Apparatus and method for thermocracking a fluid

A reactor for thermocracking a fluid comprising a heat exchanger having at least one tube for conveying the fluid stream from a respective tube inlet to a tube outlet while contacting the at least one tube with a high temperature medium to effect heat transfer to the fluid stream sufficient to cause thermocracking of the fluid. A quench is provided for discharging a quench liquid so as to be positioned within the thermocracked fluid stream exiting the tube outlet during a cracking operation to immediately lower the temperature of the thermocracked fluid stream sufficient to terminate further thermocracking of the fluid as it emerges from the tube outlet thereby preventing carbon deposition downstream.

FIELD OF THE INVENTION 
The present invention generally relates to thermal cracking (or 
thermocracking) including visbreaking of a hydrocarbon and more 
particularly towards an apparatus and method for such processes that 
reduces unwanted carbon deposits during the proceeds. 
BACKGROUND OF THE INVENTION 
It is well known in the petroleum refining industry to physically treat 
hydrocarbons thereby chemically changing their molecular structures and 
converting less valuable compounds into those which are in demand. 
One such conversion process is broadly referred to as "cracking", the 
thermal decomposition of long-chained hydrocarbon molecules into shorter 
hydrocarbon molecules having lower boiling points. In its broadest sense, 
thermocracking is typified by processes in which an unrefined hydrocarbon 
feed is converted by heating within a reactor vessel to a temperature 
between 800.degree. and 1500.degree. F. and at a pressure of about 200 to 
600 pounds per square inch. 
There are two general types of thermocracking processes. The first is known 
as vapor phase while the second is referred to as liquid or mixed phase. 
In vapor phase thermocracking, the charge stream is completely vaporized 
during the high temperature cracking process. In liquid or mixed phase 
cracking, the charge stream is essentially liquid but there does exist 
some vaporization and generation of non-condensable gases. 
Yet another thermocracking process is known as visbreaking, so named 
because the process reduces the viscosity of heavy crude oil residues 
thereby making them more suitable for an inclusion into, for example, fuel 
oils. In visbreaking, a heavy crude oil residue is passed through a 
thermal reactor or heat exchanger comprising a series of tubes which are 
subjected to high temperature heat exchange. The heavy crude oil residue 
is heated above 700.degree. F. to about 900.degree. F. or higher and held 
at that temperature within the reactor tubes for a period of time 
sufficient to produce the desired amount of cracking. A gas oil distillant 
is continually produced and removed as it is generated. 
Regardless of the type of thermocracking, all cracking processes deposit or 
accumulate carbon or coke on the reactor surfaces as well as in apparatus 
downstream of the reactor. For example, impurities in the charge material 
such as salts or metal compounds may become deposited on the heat 
exchanger reactor walls. The deposits gradually increase in thickness and 
eventually cause a reduction in cracking efficiency of the heat exchanger 
through the loss of heat transfer. In addition, the excessive carbon 
deposits slowly insulate the reactor or heat exchanger surfaces as they 
build up requiring greater and greater quantities of heat to maintain 
cracking temperatures. This additional heat only further exasperates the 
problem by producing even more carbon deposits on the reactor surfaces. 
Eventually, the reactor must be shut down and the deposits are manually 
removed. 
Numerous prior art attempts have been made to prevent the build-up of 
carbon on the interior walls of a parallel pass reactor or heat exchanger. 
Many parallel pass reactors or heat exchangers incorporate abrasive, 
granular media which fluidizes in the process liquid as it travels through 
the reactor. The granular media impact against the interior tube walls and 
abrade the carbon as it is formed. The abraded carbon particles are then 
removed from the reactor during processing without the need for reactor 
shutdown. For example, U.S. Pat. No. 4,427,053, to Klaren discloses a heat 
exchanger of the type in which a liquid is passed through a vertical riser 
tube connected at its upper and lower end to upper and lower tanks 
respectively and in which a granular mass is present. As the granules are 
fluidized by the liquid in the reactor, they travel upwardly through the 
tubes and have a scouring and cleansing effect upon the tube walls. 
Although the Klaren device and similar apparatus have addressed the problem 
of excessive carbon build up, such reactors are not entirely satisfactory 
when used in connection with a thermocracking or visbreaking operation. 
