Note: Descriptions are shown in the official language in which they were submitted.
` 11,451
~13Z~7~
Detailed Explanation ~f the Invention
The present invention relates to a process for produc-
ing various pitches of high quality from tar pitch which
has been produced by thermally cracking petroleums at high
temperatures and, mor~ particularly to a process for.pro-
ducing a pitch of high quality with high yield which
comprises adiabatically thermally cracking a suitable
starting oil as defined hereinafter in an ACR thermal crack-
ing process using hot steam as a heat medium at a relatively
high temperature for a relatively short period of time in
a condition that ethylene/acetylene ratio is at least 50 to
obtain gaseous hydrocarbons containing olefins such as
ethylene, propylene, butadiene and/or light gases such as
hydrogen, methane and carbon monoxide; light aromatic com-
pounds, such as benzene, toluene, xylenei and tar pitch
as heavy aromatic compounds and subsequently heat-treating
the tar pitch to obtain a pitch of high quality.
The starting oil to be cracked in the ACR process is
one of the essential elements of the present invention and
defined as follows. That is, the starting oil is selected
from (i) suitable oil fractions which have been produced
by treating crude oils in a suitable process (for example,
normal pressure distillation, vacuum distillation, various
processings with hydrogen, pyrolysis, solvent extraction)
. to remove impurities including asphalt fraction (asphaltene),
sulfur, metal contents, nitrogen contents to asceptable or
'`~ allowable amounts and contains heavy oil fractions having a
boiling point above 350C. (such as vacuum gas oil) and (2)
crude oils containing the above impurities in acceptable
- 2 -
11,451
~ Z~7Z
amounts and containing heavy oil fractions having a boil-
ing point above 350C. Thus, the starting oil of the present
invention has a wide distribution of molecular weights
ranging from light fractions such as naphtha to heavy frac-
tions, which, together with the thermal cracking conditions
of the ACR process, produces a great amount of tar pitch
of good quality. Further, this tar pitch is converted into
a pitch of high quality with high yield by the heat-treatment
of the present invention uslng a high tem?erature, a short
residence time and a high pressure.
The ACR process which processes the above-defined start-
ing oil should be understood to be the following process
(see "Chemical Engineering Progress" Vol. 71, No. 11, 1975,
Nov ., pp 63- 67 , entitled "Ethylene from Crude Oil")
Brief Explanation of ~he Drawings
Fig. 1 is a flow sheet showing the ACR thermal cracking
process for treating starting oils, Fig. 2 is a flow sheet
showing the conventional process for pitch production appli-
ed to the tar pitch formed as a by-product in the convention-
al ACR process, and Fig. 3 is a flow sheet showing the pitch
production according to the present invention.
Referring to Fig. 1, superheated steam is generated
in a burner 1 by the combustion of oxygen and fuel (mainly
H2 or CH4 or suitable liquid hydrocarbon) to generate a
combustion gas of a temperature of about 2000~C. (Also,
in another case, a combustion gas containing hot H2, CO etc.
may be generated simultaneously with hot steam by changing
the ratio of oxygen to fuel.) This steam is supplemented
by externally supplied superheated steam which is for
`` ~perature control. Preheated starting oil as defined
above is injected into the combustion gas at a location
downstream of this combustion zone to crack it. The
starting oil and the combustion gas a-e mixed and ac-
celerated by an orifice or throat to enter a diffuser
(reactor) 2 where adiabatic cracking is performed. There-
after, the steam and the reaction product are ~uenched
with quench oil 4 (Q) in a ~uencher 3 and a cooler 4
(provided with a water jacket of high temperature and high
1~ pressure which generates steam for heat recovery) and tar
pitch and gaseous product a-e separated in a separator 5,
from which the gaseolls product is led to a fractiona~or 6
to separate a stre~ of light hydrocarbon oil 10. An
olefi~-rich stream 9 (containing ethylene, acetylene,
propylene, butadiene, carbon monoxide, hydrogen, etc.) is
led to succeeding refining step~ via ~ separator 7. The
reaction temperature of the reactor 2 is a~out ?00-1000C,
the pressure is less than about S ~g/cm2(G) and the reac-
tion time is about 3-100 milliseconds. ~n most cases, a
part of hydrogen and methane gases of the produced crackea
gases is recycled as a fuel for generating the superheated
steam. The tar pitch in the bottom residue of the separ-
ator 5 is relatively rich in aromatic rings. A part of
the bottom residue of the fractionator 6 (heavy tar) is
recycled by ~ pump B as the quench oil 4 (~ and another
part is combined with the tar pitch from the separator 5
for refining in succeeding steps. In short, the ACR
thermal crackins pr~cess in the present invention is a
proce~s where the ~ove-defined ~tarti~g ~il is
-- 4 --
.
