Method and Apparatus for Treating the Distillation Products from Carbonaceous Materials and the like.
Year: 1898

page_text: Date of Application, 6th Jan., 1898
Complete Specification Left, 6th Oct., 1898-Accepted, 3rd Dec.,
1898
PROVISIONAL SPECIFICATION.
Method and Apparatus for Treating the Distillation Products from
Carbonaceous Materials and the like.
I, CHARLES DENTON ABEL, of Birkbeck Bank Chambers, Southampton
Buildings, Chancery Lane, London, W.C., Consulting Engineer and Chartered
Patent Agent, do hereby declare the nature of this invention (which has been
communicated to me from abroad by Eduard Theisen, of 9, Werderstrasse, Baden-
Baden, Germany, Engineer) to be as follows:-
This invention relates to a process and apparatus whereby, in gas manufactories,
in particular those for the manufacture of coke-gas, illuminating gas, and water
gas, those cumbrous apparatus which now serve for the separation and purification
of the various substances contained in these gases are replaced by a simple and
easy treatment by means of centrifugal force.
In this treatment the gases coming from the retorts or gas producers are first
subjected, while hot, to centrifugal action in such manner that the gases are
thrown against a casing surrounding the centrifugal apparatus which is covered
with cooling water, so that the heat of the gases is utilised in heating and
partially evaporating such water. The further treatment varies according to
the nature of the substances contained in the gases and of the end products
desired to be obtained.
For the separation of ammonia the gases cooled to a temperature of about
60° C. are subjected to a second centrifugal action where the casing surrounding
the centrifugal apparatus has water supplied to it in such manner that its flow
can be accurately regulated, and the gases thrown against it give off the whole
of their ammonia to it. The gases then contain separable products such as
benzene, and also this can be obtained in a centrifugal apparatus of special
construction. In this centrifugal apparatus the surrounding casing has its
surface supplied with oil in which benzene is easily dissolved, and in addition
the temperature is here advantageously reduced to 0° C. and lower.
The gases passing away can be employed for heating retorts.
If illuminating gas is produced, the benzene is not separated, but any which
may be accidentally separated is added to the gas again in order to increase its
illuminating power.
The accompanying drawings shew a series of apparatus which by their con-
secutive application will effect the separation from the gases of the various con-
stitutents in an advantageous manner.
The several apparatus are shewn partly in elevation and partly in section.
In the case of water gas the treatment is the simplest on account of the com-
position of the water gas, while with the treatment of coke gas and illuminating
gas, farther operations have to be carried out.
In the drawings Figure 1 shews a diagrammatic elevation of a plant for treat-
ing water gas.
Figure 2 shews a plan of the same, Figure 3 an elevation of a plant for

page_text: treating illuminating gas, Figure 4 a plan thereof. Figure 5 an elevation of a
plant for treating coke gas, Figure 6 a plan thereof, Figures 7 and 8 are part
elevations and part sections of an apparatus for the separation of tar and for
cooling the gases passing upward from the tar-separating apparatus.
Figures 9 and 10 shew respectively an elevation, partly in section and a plan
of an apparatus for obtaining ammonia from the gases.
Figures 11 and 12 shew respectively a section and plan of an apparatus for
purifying gases from sulphur.
Figures 13 and 14 shew respectively an elevation partly in section and a plan
of an apparatus for purifying gases by the separation of dust.
Figures 15 and 16 shew respectively an elevation partly in section and a plan
of a distilling apparatus for separating ammonia or benzene from their solutions.
In treating water gas, the gaseous mixture passes from the gas generator into
the centrifugal dust collector d which serves at the same time as cooler.
In this the gas is subject to rapid rotary motion, and it can for this purpose
be arranged in a similar manner to that described in the British Patent No. 16726
of 1892. By means of this rotation the dust contained in the gases, and other
impurities are separated and fall to the bottom, whence they can be removed.
