l m ix tu r e s of bodies in solu b le in one another [m e ta ls and o ils]. M. Po l a n y i and S. von Bogdandy (B .P . 286,316, 3.3.28. Ger., 4.3.27).— One substance is vapor
ised or cathodically atomised and brought into contact with th e other, liquid, substance of which th e surface is continually being renewed, preferably by allowing it to
B r itis h C h e m ic a l A b s t r a c t s — B .
70 2 C l. I .— Ge» Kr a l ; Pi,a m t ; Ma c h i n'k r y.
circulate through a centrifugal bowl to the centre of which the atomised or vaporised substance is adm itted.
The process is described as applied to th e production of colloidal suspensions of m etals in oils.
B . M. Ve n a b l e s.
^ F i l t e r e le m e n t. G. J . Lipsco m b (U.S.P. 1,716,786, 11.6.29. Appl., 10.5.28).—A cartridge for a vacuum filter is composed of a num ber of annular filtering elements each comprising a sandwich of a pair of per
forated sheets and a filtering m aterial, the former having projections which embed in th e latter.
B. M. Ve n a b l e s. M ixer. L. Laing (U.S.P. 1,718,745, 25.6.29. Appl.-, 1.6.27).—A receptacle is provided with a vertical central stirring shaft carrying mixing blades which rotate near th e bottom , and a stem near the wall carries a baffle blade which can be adjusted vertically.
B. 31. Ve n a b i.e s. M ixin g foam w ith p la stic m a ter ia ls. E. M.
Rick a r d and J. A. Ric e, Assrs. to Bubbuestone Co.
(U.S.P. 1,716,932, 11.6.29. Appl., 26.10.26).—A num ber of helical agitators are arranged on a rotating shaft w ithin a container. At any point of th e shaft there are two helices of different diameter and opposite hand, and a t intervals along th e shaft th e hand reverses, i.e., an inner helix is th e same hand as th e outer one next along the shaft. B . M. Ve n a b l e s.
V acuum d istilla tio n . C. R . Bur c h, F. E . Ba n c r o f t, and Asso c ia te d El e c t r ic a l In d u s t r ie s, Lt d. (B.P.
315,186,19.7.28).—In a high-vacuum distilling apparatus as described in B.P. 303,078 (B., 1929, 269) th e evapora
tion takes place from heated tray s which arc nested to form their own baffle (there is an extra heated baffle a t th e top) so th a t drops of distilland have no opportunity of reaching th e condensing surface, which is the walls of the vessel. The distillate vapour leaves the edges of th e tray s in an upw ard direction, which assists th e complete evacuation of th e lower p art of th e chamber.
[Stat. ref.] B . M. Ve n a b l e s. k F ractionating co lu m n . R . E . Wil s o n, R . D . Hu n n e m a n, W . H . Ba iil k e, and F. M. Rog er s, Assrs.
to Sta n d a rd Oi l Co. (U.S.P. 1,716,939, 11.6.29. Appl., 31.1.25).— A tower is provided with internal angle rings to support th e fractionating plates and w ith openings in the shell to insert th e plates, which arc in sections and bolted together through downwardly depending flanges. B . M. Ve n a b l e s.
D eodorisation o r like treatm en t of fum es and g a se s. J. W. Ve r n o n (B.P. 314,187, 16.5.28).— Gases, such as those evolved in th e production of artificial silk, containing hydrogen sulphide or other sulphur compounds, are treated w ith sulphuric acid of con
centration not less th a n 82%, preferably in th e form of a mist or spray. The gases m ay first be washed with w ater a t 95°, and subsequently treated with th e acid, which may either be cold or m ay also be heated to 80—95°. After removal of th e sulphur by filtration th e acid is concentrated if necessary and returned for further use. Coal gases m ay be similarly treated, the u nsaturated hydrocarbons other th a n ethylene being
firs t re m o v e d by s u lp h u ric a c id of lo w er c o n c e n tra tio n
t h a n 82%. A. B. Ma n n in g. J
W ashing of g a se s and vap ou rs. I. G. Fa r b e n in d. A.-G. (B.P. 293,003, 26.6.28. Ger., 29.6.27).—A wetting agent (0-1—0-2% ) is added to th e aqueous washing
liquor. C. Ho l l in s.
C arrying out exo th erm ic ch em ica l reactions under p ressu re and at a h ig h tem p era tu re. L ’Air
Liq u id e Soc. Anon, po u r l’Etu d e e t l’Ex p l o it. des
Pro c. G. Cla u d e, Assees. of Soc. Ch im. d e la Grande
Pa r o isse (Azotee t Pro d. Ciii m.) (B.P. 305.534, 23.1.29.
Fr., 6.6.28).—In th e apparatus described in B.P. 268,721 (B., 1927, 688) th e gases after having served as a heat- protecting screen to th e pressure-resisting wall are brought out of th e apparatus and further heated before returning to th e reaction zone. The application of the invention to ammonia synthesis is claimed.
B . M. Ve n a b l e s.
L aboratory apparatus for h eatin g or evaporating liq u id s. H. J. S. Sa n d, and Br o w n & Son (Alembic
Wo r k s), Lt d. (B .P . 314,923, 2.4.28).—A still, water oven, or similar laboratory apparatus is made in two parts so th a t th e lower heated p a rt (water bath) m ay be easily cleaned or repaired. The upper rim of th e lower p a rt is in th e form of a channel w ith m outh upwards, and the lower edge of th e upper p a rt is inserted into this.