~L~3Z~'7~ 11,451
adiabatically thermally cracked in a reactor 2 using steam
as a heat medium under the above-mentioned conditions, i.e.
a temperature of about 700-1000C, a pressure of less than
5 kg/cm (G), and a time of 3-100~ sec. and a ratio of
ethylene/acetylene of ~ore than 5 (weight ratio).
In this case, if the oleflnes to be produced by the ACR
thermal cracking process consist mainly of ethylene, a
temperatur~ of 8;0-1000C is mostly used but generally a
reaction temperature of 700-1000C may be used. Suf~icient
cracking will not ~e expected below 700C while, above
1000C, not only acetylene in the cracked gases but also
carbonacious material in the tar pitch will be undesirably
increased.
Incidentally, in this specification, tar is defined
as oil having a boiling point between 200C and 550C
and relatively high aromacity and pitch is defined as one
having a boiling point above 550C. Further, tar having
a boiling point between 200C and 350C is called light
tar and tar having a boiling point between 350C and 550C
i5 called heavy tar.
The tar pitch from the ACR process using the above-
defined starting oil is of high quality and is relatively
large in quantity because of the fact that the tar pitch
is formed under cracking conditions of relatively high
temperatuxe and short time from a starting oil containing
relatively heavy fractions. That is, the ACR process
in the present invention is characterized in that the
thermal cracking is performed in an adiabatic condition
using a high temperature steam as internal heat medium
_ 5 _
~32~372
for a short period of time thereby to make it possible to
sufficiently crack even heavy fractions to give a greater
amount tar pitch. For example, in the working examples,
the quantity of tar pitch amounts to at least 50 wt% of
that of ethylene. Also, because of the reaction condi-
tions which result in production of ethylene and propylene
as main products (E/A>5~ carbonaceous materials are
little formed in the reaction and accordingly the tar pitch
contains less quinoline insoluble content (giant molecular
materials) and less free carbon content. Further, because
of the fact that the tar pitch is from a starting oll con-
taining heavy fractions, the tar pitch is different from
that used in the conventional pitch refining process in
that it contains fractions of suitably large molecular
weights and is rich in aromaticity.
The present invention is based on the discovery that
tar pitch of high quality is obtained with high yield by
the ACR process wherein the above-defined starting oil is
processed in the above-defined conditions, said starting
oil containing wide range of fractions ranging from light
fractions (such as naphtha) to heavy oil fractions or at
least heavy oil fractions having a high boiling point.
In the past, the following process was relied on in
preparing pitch from bottom residue of ACR thermal crack-
ing process. That is, referring to Fig. 2, grade A pitch
(a pitch having a lower softening point and used as quench
oil or impregnation pitch) and the bottom residue of a
fractionator of ACR system are pumped with a pump P to a
soaker S where the material is treated, typically, at about
-- 6 --
11, 45
1~3'~07~
370C and about 3 kg/cm2(G) for about 40 hours. The un-
stable components in the tar are converted into pitch, which
is then withdrawn from the bottom of the soaker as a binder
pitch (grade C pitch). On the other hand, the tar contain-
ing light fraction is led from the top of the soaker to the
fractionator. In such conventional technique, the tar
fraction which is. not converted into pitch amounts to a
; substantial portion and the yield in producins grade C pitch
from grade A pitch is lower than the present invention.
