Note: Descriptions are shown in the official language in which they were submitted.
CA 02349867 2001-05-04
Process and Apparatus for Producing Hydrocarbons from
Residential Trash or 'Vaste and/or Organic 'Vaste Materials
FIELD OF THE INVENTION
The present invention is directed to a process and apparatus for producing
hydrocarbons from residential trash or waste and/or organic waste materials,
in
particular, to a process and apparatus for producing hydrocarbons from
residential
trash or waste and/or organic waste materials by pyrolysis and catalytic
cracking.
BACKGROUND OF THE INVENTION
With the progress of the society and the improvement of people's life, organic
components in residential trash or waste are continuously increasing, and are
therefore
1 ~ seriously harmful to the environment. It has become a popular topic in the
world to
treat residential trash or waste and/or organic waste materials and make them
harmless and reused.
The composition of residential trash or waste is very complicated. The burning-
process in the prior art is of higher costs. Tail gases resulting from the
process pollute
the air. Another process in the prior art, the burying-process, occupies many
cultivated
lands, pollutes water resource under the ground and the materials cannot be
reused.
Several technical solutions to these problems have been disclosed in the art.
2~ Chambers in USP4,235,676 teaches an apparatus for producing hydrocarbons
from
waste plastics and industrial and residential waste. Said apparatus comprises
a
vacuum system and a fixed reactor. The problem to use the apparatus is that
production cannot be successively undergone. In addition, the reactor is
readily coked,
and it is very hard to discharge residues generated from the reaction out of
the reactor.
EP-A-0607862 (applicant being Nlazda Motor Corporation) discloses a process
and
apparatus for producing hydrocarbons from waste plastics and waste rubbers. A
vertical reactor is used therein. However, this publication does not show how
to
discharge the residues from the reaction. All the processes stated above
cannot
simultaneously and successively treat residential trash or waste ancL'or
organic waste
materials with a complex composition.
PCT/CN97/001?=1 filed by the applicant discloses a process and apparatus for
CA 02349867 2001-05-04
7
producing hydrocarbons from organic and polymeric waste materials. A
horizontal
rotary reactor is utilized therein. The reactor should be maintained at a high
temperature to keep the perfom~ance of the reaction of cracking because all
reactions
are carried out in one reactor. However, the high temperature to be used
therein is
critical to the quality of the reactor. It is difficult to rotate the reactor
if it is made of
the normal steel. In this case, the temperature of the reaction should be
lowed to keep
the reactor in shape. Thus, the reaction of cracking is not complete and the
materials
cannot be fully decomposed. In addition, the materials are intermittently
charged and
the residues from the reaction are also intermittently discharged.
The invention is hereby provided to solve these problems in the prior art.
SUNI>VIARY OF THE INVENTION
Accordingly, an object of the invention is to provide a process and apparatus
for
producing hydrocarbons from residential trash or waste and/or organic waste
materials. Particularly, the invention provides a process and apparatus for
producing
hydrocarbons from residential trash or waste and/or organic waste materials by
virtue
of two-step cracking at different temperatures with successive feeding and
dischar~in~.
According to the invention, the process comprises two steps. The first
cracking is
performed in the first reactor (horizontal spiral reactor) which is designed
in a larger
size so that more materials can be treated. The specific size of the reactor
depends on
2~ the properties of the materials to be treated. For example, the reactor, in
general, is
designed to be of 1.0-3.0 meters in diameter.
Gaseous components from the first cracking reaction are discharged OLIt of the
reactor
after the reaction is complete. Resultant residues enter the second reactor
(spiral
stirring reactor) to undergo the second cracking reaction. The second reactor
may be
designed in a small size because the volume of the materials has been greatly
decreased after the first cracking. The size of the second reactor may be
varied
depending on the properties of the materials and the condition of the
treatment. In
general, the second reactor may have a diameter as 1/2 of the first reactor,
such as 0.~
1.~ meters.
Although the temperature to be maintained in the second reactor is much higher
than
in the first reactor, the second reactor is not readily deformed at such a
higher
CA 02349867 2001-05-04
3
temperature because it is kept stationary and its volume is relatively small.
It has no
influence on the reaction of cracking even if the second reactor becomes
little
deformed. The invention, therefore, overcomes the problems in the prior art.
p The present invention provides a process for treating residential trash or
waste and/or
organic waste materials comprising the steps of:
feeding the materials into a horizontal rotary reactor to perform the first
cracking
reaction; and
charging the residues from the first cracking into a spiral stirring reactor
to perform
the second cracking reaction.