The channel forms a w ater seal k ep t replenished by condensate running down from th e upper p art. The outer wall of th e channel is higher th a n th e inner, so th a t excess condensate runs back to th e w ater bath.
B. M. Ve n a b l e s.
F ir e -e x tin g u ish in g co m p o u n d . Cla yto n In s t a l l a
t io n s, Lt d., and J . E. ILvckford(B.P. 315,123,10.8.28).
—A m ixture of sodium sulphite or m etabisulpliite with sodium bicarbonate, in about equal proportions, is added to an acid solution containing, e.g., 10% of alum and 1% of sulphuric acid, with a foaming agent.
H . Roy al-Daw so n. C rushing or p u lverisin g m a ch in e. W . R . Hume
(U.S.P. 1,719,549, 2.7.29. Appl., 18.7.27. Austral., 9.10.26).—See B.P. 289,721; B„ 1928, 506.
F ilterin g or lik e device. H . A. Th o m pso n, Assr. to Sw in n e y B ro s., Lt d. (U.S.P. 1,719,346, 2.7.29. Appl., 12.1.29. U .K ., 26.10.28).—See B.P. 308,166; B„
1929, 499.
A bsorption refrigeratin g m a c h in e s. Su l zer
Fr e r e s Soc. An o n. (B.P. 295,371, 14.5.28. Switz., 11.8.27).
B earin gs for sp in d les of cen trifu gal sep arators.
Ak t ie b o l a g e t Se p a r a t o r (B.P. 299,977, 24.10.28.
Swed., 3.11.27).
D riv in g m ea n s for m ix in g or s im ila r apparatus for liq u id s. M. H. Ca r p m a e l. F rom Sn ia-Viscosa
(B.P. 315,164, 24.10.28).
S ep aration of d u st from boiler flue g a se s. J . T.
Baronand J . B . Cla r k e (B .P . 314,886, 30.3.28).
S eparating liq u id s (U.S.P. 1,716,957).—See III.
L eaching so lid m a te ria ls (B.P. 301,306).—See VII.
M elting fin ely-d ivid ed m a te ria ls (B.P. 297,813).—
See X.
Cl. I I .— Fu el ; Gas ; Tar ; Min e r a l Oil s. B r itis h C h e m ic a l A b s t r a c t s — B .
703
II.— F U E L ; G A S ; T A R ; MINERAL OILS.
R elation b etw een bitu m en content, caking pow er, and stru ctu re of b itu m in ou s coals. W. Mu i i l s t e p h
(Brennstoff-Chem., 1929, 10, 241—247).—A number of coals have been subm itted to the Bochum crucible test, and their caking indices (Kattwinkel, B., 1926, 257) and oily and solid bitumen contents (Fischer, B., 1925, 233) have been determined. Each method of examination revealed differences between the coals, bu t no definite relationship between the different series of results could be recognised. I t was, for example, impossible to relate the caking index of a coal or of a blend of a coal with a non-caking material with its bitumen content. Other factors, the mode of action of which could not be determined by the methods employed, play an im portant p art in the coking process.
The coals have also been separated into fractions of increasing sp. gr., and these examined separately.
In general the caking power of the coal fell off with a decrease in the proportion of the lightest constituents.
There were, however, exceptions to this rule, due prin
cipally to the different caking power of these constituents in different coals. Extraction of coal with benzene brought about a very considerable decrease in the proportion of lighter co n stitu en ts; the fraction of d <" 1-28 alm ost completely disappeared. Oxidation of the coal a t 120° had the same effect, b u t to a small degree, and also decreased the am ount of benzene- soluble bitumens. Owing to the varying ash content of “ dull ” coal, an accurate separation of “ bright ” coal, “ dull ” coal, and fusain on the basis of sp. gr.
differences was not possible. The influence of the various factors which have been investigated on the coking process is discussed. A. B. Ma n n i n g.
Evaluation of bitu m in ou s coals for g a s w orks from th eir a n a ly ses. R . M ezger (Brennstoff-Chem., 1929, 1 0 , 237—241).—Proxim ate and ultim ate analyses and determ inations of the calorific value m ust be supple
mented by other data in order to assess accurately the value of a coal for gas production. Large-scale experi- -mental retorts have the disadvantage of high initial cost as well as th e large quantity of coal and the length
•of time necessary for a test. Laboratory methods of assaying coal for gas-works purposes arc divisible into two classes, (a) those in which all the products of carbonisation are separately determined, and (b) those in which only the volume and calorific value of the gas and the yields of coke and ta r are determined. Of the former th a t due to Schlapfer (Monats-Bull. Schweiz. Ver.
Gas- Wasserf., 1929, 1, 5 ; 2, 47), and of the latter
•that due to Geipert (B., 1926, 938), are recommended.
A. B. Ma n n i n g.
D eterm in ation s of ign ition points of cok es.