Also, if the grade A pitch is treated at ~ higher temperature
for a lon~er period of time in order to increase the yield,
there was a possibility that the portion of the pitch having
a high softening point is converted into coke ~r precursor
of coke, a part of which sticks to the wall of the soaker.
Further, the reaction temperature is relatively low, result-
ing in a large soaker and high plant and operation costs.
On the other hand, a process similar to the present in-
vention has been proposed by Japanese Patent Application
Publication No. 29602/1973 (Shell),wherein a petroleum frac-
tion having a boiling point between 50 and 200~C or having
a boiling point between 170 and 370C is thermally cracked
at a temperature above 750 to produce tar as a by-product,
which is then separated into a light fraction and a heavy
fraction. The heavy fraction is heated at 350-500C and
the product pitch is separated from the resulting product.
The treatment is perfor~ed for example at 450C for 15 min-
utes or at 350C for at least 25 hours while the pressure
is less than 15 atm. This prior art technique has a few
problems in that the range of molecular weight distribution
, 45
~32~7Z
of the raw material is narrow and hence the tar pitch is
less in quantity with respect to the raw material to be
cracked that the total pitch yield is low because no
particular efforts is made to increase the pitch yield as
it states that the fractions having boiling points below
350C do not contribute to the production of the pitch (low
yield), and that, more importantly, the raw materials are
restricted to light ones due to the fact that the thermal
cracking reaction is not "adiabatic", with the result
that the quantity of tar pitch is less and pitch content
in the tar pitch is also less.
On the other hand, the process disclosed in Japanese
Patent Application Publication No. 17563/1976 are similar
to the process of the above Japanese Patent Application
Publication No. 29602/1973 in the point that it utilizes a
relatively light starting oil similar to the starting oils
in the above-mentioned patent and the tar pitch to be heat-
treated is that obtained by using an externally heated
tube reactor and hence the total quantity of available
tar pitch is restricted. Further, according to the teach-
ing of this patent, the tar pitch is treated under pres-
sure of 20-200 kg~cm at temperature of 400-600C for
10-1200 seconds, tar fraction is removed from the by-
product tar pitch, and the remaining pitch is treated at
300-480C under pressure of 1-50 kg/cm2 for 1-10 hours.
However, as the pitch is produced from the pitch frac-
tion in the tar pitch from which the tar fraction is
removed, there is no idea of producing pitch from the
tar with high yield and thus the total yield of the
-- 8 --
~;3~2 11, 451
pitch is restricted.
This can also be readily seen from the working examples
of said application. That is, according to Japanese Patent
~pplication Publication No. 17563/1976, the composition of
the starting tar pitch comprises less than about 15% of
pitch. Comparing this with about 30 wt% of pitch in the tar
pitch obtained according to the present invention, it is
seen that the pitch content of the application is low.
Further, according to Japanese Patent Application Publica-
tion No. 17563/1976, the yield of the pitch is about 40%,
based on the starting tar pitch, which is quite different
from the yield of more than 60 wt% of the present invention.
Further, looking at these cases from a commercial
standpoint, an ethylene production plant by naphtha pyroly-
~; sis and an ACR plant, both of the scale of 450,000 tons,
. produce(s) 15,000-30,000 tons and 200,000-300,000 tons of
tar pitch, respectively, and 5,000-10,000 tons and 70,000-
100,000 tons, respectively, in terms of pitch content.
Thus, from the industrial standpoint they are quite differ-
ent from each other.
Further, the technique in Japanese Patent Application
Publication No. 43641/1977 was proposed by the present in-
ventor, et al, in which a crude oil or a suitable petroleum
: fraction is thermally cracked at 900-2000C for less than
0.1 second, the formed hydrogen, acetylene, olefins and tar
materials are fractiona~ed and the separated tar ma~erials
are treated at 250-550C for 1 min.-5 hours for refining the
materials. The product is separa~ed into pitch fraction and
other fractions. However, in this case, as there is given no
consideration to the raw material ~o be crac~ed, the quality
11,451
3'~
of produced pitch is low when a crude oil is used as the
starting oil and low in yield when naphtha is used.
