Improvements in the Production of Illuminating Gas from Mineral Oils, and in Apparatus therefor, and for Producing Water Gas.
Year: 1893

page_text: Date of Application, 23rd June, 1893
Complete Specification Left, 24th Mar., 1894-Accepted, 23rd June, 1894
PROVISIONAL SPECIFICATION.
Improvements in the Production of Illuminating Gas from Mineral
Oils, and in Apparatus therefor, and for Producing Water Gas.
I, WILLIAM YOUNG of Priorsford Peebles in the County of Peebles Consulting
Chemist, do hereby declare the nature of this invention to be as follows:-
-
This invention has for its object to still further improve and develop the system
or process of decomposing mineral oils described in the Specification of Letters
Patent granted to the present applicant and Alexander Bell and dated 5th July 1892
No. 12,421 and it comprises improved arrangements of apparatus specially adapted
for the decomposition of crude tar oils which when gasified leave a large quantity
of solid carbon in the retort or decomposing chamber and by which the solid carbon
so deposited can be directly applied to produce by its combustion the heat necessary
to effect the decomposition of the oils and the production of water gas to wash out
the residual oil vapour and if desired increase the volume and reduce the illuminating
power of the resulting rich oil gas.
The modification of the process and the form of apparatus may be considerably
varied but the essential feature of the invention consists in combining a combustion
and gas generating chamber in which the carbon resulting from the decomposition
of the oils is consumed or partially consumed in air and made to heat up a second
chamber or arrangement of chambers in which the oil is decomposed.
A convenient form of apparatus consists of a vertical cylinder built of riveted
boiler plates, and lined with fire bricks. The lower part is provided with fire bars
and clinker door and pipes and valves for the admission of steam and air. There
are built into the upper part of the chamber a number of retorts or decomposing
chambers. These are placed at a slight inclination alternately in the reverse
direction and are connected by chambers or passages to each other so as to form a
continuous incliuation from top to bottom.
These retorts are separated externally from the lower combustion and gas
generating chamber by a fire brick arch but they are in direct internal
communication, an opening passing through the arch from the end of the lower
retort into the combustion and gas generating chamber. The upper end of the
retort opens into the space surrounding the outside of the retorts and here a
secondary supply of air is introduced.
The apparatus at starting is brought up to the necessary temperature by means
of coke or other fuel charged into the combustion and gas generating chamber
kindling and blowing it up by means of a blast of air part passing up through the
ignited coke and part being supplied as secondary air to consume the resulting
carbonic oxide in heating up the external surface of the retorts and sides of the
containing chamber, the waste products passing away by an outlet provided with a
valve.
On a store of heat of the necessary temperature been attained in the combustion
and gas generating chamber and upon the retorts the air is shut off and steam
admitted into and passed up through the incandescent carbon in the generator when
it gets converted into water gas (H and CO) which by passing up through the
retorts and down around them displaces the products of combustion. So soon as
that object is effected the steam is stopped or nearly so and the oil to be decomposed
is allowed to flow or is pumped into the upper inclined retort from which it flows
down the inclined bottom of the successive retorts getting in its passage vaporized
and partially decomposed into permanent gas. The resulting products of
decomposition are drawn off through a pipe sealed in the oil to be subsequently

page_text: decomposed condensed and treated all as described in the Specification of Patent
No. 12,421-1892.
The condensed products and oil to be decomposed are continuously pumped back
into the decomposing retorts at first when the heat is high rapidly and in diminishing
quantities as the stored up heat falls, the oil being altogether stopped before the
heat falls below that required to decompose, the particular oil being gasified and
care being taken that at all times sufficient undecomposed oil accompanies the
products leaving the arrangement to wash back the sooty matters and prevent
pitchy sooty deposits taking place.
On the heat in the decomposing part of the apparatus falling and the oil being
shut off the steam is again turned into the mass of coke still in an incandescent state
and sufficient water gas produced to sweep out of the arrangement the residual oil
gas and vapour and if desired to dilute the rich oil gas previously produced.