G. Ag d e and M . Sc h n i t t s p a h n (Brennstoff-Chem..
1929, 1 0 , 257—261, 282—287; cf. B., 1927, 930).—
A series of cokes have been prepared by carbonising two coals a t tem peratures ranging from 500° to 1100°
and a t two different rates of heating, and determinations have been made of their ignition points, the tem peratures a t which they begin to reduce carbon dioxide (reduction point), and their adsorptive capacities for hydrogen
■and carbon dioxide. The ignition points were deter
mined by passing air a t 15 litres/hr. through 2 c.c. of coke, of 2—3 mm. particle size, in a quartz tube the tem perature of which was raised a t 5°/min. The point a t which th e rise in tem perature of the coke showed a sudden increase was taken as the ignition point. Certain of the cokes produced a t 900—1100° showed no ignition point. This was due to the presence of an insufficient am ount of easily accessible amorphous carbon, as is shown by the observed relationship between the ignition points and the am ounts of gas adsorbed by the cokes, which give a measure of the available amorphous carbon. No difficulties arose in the determ inations of the reduction points, which require the presence of only very small quantities of available amorphous carbon in order to give consistent results. A. B. Ma n n i n g.
Effect of p re-oxid ation on p rim a ry d istilla tio n products of co a l. V I. T h e ta r s. J. T. Do n n e l l y,
C. H. Fo o t t, and J. Re i l l y (J.S.C.I., 1929, 48, 101—
105 t).—Coal in batches varying from 700 to 800 g.
was oxidised a t 190° and th e products of oxidation were collected and determined. Samples of coal were oxidised to varying degrees of oxidation, depending on the
“ to tal oxygen used ” ; th e “ to ta l oxygen used ” was calculated from the weights of carbon dioxide and monoxide and w ater formed, t h u s : “ to ta l oxygen used ” = increase in wt. of coal -f- w t. C 0 2 + wt. CO -f- wt. H 20 . Distillations a t 600° were carried out on the oxidised samples and on untreated coal, th e resulting tars being accurately determined. The ta rs were then compared by a m ethod of selective solvent extraction.
The results show th a t pre-oxidation seriously influences the ta r yield, gradually destroying th e heavier ta r and causing more gas and volatile ta r to be formed.
T ran sform ation of m eth an e or coke-oven gas b y electric d isch a rg es under reduced pressu re.
F . Fi s c h e rand K. Pe t e r s (Brennstoff-Chem., 1929, 1 0 ,
108—113).— By subjecting m ethane to a high-tension electric discharge a t 15—50 mm. pressure it is almost completely converted into acetylene. If undiluted m ethane is used some carbon deposition occurs and the discharge tube is soon short-circuited. I t is pre
ferable therefore to use a diluted gas, e.g., coke-oven gas. W ith th e la tte r (CH4 23-4% , H 2 52-3% ) the optimum yields of acetylene, up to 9-2% in the exit gases, were produced a t 40—50 mm. pressure in a cylindrical tu b e with the electrodes 40—50 cm. apart, using a transform er giving 5—7 kilovolts as a source of potential. The gas was adm itted a t both ends of th e discharge tu b e and withdrawn from the centre, the gas current thereby helping to cool the electrodes and prevent any deposition of carbon thereon . The efficiency of conversion, expressed as kw.-hrs./m.3 of acetylene produced, fell with th e ra te of passage of the gas from 178 a t 58 litres/hr. to 31 a t 367 litres/hr.
A. B. Ma n n i n g.
F orm ation of liquid hydrocarbons from a c e ty l
en e. I. P o ly m erisa tio n of acetylen e. F . Fi s c h e r,
F. Ba n g e r t, and H. Pic h l e r (Brennstoff-Chem., 1929,
1 0 , 279—282).—The passage of acetylene over activated charcoal or silica gel a t 600—700° leads a t first to the formation of hydrogen, m ethane, and carbon. The carbon, which is deposited on th e m aterial used, appears
B r itis h C h e m ic a l A b s t r a c t s — B .
70-t Cl. I I .—Fuel ; Gas ; Tab ; Min er a l Oil s.
to form a suitable condensation catalyst, for the pro
duction of liquid hydrocarbons increases with tim e of passage of the gas until 70% of th e acetylene is converted into liquid products (cf. Zelinski, B., 1924, 242). The ratio of light oil to heavy oil in th e product is approxi
mately 1 : 1 . The light oil (boiling up to 150°) contains no paraffins, 70% of arom atic and 30% of unsaturated hydrocarbons. W ith diluted acetylene, such as can be produced from coke-oven gas (cf. preceding abstract), th e to ta l yield is smaller (40%), although th a t of th e light oil fraction remains about th e same as with the undiluted gas. Addition of carbon dioxide to the gas favours th e form ation of th e lighter oil at the expense of th e heavier. The life of the catalyst is lengthened, and an exhausted catalyst can be re
generated, by th e addition of carbon dioxide to the acetylene. By th e use of acetylene-carbon dioxide m ixtures even with an em pty tube 70% of th e acetylene can be converted into oil. The efficiency of the process is not increased by th e use of lower pressures.
A. B. Ma n n i n g.
D etection of coal-tar pitch in natural and p etrol
eu m asp h alt m ix ed w ith colop h on y. F. J . Ne l l e n- s t e y n and J . C. M. Sa u e r b i e p. (Z. angew. Chem., 1929, 42, 722).—The diazo tests for th e presence of phenols, always present in coal-tar pitch, is unreliable in th e presence of colophony, b u t good results arc obtained by Millon’s reagent. The asphalt m ixture (10 g.) is boiled for 20 min. w ith 25 c.c. of A’-sodium h y d ro x id e ; th e solution is filtered, rendered feebly acid w ith nitric acid, evaporated to 5—10 c.c., and treated w ith 5 c.c. of Millon’s reagent. If coal-tar pitch is present in am ounts exceeding 1% a colour develops after heating for 30 min. on th e water-batli (cf. Chapin, B., 1920, 652 a).