Particularly, it should be noted that the thermal crack-
ing is performed in very severe conditions, so that themain product sases of ~the thermal cracki~g reaction con-
tain a large amount of acetylene (ethylene/acetylene
ratio is less than 5). Correspondingly, the by-product
tar pitch contains free carbon and quinoline insoluble
in greater amounts compared with the tar pitch from the
defined ACR for producing ethylene as a main product using
the defined starting oil. Further, looking the matter
from the commercial standpoint, acetylene production is
restricted in quantity under the present industrial circum-
stances and accordingly, the quantity of tar pitch, too.
The present invention provides a process for produc-
ing pitch of high quality (good thermal stability and
superior coking property) with high yield within a much
` shorter priod of time compared with the conventional pro-
cess without causing carbon deposition, by subjecting a
starting oil as defined to an ACR process as defined to
form by-product tar pitchl carrying out as processing
steps of thusly formed tar pitch a first step characterized
by treating the tar pitch for a short period of time
(within about 15 minutes) at relatively high temperature
and relatively high pressure and then carrying out a second
step characterized by treating the tar pitch for a com-
paratively long period of time (within several hours) at
relatively low temperature and low pressure.
The second step is preferably performed in a kettle-
-- 10 --
11,451
~3'~'7;~
type soaker. It has been found that a high efficiencypitch produc~ion ~s made possible in cooperation with
the first step performed preferably in a tube heater.
The first step mainly converts e~ficienlly those
fractions o~ lower molecular weight in the ACR tar pitch
- having a wide distribution of molecular weights (by-
product tar pitch obtained from adiabatic thermal crack-
ing at 700-1000C with ethylene/acetylene ratio of at
least 5) into a heavy tar and a pitch of high aromacity
while suppressing evaporation, and on the other hand,
decomposes a part of pitch of high molecular weight into
gaseous components as well as upgrading tar and pitch
components to attain a pitch of high quality. The second
step mainly conditions the quality of the product pitch
while ultimately converting tar pitch into the product
pitch with high yield through polycondensation reaction
and the like.
The pitch conte~t of tar pitches to be treated accord-
ing to the present invention should be controlled within
a range of 20-80 wt~, and preferably 25-60 wt%. Pitch
content below 20 wt~ will increase the process cost and
make the process uneconomical while pitch content over 80
wt% will cause carbon deposition, thereby making the oper-
ation difficult.
Tar pitch produced by thermal cracking processes
other than the ACR process may be introduced into the tar
pitch treatment process according to the present inven-
tion as a minor constituent. For example, conventional
ethylene bottom oil which is a by-product of the
ll, 45
3~72
conventional process of ethylene production using the con-
ventional tubular furnace such as in Japanese Patent Appli-
cation Publication Nos. 17563/1976 and 29602/1973 may be
treated according to the present invention. Other tar
pitches which have a relatively high aromaticity and a
carbon/hydrogen (atomic) ratio exceeding 1/0.65 (or specific
gravity exceeding 0.95 at 15~/4C) and having low asphal-
tene content may be treated in the present process as a
- minor constituent to produce pitch products rich in aroma-
; 10 ticity. However, the yield and the quality of the product
pitch are inferior to those of pitch product produced using
only the tar pitch of the ACR process.
Further, olefins may be added to the tar pitch process
according to the present invention in order that the con-
version of tar into pitch is accelerated or unstable olefins
are converted to stable ones at the high temperature and
high pressure conditions in this process (refer to ll in
Fig. l). More particularly, such materials as indene,cyclo-
pentadiene, styrene, methylstyrene formed and accumulated
in the ~CR thermal cracking process may be appropriately
recycled in the process of the present invention so that
they participate in the acce1eration of pitch formation
and are stabilized by themselves in this process, whereby
the thermal stability of tar in the entire system of the
ACR process is enhanced and consequently the entire system
is stabilized, contributing to prevention of the fouling
problem in the system.