This dust collector can at the same time serve as cooler, if its inner surface has
water flowing over it, as is shewn in the lower part of the apparatus at Figure 7.
In this case a very energetic reciprocal action takes place between the rotating
gases and the water, causing an evaporation of the water, and very considerable
cooling of the gases.
The circumstances are very peculiar, with a rapid rotation, as a formation of
strong vapours takes place considerably below the evaporating temperature in
consequence of the intensive friction of the gases upon the water. In this way
it is possible to withdraw the gases at the upper part of the apparatus with a
temperature of about 60° C. in a condition thoroughly charged with aqueous
vapour. A cooling device 9 may be used for continuously cooling the heated
cooling water.
From the gas thus purified the ammonia still has to be separated, this being
effected in the apparatus b, which is shewn in detail in Figures 9 and 10.
The gases enter the inner space of the centrifugal apparatus through a pipe B.
In this apparatus a series of blades or vanes X fixed on the shaft B are made
to rotate at a high speed, which blades throw the entering gas outward, with
great force. Y is the fixed casing of the apparatus and upon it are fixed a series
of annular chambers y which serve for the reception of liquid and which may
also contain cooling pipes Z. Into these chambers water is introduced through
a pipe B which first fills the top annular chamber, from which it passes into
the next following one either by overflowing the edge, or through a special con-
necting channel. By this means it is rendered possible to determine the rate
of flow of the water from top to bottom along the walls Y, by regulating the
supply through the pipe B by which regulation consequently the duration of
the action of the gases upon this liquid will be determined.
The gases thus subjected to centrifugal action discharge their ammonia, which,
owing to the strong friction with the water, and also by direct separation by
the centrifugal force readily becomes taken up and dissolved in the water.
It is to be observed that the speed of rotation can be taken so high that the
pressure of the gases causes the water to rise up upon the wall of each chamber
so that a liquid surface is produced which is directly opposed to the pressure of
the gases, and which consequently effectually absorbs the ammonia.
By the rotation of the gases also, a rotation of the water would be produced,
but at a less speed, if the several chambers were not provided with transverse
partitions which partially or wholly prevent such rotation.
In this way, a discharge of water saturated with ammonia will be produced
at bottom through the pipe D³, while from the upper part the gases purified from
ammonia are led off in order to be used for heating purposes. The arrangement

page_text: may also be such that the same quantity of water shall pass several times through
all the chambers. In this case the apparatus is connected with a conical
mantle B provided with a gutter 136 at its lower end, in which gutter the ammonia
water can collect. By the rotation of this cone the water will be caused, as is
well known to mount up its sides and will flow over the upper edge through a
pipe B into the top chamber.
In the manufacture of illuminating gas the first stages of the treatment of the
gas are conducted in a precisely analogous manner.
As shewn in Figure 3, the gases issuing from the generator or retort through
pipe B enter into the bottom of an apparatus a¹. In this apparatus the separa-
tion of dust together with tar is effected.
The gases are here still at their. full temperature and at this temperature the
centrifugal force can act only on that portion of the tar which can condense on
the rotating walls and flow away.
In Figures 7 and 8 the construction of this apparatus is shewn separately.
The gases enter at A and are caught by the fans A2 mounted on the shaft A'
and are rapidly rotated thereby. The tar and dust particles are thrown outwards
and collect on the walls A³, these are set conically so that the tar is caused to
rise up them and to collect in a chamber A' whence it can be withdrawn through
a pipe A5.
After this treatment the gases pass on by way of the upper part a² of the
apparatus, where provision is made for cooling them in the manner adopted for
water gas; at the same time a slight separation of ammonia may occur here
owing to the fall of temperature. The gases laden with water vapour and
cooled to a temperature of about 60° C. then pass through the pipe Aº. The
inlet for the condensation water is at A7. A further cooling of the gases can
then be effected in a cooler f of any desired construction in which their tempera-
ture can be lowered to from 18 to 20° C.; this is most advantageous for the
subsequent separation of ammonia unmixed with other matters. Next the gases
enter into the centrifugal apparatus b which effects the separation of the ammonia
in the way already described.