A. 11. Po w e l l.
Wood tar. I. Y. Po s t o v s k i and B. 6 . Pe r e t z
(J. Chem. Ind. Moscow, 1928, 5 , 625— 628).-—The dehydrated ta r (chiefly from pine and aspen wood) contained C 79-95, H 6-23, O 13-82% ; ether dissolved 86%, leaving carbon. The fa tty acids (2-1%) consisted of formic, acetic, propionic, butyric, and valeric acids.
Of the phenols (30% of tar) 20% was liquid. Pyridine (0-1%) was present. Of the neutral substances 5%
(probably naphthylfulvene) was volatile w ith steam, th e remainder being hydroaromatic substances of high mol. w t. The ta r contained 48-8—55% of w ater and 0-1—0-3% of inorganic substances. Its use as fuel is suggested. The calorific values of the crude and heat- dehydrated ta r are 3970 and 7550 g.-cal., respectively.
Ch e m ic a l Ab s t r a c t s."
S ilica gel for the extraction of high-sulph ur oils from crude p etroleu m . G. E. Wo o d w a r d (lug. Eng.
Chem., 1929, 21, 693—695).—The sulphur content of naphtha solutions of Inglewood crude petroleum was reduced 18% and 37% respectively by stirring w ith a commercial silica gel and Holmes gel respectively.
Holmes gel removed most colour. 90% of the adsorbed m aterial was removed from the gel by washing w ith naphtha, then benzene, and finally ether, and the remainder was recovered by treatm ent w ith sodium
hydroxide. D. Wo o d r o f f e.
A n om alies in th e m ea su rem en t of the v isc o sity o f m in era l o ils containing suspended paraffin w a x .
L. Em a n u e l i and E . Da Fa n o (Giorn. Chim. Ind.
Appl., 1929, 11, 261—263).—An extra dense mineral oil (cylinder oil) was found to exhibit viscosity in dis
agreement w ith Poiseuille’s law, abnorm ally high efflux tim es being observed a t the lower pressures.
This behaviour is attrib u ted to the presence of particles of solid paraffin wax in the oil. T. H. Po p e.
U tilisa tio n of natural g a s e s for th e am m onia p r o cess. Li a n d e r. A m m on iacal and sp en t liquors.
Ba i l e y. M anganese carbide. Fi s c h e r and Ba n- g e r t.—See V II. P rotection of lig h t a llo y s b y tars.
Au b e r t and Pi g n o t. C orrosion of m eta ls by benzene. Fu j i o.—See X.
Pa t e n t s.
U tilisa tio n of coal. H . S. Re e d and R . D. La m ie
(U.S.P. 1,696,731, 25.12.28. Appl., 16.10.25).—Coal, e.g., slack, is delivered by a multiple-feed screw to an externally heated, rotating, ball-mill retort, divided into a series of chambers so th a t the coal particles become successively smaller w ith their passage through the retort. The powdered coal is delivered direct to a furnace with prim ary and secondary air, or is briquetted.
R. BKiGrroiAN.
T reatm en t of artificial fu els. H . E . We t h e r b f.e,
Assr. to R. F . Gr a n tand II. M . Ha n n a(U.S.P. 1,696,511, 25.12.28. Appl., 22.10.25).—Carbonaceous particles are agitated in presence of w ater and 1— 2% of oil or other binding m aterial capable of displacing w ater to give an adherent film. The excess of w ater is drained off and fuel particles are briquetted by pressure after, e.g., oxidation of the film of drying oil. R. Brigiit.man.
C om bustion of pulverised fuel and m ea n s there
for. E. W. Gr e e n, G . R . Un t h a n k, and D . Du n n
(B.P. 314,614, 13.4.28).—A stream of pulverised fuel is evenly mixed in a whirl chamber and is then discharged from an annular conduit into the furnace. The stream is directed outwards by a deflector on the end of the central tube, through which a current of air is supplied to eliminate the rarefaction so produced. Streams of air supplied through perforated plates surrounding the central tube mix w ith the deflected stream of fuel, the volumes and velocities of the several air streams being such as to bring about complete combustion of the fuel.
A. B . Ma n n i n g.
P roduction of carbon. T. E w a n , and Im p e r i a l
C h e m . I n d u s t r i e s , L t d . (B.P. 314,163, 19.4.28).—
Carbon monoxide obtained as a by-product in the industrial manufacture of hydrogen from water-gas is used for the production of carbon. After treatm ent of the water-gas w ith steam in the presence of a suit
able catalyst a t 500° the resulting gas m ixture is washed w ith w ater or ammonia liquor to remove carbon dioxide and sulphur compounds, and the residual carbon mon
oxide is absorbed under pressure in an ammoniacal cuprous solution. On releasing the pressure and heating the solution, carbon monoxide free from c a t a l y s t
poisons is produced and is used for the catalytic pro
duction of carbon. The cuprous solution should contain no halogen : an ammoniacal solution of cuprous formate, acetate, or carbonate gives good results.