Said process further comprises a step to collect gaseous hydrocarbons from the
first
and second cracking reactions.
l~ In said process, the materials may be pretreated, if desired.
In said process, the reactions of the first and second cracking comprise
pyrolysis
and/or catalytic cracking.
?0 Said cracking reaction is carried out at an atmospheric pressure or higher.
In general,
the cracking is perfornied at a pressure of 0.02-0.6yIPa. The temperature of
the first
crackin~ is maintained at 350-600°C, and that of the second cracking at
600-1200°C.
Preferably, the temperature of the first cracking is kept at 400-500°C
and that of the
second cracking at 600-800°C.
Catalyst SR-1 is employed in the catalytic cracking.
The invention further provides an apparatus for treating residential trash or
waste
and/or organic waste materials, which mainly comprises a horizontal rotary
reactor
and a spiral stirring reactor.
Said horizontal rotary reactor comprises a first cylindrical housing; a
circular gear
wheel, looping on the outer wall of the cylindrical housing; a spiral strip
steel, tined
on the inner wall of the cylindrical housing; a feeder, arranged at an end of
the
3~ horizontal rotary reactor; and the first treatment chamber, installed at
another end of
the horizontal rotary reactor (terminal end). Said horizontal rotary reactor
further
comprises a device for internal heating.
CA 02349867 2001-05-04
Said feeder comprises a screw Feeder or a reciprocating feeder.
Said spiral stirring reactor comprises a second cylindrical housing, one end
of which
is connected with the first treatment chamber; a spiral stirrer, installed in
the second
s cylindrical housing a second treatment chamber, arranged at another end of
the
second cylindrical housing and a spiral drainer, installed at the bottom of
the second
treatment chamber.
A tired bed is installed in the interior upper part of said first and second
chambers
respectively.
The apparatus according to the invention, if desired, further comprises a
pretreatment
device, by which the moisture in the materials can be removed.
The pretreatment device may be designed a shape like the first reactor. The
temperature therein may be maintained by hot uses and is not needed as high as
in
the first reactor.
The apparatus according to the invention further comprises a device for
collecting
hydrocarbons, which may be a conventional device for separating oil and water
in the
art. For example, it may include a condenser, a tank for collecting
hydrocarbons and a
water-sealed tank.
BRIEF DESCRIPTION OF THE DR_WVINGS
Fig. 1 is a schematic view of a preferred embodiment of the apparatus
according to
the invention.
DETAILED DESCRIPTION OF THE INVENTION
According to the process of the invention, the residential trash or waste
and/or organic
waste materials, pretreated or not are successively introduced into a sealed
horizontal
rotary reactor by a screw feeder. The reactor is driven to rotate and heated,
and the
first cracking is carried out therein. Gaseous hydrocarbons resulting from the
reaction
3p is drained out of the reactor. At the same time, resultant residues, which
have not been
decomposed completely in the reaction, are successively charged into an other
sealed
spiral stirring reactor. The spiral stirring reactor is heated and a screw
stirrer therein is
electrically driven to rotate continuously. The second cracking is carried out
in the
CA 02349867 2001-05-04
J
spiral stirring reactor at a high temperature to fully decompose organic
components in
the residues from the first cracking. Meanwhile, inorganic residues resulting
from the
second cracking are successively discharged out of the spiral stirring
reactor. Gaseous
hydrocarbons from the second cracking are drained out of the reactor and
collected.
In said process, both the first and second cracking comprise a pyrolysis
reaction
and/or a catalytic cracking. Pyrolysis may be carried out alone if no
catalytic cracking
is needed. Catalytic cracking undergoes in the fixed bed installed inside the
reactors.
Heat needed in the catalytic cracking is supplied by the reactors themselves.
The
catalyst may not be carried in the fixed bed if no catalytic cracking for the
materials is
needed. The cracking is carried out at an atmospheric pressure or higher. In
general,
the cracking is performed at a pressure of 0.02-0.6NIPa. The temperature of
the first
catalytic cracking is maintained at 350-600°C, and that of the second
catalytic
cracking at 600-1200°C. Preferably, the temperature of the first
catalytic cracking is
1~ kept at 400-X00°C and that of the second catalyrtic cracking at 600-
800°C. The
catalyst used in the invention is selected from catalyst SR-l, which comprises
~%
CHO-1 (commercial name, produced by Qilu Petroleum & Chemical Co., China),
20% REY, 30% mercerized zeolite and 45% catalyst ZSM-~, by weight.