The tar pitch treating process of the present inven-
tion will now be described in greater detail. The process
- 12 -
11,451
~3~0~
is a process of producing pitch which comprises heat-treat-
ing tar pitch in a heater (typically, tubular and externally
heated) at a temperature of about 450C - 550C under a
pressure o about 50 - 150 kg/cm2(G~ for about 1-15 minutes
and then heat-treating-the tar pitch in a soaker (typically,
kettle-type) with or without agitator at a temperature of
about 350-450C under a pressure of about 0.5 - 10 kg/cm2(G)
for about 15 minutes - 10 hours. More preferred ranges for
the heater and soaker conditions are as follows.
Heater: temperature: 470-520C
pressure: ~0-120 kg/cm (G)
residence time: 2-8 mins.
Soaker: temperature: 380-420C
pressure: 0.5-5 kg/cm (G)
residence time: 0.5-5 hours
It should be noted that these conditions may vary with
in the above ranges depending on the starting material and
the specification of the product pitch.
The chemical reactions accompanying the present tar
pitch process are complicated and depend on the origin of
the starting material, pressure, time, concentration of
pitch in liquid tar, etc. ~owever, it is known that, in
general, gasification, decomposition (decrease in the mole-
cular weight), dealkylation, transfer of alkyl group, ring
formation, polymerization and condensation take place in
the temperature range of 350-550C. Evaporation and/or
distillation step may be suitably combined with the present
process so as to control the composition of the tar pitch
flowing in the system. Thus, the distillation may be
- 13 -
11,451
~ 13Z~t7~
carried out prior to the heater, or after the soaker.
However, the inlet condition of the process (that is, inlet
of the heater) is so controlled that the pitch content in
the tar pitch is in the range of 20-80 wt%, and preferably
25-60 wt%. Incidentally, Fig. 1 illustrates a manner of
combination of distillation step in the ACR process and
heater and soaker.
Fig. 3 illustrates one system for working the present
invention. Tar pitch derived from the ACR process (refer
to Fig. 1) is led first to a heater 13 and then to a soaker
14 from which the pitch is led through a line 15 to a
softening point adjusting vessel 18. The heater 13 is
preferably an externally heated tu~ular heater and treats
the tar pitch under the conditions described hereinbefore.
The soaker 14 is provided with a rotating agitator 17 and
treats the tar pitch under the conditions as already
prescribed. Element 21 is also a rotating agitator.
The outflowing streams from the tops of the soaker 14
and the soLtening point adjusting vessel 18 may be returned
to the fractionator 6 (Fig. 1) for conditioning the tar
pitch and for recovering gas constituents. Further, in
order to control the process and the product, a portion of
the output of the soaker 14 may be recycled as recycling
stream 16 to the heater 13, or the light and/or heavy tar
from the fractionator 6 may be fed to the heater 13 together
with the quench oil stream. Further, the streams from the
fractionator 6 may be first suitably heated and then added
to the heater 13 or the quench stream 4 (Q) for recycling.
These recycles are an important factor in adjusting
- 14 ~
11,451
~ ~ 3'~ 0 ~ 2
operational conditions of the process and the quality of the
pitch and also to increase the yield. At least one recycle
among them will be necessary in practice. Further, fuel gas
or inert aas may be injected into the soaker or the soften-
ing point control vess~el to control the pitch concentration
or the softening point. The product pitch is withdrawn from
l9. As seen from Table 4 and examples hereinafter described,
a pitch of high CV value can be obtained without causing the
viscosity to increase significantly.
In general, the properties of the pitch, which are
required for various pitches including electrode binder pitch,
are good graphitization, high densi~y, high aromatic content,
and thermal stability up to a relatively high temperature.
The followings are considered as a typical industrial
specification.
Softening point: 60-130C
Fixed carbon: ~45 wt%
BI: >20-50 wt%
QI: <20 wt%
2~ BI-QI:~20 wt%
These values are determined case by case by the requirements
for the final products. The pitch produced according to the
present invention can easily satisfy this specification.
