U.S. patent application number 14/286530 was filed with the patent office on 2014-09-11 for in-situ gasification of soot contained in exothermically generated syngas stream.
The applicant listed for this patent is William Robert Licht, Shankar Nataraj, Xiang-Dong Peng, John Michael Repasky. Invention is credited to William Robert Licht, Shankar Nataraj, Xiang-Dong Peng, John Michael Repasky.
Application Number | 20140250785 14/286530 |
Document ID | / |
Family ID | 34574274 |
Filed Date | 2014-09-11 |
United States Patent
Application |
20140250785 |
Kind Code |
A1 |
Licht; William Robert ; et
al. |
September 11, 2014 |
IN-SITU GASIFICATION OF SOOT CONTAINED IN EXOTHERMICALLY GENERATED
SYNGAS STREAM
Abstract
A system is set forth for the exothermic generation of soot
depleted syngas comprising (i) reacting a hydrocarbon-containing
fuel with an oxygen containing gas in a first reactor to produce
the syngas and byproducts comprising CO.sub.2, H.sub.2O and soot;
and (ii) introducing the syngas and byproducts into a second
reactor containing a non-carbonaceous material that traps the soot
for a sufficient time such that the majority of the byproduct soot
is gasified via reaction with the byproduct CO.sub.2 and/or
H.sub.2O to produce a syngas stream that is depleted in the soot.
The system is particularly suitable for the practice of heat
exchange reforming therein a portion of the heat is recovered from
the soot depleted syngas stream and used as at least a portion of
the heat to facilitate the additional production of syngas via the
(endothermic) catalytic reforming of natural gas and steam.
Inventors: |
Licht; William Robert; (New
York, NY) ; Nataraj; Shankar; (New York, NY) ;
Peng; Xiang-Dong; (New York, NY) ; Repasky; John
Michael; (New York, NY) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
Licht; William Robert
Nataraj; Shankar
Peng; Xiang-Dong
Repasky; John Michael |
New York
New York
New York
New York |
NY
NY
NY
NY |
US
US
US
US |
|
|
Family ID: |
34574274 |
Appl. No.: |
14/286530 |
Filed: |
May 23, 2014 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
|
|
12468815 |
May 19, 2009 |
8771386 |
|
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14286530 |
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|
10715757 |
Nov 18, 2003 |
7534276 |
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12468815 |
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Current U.S.
Class: |
48/127.9 ;
48/128 |
Current CPC
Class: |
C10J 2200/06 20130101;
C10J 2300/1846 20130101; C10J 3/466 20130101; C10J 3/721 20130101;
C10J 2300/094 20130101; C01B 2203/049 20130101; C01B 2203/04
20130101; C01B 2203/0255 20130101; C01B 2203/141 20130101; C01B
2203/0838 20130101; C01B 3/36 20130101; C10J 3/84 20130101; C10J
2300/0983 20130101; C01B 2203/0233 20130101; C10K 3/003 20130101;
C10K 1/02 20130101 |
Class at
Publication: |
48/127.9 ;
48/128 |
International
Class: |
C10K 1/02 20060101
C10K001/02 |
Claims
1. A process for the exothermic generation of syngas by the partial
oxidation of a hydrocarbon-containing fuel comprising: (i) reacting
the hydrocarbon-containing fuel with an oxygen containing gas in a
first reactor to produce the syngas and byproducts comprising
CO.sub.2, H.sub.2O and soot; and (ii) introducing the syngas and
byproducts into a second reactor containing a non-carbonaceous
material that traps the soot for a sufficient time such that the
majority of the byproduct sect is gasified via reaction with the
byproduct CO.sub.2 and/or H.sub.2O to produce a syngas stream that
is depleted in the soot.
2. The process of claim 1 which further comprises: (iii) recovering
a portion of the heat from the soot depleted syngas stream and
using at least a portion of the recovered heat to facilitate the
additional production of syngas via the (endothermic) catalytic
reforming of natural gas and steam.
3. The process of claim 1 wherein substantially all of the
byproduct soot is gasified in step (ii).
4. The process of claim 1 wherein the non-carbonaceous material
comprises alumina.
5. The process of claim 1 wherein the non-carbonaceous material
contained in the second reactor is in the term of spherical
particles.