A . B . Ma n n i n g.
B r itis h C h e m ic a l A b s t r a c t s — jB.
Cl. I I . — Fu e l ; Gas ; Tar ; Min e r a l Oil s, 7 0 6
A ctivation of carbon. J. Dr u c k e r and II. Th i e n e- m a n n, Assr. to I. G. Fa r b e n i n d A.-G. (U.S.P. 1,709,611, 16.4.29. Appl., 25.10.26. Ger., 10.11.25).—Carbon is activated by treatm en t w ith sulphur vapour a t 800—
1000°, until 40—80% of the carbon is converted into carbon disulphide. R. Br ig h t m a n.
M anufacture of activated charcoal. E . F. Sc h e l l e r ( U .S .P . 1,704,765,12.3.29. Appl., 2.5.27. Ger., 3.5.26).—
Carbonaceous m atter is mixed with sodium monoxide and after reaction the mass is heated a t 500—700°.
Of the carbon thus obtained 0-1 g. will produce 60%
decolorisation in 100 c.c. of standard molasses solution.
R . Br i g h t m a n.
C arbonising and burning bitu m in ou s fuel.
Hu m p h r e y s & Gl a s g o w. Lt d., Assees. of J . 31. Bu s b y
and W. I. Ba t t i n ( B .P . 301,796,28.9.28. U.S., 5.12.27).—
The fuel passes down a vertical reto rt on to a travelling grate which carries the carbonised fuel into the com
bustion chamber of a boiler. The lower zone of the column of fuel in the reto rt is interm ittently air-blasted, the blow gases passing through an offtake a t the top of th at zone to the combustion chamber. The fuel in the upper zone of the retort is carbonised by recirculating part of fk ■ gas generated in the reto rt through the lower and upper zones in succession, this operation alternating with the air-blasting periods. The excess coal gas generated is led off and collected. A. B . Ma n n i n g.
Carbonisation of coal and other so lid carbon
aceous su b sta n ces. Co n t i n u o u s Co a l Ca r b o n i s a t io n, Lt d., C. B. Wi n z e r, and R. Ni s b e t (B.P. 314.665, 13.6.28).—Coal is carbonised in narrow ovens, through which it is carried within vertical containers. The latter are divided into two compartments by a central partition, and are constructed of two halves pivotally connected a t their upper ends and provided with latches for locking the two parts together. They are open a t the top, and are charged from hoppers, a pair of which are arranged in series, the lower being of capacity about equal to th a t of each container. The containers are carried on rollers running on girders which extend through th e oven. A t the discharge end of the oven mechanism is provided for swinging the two halves of the container ap art and so discharging the carbonised
fuel. A. B. Ma n n i n g.
D istillation o f so lid carbonaceous m aterial.
C. Po s t e l, Assr. to Am e r. Sh a l e Re d u c t i o nCo. (U.S.P.
1,717,808, 18.6.29. Appl., 11.6.23).—The m aterial is passed continuously through an inclined jacketed cham
ber which is externally heated. The jacket is filled with molten m etal and the chamber is rotated so th a t the metal bath moves continuously past the source of heat, thereby ensuring uniform heating of the material to be distilled. A. B . Ma n n i n g.
In term itten tly operating carbonising ch am b ers.
Wo o d a l l- Du c k h a m (1920), Lt d., and ( Si r) A. McD.
Duckham (B.P. 314,659, 9.6.28).—Each chamber is provided w ith a bottom offtake in addition to the usual top offtake, the former being normally closed by a seal in a lower foul main ; it opens when the pressure m the lower p a rt of the carbonising chamber exceeds a predetermined maximum and closes again when this
pressure has been released. An uptake provided with a by-passed cut-off valve connects th e upper and lower foul mains. Liquor sprays within the uptake m aintain the required level of liquid in the lower main.
A. B. Ma n n i n g.
Vertical retorts for carbonisation of coal and lik e m aterials. E. We s t, and We s t’s Ga s Im p r o v e m e n t
Co., Lt d. (B.P. 314,231, 9.7.28).—The reto rt walls are built up of superposed sections, each comprising (a) a ledge course which projects beyond the retort and serves to support the floor tiles of each combustion chamber, (6) a key course, and (c) chamber tiles extending from the key course to the next ledge course. The sections of each course are grooved and tongued so as to interlock with the courses above and below. The ledge course is designed to overlap the external horizontal joint between th a t course and the chamber tiles below, whilst the horizontal joints above and below the key course are covered by the floor tiles of the combustion chambers.
A. B. Ma n n i n g.
D estru ctive hyd rogen ation of so lid carbonaceous m aterial. A. Ru l e, and Im p e r ia l Ch e m. In d u s t r i e s, Lt d. (B.P. 314,213, 22.6.28).—Coals, lignites, etc., which on hydrogenation under 200 atm. pressure yield viscous products containing a high proportion of solid material, are hydrogenated under pressures of a t least 500 atm . and a t a tem perature of 420°. A suitable oil or ta r may be added as a vehicle. Mobile products are formed having a ratio of to ta l oil to m atter insoluble in benzene of a t least 10:1. Hydrogenation under the conditions mentioned is generally complete in 1 hr.
A. B. Ma n n i n g.
M anufacture of fuel gas and sim ila r com b u stib le g a ses and apparatus therefor. J. Y. Jo h n s o n.