From the foregoing, it has been made clear that the
tar pitch process of the present invention provides a pro-
cess for treating a tar pitch from the ACR thermal cracking
process at relatively high temperatures and under rela-
tively high pressure for relatively ~hort periods of time,
using a heater (tubular) and a soaker (kettle-type) and,
- 15 -
ll 45
3L13207~
if necessary, in comblnation with evaporation and fraction-
ation and using the concept of the above-mentioned recycles
to produce a pitch of high quality with hish yield. Fur-
ther, this process has an im~ortant feature over the con-
ventional process in that the entire process can be rela-
tively easily stabilized within a short period of time
when the feedstock to the process varies or the operational
conditions are changed because of the short average resi-
dence time in the process.
Although various types of starting material may be used
in the present tar pitch process as already descri~ed, the
tar pitches obtained from the ACR process using the starting
oils as defined in this specification have "good birth"
characterized by "high temperature and short time". On the
other hand, the process of the present invention produces
pitch products of superior quality from various tar pitches
because of their !'breeding" characterized by "relatively
high temperature, high pressure and short time".
The present invention will be fully understood from
the following examples.
Manufacturing Example 1
Accordina to the process flow as shown in Fig. 1, tar
pitch was prepared. All distillates of Arabian light crude
oil having the properties listed in Table 1 were intro~uced
into an ACR pilot plant of a capacity of 100 kg per hour
and light tar, heavy tar and quench oil were obtained.
They had the fractions as shown in Table 2. The operational
conditions of the ACR plant were as follows. Steam tem-
perature at the burner 1: about 2,000C, the weight ratio
- 16 -
` 11,451
'. ' .
~L~3~0~7f~
.
of the steam to the introduced starting oil (S/F~: 1.5,
temperature of the outlet of the reactor 2: 890C, reac-
tion time: 14.5 m sec., temperature of separator 5: about
300C, temperature of the bottom of the fractionator 6:
283C, pressure of the~ bottom of the fractionator: 3.0 kg/cm2
(G), temperature of the top of the fractionator: 136C.
The yield of the gaseous product was as shown in Table 3.
The cracked gas had a ethylene/acetylene ratio of about 15.
The pitch content in the product tar pitch was about 27 wt~.
From the heavy tar and the quench oil in Table 2 pro-
duced in Manufacturing Example 1, tar pitch formulations
and 2 were prepared by mixing them in suitable ratios. The
prepared tar pitch formulations are shown in Table 4.
Table 1
Arabian_ight Crude Distillate (Total Distillates)
Specific gravity 0.824
S content 0.89 %
C~C.R. tConradson carbon) 0.37 %
I.B.P. 30C
50 % 264C
E.P. 538C
Table 2
Tar Pitch
Light tar heavy tar quench oil
IBP 150C 260C 300C
10 % 206 296 350
260 360 47
340 480
380 510
7;~
Tar pitch yield (with respect to starting oil)
5.5 wt% + 2.5 wt% + 12 wt% = 20wt~(total)
(light tar) (heavy tar) (quench oil)
. .
Table 3
Cracked Gas Prod~cts (with respect to startina oil)
H2, CH4 10.0 wt~
C2H2 2.1
2 4 31.7
C2H6 2.4
3 4 0.9
3 6 9.6
C3H3 0.4
C4H4 0.2
C4H6 4-3
C4 8 2.0
C4Hlo 0.1
C as CO, CO2 and H2S 1.5
C5 - 160F 3.6
C6 ~ C8 Aromatic 9.2
C6 ~ C8 Non aromatic 1.8
Cg - 0.6
Total 80 wt%
- 18 -
11,451
~3207~
Table 4
Tar Pitch Formula,ion 1_ Tar Pitch Form.llaion 2
theavy tar + quench oil) (heavy tar + quench oil)
2.5 : 12 5 : 12
IBP - 350C 21.8 wt% 6.2 wt~ ~-
350 - 550C ~1.0 54.0
550C + 37.2 39.8
2 400C + 60.3 64.5
Properties of
400C + SP120C 121C
BI10.2 wt~ 11.0 wt~
QI 0 0
CV31.1 wt% 32.2 wt%
Example 1
The tar pitch obtained in Manufacturing Example 1 was
processed according to the process flow illustrated in Fig.