The apparatus of the invention mainly comprises a horizontal spiral reactor, a
spiral
stirring reactor and a device for collecting hydrocarbons.
Said horizontal rotary reactor comprises a cylindrical housing, supported
thereunder
by several groups of circular brackets (two each group) on the round under the
2~ housing for rotating clockwise or counter-clockwise; a circular gear wheel,
looping on
the outer wall of the cylindrical housing and connected therewith or fixed
thereto by
means of welding or a binder bolt to drive the housing to synchronously
rotate; a
spiral strip steel, fixed on the inner wall of the cylindrical housing like a
female screw;
a feeder, arranged at an end of the horizontal spiral reactor, the stationary
outer wall of
which is connected with the rotated housing of the reactor by virtue of a
mechanically
sealing method and other sealing methods in the art; and the first treatment
chamber,
installed at another end of the horizontal spiral reactor, which is stationary
and
connected with the rotated housing by means of a mechanical seal or other
sealing
methods in the art; and a fixed bed, vertically installed at the upper inside
said first
3~ treatment chambers and connected with an outlet of the reactor for
discharging
gaseous products.
Said spiral stirring reactor comprises a cylindrical housing, fixed on the
ground and
CA 02349867 2001-05-04
connected with an inlet for the materials at the upper of one end thereof; a
second
treatment chamber, arranged at another end of the cylindrical housing a fixed
bed,
vertically arranged at the upper inside the second treatment chamber and
connected
with an outlet of gaseous products; a spiral stirrer, installed in the
cylindrical housing
and driven by a governor motor; a spiral drainer, installed at the bottom of
the second
treatment chamber, wherein an outlet for the residues in the second treatment
chamber
is connected with an inlet for the materials in the spiral drainer.
Said device for collecting hydrocarbons may be a conventional device for
separating
oil and water in the art. For example, it may include a condenser, a
hydrocarbons
collecting tank and a water-sealed tank.
A preferred embodiment of the process of the invention comprises grounding the
residential trash or waste and/or organic waste materials to be of a diameter
below 35
t ~ centimeters; charging resultant materials into the sealed horizontal
spiral reactor;
rotating and heating the horizontal rotary reactor to perform the first
cracking
introducing the residues from the first cracking into the sealed spiral
stirring reactor to
undergo the second cracking, while draining gaseous substances resulting from
the
first cracking out of the horizontal rotary reactor away; and collecting
gaseous
hydrocarbons produced from the first and second crackings in virtue of the
conventional means. The residues from the second cracking have been completely
decomposed, and contain, therefore, no organic components. The residues are
ground,
magnetically selected and separated to obtain industrial fillers and waste
metals.
In the above process, the cracking comprises pyrolysis and/or catalytic
cracking. Only
pyrolysis proceeds if the materials such as the residential trash or waste
contain less
organic components. Both pyrolysis and catalytic cracking proceed when the
materials contain a lot of polymeric substances such as waste plastics, waste
robbers
and waste oils, and the like.
The catalytic cracking is carried out in the fixed bed installed in the
reactors. Heat
needed for the catalytic cracking is supplied by that inside the reactor. The
temperature of the first cracking is kept at 3~0-600°C and that of the
second cracking
at 600-1200°C. The actual temperature depends on the properties of the
materials to
3~ be treated. The catalyst selected from SR-1 is carried on the fixed bed.
The catalyst
SR-1 comprises ~% CHO-l, 20% RE Y, 30% mercerized zeolite (molar proportion
between Si and Al being 12:1) and 4~°ro ZMS-~. It is produced by fully
mixing all the
above components.
CA 02349867 2001-05-04
7
The reactions can be carried out at the atmospheric pressure or higher. The
gaseous
products resulting from the first and second crackings are sequentially
condensed and
separated to get hydrocarbons with different fractional cuts and combustible
gases by
~ the conventional manner. The inorganic residues resulting from the second
cracking
are discharged out of the spiral stirring reactor. They are ground and
magnetically
selected to obtain inorganic fillers in industry and waste metals.
The materials of residential trash or waste and,~or organic waste materials to
be treated
in the process of the invention comprise residential trash or waste, waste
products,
waste plastics, waste robbers including waste tires, sludge, human or animal
excrements, woodflours, cmde oils, waste oils, heavy oils and any other
materials
containing organic or polymeric components.