Since both thermocracking and visbreaking require heating of the 
hydrocarbon oil above 700.degree. F., coke and carbon is readily formed as 
a byproduct. While reactors and heat exchangers which incorporate abrasive 
particles for circulation do in fact continually clean the interior walls 
of the riser tubes of deposits, once the visbroken or thermocracked 
liquids and vapor exit the riser tubes and enter the head portion of the 
reactor, they continue to crack and deposit carbon within the upper 
chamber of the reactor and downstream of the reactor. Eventhough the 
abrasive particles are effective in cleaning the interior of the heat 
exchanger riser tubes, once outside the narrow tubes the abrasive media is 
ineffective. Consequently, the thermocracking liquid vapors and gases 
continue to crack and deposit carbon. Thus, even reactors containing 
abrasive particles must be shut down for periodic cleaning if the reactors 
are being used in thermocracking or visbreaking operations. Previously, 
there has been no effective way to control such carbon deposition within a 
heat exchanger or reactor employed in such processes. 
A need has therefore existed within the art to provide a cracking and 
visbreaking heat exchanger reactor which minimizes carbon deposition to 
the reactor as well as downstream of the reactor and thereby ensures long 
periods of operation without the need for reactor shutdown or periodic 
cleaning. 
OBJECTS AND SUMMARY OF THE INVENTION 
The present invention is directed to a reactor for thermocracking a fluid 
comprising a heat exchanger means having at least one tube for conveying 
the fluid stream from a respective tube inlet to a tube outlet while 
contacting the at least one tube with a high temperature medium to effect 
the transfer to the fluid stream sufficient to cause thermocracking. A 
quench means is provided for discharging a quench liquid so as to be 
positioned within the thermocracked fluid stream exiting the fluid tube 
outlet during a cracking operation to immediately lower the temperature of 
the thermocracked fluid stream sufficient to terminate further 
thermocracking of the fluid as it emerges from the tube outlet thereby 
preventing carbon deposition. 
The present invention is additionally directed to a method for 
thermocracking a fluid comprising the steps of providing a heat exchanger 
means having at least one tube for conveying a fluid stream from a 
respective tube inlet to a respective tube outlet. Providing quench means 
for discharging a quench liquid so as to be positioned within the 
thermocracked liquid stream exiting the outlet during cracking. Directing 
a fluid stream into the heat exchanger. Contacting the at least one tube 
with a high temperature medium to effect heat transfer to the fluid stream 
sufficient to cause thermocracking and quenching the thermocracked fluid 
stream exiting the tube outlet with the quench liquid to immediately lower 
the temperature of the thermocracked fluid stream sufficient to terminate 
further thermocracking of the fluid as it emerges from the tube outlet 
thereby preventing carbon deposition. 
It is an object of the present invention to lower the temperature of a 
thermally cracked oil within a heat exchanger or reactor to a temperature 
below cracking thereby preventing carbon deposition within the reactor and 
downstream of the reactor. 
It is a further object of the present invention to provide a heat exchanger 
or reactor which is adaptable for visbreaking or thermocracking operations 
and which will effectively quench a thermocracked hydrocarbon stream of 
fluid, vapors or intermixed fluid and vapors thereby preventing carbon 
deposition within the heat exchanger and downstream of the heat exchanger. 
It is a further object of the present invention to provide a quench for a 
heat exchanger or reactor in a visbreaking or thermal cracking operation 
which uses the crude oil process liquid as the quench. 
A still further object of the present invention is to provide a quench in 
the head portion of a heat exchanger or thermal reactor used in a 
visbreaking or thermal cracking operation which ensures that the entire 
thermocracked fluid is effectively quenched below cracking temperatures. 
A still further object of the present invention is to increase retention 
time of the quench and the cracked hydrocarbon by incorporating in the 
reactor, baffles, dams, multiple inlets, and spray manifolds. 
A further object of the present invention is to provide a reactor or heat 
exchanger for a thermocracking or visbreaking operation which incorporates 
a mixer at the discharge end of the reactor to ensure that the cracked 
hydrocarbon is thoroughly intermixed with the quench fluid prior to 
discharge from the reactor. 