3, using an experimental system having a capacity of 1.5 kg/hr.
The heater 13 was an externally heated tube heater, the
soaker 14 was a kettle type vessel (although Fig. 3 is a
flow sheet of a practical plant, the experiment was performed
in a system of laboratory scale and the adjustment of the
softening point was performed in a usual distillator).
The operational conditions in the heater were as follows:
outlet temperature of the tube heater 13: 500C, pressure
in the tube heater: 100 kg/cm (G), residence time in the
heater: 5.5 min. Tar pitch formulation 1 in Table 4
prepared by mixing heavy tar and quench oil was introduced
into the experimental system. Thus, the tar pitch used
here corresponds to the bottom oil (a mixture of quench
-- 19 --
11,451
~ ~ 3 2 ~ ~
oil and bottom heavy oil from the fractionator) in Fig. 1,
which is fed to the heater. The treated tar pitch was then
introduced into the soaker and treated at a temperature or
400C under a pressure of 6 kg/cm (G) at a residence time of
1 hour. From the top of the soaker, 4.0 wt% pf a by-product
gas (gaseous at normal temperature and normal pressure) was
discharged and the yield of 360C + (1 atm) in the liquid
product was 61.5 wt%. This 360C + is the product pitch.
The pitch exhibited the following properties.
SP (softening point) (R & B)* 121C
BI (benzene insoluble)* 3~.8 wt%
QI (quinolin insoluble)* 1.2 wt%
CV (carbon value)* 49.6 wt%
*~ote: R & B, BI, QI .... Japan Industrial
Standard No. K-2425
Carbon value .... Japan Industrial
Standard No. M-8812
The pitch obtained in this example exhibited superior
properties as binder pitch for carbon electrode. As is seen
from this-example, a pitch of high quality for such as
binder is obtained with a high yield of 61.5 wt%.
Example 2
i Using the same system and the same tar pitch formulation
as in Example 1, the first step treatment was effected at
a heater outlet temperature of 500C under a tube heater
pressure of 50 kg/cm2(G) at a heater residence time of
5.5 min. and then the second step treatment was effected
at a soaker temperature of 400C under a pressure of 6
kg/cm2(G) at a soaker residence time of 1 hx. The by-product
gas discharged from the top of the soaker was 3.6 wt% based
- 20 -
11 45
2(~7Z
on the starting tar pitch and the yield of 360C + in the
liquid product was 60.2 ~. The pitch thusly produced had
the following properties and met the standard of electrode
binder pitch.
SP (R & B)120C
BI 33.7 wt~
Qr 1.1 wt~
CV 48.1 wt~
Example 3
Usins the same system and the same tar pitch formu-
lation in Example 1, the first step treatment was ef~ected
at a heater outlet temperature of 470C, under a heater
pressure of 100 kg/cm2(G) at a residence time of 10 min.
and then the second step was effected at a soaker temper-
ature of 400C under a soaker pressure of 6 kg/cm2(G) at
a soaker residence time of 2.5 hrs. The by-product gas
was 3.9 wt% based on the starting tar pitch and the yield
of the pitch content, i.e. 360C + in the liquid product
was 61.0 %-. The properties were as follows and the pitch
; 20 was satisfactory as a binder for electrode.
SP 120C
BI 34.1 wt%
QI 1.4 wt%
CV 49.0 wt%
Example 4
Using the same system and the same starting tar pitch
formulation as in Example 1, the first step was effected
at a heater outlet temperature of 450C under a heater
pressure of 100 kg/cm2(G) at a residence time of 10 min.
and then the second treatment was effected at a soaker
- 21
11,451
~ ~ 3'~ ~ 2
temperature of 400C under a soaker pressure of 6 ks/cm
at a residence time of 5 hrs. The by-product gas was 1.9
wt% based on the starting tar pitch formulation and the
yield of 400C + pitch was 54.9 wt% and the properties
were as follows.