From I. G. Fa r b e n i n d. A.-G. (B.P. 314,239, 18.7.28.
Addn. to B.P. 214,544 ; B., 1924, 549).— In carrying out the process described in the main p aten t the gasify
ing medium (air or steam) is preheated in a device arranged in the shaft of the producer above the fuel bed. The preheater may consist of a num ber of separate hollow members, constructed, e.g., of silicon carbide brick, and open below so th a t the preheated medium impinges directly on the top of the charge.
An am ount of steam and air sufficient to keep the charge of small fuel in motion is introduced through the grate from below. In an alternative arrangem ent a tube preheater is arranged in th e upper p art of the shaft with a solid heat-accum ulator beneath it ; the fuel is then preferably introduced through the latter, and thereby dried and partially gasified. A. B. Ma n n i n g.
A pparatus for th e m anufacture of w ater-g a s.
Tu l l y, So n s, & Co., Lt d., and A. V. To l l y (B.P.
314,601, 4.4.28).—The apparatus comprises a gas producer, a superposed reto rt surrounded by a chequer- work heating jacket (cf. B.P. 271,765 ; B., 1927, 548), and a cyclone dust extractor, the outlet of which is connected to the stack valve. The dust extractor, which is adapted for the recovery of th e sensible heat of the blow gases, serves to superheat the steam for the down run. When p a rt of the water-gas is enriched with oil in the chequerwork jacket the dust extractor serves as a fixing chamber for the oil vapours. A. B. Ma n n i n g.
B r itis h C h e m ic a l A b s t r a c t s — B .
7 0 6 Cl. I I . — Fu e l ; Ga s ; Ta b ; Mi n e r a l Oi l s.
D irect production of am m o n ia . C. Ot to (U.S.P.
1,696,446, 25.12.28. Appl., 15.8.27. Ger., 9.8.26).—
Distillation gases from coal gas-prodticing furnaces pass to a gas cooler, and the condensate is fed partly to the hydraulic main and p artly is used to irrigate and cool the"gases in the pipe leading to the cooler.
R. Br ig h tm a n. Gas purification p rocess. G. E. S eil, Assr. to
Ko p p e r s Co. (U.S.P. 1,701,825,12.2.29. Appl., 26.12.25).
—The hydrogen sulphide is absorbed by an alkaline solution, liberated from it by an air current, and oxidised by means of an aqueous medium containing a bacillus capable of oxidising hydrogen sulphide.
R, Br ig h t m a n.
R egeneration of w ash in g liquids em ployed in rem ovin g carbon d ioxid e and other soluble con stitu en ts from g a se s. K. Go r d o n, and Im p e r ia l Ch e m. In d u s t r i e s, Lt d. (B.P. 314,842, 11.4.28).—
The gases are scrubbed under pressure with water free from oxygen and the dissolved gases are removed by releasing the pressure in stages, or mainly a t ordinary pressure, the final stage being below atmospheric pressure ; the w ater is then returned to the absorption process without aeration. W . G . Ca r e y.
Production" ^of com p ressed g a s. J . T h i e c k e , M i n im a x , A.-G., and H . H e r z o g (B.P. 314,604, 4.4.28).
—Compressed gas for compressed-air brakes, pneu
matic hammers, paint or cement guns, and other industrial uses is produced by burning a m ixture of about 85 pts. of ammonium n itrate and 15 pts. of charcoal in a closed vessel. Owing to th e slow speed of combus
tion a safe and uniform development of pressure is obtained. The m ixture m ay be compressed in the form of a cartridge and have a suitable priming embedded in it. A waterproof coating of shellac is provided.
A. B. Ma n n i n g.
O perating w ith g a ses containing carbon m o n oxide at elevated tem p eratu res. J . Y. Jo h n s o n.
From I . G. Fa r b e n i n d. A.-G. (B.P. 314,129, 30.12.27).—
Apparatus for carrying out processes, e.g., the synthesis of m ethyl alcohol, involving the use of gases contain
ing carbon monoxide a t high tem peratures and pressures is constructed of iron in all parts except those main
tained a t tem peratures between 150° and 250°. These are constructed or coated with materials, e.g., copper, silver, special steels (cf. B.P. 231,285; B., 1925, 425), which do not form metal carbonyls under the working conditions. Carbon monoxide is excluded from the apparatus, and is preferably replaced by hydrogen, while it is being heated up or cooled down.
A. B. Ma n n i n g.
T reatm en t of tarry m atter, heavy hydrocarbon resid u es, and the lik e. A. S . Kn o w l e s, Assr. to
Ta r & Pe t r o l e u m Pr o c e s s Co. ( U .S .P . 1,717,884, 18.6.29. Appl., 12.6.25).—The ta r or other heavy liquid hydrocarbon is sprayed on to a bed of loose material, principally carbon, within a closed chamber heated externally from below. The liquid flows through the bed, in the lower layers of which it becomes coked.
The gases and vapours evolved escape through an outlet in the top of the chamber, whilst the solid residue is removed as coke. A. B. Ma n n i n g.
P urification of tar acid b earin g o ils. S . Ca p l a n.