By the repeated alternate blowing up with air and combustion of the carbon in
the gas generator and the employment of the resulting stored up heat in decomposing
the oil, the carbon is burned away in the gas generator but the carbon deposited
from the decomposition of the oil as rapidly accumulates in the decomposing retorts
and this carbon is by means of suitable doors raked or pushed down into the gas
generator to take the place of that which has been consumed, and the process is
thus continued by the combustion of the carbon deposited from the oil.
By another modification the combustion and gas generator is surmounted by a
vertical retort or chamber having an annular flue space around it so that its walls
may be heated externally by the combustion of the carbonic oxide from the gas
generator by a secondary supply of air, preheated by the waste products of
combustion.
The combustion and gas generating chamber is also provided with sloping fire
bars and doors so arranged that a portion of the contents of the lower part of the
chamber can be conveniently removed when found desirable.
When starting this modified form of apparatus the combustion and gas generating
chamber as well as a part of the vertical retort are filled with coke which is kindled
and blown up with air, a secondary supply of air entering at the top of the retort
where meeting the carbonic oxide from the combustion of the carbon in the gas
generating chamber it is consumed and descends in the flue space around the retort
heating its walls and the carbon or coke contained in the retort.
As soon as the apparatus and its contents have accumulated a store of heat of the
necessary temperature the air blast is shut off and steam turned into and up through
the incandescent carbon to produce water gas to displace the products of combustion,.
the stack valve is then closed and the steam shut off or at least the supply limited,.
and the oil to be decomposed pumped or run into the top of the vertical retort
entering by the outlet for oil vapours at first when the heat is high fast, slowing as
the heat falls.
The oil falling through the vacant space in the upper part of the vertical retort
drops upon the top of the highly heated coke gets rapidiy vaporized and in part
decomposed by the heat radiated from the walls of the retort the liberated finely
divided carbon and dense hydro carbons falling down upon the surface of the coke,
the gas with a quantity of oil vapours sufficient to prevent pitchy deposits passing
away by the outlet to the seal box to be cooled and treated as already described.
When decomposing mineral oils composed largely of tar such as those produced
from the condensation of blast furnace gases or those obtained from the distillation
of coal in gas works the quantity of carbon deposited is very large amounting to
from eight to fitteen cwts. per ton decomposed. That quantity of carbon is far
in excess of what is required to decompose the tars alone and produce sufficient
water gas to wash out the apparatus as herein described.
Furthermore the deposited carbon cakes together and plugs up the upper portion
of the coke in the vertical retort. In order to prevent this occurring it is necessary
either to utilize the surplus carbon by consuming it to produce water gas or to
periodically remove a part of it from the lower part of the combustion and gas

page_text: generating chamber so as to allow the mass to fall and get broken up leaving a free
way for the passage of the gases.
The apparatus hereinbefore described is applicable for use in the production of
water gas.
Dated this 22nd day of June 1893.
CRUIKSHANK & FAIRWEATHER,
62, St. Vincent Street, Glasgow, Agents.
COMPLETE SPECIFICATION.
Improvements in the Production of Illuminating Gas from Mineral
Oils, and in Apparatus therefor, and for Producing Water Gas.
I, WILLIAM YOUNG of Priorsford, Peebles in the County of Peebles,
Consulting Chemist, do hereby declare the nature of this invention and in what
manner the same is to be performed, to be particularly described and ascertained
in and by the following statement :-
This invention relates to the production of illuminating and heating gases by
that class of processes in which a mass of carbon placed in a cupola arrangement
is fired and blown up by a current of air so as to become highly heated and heat
up a mass of brickwork or other material contained in the cupola or an attached
chamber, thereafter employing the heat so obtained and stored up to produce water
gas and decompose liquid hydrocarbons to carburette the water gas.
By all such processes the major part of the carbon employed to produce the heat
has been obtained from sources outside the hydrocarbon employed and has consisted
of anthracite, gas coke or other carbonaceous substances, and the water gas has been
produced at the same time that the hydrocarbon was decomposed.
Now most liquid hydrocarbons employed for the production of illuminating gas
contain in their constitution a considerable quantity of carbon in excess of what can
be rendered gaseous by destructive distillation, especially is that the case with crude
tarry oils of high specific gravity.