6. The process of claim 1 wherein the non-carbonaceous material
contained in the second reactor is in the form of rings.
7. The process of claim 1 wherein the non-carbonaceous material
contained in the second reactor has a catalytic functionality to
facilitate the gasification of the soot.
8. The process of claim 1 wherein first and second reactors are
operated in a temperature range from 2100F to 2800F.
9. The process of claim 1 wherein a fluid is added to the syngas
and byproducts produced by the first reactor prior to introducing
the syngas and byproducts into the second reactor.
10. In an apparatus for the exothermic generation of syngas by the
partial oxidation of a hydrocarbon-containing fuel comprising: (i)
a first reactor for reacting the hydrocarbon-containing fuel with
an oxygen containing gas to produce the syngas and byproducts
comprising CO.sub.2, H.sub.2O and soot; and (ii) a second reactor
for receiving the syngas and byproducts containing a
non-carbonaceous material that traps the soot for a sufficient time
such that the majority of the byproduct soot is gasified via
reaction with the byproduct CO.sub.2 and/or H.sub.2O to produce a
syngas stream that is depleted in the soot.
11. The apparatus of claim 10 which further comprises: (iii) a heat
exchange reformer for recovering a portion of the heat from the
soot depleted syngas stream and using at least a portion of the
recovered heat to facilitate the additional production of syngas
via the (endothermic) catalytic reforming of natural gas and
steam.
12. The apparatus of claim 10 wherein substantially all of the
byproduct soot is gasified in the second reactor.
13. The apparatus of claim 10 wherein the non-carbonaceous material
comprises alumina.
14. The apparatus of claim 10 wherein the non-carbonaceous material
contained in the second reactor is in the form of spherical
particles.
15. The apparatus of claim 10 wherein the non-carbonaceous material
contained in the second reactor is in the form of rings.
16. The apparatus of claim 10 to wherein the non-carbonaceous
material contained In the second reactor has a catalytic
functionality to facilitate the gasification of the soot.
17. The apparatus of claim 10 wherein first and second reactors are
operated in a temperature range from 2100F to 2800F.
18. The apparatus of claim 10 further comprising a means to add a
fluid to the syngas and byproducts produced by the first reactor
prior to the second reactor receiving the syngas and byproducts.
Description
BACKGROUND OF THE INVENTION
[0001] Synthesis gas comprising carbon monoxide and hydrogen
(hereafter syngas) is commonly produced by the partial oxidation
(POX) of a hydrocarbon-containing tool (hereafter, the POX
process). The POX process is a highly exothermic process and
produces a syngas stream at temperatures typically in range of 2100
to 2800.degree. F.
[0002] A key challenge in the POX process, especially for carbon
heavy fuels, is the removal of the entrained solid carbon
(hereafter soot) produced as an undesirable byproduct. In
particular, the soot that is generated in the POX reactor will tend
to foul conventionally designed heat exchangers that are used to
recover a portion of the heat from the exothermically generated
syngas stream. Although special boilers have been developed to
process soot-containing syngas, these designs cannot be readily
transferred to heat exchange reforming wherein a portion of the
heat is recovered from the POX generated syngas stream and used as
at least a portion of the heat to facilitate the additional
production of syngas via the (endothermic) catalytic reforming of
natural gas and steam. Thus a system which can remove soot from
syngas at high temperature offers a key advantage to the practice
of heat exchange reforming.
[0003] Typically, the soot is removed by quenching and scrubbing
the syngas with water. See for example EP0 648 828 B1 and WO
00/29323, both assigned to Texaco Development Corporation.
[0004] Alternatively, JP 50040117 teaches directly filtering the
syngas through a carbonaceous material that traps the soot for a
sufficient time period such that the oxygen containing molecules
that are also produced as byproduct in the POX process (i.e.
CO.sub.2 and H.sub.2O) are given an opportunity to react with, and
gasify, the soot. After such in-situ gasification of the soot, JP
'117 introduces the syngas (or "reducing gas" as referred to
therein) into a blast furnace.
[0005] A concern with the in-situ gasification scheme as taught in
JP '117 is the use of a carbonaceous material as the material for
trapping the soot and subsequently allowing it to be gasified by
reaction with the byproduct CO.sub.2 and/or H.sub.2O. In
particular, the carbonaceous material will be susceptible to the
vary same gasification reactions that the carbonaceous soot is
intended to undergo (i.e. via reaction against the byproduct
CO.sub.2 and/or H.sub.2O). Consequently, a carbonaceous material
will require more frequent replacing than a non-carbonaceous
material.