Assr. to Co m b u s t i o n Ut i l i t i e s Co r p. ( U .S .P . 1,710,764, 30.4.29. Appl., 29.9.24).—The oil is agitated with about 1-5 vols. of 1% aqueous ammonia or other buffer agent a t 50°, separated from the aqueous layer, and.
agitated a t 50° with about 1-5 vols. of water.
R . Br i g h t m a n.
T reatm en t of benzene to e lim in a te corrosive properties. T . R. Tr a i n o r, Assr. to J . A. Ke l l y
(U.S.P. 1,711,367, 30.4.29. Appl., 30.4.27).— The benz
ene is treated successively w ith lime w ater and sodium bicarbonate solution while circulating in a closed system.
R . Br i g h t m a n.
Separation of oils from m ix tu r e s w ith solid su b sta n ces. J . Y. Jo h n s o n. From I. G. Fa r b e n i n d.
A.-G. ( B .P . 314/105, 23.1.28).—Oily residues obtained in the low-temperature carbonisation, cracking, extrac
tion, or destructive hydrogenation of carbonaceous materials are mixed w ith about 30% of a liquid in which th e oil is soluble and with a small q u an tity of a wetting agent, and are centrifuged. Aromatic or hydroaromatic hydrocarbons, ta r oil fractions, etc. m ay be used as the solvent, and alkylated sulphonic acids of aromatic hydrocarbons, fatty acids or their salts, etc. as the wetting agent. I t is sometimes advantageous to work in an alkaline medium. A. B . Ma n n i n g.
P roduction of low b .p . and oth er hydrocarbons and derivatives thereof b y th e d estru ctive hydro
genation of co a ls, o ils, e tc ., and treatm en t of the resid u es. I. G. Fa r b e n i n d. A.-G. ( B . P . 288,148, 28.3.28. Ger., 31.3.27).—The oily residues from hydro
genation processes are treated while still h o t with hot gases or vapours, especially steam, to recover the oils.
The material, for example, may be passed through a pipe by means of a worm conveyor, wdth or counter- current to the hot gases or vapours. The de-oiled resi
dues m ay be carbonised and gasified, th e h o t gases being used in the oil recovery tre a tm e n t; the car
bonised residues m ay be used for the production of activated carbon. The oils recovered m ay be used as a vehicle in the hydrogenation of a further quantity of coal etc. A. B . Ma n n i n g.
Cracking of hyd rocarb on s. G. H. Ta b e r, j u n.,
Assr. to Si n c l a i r Re p i n i n g Co. ( U . S . P . 1,705,077, 12.3.29. Appl., 26.11.27).—The gas-vapour mixture from the cracking operation passes through a fraction
ating tower, vapour from which passes to a condenser and receiver. Vapours from the receiver are scrubbed with a higher-boiling oil fraction from the fractionating column. Vapour from the scrubber passes to the gas
holder, whilst the scrubbing oil is returned to the fractionating column and stripped by th e ascending vapours from th e still. R. Br i g h t m a n.
C racking of h y d ro ca rb o n s. M . J . Tr u m b l e (U.S.P.
1,696,658, 25.12.28. Appl., 2.9.24. Renewed 24.10.28).
— H ydrocarbon oil is cracked under pressure by flowing in a th in film over th e external surface of a furnace flue.
The volatile products escape through a dephlegmator and are condensed. The phlegms, together w ith a relatively large volume of circulating solvent of b.p.
above th e cracking tem perature used, and after settling from carbonaceous m atter, are retu rn ed w ith raw oil
B r itis h C h e m ic a l A b s t r a c t s — B .
Cl. I I I .— Or g a n ic In t e r m e d ia t e s. 707
to the cracking still, th e solvent removing th e residual carbonaceous products from th e flue surface, and carrying them into th e settling chambers.
R . Br i g h t m a n.
D is tilla tio n of s h a le . H. S. Re e d and R . D. La m ie
(U.S.P. 1,696,730, 25.12.28. Appl., 16.10.25).— Oil shale is continuously distilled in a closed ball-mill retort, divided into com partm ents such th a t th e size of the shale particles diminishes successively as th e shale advances through th e retort, until spent shale is discharged from the final chamber as a fine powder.
R. Br i g h t m a n.
M anufacture of paraffin. C. A. Wa r d, Assr. to
St a n d a r d Oi l De v e l o p m e n t Co. (U.S.P. 1,718,672, 25.6.29. Appl., 20.11.25).— Slack-wax, produced by filter-pressing chilled paraffin slop, is distilled to produce a sweat-able wax. J . S. G . Th o m a s.
Production of liquid p o ly m e risa tio n products [fuels] from g a se s containing hydrocarbons.
C. Ep n e r (B.P. 294,100, 8.6.28. Ger., 16.7.27).—
Methane or other hydrocarbon gas [e.g., coke-oven gas) is subjected to the silent electric discharge (e.g., 20,000 volts a t 10,000 cycles) a t such a ra te (2 litres per hr. through an ozoniser 4 cm. diam. X 15 cm.) th a t form ation of lubricating oils is avoided. The methane content of a coke-oven gas falls from 50% to 10%j with production of fuel oils. The gas is preferably preheated to avoid condensation in th e ozoniser. The products m ay w ith advantage be subsequently hydro
genated. C. Ho l l i n s.