Illuminating gas contains sulphur, in the form of sulphuretted hydrogen,
which must be removed before the combustion of the gas. For this purpose the
gases are passed through another centrifugal apparatus c, more clearly shewn in
Figures 11 and 12.
The gases enter through the pipe C into the interior of a revolving drum C¹.
Against the outer wall of this drum materials are disposed which serve to com-
bine with the sulphur such as oxide of iron. These materials may be placed in
the drum and held against the walls by centrifugal force, in which position they
may be caused to travel along by any appropriate means.
In such an arrangement a part of the drum C2 is provided with an impervious
wall so that the gas shall come under the influence of centrifugal force into
intimate contact with the absorbent for the sulphuretted hydrogen. In the
second half of the drum C³ the wall is made pervious so that the gases can pass
through the absorbent, be purified thereby and pass away through the pipe C+
Instead of granular absorbents liquids may be employed these, in a similar
manner, will be held against the wall of the rotating cylinder by centrifugal
force.
If the gas is to be enriched by benzene to enhance its illuminating power, it
may be passed through a carburetting apparatus into which benzene is admitted
for supplying the vapour.
Such an apparatus e is shewn in Figures 15 and 16. In this the gases are
brought into contact with a solution of benzene obtained from some other source,
and the solution is heated so that the benzene is entirely evaporated. For this
purpose the gases are led through the pipe E into the bottom of the apparatus
where they are immediately caught and centrifuged by the fans F³ rotating
with the shaft E¹. The solution of benzene flows through the pipe E³ into a

page_text: system of chambers, exactly corresponding with ammonia absorption apparatus
Figures 9 and 10, save that in this case the contents of the chambers are heated.
Owing to this heating and to the gases which are streaming over the surface of
the liquid with great speed and under pressure, a distillation of the benzene
ensues, and when the method is properly conducted, that is to say at the right
temperature and right number of rotations, the distillation of other products
may be completely avoided. Moreover the distillation attains a rapidity which
cannot be achieved in other apparatus if due regard be had to the purity of the
product. Care must be taken that the solution is caused to flow down the surface
of the apparatus in the thinnest possible layer.
The result of the rapid distillation is that the products are immediately whirled
away by the revolving fans E3 and fresh quantities of gas, not yet laden with
distillation products, are brought into energetic contact with the surface of the
liquid.
In case liquid particles be carried over by spirting during the distillation,
these will be at once set in rapid rotation by the fans and will be thrown back
into the liquid by centrifugal force. In addition, owing to the high pressure
and drastic friction on the surface of the liquid a much more uniform evolution
of the distillation products takes place.
If the apparatus be conically enlarged in an upward direction and the centri-
fuging fans be correspondingly lengthened, a smaller degree of suction will result,
which may be very favourable for the distillation and movement of the gas
current.
Finally, in the distillation of coke gases the treatment is at first, on the whole
the same as in the manufacture of illuminating gas. The principal difference
is that separation of sulphuretted hydrogen is not essential but the separation
of benzene must be effected.
In this case the gases passing away from the last apparatus are used solely
for heating the coke ovens, where the sulphuretted hydrogen does no harm,
but the benzene is too dear for a fuel.
Other, smaller changes are necessary on account of the different nature of
the gases.
The gases are first passed into the centrifugal apparatus d, in which the tar
is separated and, if necessary, a slight cooling may be effected. In the cooler f
the vapours which have been carried forward are condensed and in the appara-
tus b the ammonia is recovered.
In the similarly constructed apparatus 61 the benzene is recovered and for this
purpose an appropriately proportioned quantity of cold (if possible at a tempera-
ture below 0° C.) light tar oil (which however should boil at a temperature
above 200° C.) is injected as an absorbent.