In existing forms of apparatus and as that class of processes are at present
conducted, that excess of carbon has hitherto caused considerable trouble either
from the carbon being deposited upon and closing up the brickwork passages, or
being set free as flocculent carbon which being carried forward in the current of
gases choked up the condensing apparatus rendering the resulting tars thick and
pitchy.
This invention has for its object to overcome those difficulties and it comprises
improved arrangements by which the process of producing gas from liquid hydro-
carbons may be so conducted that the excess of carbon which has hitherto been
source of trouble may be eliminated during the process of decomposition, in such
a form and under such conditions as to be available to produce by its partial
combustion in air the heat necessary to decompose the hydrocarbon fluids and also
to produce water gas sufficient to wash out the apparatus and if desired dilute the
rich hydrocarbon gases.
The accompanying drawings represent four modifications of the apparatus
which I believe will most conveniently and commercially produce the results
aimed at.
Figure 1 is an elevation partly in section showing one modification of the general
arrangement of apparatus,
Figure 2 is a plan corresponding to Figure 1,
Figure 3 is a cross section of the gas producing arrangement,
Figures 4 and 5 are vertical sections at right angles to each other of the
condensing chests.
In these and the other drawings hereinafter referred to the same reference numerals
are used to mark the same or like parts wherever they are repeated.

page_text: The apparatus comprises a vertical cylindrical producer A built of riveted boiler
plates, having in the lower part a combustion and water gas generating chamber B,
the walls of which are built of firebrick and provided with file bars B', ash pit B³
and cleaning and clinkering doors B³. Over the combustion chamber is built,
also of fire brick, a decomposing chamber C in which the vapours of the liquid
hydrocarbons are exposed to the action of radiant heat. The walls of the
decomposing chamber C are perforated with a series of ports and openings D₁
and surrounded by annular spaces or flues C¹ and C' terminating in the stalk C
provided with the valve C. The annular space or flue D between the outer wall
and the wall enclosing the space C is for the admission of a secondary air supply
which enters the bottom of the decomposing chamber C by the openings D². Sight
holes D³ are provided in the sides of the producer to allow of the temperature of
these flues being observed.
The air necessary for the process is supplied from any convenient blowing
arrangement by the pipe E, the primary air for the burning of the carbon
into carbonic oxide gas being supplied through the valve El and pipe E³ to
the ashpit B, and the secondary air to consume the carbonic oxide gas into
carbonic acid gas by the valve E³ and pipe E to the annular heating space in
the flue D.
The steam necessary for the process is supplied through the pipe F and regulating
valve F into the ashpit B2 through the same pipe as the air.
In the top of the producer there is an opening G provided with a door G¹ and
the outlet pipe for the gases G' leading to the seal and wash box G³ connected up
by the pipe G to the condensing arrangement H which consists of the series of
vertical pipes H¹ rising from the main H2 and ascending and descending alternately
from the chests H³ and finally descending into the main H to the outlet pipe H
leading to the gas purifiers.
The store tank K for the supply of the hydrocarbon fluid to be decomposed
is placed at such an elevation that the fluid on its way to be decomposed can
be made to flow through the arrangement of pipes K and valves K through
all or any number of the condenser chests H3 and through the pipes G into
the seal box G³ and overflow by the pipe L into the store cistern M from which
it is drawn and raised by the pump M' through the pipe M' into the cistern N
placed on the top of the producer A. From the bottom of the cistern N the pipe O
provided with the stop cock O¹ is led to the gas outlet pipe G³.
When starting the apparatus the hydrocarbon fluid to be decomposed is charged
from the supply tank K into the various parts of the apparatus so as to seal the
condenser chests H3 and also the main seal box G and overflow into the cistern M
and a supply is pumped into the cistern N on top of producer A.
The combustion and water gas generator B is then charged by the door G¹ with
any convenient kind of carbon preferably anthracite coal, or gas or other description
of coke and kindled, the valve C on the smoke stalk C³ being opened, the primary
blast of air is turned on by opening the valve E admitting the air to the
ashpit B and the fire bars B'. The quantity of coke or other fuel should have
a depth of several feet and on this mass of carbon becoming sufficiently heated to
allow of the kindling of the carbonic oxide gas over its surface, the secondary air
valve E³ is opened and the air admitted through the pipe E and annular air space D
and ports D² into the bottom of the decomposing chamber C and over the surface
of the carbon. The air valves E' and E' are adjusted so that the carbon will be
completely consumed into carbonic acid gas.