A preferred embodiment of the apparatus of the invention comprises the
horizontal
spiral reactor, the spiral stirring reactor and the device for collecting
hydrocarbons.
The horizontal rotary reactor comprises a cylindrical housing, supported
thereunder
by several groups of circular brackets (two each group) on the ground for
clockwise
30 or counter-clockwise. A thermal insulation is positioned around the
housing. A
heating layer is situated between the housing and the stationary thermal
insulation.
Flue gases at a high temperature enter the thermal insulation to heat the
housing from
one end of the heating layer and are drained away from another end thereof.
The
horizontal rotary reactor may be designed as an inner-heating style. For
example,
2~ pipelines for flue gases may be fixed at the middle of the reactor. The
temperature
needed in the reactor can be kept with the flue gases through the pipelines.
In this case,
only the thermal insulation is needed and the heating layer can be omitted.
The spiral
strip steel is fixed to the inner wall of the housing like a female screw,
which can
drive the materials in the reactor forwards or backwards when the housing is
rotated.
30 One end of the housing is connected with a screw feeder or a reciprocating
feeder, and
another end thereof is connected with the first treatment chamber. The
mechanical
seal or other sealing manner in the art is used to connect the rotary housing
with the
stationary screw feeder, the first treatment chamber and the thermal
insulation,
respectively. The fixed bed is installed at the upper inside the first
chamber. The
3p Qaseous products resulting from pyrolysis are drained out of the reactor
away through
the fixed bed.
Said spiral stirring reactor comprises a cylindrical housing, fixed on the
ground. A
CA 02349867 2001-05-04
rotary spiral stirrer is arranged in the housing. Two ends of the housing are
respectively connected with an inlet of the residues from the first cracking
and the
second treatment chamber. A heating layer, which is embraced by a thermal
insulation,
is positioned over the housing. An inlet and an outlet of the flue gas for
heating the
housing are designed at two ends of the heating layer. The gaseous products
resulting
from pyrolysis enter the fixed bed installed at the upper in the second
treatment
chamber to perform catalytic cracking. Resulting gaseous hydrocarbons
therefrom
then are drained out of the reactor away via an outlet connected with the
fixed bed.
The invention is further described with of help of the Drawings as follows.
According to the invention, the apparatus, referred to Fig. 1, comprises a
horizontal
rotary reactor 1, a spiral stirring reactor 26 and a device for collecting
hydrocarbons
including a condenser 23, a hydrocarbons-collecting tank 24 and a water-sealed
tank
1~ 2~.
The apparatus of the invention further comprises a pretreatment device 32, if
necessary.
Horizontal rotary reactor 1 comprises a cylindrical housing 22, supported
thereunder
on the ground by several groups of circular brackets 5 (two each group) for
making
the housing rotate flexibly. A circular gear wheel 6, with the same diameter
as the
outer layer of the housing 22, is fixed to the outer wall of the housing 22.
Gear wheel
6 is gripped by a small gear wheel 7 driven by a governor motor 4. Gear wheel
6
rotates accomanying small gear wheel 7 by driving governor motor 4 to rotate,
and
thereby the housing is driven to synchronously rotate therewith. A heating
layer 11,
embraced by a stationary thermal insulation 9, is located around the housing.