SP 117C
BI 25.3 wt~
QI 0.3 wt~
CV 46.2 wt%
Comparing this example wlth Example 3, the BI content and
the pitch yield tend to be lowered at a heater outlet tem-
perature of 450C even if the other conditions are the same.
Also, it is seen that the lowering of the pitch yield
cannot be compensated by a longer residence time in the
soaker. The product pitch was not acceptable for a binder
pitch but was satisfactory as an impregnation pitch for
electrode.
Example 5
Using-the same system and the same tar pitch formu-
lation as in Example 1, the first step was effected at a
heater outlet temperature of 500C under a heater pressure
of 100 kg/cm (G) at a residence time of 2.5 min. and the
second step was effected at a soaker temperature of 425C
under a pressure of 6 kg/cm2(G) at a residence time of
1 hr. The by-product gas was 3.8 wt%, the yield of
360C ~ pitch was 60.3 wt~ and the properties were as
follows which was satisfactory as electrode binder.
11,451
1~3ZO'~
SP 120C
BI35.2 wt~
QI1.7 wt~
CVq3.2 wt%
Example 6
Using the same apparatus and the same tar pitch
formulation as in Example 1, the first step was effected
at a heater outlet temperature of 525C under a pressure
of 100 kg/cm2(G) at a residence time of 1 min. and the
second step was effected at a soaker temperature of 400C
under a soaker pressure of 6 kg/cm2(G) at a residence time
of 1 hour. The by-product gas was 3.7 wt~ and the yield of
360C + pitch was 60.0 and the properties were as follows,
which were satisfactory as a binder for electrode.
SP 121C
BI33.6 wt~
QI0.9 wt%
CV49.1 wt%
Example 7
Using the same system and the same tar pitch formu-
lation as in Example 1, the first step was effected at a
heater temperature of 500C, under a heater pressure of
100 kg/cm2(G) at a residence time of 1 min. and the second
step was effected at a soaker temperature of 425C under a
soaker pressure of 6 kg/cm2(G) at a xesidence time of
1.5 hr. The by product gas was 1.8 wl%, and the yield of
400C + pitch was 54~3 wt% and the properties were as
fOllGWS .
- ~3 -
11,451
~32~2
SP119C
BI23.5 wt%
QI0.5 wt%
CV45.8 wt%
The pitch is satisfac~ory as an inpreparation pitch.
Comparing this example with Example 5, it is seen
that, at such short heater residence time as 1 min., the QI
content and the pitch yield tend to be lowered even if the
other conditions are the same.
Example 8
rJsing the same apparatus as in Example 2 and using the
tar pitch formulation 2 in Table 4, the first step was ef-
fected at a heater outlet temperature of 500 DC under a
heater pressure of 100 kg/cm2IG) at a residence time of 5
mins. and then the second step was effected at a soaker
temperature of 400C under a soaker pressure of 6 kg/cm2(G)
at a residence time of 1.5 hr. The by-product gas was 3.8
wt% and the yield of 240C + pitch was 65.2 wt~ and the
properties were as follows.
SP121C
BI33.0 wt%
QI1.5 wt%
CV49.2 wt%
The pitch was satisfactory as binder pitch. Incidentally,
this example corresponds to the case where the conditions
of the bottom oil (an mixture of quench oil and heavy tar
from the fractionator) in Fig. 1 are changed. This can be
materialized by, for example, changing the recycling stream
from the fractionator to the quencher.
- 24 -
7f~
Although the above examples were described in relation
to production of pitches for carbonatious electrode indus-
tries, a person skilled in the art will readily understand
that the present invention is not restricted to pitches
for carbonaceous electrode industries but can be applied
to the production oS pitches for other purposes, without
departing from the spirit of the present invention.
- 25 -
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