Yet a further object of the present invention is to provide a reactor or 
heat exchanger for a thermocracking or visbreaking operation which can 
provide a quench that is discharged directly into the thermocracked liquid 
stream as it exits the heat exchanger tubes to immediately quench the 
thermocracked hydrocarbon below quenching temperature thereby preventing 
carbon deposition from occurring. 
Still a further object of the present invention is to provide a quench 
which is selectively preheated to precisely lower the temperature of the 
cracked effluent below cracking temperatures. 
Yet another object of the present invention is to provide a quench manifold 
which effectively quenches both thermocracked hydrocarbon liquids and 
vapors to lower the temperature below cracking temperature and prevent 
carbon deposition. 
Yet another object of the present invention is to provide a quench inlet 
for quenching the thermocracked hydrocarbon within the heat exchanger 
while also distributing the process fluid with the reactor. 
Still a further object of the present invention is to provide a reactor or 
heat exchanger for visbreaking or thermocracking whereby all the 
thermocracked liquids and vapors generated are intermixed and quenched to 
a temperature below thermocracking so that they may only be discharged 
from the reactor after they are no longer cracking. 
Yet a further object of the present invention is to provide a heat 
exchanger or reactor for visbreaking or thermocracking which will 
simultaneously handles cracked liquids and vapors produced during the 
cracking operation. 
Still a further object of the present invention is to provide a heat 
exchanger or reactor which may be used in any type of process or operation 
whereby the process fluid to be treated is of the type causing fouling of 
the heat exchanger surfaces. 
Still a further object of the present invention is to provide a heat 
exchanger quench manifold which is unique in construction and which 
provides enhanced quenching capability for both liquids and vapors. 
Yet a further object of the present invention is to provide a heat 
exchanger or reactor for visbreaking or thermocracking operations having 
multiple quench inlets and distribution manifolds depending upon the type 
of thermocracked fluid. 
Yet a further object of the present invention is to provide a method for 
thermocracking or visbreaking fluids whereby the quench fluid temperature 
is closely monitored and controlled to quench the thermocracked fluid 
within a reactor to a temperature sufficient to terminate cracking 
immediately after discharge within the reactor. 
The manner in which these as well as other objects of the present invention 
can be accomplished will be apparent from the following detailed 
description and drawings.

DETAILED DESCRIPTION OF THE INVENTION 
As best shown in FIG. 1, a thermal cracking heat exchanger or reactor A 
according to the present invention is shown comprising an outer casing or 
shell 2 including upper and lower header plates 4 and 6 dividing the heat 
exchanger A into an upper chamber 8, lower chamber 10 and heat exchange 
chamber 12. A plurality or bundle of parallel, vertically extending riser 
tubes 14 are disposed within the heat exchanger chamber 12 supported by 
the upper header plate 4 and lower header plate 6. Each of the riser tubes 
14 are provided with respective inlets 16 in lower chamber 10 and outlets 
18 opening into upper chamber 8. The space surrounding each of the riser 
tubes 14 within heat exchange chamber 12 contains a heat transfer medium 
such as steam entering via connection 20 and exiting via connection 22 as 
indicated by arrows 24 and 26 respectively. The heat exchange medium will 
contact the exterior of the riser tubes 14 and cause a heat transfer to 
whatever fluid is traveling within the riser tubes 14. The base of the 
lower chamber 10 is provided with a horizontal, perforated flow 
distribution plate 28 with inlet 30 for a process fluid such as crude oil 
to enter the reactor A. Arrow 32 indicates the direction of inlet flow. 
The apparatus includes a granular mass which is fluidized by the process 
fluid to be thermocracked or visbroken so as to occupy the space within 
the tubes during operation. The granular mass within the scope of the 
present invention is well known in the art and may include any of a 
variety of abrasive particulate media materials available including but 
not limited to glass, metal beads, shot, small pieces of wire or the like. 
Small carborundum balls, irregular pieces or other odd shaped media 
comprising hard material have been used with success. Denstone.RTM. balls 
(manufactured and marketed by Norton Products Corp.) comprising corundum 
and silica dioxide is a preferred particulate media. Generally speaking, 
the selected abrasive media has a preferred size from between about 1/8 
inch to about 1 inch in diameter but not larger than about 3/4 of the 
reactor tube diameter. 