In a second similar apparatus 6 the same process is carried out with a heavy
oil, which absorbs the last portions of the benzene.
The recovery of the ammonia from the ammoniacal liquor and of the benzene
from the oils is effected in an apparatus e as has been already described.
Dated this 6th day of January 1898.
ABEL & IMRAY,
Agents for the Applicant.
Method and Apparatus for Treating the Distillation Products from
Carbonaceous Materials and the like.
I, CHARLES DENTON ABEL, of Birkbeck Bank Chambers, Southampton
Buildings, Chancery Lane, London, W.C., Consulting Engineer and Chartered

page_text: Patent Agent, do hereby declare the nature of this invention (which has been
communicated to me from abroad by Eduard Theisen, of 9, Werderstrasse, Baden-
Baden, Germany, Engineer) 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 a process and apparatus whereby, in gas manufactories,
in particular those for the manufacture of coke gas, illuminating gas, and water
those cumbrous apparatus which now serve for the separation and purification
of the various substances contained in these gases are replaced by a simple and
easy treatment by means of centrifugal force.
gas,
In this treatment the gases coming from the retorts or gas producers are first
subjected, while hot, to centrifugal action in such manner that the gases are
thrown against a casing surrounding the centrifugal apparatus which is covered
with cooling water, so that the heat of the gases is utilised in heating and
partially evaporating such water. The further treatment varies according to
the nature of the substances contained in the gases, and of the end products
desired to be obtained.
For the separation of ammonia the gases cooled to a temperature of about
60° C. are subjected to a second centrifugal action, where the casing surrounding
the centrifugal apparatus has water supplied to it in such manner that its flow
can be accurately regulated, and the gases thrown against it give off the whole
of their ammonia to it. The gases then contain separable products such as
benzene, and also this can be obtained in a centrifugal apparatus of special
construction. In this centrifugal apparatus the surrounding casing has its
surface supplied with oil in which benzene is easily dissolved, and in addition
the temperature is here advantageously reduced to 0° C. and lower.
The gases passing away can be employed for heating retorts.
If illuminating gas is produced, the benzene is not separated, but any which
may be accidentally separated is added to the gas again in order to increase its
illuminating power.
The drawings accompanying my Provisional Specification shew a series of
apparatus which by their consecutive application will effect the separation from
the gases of the various constituents in an advantageous manner.
The several apparatus are shewn partly in elevation and partly in section.
In the case of water gas the treatment is the simplest on account of the com-
position of the water gas, while with the treatment of coke gas and illuminating
gas, farther operations have to be carried out.
In the drawings Figure 1 shews a diagrammatic elevation of a plant for treat-
ing water gas.
Figure 2 shews a plan of the same, Figure 3 an elevation of a plant for
treating illuminating gas, Figure 4 a plan thereof. Figure 5 an elevation of a
plant for treating coke gas, Figure 6 a plan thereof, Figures 7 and 8 are part
elevations and part sections of an apparatus for the separation of tar and for
cooling the gases passing upward from the tar-separating apparatus.
Figures 9 and 10 shew respectively an elevation, partly in section and a plan
of an apparatus for obtaining ammonia from the gases.
Figures 11 and 12 shew respectively a section and plan of an apparatus for
purifying gases from sulphur.
Figures 13 and 14 shew respectively an elevation partly in section and a plan
of an apparatus for purifying gases by the separation of dust.
Figures 15 and 16 shew respectively an elevation partly in section and a plan
of a distilling apparatus for separating ammonia or benzene from their solutions.
In treating water gas, the gaseous mixture passes from the gas generator into
the centrifugal dust collector d which serves at the same time as cooler.
In this the gas is subject to rapid rotary motion, and it can for this purpose
be arranged in a similar manner to that described in the British Patent No. 16726
of 1892. By means of this rotation the dust contained in the gases, and other
impurities are separated and fall to the bottom, whence they can be removed.