The two adjusted blasts of air are kept blowing into the arrangement till the
desired temperature is attained in the mass of carbon in the chamber B and in the
walls of the decomposing chamber C and also the walls of the surrounding annular
flue spaces C and C³.
On the desired temperature being reached, which can be observed by the sight
holes D provided for the purpose in sides of producer and which necessarily
varies dependent upon the nature of the liquid hydrocarbon being employed but

page_text: which is soon ascertained in practice, both air valves are closed and steam admitted
under the fire bars by opening the valve F2. The steam passing up through the
carbon in chamber B becomes decomposed into water gas and the process is
continued till all the air and products of combustion have been entirely displaced
by the water gas. The stalk valve C is then closed and the flow of steam into the
arrangement stopped or at least 30 greatly reduced that only sufficient water gas is
made to prevent the vapours of the liquid hydrocarbons from their high specific
gravity sinking through the mass of heated carbon. The object of lessening or
stopping the production of water gas during the decomposition of the liquid hydro-
carbon is that the presence of the water gas interferes with the decomposition of
hydrocarbon vapour in various ways, particularly when the decomposition is effected
by radiant heat.
The stop cock O' on the pipe O is now opened which admits the hydrocarbon
fluid into the gas outlet pipe G2 flowing down which it drops through the whole
depth of the decomposing chamber C upon the surface of the highly heated coke
in the chamber B where it spreads and is rapidly volatilized and rising in vapour
through the decomposing chamber C it is subjected to the action of the heat from
the walls of the chamber becoming to a considerable degree gasified. The flocculent
carbon and dense hydrocarbon set free or produced during the decomposing process
owing to the slow upward current in the decomposing chamber C to a large extent
keep falling or get entangled in the descending inflowing hydrocarbon liquid and
agglutinate or cake upon the surface of the hot carbon in a hard or solid condition
which will stand the blast of air in blowing up for the next run.
The rate at which the hydrocarbon is allowed to flow into the decomposing
chamber and upon the surface of the heated carbon B is so adjusted that a
considerable quantity of the hydrocarbon will escape as vapour and accompany
that portion that has been completely gasified. To ensure such being the case the
hydrocarbon fluid is run into the arrangement at a greater rate at first when the
temperature of the heat is high, gradually slowing as the temperature falls.
This is automatically accomplished by the greater pressure upon the cistern N
at first when full lessening as it empties, but any other convenient means of
adjusting the flow may be used, the object being that the hydrocarbon vapour
accompanying the gasified portion will in condensing hold in solution any flocculent
carbon that may be present and keep the apparatus free from all obstruction and
enable the flocculent carbon to be returned to the producer to form hard coke for
use there.
The gases and vapours leaving the arrangement by the pipe G enter and pass
through the hydrocarbon liquid in the seal box G³ thence to the condensers H
where they are subjected to the alternate cooling action in the series of vertical
pipes Hand to the washing action of the hydrocarbon liquid contained in the
chests H which are provided with the serrated partition H (shown in Figures 4, 5
and 6) under which the gases are made to bubble and pass through the contained
liquid.
The operation of producing gas by the decomposition of the liquid hydrocarbon
is continued till the heat in the decomposing chamber falls to a temperature so low
that the process of gasifying becomes slow. The hydrocarbon fluid is then stopped
by closing the stop cock O and steam is again turned into the mass of carbon by
opening the valve F', still in an incandescent state and sufficient water gas produced
to sweep out of the arrangement to the condensers the residual hydrocarbon
vapours and gases, and should vapour still remain in the flue space it
may be swept
Sufficient water gas having been produced for the purpose, the steam is shut off,
the stalk valve C opened and the air valve E² for the admission of the primary
air under the fire bars B' opened, the secondary air supply valve E³ being then
also opened, care being taken to see that the carbonic oxide gas fires immediately
on the admission of the secondary air so as to prevent explosion. The ignition of
out by means of steam.