A nti-knock fu el. G. Ha m m o n d, Assr. to Fu e l De v e l o p m e n t Co r p. (U.S.P. 1,713,530, 21.5.29. Appl., 15.3.26).—B utyl alcohol together with commercial alcohol, or ethylene glycol and water, is added to
gasoline. R . Br i g h t m a n.
L ubricating o il. K. G. Ma c k e n z i e and R. Ha s k e l l,
Assrs. to Te x a s Co. (U.S.P. 1,705,298, 12.3.29. Appl., 21.8.24).—A nti-chattering properties are im parted to lubricating oil by adding about 2% of oxidised paraffin
u'a X- R. Br i g h t m a n.
O perating m o lle n -sla g g a s producers. H. J. F.
P h i l i p o n , Assr. t o Soc. Anon. “ l ’A i r C h a u d ” (U.S.P.
1,720,290, 9.7.29. Appl., 31.1.23. Belg., 8.3.22).—
See B.P. 194,648 ; B., 1923, 702.
G as purification p ro cess. H. A. Go l l m a r. Assr.
to Ko p p e r s Co. (U.S.P. 1,719,177 and 1,719,762, 2.7.29.
Appl., 7.3.27 and 5.11.26).—See B.P. 280,165 and 286,633 ; B., 1929, 8.
G as purification p ro cess. D. L. Ja c o b s o n, Assr.
to Ko p p e r s Co. (U.S.P. 1,719,180, 2.7.29. Appl., 5.11.26).— See B.P. 286,663 ; B., 1929, 8.
G as a n a ly ser. A. B. Cu n n i n g h a m, Assr. t o Re p u b l ic Fl o w Me t e r s Co. (U.S.P. 1,719,593, 2.7.29. Appl., 19.5.23).—See B.P. 288,510 ; B., 1928, 508.
[A pparatus for] com b u stion of [sm a ll] fuel.
W. R . Sm a l l (B.P. 314,469, 9.8.28).
Liquid fuel oil b u rners. To d d Oi l Bu r n e r s, Lt d.,
and E. Cl a r k ( B .P . 315,056, 21.5.28).
L ow -pressure liquid fuel b u rn ers. S. E . Ma j o r
and E. F. Ba k e r ( B .P . 294,577, 23.7.28. Austral., 26.7.27).
[D ow n-draught] g a s producers [w ith depth tubes], II. C. Re a d i n g ( B . P . 315,090, 4.7.28).
O perating furnaces (B.P. 292,146). D eodorisation of g a se s (B.P. 314,187).—See I. C leaning etc. a g en ts (B.P. 313,861).—See III.
i ll.— ORGANIC INTERMEDIATES.
S yn th etic carbam ide from am m on ia and carbon d ioxid e. G. A. Ya k o v k i n (J. Appl. Chem. Russia, 1928,1, 70—77).-—Carbamide was obtained in 40% yield from liquid ammonia saturated w ith carbon dioxide under pressure, w ithout supercooling, followed by heating a t 160—170° and increasing the pressure to 75—80 atm . Ch e m ic a l Ab s t r a c t s.
T h erm a l reaction s of pure organic su b stan ces under h igh h ydrogen p r e ssu r e s. F. Ho f m a n n and
K. La n g (Brennstoff-Chem., 1929, 10, 203—205).—
A num ber of pure hydrocarbons have been treated with hydrogen a t 400— 500° under pressures of 200—250 atm . Benzene was unchanged except for the production of 1-2—2-3% of diphenyl. Diphenyl itself was tran s
formed to th e extent of over 90% into benzene. W ith a suitable choice of tem perature and tim e of heating, up to 50% of toluene was converted into benzene, the methyl group appearing p artly as m ethane and partly as ethane. Small am ounts of diphenyl, monomethyl- diphenyl, and ditolyl were also formed. In the absence of high-pressure hydrogen, toluene remained stable a t 470°. ci/cZoHexane was unchanged when heated w ith hydrogen a t 460° and 212 atm. pressure. A t a slightly higher tem perature, however, gaseous hydrocarbons and methylce/cZopentane were produced. In the absence of hydrogen, cycZohexane was decomposed a t the lower tem perature. cycZoIIcxene was p artly hydrogenated to cycZohexane and partly converted into polymerisation and other p ro d u c ts; among the la tte r methyl- and dimethyl-cj/cZopentane and dicf/cZohexyl were identified.
Ethylene was almost completely converted into saturated hydrocarbons. Although a t 490° pyridine remained stable in the absence of hydrogen, w ith hydrogen under 240 atm . it yielded 90% of ammonia and gaseous hydro
carbons. In the residual oil, besides unchanged pyridine, nitriles and higher tertiary bases were identified.
A . B. Ma n n i n g.
T h e 7t of sulphonation . C . Co u r t o t(Rev. Gen. Mat.
Col., 1929, 33, 177— 183).—The n of sulphonation is defined by Guyot (B., 1919, 811a) as the lim it of con
centration of sulphur trioxide a t which no further sulphonation of a given organic molecule a t a given tem perature can take place. The quantity of acid, X , containing a % of sulphur tri oxide, required for the monosulphonation of 1 mol. of an organic compound, R H , is given by X = S 0 3 (100 — tt) j (a — n). Before the sulphonic acid can be separated, it is necessary to remove the acid of u concentration by the very incon
venient methods of Jiming o u t or salting out. In order to eliminate the w ater produced during th e reaction, Guyot proposed passing through the sulphonation