page_text: This dust collector can at the same time serve as cooler, if its inner surface has
water flowing over it, as is shewn in the lower part of the apparatus at Figure 7.
In this case a very energetic reciprocal action takes place between the rotating
gases and the water, causing an evaporation of the water, and very considerable
cooling of the gases.
The circumstances are very peculiar, with a rapid rotation, as a formation of
strong vapours takes place considerably below the evaporating temperature in
consequence of the intensive friction of the gases upon the water.
In this way
it is possible to withdraw the gases at the upper part of the apparatus with a
temperature of about 60° C. in a condition thoroughly charged with aqueous
vapour. A cooling device g may be used for continuously cooling the heated
cooling water.
From the gas thus purified the ammonia still has to be separated, this being
effected in the apparatus b, which is shewn in detail in Figures 9 and 10.
The gases enter the inner space of the centrifugal apparatus through a pipe B.
In this apparatus a series of blades or vanes X fixed on the shaft B are made
to rotate at a high speed, which blades throw the entering gas outward, with
great force.
Y is the fixed casing of the apparatus and upon it are fixed a series
of annular chambers y which serve for the reception of liquid and which may
also contain cooling pipes Z. Into these chambers water is introduced through
a pipe 12 which first fills the top annular chamber, from which it passes into
the next following one either by overflowing the edge, or through a special con-
necting channel. By this means it is rendered possible to determine the rate
of flow of the water from top to bottom along the walls Y, by regulating the
supply through the pipe B by which regulation consequently the duration of
the action of the gases upon this liquid will be determined.
The gases thus subjected to centrifugal action discharge their ammonia, which,
owing to the strong friction with the water, and also by direct separation by
the centrifugal force readily becomes taken up and dissolved in the water.
It is to be observed that the speed of rotation can be taken so high that the
pressure of the gases causes the water to rise up upon the wall of each chamber
so that a liquid surface is produced which is directly opposed to the pressure of
the gases, and which consequently effectually absorbs the ammonia.
By the rotation of the gases also, a rotation of the water would be produced,
but at a less speed, if the several chambers were not provided with transverse
partitions which partially or wholly prevent such rotation.
In this way, a discharge of water saturated with ammonia will be produced
at bottom through the pipe D³, while from the upper part the gases purified from
ammonia are led off in order to be used for heating purposes. The arrangement
may also be such that the same quantity of water shall pass several times through
all the chambers. In this case the apparatus is connected with a conical
mantle B5 provided with a gutter B36 at its lower end, in which gutter the ammonia
water can collect. By the rotation of this cone the water will be caused, as is
well known to mount up its sides and will flow over the upper edge through a
pipe B7 into the top chamber.
In the manufacture of illuminating gas the first stages of the treatment of the
gas are conducted in a precisely analogous manner.
As shewn in Figure 3, the gases issuing from the generator, or retort, through
pipe B enter into the bottom of an apparatus a¹. In this apparatus the separa-
tion of dust together with tar.is effected.
The gases are here still at their full temperature and at this temperature the
centrifugal force can act only on that portion of the tar which can condense on
the rotating walls and flow away.
In Figures 7 and 8 the construction of this apparatus is shewn separately.
The gases enter at A and are caught by the fans A2 mounted on the shaft A¹
and are rapidly rotated thereby. The tar and dust particles are thrown outwards
and collect on the walls A³, these are set conically so that the tar is caused to

page_text: rise up them and to collect in a chamber A', whence it can be withdrawn through
a pipe A³.
After this treatment the gases pass on by way of the upper part a³ of the
apparatus, where provision is made for cooling them in the manner adopted. for
water gas at the same time a slight separation of ammonia may occur here
owing to the fall of temperature. The gases laden with water vapour and
cooled to a temperature of about 60° C. then pass through the pipe A. The
inlet for the condensation water is at A. A further cooling of the gases can
then be effected in a cooler f of any desired construction in which their tempera-
ture can be lowered to from 18 to 20° C.; this is most advantageous for the
subsequent separation of ammonia unmixed with other matters.