page_text: the
gas can be readily accomplished by inserting a flame of gas or a torch through
the sight holes D*.
The two currents of air are kept blowing into the arrangement till the carbon in
the producer and the walls of the decomposing chamber are again brought up to
the proper temperature. Meantime a supply of hydrocarbon fluid is raised by the
pump M from the cistern M into the supply cistern N on the top of the producer A,
and a supply of the bydrocarbon liquid as near as can be calculated equal to what
is being gasified in the producer run into the condensing arrangement H from the
tank K.
On the desired temperature being attained in the carbon in the producer and in
the walls of the decomposing chamber, both the air valves are closed and the steam
turned on under the fire bars and up through the carbon, producing water gas to
displace the products of combustion, the stalk being then closed and the steam
stopped or checked and the hydrocarbon fluid run into the arrangement all as
before described.
The processes of blowing up with air so as to heat the carbon and the walls of
the decomposing chamber to the desired temperature and thereafter employing the
stored up heat to produce water gas and decompose the liquid hydrocarbon are
carried on consecutively in a continuous manner.
The carbon originally charged into the combustion chamber is rapidly consumed
by the air blast and in decomposing the steam into water gas, but from the manner
of conducting the process by which the hydrocarbon fluid and condensed products
are returned from the condenser to the gas producing arrangement there is
deposited upon the surface of the carbon contained in the combustion and gas
generating chamber a quantity of carbon from the decomposed liquid hydrocarbon
equivalent to the carbon consumed in performing the operation of the process.
Indeed most liquid hydrocarbons when gasified in accordance with this invention
produce more fixed carbon than is necessary to simply gasify themselves and supply
water gas to wash out the apparatus, and in such cases it is necessary either to
withdraw a part of the carbon from the producer, which is done through the
clinkering doors B3 by withdrawing the guard piece P* and raking out the desired
quantity of coke, or the surplus carbon is employed to produce a larger quantity
of water gas.
When such is the object of the process the gas producer is preferably modified
as shown in Figures 7, 8 and 9, which are respectively sectional elevation, plan and
cross section of the producer. The essential modification consists in altering the
flue and air spaces surrounding the decomposing chamber C by which the secondary
air supply can be more highly heated and introduced to the carbonic oxide gases
coming from the combustion chamber at the top of and external to the decomposing
chamber instead of at the bottom and internal as in the previously described
arrangement thereby enabling a much larger quantity of carbon to be accumulated
in the producer. C1 and C2 are the annular spaces or flues for the products of
combustion terminating in the smoke stalk C³ and the secondary air to be heated
enters by the pipe E into the heating annular space D descending and again
ascending and meeting the carbonic oxide gases as they come through the ports D'
at the top of the decomposing chamber.
The admission of the secondary air at the top and external to the decomposing
chamber allows the surplus carbon deposited from the liquid hydrocarbon to
accumulate not only in the combustion chamber but also partially in the
decomposing chamber and to become highly heated not only by the hot producer
gases from the combustion chamber but also by the combustion of the carbonic
oxide gas by the secondary air around the walls of the decomposing chamber.
The process of gasifying the liquid hydrocarbon by this modified arrangement
is in every other respect identical with that of the arrangement previously
described. The increased quantity of carbon contained in the producer enables a
greater store of heat to accumulate each time the carbon is blown up with air.

page_text: This increased store of heat in turn is devoted to a larger production of water gas
intermittent with the decomposition of the liquid hydrocarbon. Or should the
carbon accumulate then the process may be so modified that the accumulated heat
of the one blowing up of the arrangement may be as far as possible devoted to
gasifying the liquid hydrocarbon only sufficient water gas being made to wash out
the apparatus, the next two or more blowings up of the carbon to incandescence
being devoted to the production of water gas alone. When such a modified process
is adopted the steam for the production of the water gas may be introduced by the
pipe S shown in dotted lines into the flue space C descending which it ascends the
flue space C¹ and getting highly heated passes down through the highly heated
carbon getting decomposed into water gas which would pass into the ashpit B'
and away by the pipe S³, shown by dotted lines, to any suitable cooling
arrangement.