Flue
uses for heating the housing enter the heating layer 11 from one end thereof
and are
drained away via another end thereof. Alternatively, pipelines for flue gases
may be
installed at the middle of the reactor (not shown in the Fig.). The
temperature needed
for the reaction in the reactor is kept with flue gas through the pipeline. In
this case,
the heating layer is not needed. The inner wall of the housing 22 is
homogeneously
distributed by a spiral strip steel 2 like a female screw. When the housing 22
is rotated
clockwise or counter-clockwise, the materials in the reactor are driven
thereby to
3~ move forwards or backwards. One end of the housing is connected with a
screw stirrer
(a reciprocating stirrer) 3 and the other end thereof connected with the first
treatment
chamber 13. The mechanical seal or other seal manner in the art is used to
connect
the rotary housing ?? with the stationary screw feeder 3, first treatment
chamber 13
CA 02349867 2001-05-04
and thermal insulation 9, respectively. A fixed bed 14 is vertically installed
at the
upper inside first treatment chamber 13 and connected with an outlet 1 ~ for
discharging gaseous products resulting from the cracking. The gaseous products
enter
a tank for collecting hydrocarbons 24 via a condenser 23. The gases not being
condensed are introduced into a water-sealed tank. 2~ and discharged from the
top
thereof. Resulting residues from horizontal rotary reactor 1 directly enter an
inlet 18
of a spiral stirring reactor 26 through the first treatment chamber 13. Spiral
stirring
reactor 26 comprises a cylindrical housing 21 fixed to the ground. Two ends of
the
housing 21 are respectively connected with an inlet 18 for the feedings and
the second
treatment chamber 27. A screw stirrer 19 driven by a governor motor ~ is
installed in
the housing 21. A heating layer 11, embraced by a stationary thermal
insulation 9, is
located around the housing 21. An inlet 12 and an outlet 8 of flue gases at a
high
temperature for heating the housing 21 are arranged at two ends of the heating
layer
11. Gaseous hydrocarbons resulting from the second cracking are drained out of
the
1~ reactor away via a fixed bed 16. The gaseous products enter a tank for
collecting
hydrocarbons 24 via a condenser 23. The gases not being condensed are
introduced
into a water-sealed tank 25 and discharged from the top thereof.
The apparatus of the invention further comprises a pretreatment device 32 when
water-containing materials are to be treated. The device 32 may be designed to
be
similar to the first reactor, as shown in Fig. 1. The same reference numeral
therein
represents the same element as in the first reactor, provided that the
temperature in the
device 32 can be maintained at 100-200C and the materials heated by means of
directly contacting a hot wind. Reference numerals 30 and 31 represent an
inlet and an
2~ outlet of the hot wind, respectively.
The process of the invention will be filrther explained in combination with
Fig. 1.
The residential trash or waste and/or organic waste materials are ground to be
a piece
with a diameter below 35 centimeters. The resultants then are charged into a
hopper
28. If the materials are flLlld, they may be pumped into hopper 28. The
materials are
driven by screw feeder 3 to enter horizontal rotary reactor 1. Flue gases of
high
temperature from heating furnace 10 supply the reactor 1 with heat needed
therein via
heating layer 11. Gear wheel 6 is driven by small gear wheel 7, which is
driven by a
3~ governor motor, thereby circular housing 22 is synchronously rotated. The
materials
in the reactor move forwards under the action of spiral strip steel 2
installed in the
inner wall of the reactor. Governor motor 4 can be regulated to rotate
clockwise or
counter-clockwise so that the reactor 1 may synchronously rotate. The
materials in the
CA 02349867 2001-05-04
reactor 1 are heated to perform a pyrolysis reaction and the residues
resulting
therefrom fall into spiral stirring reactor 26 through the first treatment
chamber.
Gaseous hydrocarbons from the reaction enter fixed bed 14 to perform catalytic
cracking. The catalytic cracking is not carried out if no catalyst is carried
in the fixed
bed. Gaseous hydrocarbons generated from the reaction enter a condenser 23 via
an
outlet of the reactor, then enter a tank 2~1 for collecting hydrocarbons. The
collected
hydrocarbons may be fractionalized to be gasoline, diesel and heavy oil. The
heavy oil
can be returned to the reactor 1 to perform cracking or sold as a fuel. Gases
not being
condensed can be introduced back to the furnace 10 to burn after they enter
water-
10 sealed tank 2~. The reactor 1 according to the invention has significant
advantages
such as quick reaction, high efficiency of heat transfer, unlikeness of
materials' being
coked and successive production process. To meet the requirements of the
industry,
the reactor 1 should be designed as large as possible. However, the larger the
reactor
is, the more readily the reactor deforms at a high temperature. Thus, the
reactor is
hard to rotate. Therefore, it is desirable to undergo the first cracking at a
relatively low
temperature. The problem resulting therefrom is that the cracking reaction is
not
complete at such a low temperature and organic components in the materials are
not
thoroughly decomposed.