The horizonal flow distribution plate 28 is perforated to allow the process 
fluid being treated to enter the inlet 30 and pass through the plate for 
appropriate heat exchange treatment within heat exchange chamber 12 while 
at the same time retaining the particulate mass intermixed with it thereby 
allowing the mass to be conveyed through each of the riser tubes 14. 
The upper chamber 8 includes a retaining wall 34 extending upwardly from 
upper header plate 4 and circumferentially around the various riser tubes 
14. Retaining wall 34 functions to increase retention time in the chamber 
8 of the thermocracked hydrocarbon liquid to be quenched. A series of 
baffle plates 36 are disposed a distance above the tube outlets 18 to 
assist in deflecting vapors back down the lower portion of the upper 
chamber 8. A static mixer 38 is shown connected to outlet 40 with arrow 42 
indicating direction of flow from the heat exchanger A. The static mixer 
38 assists in thoroughly intermixing the quench liquid with any 
thermocracked vapors or liquid prior to discharge from the reactor A. A 
preferred static mixer according to the present invention is the 
Kenits.RTM. HEV high efficiency static mixer (manufactured and marketed by 
Chemineer, Inc., North Andover, Mass.) or equal. The Kenics.RTM. mixer is 
disclosed in U.S. Pat. No. 4,929,088, the relevant portions of which are 
incorporated herein by reference. 
As best shown in FIG. 2, the quench inlets 44, 46 and 48 are disposed about 
the perimeter of upper chamber 8 so as to allow the quench fluid to enter 
into the upper chamber 8 in the direction of arrows 50 and adjacent the 
riser tube outlets 18. The embodiment shown in FIG. 1 and 2 is especially 
directed to those thermocracking or visbreaking operations wherein the 
hydrocarbon fluid to be cracked is not substantially vaporized as it 
passes through the heat exchanger and exits riser tubes 14. Instead, the 
still cracking hydrocarbon fluid leaving the riser tube 14 will overflow 
the riser tubes outlets 18 and immediately be contacted by the quench 
fluid entering the reactor via the quench inlets 44, 46 and 48. As can be 
appreciated, additional quench inlets may also be provided. The still 
cracking hydrocarbon is immediately contacted by the quench fluid reducing 
the temperature of the thermocracked fluid below a temperature of about 
700.degree. F. and thus below cracking temperatures. The retaining wall 34 
assists in increasing retention time of contact between the quench fluid 
and the thermocracked effluent fluid within the upper chamber 8 so that 
the quench can adequately intermix with the thermocracked effluent fluid. 
The quenched effluent exits outlet 40 and passes into static mixer 38 
further ensuring intermix of the quench with the thermocracked effluent. 
In a preferred embodiment, the quench also functions as an inlet for the 
process fluid to be treated. Thus, the quench can comprises a hydrocarbon 
oil which will eventually be visbroken or thermocracked as it is recycled 
back into the reactor. Although the quench fluid does not enter the 
interior of riser tubes 14, the abrasive particulates scour any coke or 
carbon which may deposit upon the interior of the walls of the riser tubes 
14. 
Even though the abrasive particulates have very little scouring effect 
beyond the interior of the riser tubes 14, because the quench oil lowers 
the temperature of the thermocracked effluent oil below cracking as it 
exits tube outlets 18, carbon deposition is eliminated. Generally 
speaking, this non-cracking temperature is below 700.degree. F. since oil 
will not. deposit coke or carbon below 700.degree. F. but will do so about 
about 800.degree. F. Thus, the quench fluid may be preheated to a selected 
temperature so that upon contact with the thermocracked effluent leaving 
riser tubes 14, it will lower the effluent temperature precisely below the 
700.degree. F. range. By controlling the temperature and/or volume of the 
quench oil, the combined quench fluid and thermocracked stream leaving the 
outlet 40 is below 700.degree. F. and therefore will no longer crack. 
For example, by calculating the heat content for a thermocracked crude oil 
at 800.degree. F., the heat required to be removed from the thermocracked 
crude oil to a point below cracking temperature can be determined. 
Consequently, the quench oil may be selectively heated to a required 
quench temperature and injected into the heat exchanger at certain rate 
and volume to effectively reduce the temperature of the thermocracked 
effluent below about 700.degree. F. Conversely, in the event the 
hydrocarbon oil is being visbroken at a substantially higher temperature 
where even greater quantities of vapor are produced and higher liquid 
temperatures are reached, the quench is preheated to a substantially lower 
temperature to significantly lower the crackled effluent liquid and vapors 
to the desired 700.degree. F. non-cracking range. 