Instead of producing the water gas and decomposing the liquid hydrocarbon
alternately the two processes may be conducted simultaneously, but in such a case
it is necessary to employ two or more combustion and decomposing chambers in
one producing arrangement. Such an arrangement of apparatus is shown in
Figures 10, 11 and 12, which are respectively a sectional elevation, a plan and a
cross section of a producer consisting of three separate combustion chambers B, B, B,
and decomposing vessels C, C, C. Each combustion and gas generating chamber B
is provided with clinker doors B3 and ashpit B, primary air valves E2, E', E³,
also separate valves F1, F2, F', for the admission of steam. The three separate
decomposing chambers C, C, C, are surrounded by the flue space C' in which the
carbonic oxide gases coming from all the combustion chambers B, B, B, through
the ports D' are consumed to form carbonic acid gas by the secondary current of
air admitted by the valve E' and pipe E into and superheated in the flues D, D,.
the products of combustion passing away by the stalk C³.
as
In producing illuminating gas by this modification, each of the three combined
combustion gas generating and decomposing chambers is brought into working-
order and operated in the same manner as with the arrangements already described..
Instead however of the whole three being used at the one time in the same
sequence of operating, one of the three sections of the producer may be producing
water gas alone, whilst the other two are employed to decompose the hydrocarbon
fluid, or two sections may be employel producing water gas whilst the other is
alone devoted to the decomposition of the liquid hydrocarbon and each section.
may be used in sequence, that is the sections may be used alternately for the
production of water gas and decomposing the liquid hydrocarbon, using the stored
up heat of the one blowing up with air to produce water gas, and the next blow-up
to decompose the liquid hydrocarbon, each of the sections being provided with
the steam valves F, F, F, and the valves O', O, O', and pipes O, D. O, for the
admission separately of a supply of steam and of liquid hydrocarbon into each
section of the producer as desired. The com ningled gases from the three sections
pass away by the pipe G2 to the condenser H.
Some hydrocarbon fluids during the process of volatilizing sponge or swell up
in foam and such hydrocarbon fluid when dropped on the top of the heated carbon
contained in the combustion and gas generating chamber sponges up and clo-es
the spaces between the carbon and impedes the process of gasification.
To overcome that difficulty a modified arrangement is adopted as shown in
Figures 13 and 14 which are respectively vertical sections at right angles to each
other and Figures 15 and 16 which are a plan and cross section of the producer.
The essential features of difference in the modification are the placing of the
decomposing chambers in a sloping instead of a horizontal position to prevent the
hydrocarbon fluid dropping onto the top of the carbon in the combustion and gas
producing chamber. The decomposing chambers consist of a series of retorts or
chambers C made of fire brick or other refractory or fire resisting material. These
are placed at a slight inclination alternately in the reverse direction and are con-
nected by the chambers C provided with the access doors Co. The lower inclined

page_text: decomposing chamber C is in direct communication through the opening C' with
the combustion and gas generating chamber B and the upper inclined decomposing
chamber has an opening D' communicating with the flue space C' around the outside
of the decomposing chambers C. The upper inclined chamber is provided with
a mouth piece G with door G¹ connected by the pipe G' to the seal box G³.
The decomposing chambers C are provided with iron sole plates to prevent the
liquid hydrocarbon from penetrating the fire clay soles of the chambers and the
chambers are strongly bound by fire brick blocks placed in the flue space to prevent
disintegration of the clay retorts.
This modified arrangement is operated substantially in the manner already
described, the primary air being supplied through the valve E and pipe E' and the
secondary air by the valve E³ and pipe E to the heating flues D, the carbonic
oxide gases from the combustion chamber meeting the secondary air as it enters
the flue space C' through the ports D in the upper chamber C and the combustion
of the carbonic oxide gases taking place in the space or flue around the decomposing
chamber walls. The only essential difference is that instead of the liquid hydro-
carbon dropping vertically through the decomposing chamber upon the hot carbon
it is allowed to flow from the supply tank down the pipe G into the upper inclined
decomposing chamber down the bottom of which it flows to the second chamber
and so on to the bottom chamber, being in its passage volatilized and in part
gasified.