To solve the problems, residues from the reactor 1 are introduced into spiral
stirring
reactor 26 to undergo further second cracking at a higher temperature. Flue
gases of
high temperature from burning furnace 10 supply the reactor 26 with heat
throujh
heating layer 11. Screw stirrer 19 in the reactor 26 is driven to rotate by
governor
motor 4. The second cracking of the residues from the reactor 1 proceeds at a
higher
2p temperature. The amount of the materials significantly decreases after the
first
cracking. The reactor 26 therefore is designed to be of a smaller volume. The
reactor
26 is not readily deformed at a higher temperature because the reactor is of
the small
volume and arranged stationary. Even though the reactor 26 is slightly
deformed it has
no influence on the second cracking, provided that it does not effect the
rotation of the
screw stirrer. Organic components in the materials are completely decomposed
to
gaseous hydrocarbons during the second cracking. Resultant gaseous
hydrocarbons
enter the fixed bed 16 to perform catalytic cracking. The resultant
hydrocarbons
drained out of the reactor 26 enter the condenser 23, and then reach the tank
24 for
collecting hydrocarbons. Gases not being condensed are introduced back into
the
3~ burning furnace 1 to burn after they enter the water-sealed tank 2~. The
residues
resulting from the second cracking contain no organic components. They are
drained
out of the reactor 26 by spiral drainer 29 installed at the bottom of the
second
treatment chamber 27, and are ground, magnetically selected and separated to
obtain
CA 02349867 2001-05-04
industrial materials such as inorganic fillers, waste metals and the like.
The following examples are presented in order to better communicate the
invention.
The examples are not intended to limit the scope of the invention in any way.
Example 1
Resident wastes in winter from Beijing were ground into pieces with a diameter
below 35 centimeters. After pretreated (dehydrated), the materials were
charged into
the hopper 28 and entered the reactor 1 by virtue of the screw feeder 3. A
desired
amount of the catalyst SR-1 was carried in the fixed bed 1=1 in the reactor 1.
The
reactor 1 was heated by flue gases of high temperature from the burning
furnace 10
via the heating layer 11 and driven to rotate. The materials were heated to
perform the
first cracking including pyrolysis and catalytic cracking in the reactor 1.
The cracking
was carried out at a temperature of 400-500°C under a pressure of 0.02-
0.3NIPa.
Gaseous hydrocarbons produced from the cracking were drained out of the
reactor 1
and entered the hydrocarbons-collecting tank 24 for generating hydrocarbon
oils with
a low boiling point via the condenser 23. Combustible gases not being
condensed
Such as H, and hydrocarbons C,-C~ were introduced back into the burning
furnace 10
to burn thlOllgh the water-sealed tank 25. The residues resulting from the
first
cracking felt into the reactor 26 through the bottom of the first treatment
chamber 13
to perform the second cracking at a higher temperature. Heat needed therein
was
supplied with flue gases produced from the burning furnace 10. The second
cracking
was carried out at a temperature of 600-800°C under a pressure of 0.02-
0.3 NIPa.
Gaseous products produced from pyrolysis reaction of the second cracking went
up
into the fixed bed 26 installed at the upper of the reactor 26 to undergo
catalytic
cracking with the catalyst SR-1. Heat needed for the cracking was maintained
by the
reactor itself. Residues from the second cracking were discharged into the
second
treatment chamber 27 and drained out of the reactor 26 away by the spiral
drainer 29
at the bottom the chamber 27. Gaseous hydrocarbons resulting from the second
cracking were introduced into the condenser 23 and then entered the tank 2=1
to get
hydrocarbon oils with low boiling points. The collected hydrocarbon oils from
the
first and second cracking were further fractionalized, if desired.
Analysis for the materials and products were given as follows.
Materials (by weight): volatiles 78%, fixed carbon 13.9%, ash 10.1%
Elementary analysis for the materials: H 5.6%, C 53.1%, ~ 8.S%, O 21.8%, S
0.6°r~.
Products (by weight): hydrocarbons 28%, gas (hydrocarbons) 35%, inorganic
substances and metals 16%, moisture 21%.
CA 02349867 2001-05-04
12
Example 2
Waste tires were treated in the same manner as in Example 1 except that the
pretreatment of the materials was not needed. The condition of the treatment
and the
result thereof were given as follows.
Materials: tires 1000kg
Condition:
Temperature of the first cracking: 450-600°C
Pressure of the first cracking: 0.08-0.4MPa
Catalyst for the first cracking: SR-1
Temperature of the second cracking: 7~0-8~0°C
Pressure of the second cracking: 0.08-0.4MPa
Catalyst for the second cracking: SR-1
Products:
Gasoline 98kg (RON 93.5); Diesel 432kg (cetane number 59, Freezing Point < -
20°C);
Combustible Gases (H,, C,-C,) 90kg; Steel Wire 60kg; Carbon Black 320kg
(organic
content <0.1 %).
30
3~