The quenched and thermocracked effluent containing the particulate media is 
intermixed in a static mixer 38 prior to discharge from the heat exchanger 
A as indicated by arrow 42. In a preferred embodiment, the now quenched 
oil flows into a separator 43 whereby the thermocracked hydrocarbon 
fraction can be removed or selectively recycled through pump 47 back into 
heat exchanger A via recycle inlet 52 as indicated by arrow 54. The 
recycle is closely monitored and controlled to optimize the flow and 
fluidization of the abrasive particulate mass within the heat exchanger. 
That system is the subject of my co-pending application entitled METHOD 
AND APATUS FOR THERMOCRACKING OF HYDROCARBONS, U.S. Ser. No. 
08/060,071, the pertinent portions of which are incorporated herein by 
reference. 
Turning now to FIG. 3, the heat exchanger or reactor B according to the 
present invention is shown in an alternative embodiment for use when 
thermocracking a hydrocarbon oil or other fluid at substantially higher 
temperatures where significant quantities of thermocracked vapors are 
generated. The heat exchanger B includes a shell or casing 56 divided by 
upper header plate 58 and lower header plate 60 into an upper chamber 62, 
lower chamber 64 and heat exchange chamber 66. A number of vertically 
extending riser tubes 68 are provided, each of which includes a tube inlet 
70 and tube outlet 72 extending into the lower chamber 64 and upper 
chamber 62 respectively. A steam inlet connection 74 and steam outlet 
connection 76 are also provided. Arrow 78 indicates the direction of steam 
or some other heat exchange medium into heat exchange chamber 66 while 
arrow 80 indicates the direction of steam or other heat exchange medium 
leaving the heat exchange chambers 66. 
A horizontal flow distribution plate 82 is provided with holes extending 
therethrough to retain the particulate media within the lower chamber 64 
so that once the media is fluidized, it travels into the various tube 
inlets 70. A main inlet 84 is provided for entry of the hydrocarbon fluid 
to be thermocracked. Arrow 86 indicates direction of travel into the inlet 
84. A retaining wall 88 extends upwardly from the upper header plate 58 so 
as to surround the riser tube outlets 72. A static mixer 92 is provided at 
outlet 94 to ensure thorough intermixing of the thermocracked vapors and 
liquids with the quench liquid prior to discharge in the direction 
indicated by arrow 95. Baffle plates 90 are disposed in the upper portion 
of chamber 62 to assist in deflection of vapors generated during the 
thermocracking. 
As best shown in FIGS. 3 and 4, multiple quench inlets 96 are disposed 
about the perimeter of upper chamber 62 and extend therein. Arrows 97 
indicate the direction of flow of the quench fluid into the inlets 97. A 
quench manifold 98 is horizontally disposed within upper chamber 62 to 
receive quench fluid from inlets 96 and to distribute the quench fluid 
within upper chamber 62. As best shown in FIG. 4, the manifold 98 
comprises a number of individual manifold arms 100 radially extending from 
a common central point. Each of the various manifold arms 100 are provided 
with upper apertures or holes 102 and lower apertures or holes 104 to 
distribute quench fluid from the manifold in an upward direction against 
the baffle plates 90 and downward into the path of the cracked effluent 
leaving the riser tube outlet 72. 
As can be appreciated, in the situation where the hydrocarbon oil is being 
visbroken at an extremely high temperature producing substantial 
quantities of cracked vapor, the quench manifold 98 will provide not only 
a quench fluid for the thermocracked liquid being generated but also for 
the thermocracked vapors accumulating in the upper region of chamber 62. 
In this way, carbon and coke which would otherwise accumulate within the 
interior of chamber 62 or downstream therefrom is effectively suppressed 
from forming. As with the embodiment shown in FIGS. 1 and 2, the 
temperature of the quench oil or liquid is closely controlled to allow it 
to effectively lower the temperature of the cracked effluent liquid in 
reactor B. The intermixed quench and thermocracked effluent may be removed 
from the reactor via outlet 94 to separate the cracked product, to add 
media or to remove carbon that has been abraded from the interior walls of 
the riser tubes. A recycle inlet 106 is shown entering the lower chamber 
64 in the direction of arrow 108. 