The large surface area of the bottom of the decomposing chamber allows the
1.quid hydrocarbon to spread and volatilize without foaming or seriously impeding
the action of the apparatus. By this arrangement the carbon is principally
deposited upon the bottom of the decomposing chambers and has from time to
time to be raked down into the combustion and gas generating chamber by means
of suitable tools inserted through the openings provided with doors Co.
The products of decomposition coming from the arrangement are treated in the
condenser arrangement all as already described.
The only remaining parts of this invention requiring explanation are matters
relating to the nature of the liquid hydrocarbons and the modified method of
using them or of treating them prior to their introducion to the gas producing
ai raugement.
When the hydrocarbon liquids employed are free from water and require a low
heat for their decomposition such as is the case with natural petioleum and
paraffin oils then the best results will be obtained by dividing the decomposing
process into two stages.
The portion of the oils which is purposely allowed to escape decomposition
in the decomposing chamber in order to keep the flocculent carbon in solution
and enable it to be returned from the condensers to the producer requires a
higher temperature for its decomposition than would give the best results with
the original oil.
To enable the portions to be subjected to desired temperature the arrangement
is provided with two supply cisterns N and N' as shown by Figures 2 and 8. The
fresh oil is charged into the cistern N¹ whilst the condensed returned products are
pimped into the cistern N.
When the producer has been nearly blown up with air and the carbon and the
walls of the decomposing chamber are at a high temperature and the decomposition
of the hydrocarbon commenced the returned condensed products contained in
cistern N are at first run into the producer as they require the highest temperature
for their decomposition. As the temperature of the heat of the carbon and the
walls of the decomposing chamber falls and becomes suited for the decomposition
o the fresh oil, the returned products are shut off and the fresh oil in the cistern N¹
made to take the place of the returned products.
When the liquid hydrocarbons are crude and tarry and contain water, or when as
in the case of coal tar they contain benzole, which it is desired to recover in the
liquid form, then such liquid hydrocarbons require to be passed back through the

page_text: condensing arrangement so as to enable the water and benzole to be isolated and
removed and fit them for the process of decomposition.
Even
The gases and vapours coming from the producer have so high a temperature
that in bubbling through the hydrocarbon liquids in the seal box G they heat those
liquids up to a temperature considerably over the boiling point of water.
after travelling forward through the first set of condensing pipes and entering the
first washing chest the vapours and gases will still be little if at all under the
boiling point and are still capable of holding in diffusion the volatile benzole and
water vapour. From this point the temperature of the vapour and gases gradually
falls till a little over that of the atmosphere before leaving by the pipe H
Now by causing the tarry liquid hydrocarbons to travel back against the current
of gas and vapour, and by bringing them into intimate contact with the gases and
vapours coming from the producer, first in the washing chests of the condenser, and
finally in the seal box, the tarry liquid hydrocarbons are gradually heated to such
a temperature, that the water and volatile hydrocarbons are liberated from the tar
and driven forward into the condenser chests where they are condensed. In order
to isolate or separate the water and hydrocarbons so liberated, as also water which
may be derived from steam coming froin the producer one of the condenser chests is
isolated, the flow of tar or hydrocarbon liquids being bye-passed by means of the
stop cocks K' on the pipes K', that chest being selected where the gases and vapours
have been so far cooled as to allow of the water and hydrocarbons being condensed
and collected, the condensed liquid produced being drawn off through the stop
cock K' on the chest through the pipe K' into the tank Ks provided for the
purpose.
The apparatus in the several forms described is applicable for use in the
production of water gas alone the arrangements for supplying the liquid hydrocarbons
being omitted and a supply of solid carbon to replace that deposited from such
hydrocarbons being fed into or through the decomposing chamber.