Next the gases
enter into the centrifugal apparatus b which effects the separation of the ammonia
in the way already described.
Illuminating gas contains sulphur, in the form of sulphuretted hydrogen,
which must be removed before the combustion of the gas. For this purpose the
gases are passed through another centrifugal apparatus c, more clearly shewn in
Figures 11 and 12.
The gases enter through the pipe C into the interior of a revolving drum C¹.
Against the outer wall of this drum materials are disposed which serve to com-
bine with the sulphur, such as oxide of iron. These materials may be placed in
the drum and held against the walls by centrifugal force, in which position they
may be caused to travel along by any appropriate means.
In such an arrangement a part of the drum Ca is provided with an impervious
wall so that the gas shall come under the influence of centrifugal force into
intimate contact with the absorbent for the sulphuretted hydrogen. In the
second half of the drum C³ the wall is made pervious so that the gases can pass
through the absorbent, he purified thereby and pass away through the pipe C4.
Instead of granular absorbents liquids may be employed; these, in a similar
manner, will be held against the wall of the rotating cylinder by centrifugal
force.
If the gas is to be enriched by benzene to enhance its illuminating power, it
may be passed through a carburetting apparatus, into which benzene is admitted
for supplying the vapour.
Such an apparatus e is shewn in Figures 15 and 16. In this the gases are
brought into contact with a solution of benzene obtained from some other source.
and the solution is heated so that the benzene is entirely evaporated. For this
purpose the gases are led through the pipe E into the bottom of the apparatus
where they are immediately caught and centrifuged by the fans E rotating
with the shaft E¹. The solution of benzene flows through the pipe E³ into a
system of chambers, exactly corresponding with ammonia absorption apparatus
Figures 9 and 10, save that in this case the contents of the chambers are heated.
Owing to this heating and to the gases which are streaming over the surface of
the liquid with great speed and under pressure, a distillation of the benzene
ensues, and when the method is pronerly conducted. that is to say at the right
temperature and right number of rotations, the distillation of other products
may be completely avoided. Moreover the distillation attains a rapidity which
cannot be achieved in other apparatus if due regard he had to the purity of the
product. Care must be taken that the solution is caused to flow down the surface
of the apparatus in the thinnest possible layer.
The result of the rapid distillation is that the products are immediately whirled
away by the revolving fans F and fresh quantities of gas. not yet laden with
distillation products, are brought into energetic contact with the surface of the
lionid.
In case liquid particles be carried over by spirting during the distillation,
these will be at once set in ranid rotation by the fans and will be thrown back
into the liquid by centrifugal force. In addition, owing to the high pressure

page_text: and drastic friction on the surface of the liquid a much more uniform evolution
of the distillation products takes place.
If the apparatus be conically enlarged in an upward direction and the centri-
fuging fans be correspondingly lengthened, a smaller degree of suction will result,
which may be very favourable for the distillation and movement of the gas
current.
Finally, in the distillation of coke gases the treatment is at first, on the whole
the same as in the manufacture of illuminating gas. The principal difference
is that separation of sulphuretted hydrogen is not essential but the separation
of benzene must be effected.
In this case the gases passing away from the last apparatus are used solely
for heating the coke ovens, where the sulphuretted hydrogen does no harm,
but the benzene is too dear for a fuel.
Other smaller changes are necessary on account of the different nature of
the gases.
The gases are first passed into the centrifugal apparatus d, in which the tar
is separated and, if necessary, a slight cooling may be effected. In the cooler f
the vapours which have been carried forward are condensed and in the appara-
tus the ammonia is recovered.
In the similarly constructed apparatus 61 the benzene is recovered and for this
purpose an appropriately proportioned quantity of cold (if possible at a tempera-
ture below. 0° C.) light tar oil (which however should boil at a temperature
above 200° C.) is injected as an absorbent.