[0006] The present invention addresses this concern by using a
non-carbonaceous material to trap the soot.
BRIEF SUMMARY OF THE INVENTION
[0007] The present invention is a system for the exothermic
generation of syngas by the partial oxidation of a
hydrocarbon-containing fuel comprising: [0008] (i) reacting the
hydrocarbon-containing fuel with an oxygen containing gas in a
first reactor to produce the syngas and byproducts comprising
CO.sub.2, H.sub.2O and soot; and [0009] (ii) introducing the syngas
and byproducts into a second reactor containing a non-carbonaceous
material that traps the soot for a sufficient time such that the
majority of the byproduct soot is gasified via reaction with the
byproduct CO.sub.2 and/or H.sub.2O to produce a syngas stream that
is depleted in the soot.
DETAILED DESCRIPTION OF THE INVENTION
[0010] A key to the present invention is that the material used to
trap the soot in the second reactor is a non-carbonaceous material.
This is key because if a carbonaceous material were used (i.e. such
as in JP 50040117), the material would be susceptible to the very
same gasification reactions that the carbonaceous soot is intended
to undergo (i.e. via reaction against the byproduct CO.sub.2 and/or
H.sub.2O). Consequently, a carbonaceous material will require more
frequent replacing than a non-carbonaceous material.
[0011] In a key embodiment of the present invention, the system
further comprises a heat exchange reformer for recovering a portion
of the heat from the soot depleted syngas stream and using at least
a portion of the recovered heat to facilitate the additional
production of syngas via the (endothermic) catalytic reforming of
natural gas and steam.
[0012] Alumina is one example of the material that can be used as
the non-carbonaceous material in the present invention. Various
other refractory materials such as zirconia or lanthana could also
be used, optionally in combination with alumina. In one embodiment
of the present invention, the material is packed in the second
reactor in the form of spherical particles to efficiently trap the
soot without creating excessive pressure drop. The pressure drop
and removal efficiency for an example reactor consisting of 2 feet
of 3 inch diameter spheres and 1 foot each of 2 inch, 1 inch, and
0.5 inch diameter spheres has been calculated. With a superficial
gas velocity of 7 ft/s, the pressure drop is 16 psi while the
removal efficiency is such that 85% of the soot particles 21
microns in diameter are removed (larger soot particles are removed
almost completely and smaller particle are passed through the bed
almost completely). By arranging the spherical particles in this
manner, soot panicles of different sizes are trapped within each
zone. This distributes the soot along the direction of flow and
increases the capacity of the bed to hold soot without
plugging.
[0013] Alternate packing shapes such as rings could also be used to
allow more complete removal of a wider range of soot sizes while
minimizing pressure drop. In addition, the non-carbonaceous
material could also have a catalytic functionality to facilitate
the gasification of the soot.
[0014] POX reactors can operate over a temperature range from about
1700F to 3500F; however, the most common operating range is from
about 2100 to 2800F. The system described here is preferentially
operated in a temperature range from 2100F to 2800F. At higher
temperatures, the hydrocarbon feed to the partial oxidation step is
overly oxidized, resulting in less syngas and more byproduct
CO.sub.2 and H.sub.2O. At lower temperatures, there is a
substantial amount o unconverted hydrocarbon feed. Additionally at
lower temperature, the quantity of soot held in the packing becomes
too great and the packing plugs. The system described here is
designed to operate at a steady state in which the gasification
rate is equal to the rate at which the soot is trapped. For every
100F drop in temperature between 2500F and 2100F the quantity of
soot which must be held on the bed for the gasification rate to
equal the amount of soot generated in the POX unit increases by
approximately an order-of-magnitude.
[0015] It is within the scope of the present invention to include a
fluid addition step between the first and second reactors.
Potential benefits include managing the high temperatures and
increasing the driving force for soot gasification. For example,
steam could be added to the syngas and byproducts produced by the
first reactor prior to introducing the syngas and byproducts into
the second reactor.
[0016] The skilled practitioner will appreciate that there are many
other embodiments of the present invention which are within the
scope of the following claims.
* * * * *