Having thus particularly described my said invention and arrangement of
apparatus whereby the same may be carried into effect, I wish to state that I make
no general claim for a gas producing arrangement in which water gas and
carburetted water gas is produced by the alternate blowing up with air to
incandescence of a mass of carbon contained in a combustion chamber and the
heating up of a decomposing chamber or retort in connection with the same, and
thereafter shutting off the air and blowing in steam and running into the
arrangement hydrocarbon fluid, neither do I claim the combination of a condensing
and washing arrangement in connection with such a gas producing arrangement,
because these are well known forms of apparatus and methods of producing
illuminating and heating gases but what I consider to be novel and original and
therefore claim is-
1. The method of producing illuminating and heating gases from liquid
hydrocarbons by means of the improved gas producing apparatus shown by the
accompanying drawings and used and operated as described whereby the carbon
present in the liquid hydrocarbon in excess of what can be gasified by destructive
distillation is isolated and deposited in such a form and under such conditions as
render it directly available as the source of heat by the partial combustion with air
to effect the destructive distillation of the liquid hydrocarbons and to produce water
gas sufficient to wash out the apparatus, and if the carbon is largely in excess to
produce a further quantity of water gas all as described.
2. The improved method of decomposing or gasifying liquid hydrocarbons in a
gas producing apparatus, consisting in producing water gas and decomposing the
liquid hydrocarbons alternately, instead of both at the same time whereby the
stored up
heat in the decomposing chamber is rendered more effective and better
applied to the decomposition of the liquid hydrocarbon substantially as described.
3. The improved method of treating the condensible liquid products leaving the
gas producer whilst passing through the seal box and condensing and washing
B

page_text: arrangement, and also the fresh liquid hydrocarbons on their way through the
condensing and washing arrangement to the producer whereby they are denuded of
water and rendered fit for reuse or use in the producer and by which such water
and accompanying valuable hydrocarbons are isolated, substantially as described.
4. The improved method of decomposing liquid hydrocarbons requiring different
temperatures for their decomposition, which consists in running the liquid
hydrocarbon difficult of decomposition into the gas producer to be acted on by the
heat of the high temperature stored up in the decomposing chamber of the producer,
and thereafter on the heat falling to a lower temperature, running the more easily
decomposed liquid hydrocarbons into the producer to be decomposed, substantially
as described.
5. The improved construction and combination of apparatus and accessories for
producing illuminating and heating gases from liquid hydrocarbons, substantially
as described with reference to Figures 1, 2 and 3 of the accompanying drawings.
6. The improved construction of gas producer in which the decomposing chamber
is placed vertically over the combustion chamber, without any intervening
brickwork so that the carbon and dense hydrocarbons liberated during the
decomposition of liquid hydrocarbons may fall back from the decomposing chamber
direct upon the carbon in the producer, such decomposing chamber being
surrounded with annular flue spaces and the secondary air being admitted over the
carbon in the combustion chamber for the combustion of the carbonic oxide gases
which are made to heat internally the walls of the producer and walls of the
annular space, the heat so stored up being entirely devoted to the decomposition of
the liquid hydrocarbon, substantially as described.
7. The improved construction of gas producer in which the combustion and gas
generating chamber is surmounted by a vertical retort or decomposing chamber in
which the carbon deposited from the liquid hydrocarbon is allowed to collect and
becomes not only heated by the hot products of combustion coming from the
combustion and gas generating chamber but also by the heat resulting from the
combustion of the carbonic oxide gas in the flue spaces external to the walls of
the decomposing chamber whereby more of the stored up heat is devoted to the
production of a larger quantity of water gas, substantially as described with reference
to Figures 7 and 8 of the accompanying drawings.
8. The improved construction of gas producer in which two or more producers
are combined, and in each of which the processes of producing water gas and
decomposing liquid hydrocarbons may be carried on independently at the same time,
and in sequence, substantially as described with reference to Figures 10 and 11 of
the accompanying drawings.
9. The improved construction of gas producer consisting of a combustion and gas
generating chamber surmounted by a series of inclined decomposing chambers or
retorts to deal with liquid hydrocarbons which have a tendency to foam or sponge
up during their volatilization, substantially as described with reference to
Figures 13, 14, and 15 of the accompanying drawings.
10. The improved construction of gas producing apparatus applied to the
production of water gas as shown in Figures 7 to 13 of the accompanying drawings
whereby the carbon used to decompose the water is not only heated by the primary
products of the combustion from the producer but also in considerable part by the
combustion of the carbonic oxide gases by a secondary supply of air around the
walls of the chamber or decomposing vessel containing such carbon, substantially as
described.
Dated this 21st day of March 1894.
CRUIKSHANK & FAIRWEATHER,
62, St. Vincent Street, Glasgow, Agents.