In a second similar apparatus 611 the same process is carried out with a heavy
oil, which absorbs the last portions of the benzene.
The recovery of the ammonia from the ammoniacal liquor and of the benzene
from the oils is effected in an apparatus e as has been already described with
reference to Figure 1.
Having now particularly described and ascertained the nature of this inven-
tion and in what manner the same is to be performed, I declare that what I
claim is:
-
1. The herein described process for cleansing water gas and gaining by-products
therefrom which consists in first subjecting the said gases to centrifugal action
for the separation of dust therefrom and for cooling the same, and then sub-
jecting the gases to a further centrifugal action within a casing over the inner
surface of which (preferably divided into cells or compartments) water is made
to flow, so as to take up ammonia from the gases impinging thereon, substantially
as described, with reference to Figures 1, 2, 9 and 10 of the drawings.
2. The herein described process for cleansing coal gas and gaining by-products
therefrom, which consists in first subjecting the said gases to centrifugal action
within a casing for the separation of dust and tar therefrom, and for cooling
the same, then subjecting the same gases to a second centrifugal action within a
casing over the inner surface of which (preferably divided into cells or compart-
ments) water is made to flow so as to take up ammonia from the gases impinging
thereon, and then subjecting the gases to a third centrifugal action within a
casing containing a layer of absorbent material suitable for taking up the sul-
phurous constituents contained in the gases, which may be made to pass either
over the absorbent material or through the same, or both over and through the
same, substantially as described with reference to Figures 3, 4, 7, 8, 9, 10, 11
and 12 of the drawings.
3. In combination with the process for treating coal gas referred to in the
second claim, enriching the gas after leaving the centrifugal purifying apparatus,
by subjecting it to a farther centrifugal action within a casing the outer surface
of which is heated while over the inner surface (preferably divided into cells
or compartments) benzene is made to flow, so as to be vaporised by the heat and
be taken up by the gases impinging upon the liquid, substantially as described.

page_text: 4. The herein described process for cleaning coke oven gases and gaining
by-products therefrom, which consists in first subjecting the gases within a
casing for the separation of dust and tar therefrom and for cooling the same,
then subjecting the said gases to a second centrifugal action within a casing
over the inner surface of which (preferably divided into cells or compartments)
water is made to flow so as to take up ammonia from the gases impinging thereon,
and then subjecting the gases to a third centrifugal action within a casing over
the inner surface of which liquid hydrocarbon is made to flow in order to take
up the benzene from the gases impinging thereon, substantially as described
with reference to Figures 5, 6, 9, 10, 13 and 14, of the drawings.
5. Apparatus for carrying out the process of cleaning gases and obtaining
by-products therefrom referred to in the first claim, combined and operating
substantially as described with reference to Figures 1, 2, 9, 10, 13 and 14 of the
drawings.
6. Apparatus for carrying out the process of cleaning gases and obtaining by-
products therefrom referred to in the second and third claims, combined and
operating substantially as described with reference to Figures 3, 4, 7, 8, 9, 10,
11, 12, 15 and 16 of the drawings.
7. Apparatus for carrying out the process of cleaning gases and obtaining
by-products therefrom referred to in the fourth claim, combined and operating
substantially as described with reference to Figures 5, 6, 9, 10, 13 and 14 of
the drawings.
8. Apparatus for separating dust and tar from gases combined and operating
as herein described with reference to Figures 7 and 8 of the drawings.
9. Apparatus for separating ammonia or benzene from gases combined and
operating as herein described with reference to Figures 9 and 10 of the drawings.
10. Apparatus for separating sulphurous constituents from gases combined and
operating as herein described with reference to Figures 11 and 12 of the drawings.
11. Apparatus for enriching illuminating gases with benzene vapour, combined
and operating as herein described with reference to Figures 15 and 16 of the
drawings.
ABEL & IMRAY,
Agents for the Applicant.