Turning now to FIG. 5, the heat exchanger or reactor C is shown in an 
alternative embodiment comprising a shell 110 divided by upper header 
plate 112 and lower header plate 114 into an upper chamber 116, a lower 
chamber 118 and a centrally disposed heat exchange chamber 120. A series 
of riser tubes 122 are vertically disposed as a bundle within the interior 
of heat exchange chamber 120, each of the tubes 122 includes a respective 
tube inlet 124 extending through lower header plate 114 into lower chamber 
118 and a respective tube outlet 126 extending through upper header plate 
112 into upper chamber 116. A steam inlet connection 128 and a steam 
outlet connection 130 are also provided for heat exchange chamber 120 with 
arrow 132 indicating direction of the steam or other heat exchange medium 
into the chamber and arrow 134 indicating the direction of the heat 
exchange medium from the reactor. 
A horizontal flow distribution plate 136 having apertures therein is 
disposed in lower chamber 118 a selected distance beneath tube outlets 126 
for retaining abrasive media therein prior to fluidization into the 
various riser tubes 122. A main inlet 138 is provided in lower chamber 118 
for entry of the hydrocarbon oil or other fluid to be thermocracked or 
heat exchanged. Arrow 140 indicates direction of travel of the process 
fluid into the heat exchanger or reactor C. The upper chamber 116 is 
provided with a vertical retaining wall 142 extending perpendicular from 
upper header plate 112 and circumferentially around the riser tube outlets 
126. A number of baffle plates 144 are disposed within the upper portion 
of upper chamber 116 to assist in deflecting the vapors generated during 
visbreaking. A static mixer 146 is provided at the main outlet 148 to 
ensure thorough intermixing of the quench liquid, thermocracked liquid and 
vapors immediately prior to discharge from the reactor C in the direction 
of arrow 150. 
As best shown in FIGS. 5 and 6, a number of quench inlets 152 are disposed 
about the perimeter of the upper chamber 116. A quench liquid such as 
heated crude oil enters the reactor in the direction of arrow 154. A 
quench manifold 156 is disposed within the interior of upper chamber 116 
and above the baffle plate 144 to receive and distribute the quench within 
the interior of the upper chamber 116. The quench manifold 156 is shown as 
comprising a number of concentric manifold rings 158 each of which 
includes upper holes or apertures 160 and lower holes or apertures 162 
through which the quench liquid passes into the chamber 116. 
As can be appreciated, the embodiment shown in FIGS. 5 and 6 is designed 
for the situation where the hydrocarbon oil is thermocracked at an 
extremely high temperature and where a large volume of cracked vapors are 
generated within upper chamber 116. Thus, the quench manifold 156 is 
positioned such that the generated thermocracked vapors are immediately 
quenched by the quench oil it sprays into chamber 116. As noted earlier, 
the quench oil is preheated to a selected temperature to effectively 
remove heat from the thermocracked vapors and reduce the upper temperature 
below 700.degree. F. thereby eliminating carbon deposition within the heat 
exchanger as well as downstream. A recycle inlet 164 is also provided to 
allow quenched and thermocracked effluent removed from outlet 148 to be 
recycled back into the lower chamber 118 for further thermocracking. As 
with the previous embodiments, the quenched and thermocracked effluent 
intermixed with particulate media may be treated to remove carbon 
particles abraded from the interior of the riser tubes 122 as well as to 
add process fluid or particulate media and to selectively adjust the 
fluidization rate into the heat exchanger C. 
As can be appreciated, each of the various arrangements for distributing 
the quench shown in FIGS. 1-6 can be incorporated into a single heat 
exchanger or reactor in various combination depending upon the nature of 
the thermocracked fluid which is being generated within the upper chamber 
of the reactor. 
While this invention has been described as having a preferred design, it is 
understood that it is capable of further modifications, uses and/or 
adaptations of the invention following in general the principle of the 
invention and including such departures from the present disclosure as 
come within the known or customary practice in the art to which to 
invention pertains and as may be applied to the central features 
hereinbefore set forth, and fall within the scope of the invention and of 
the limits of the appended claims.