U.S. patent number 3,769,002 [Application Number 05/155,354] was granted by the patent office on 1973-10-30 for reduction of nickel and cobalt oxides in a molten metal bath of controlled oxygen content.
This patent grant is currently assigned to The International Nickel Company, Inc.. Invention is credited to Malcolm Charles Evert Bell, Charles Edward O'Neill, John Stuart Warner.
United States Patent |
3,769,002 |
O'Neill , et al. |
October 30, 1973 |
REDUCTION OF NICKEL AND COBALT OXIDES IN A MOLTEN METAL BATH OF
CONTROLLED OXYGEN CONTENT
Abstract
Metal oxides, including oxides of nickel and cobalt and
compounds heat decomposable thereto, and a carbonaceous reductant
are introduced into a turbulent bath of the corresponding metal
which bath contains at least about 0.01 percent dissolved oxygen to
maintain the dissolved oxygen content of the bath at at least about
0.01 percent but less than saturation, while the carbonaceous
reductant reacts to generate carbon monoxide. The metal bath is
maintained in the molten state by burning above the bath carbon
monoxide generated in situ and hydrocarbon fuels with an excess of
free oxygen. Impurities oxidizable to volatile oxides can be
eliminated by subjecting the oxygen-containing bath, or a part
thereof, to subatmospheric pressures, or the metal bath can be
surface blown with a free oxygen-containing gas to adjust the
oxygen content of the bath before subatmospheric treatment.
Inventors: |
O'Neill; Charles Edward (Port
Credit, Ontario, CA), Warner; John Stuart (Oakville,
Ontario, CA), Bell; Malcolm Charles Evert (Oakville,
Ontario, CA) |
Assignee: |
The International Nickel Company,
Inc. (New York, NY)
|
Family
ID: |
4087157 |
Appl.
No.: |
05/155,354 |
Filed: |
June 21, 1971 |
Foreign Application Priority Data
Current U.S.
Class: |
75/627;
75/629 |
Current CPC
Class: |
C22B
23/02 (20130101) |
Current International
Class: |
C22B
23/02 (20060101); C22B 23/00 (20060101); C22b
023/00 () |
Field of
Search: |
;75/82 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Rutledge; L. Dewayne
Assistant Examiner: Andrews; M. J.
Claims
We claim:
1. A process for reducing a metal compound which comprises:
establishing a bath of at least one metal selected from the group
consisting of nickel and cobalt, which bath contains at least about
0.01 percent dissolved oxygen; feeding at least one compound
selected from the group consisting of nickel oxide, cobalt oxide,
and compounds heat decomposable thereto and a carbonaceous
reductant to the bath while the dissolved oxygen content of the
bath is maintained at at least about 0.01 percent whereby the
carbonaceous reductant reacts with the dissolved oxygen in the bath
to generate carbon monoxide; burning the generated carbon monoxide
and a fuel with a free-oxygen-containing gas above the bath to
produce heat for maintaining the bath at operating temperatures;
and recovering a portion of reduced metal from the bath.
2. The process as described in claim 1 wherein the bath contains at
least about 0.1 percent dissolved oxygen but is not saturated
therewith.
3. A process for reducing a nickel compound which comprises:
establishing a turbulent nickel bath which contains at least about
0.01 percent dissolved oxygen but not saturated therewith; feeding
at least one nickel compound selected from the group consisting of
nickel oxide and compounds heat decomposable thereto and a
carbonaceous reductant to the nickel bath while maintaining the
dissolved oxygen level of the nickel bath at at least about 0.01
percent but less than saturation whereby the carbonaceous reductant
reacts with the dissolved oxygen content in the nickel bath to
generate carbon monoxide; burning the generated carbon monoxide and
a fuel with a free-oxygen-containing gas above the nickel bath to
produce heat for maintaining the bath at operating temperatures;
and recoverng nickel from the nickel bath.
4. A process for reducing a cobalt compound which comprises:
establishing a turbulent cobalt bath containing at least about 0.01
percent dissolved oxygen but not saturated therewith; feeding at
least one cobalt compound selected from the group consisting of
cobalt oxide and compounds heat decomposable thereto and a
carbonaceous reductant to the cobalt bath whereby the carbonaceous
reductant reacts with the dissolved oxygen in the cobalt bath to
generate carbon monoxide; burning the generated carbon monoxide and
a fuel with a free-oxygen-containing gas above the cobalt bath to
produce heat for maintaining the cobalt bath at operating
temperatures; and recovering cobalt metal from the cobalt bath.
5. The process as described in claim 1 wherein the compound is fed
to the bath as briquettes.
6. The process as described in claim 5 wherein the carbonaceous
reductant is incorporated in the briquetted compound.
7. The process as described in claim 6 wherein the carbonaceous
reductant is a liquid hydrocarbon.
8. The process as described in claim 7 wherein the liquid
hydrocarbon is Bunker C oil.
9. The process as described in claim 8 wherein the liquid
hydrocarbon is incorporated in the briquette in amounts less than
is required to satisfy the stoichiometry of the reduction
reactions.
10. The process as described in claim 8 wherein the liquid
hydrocarbon is incorporated in the pellets in amounts substantially
equal to that required to satisfy the stoichiometry of the
reduction reactions.
11. The process as described in claim 8 wherein the liquid
hydrocarbon is incorporated in the briquettes in amounts in excess
of that required to satisfy the stoichiometry of the reduction
reactions and the surface of the metal bath is surface blown with a
free-oxygen-containing gas to maintain the dissolved oxygen content
of the bath at at least about 0.01 percent.
12. The process as described in claim 1 wherein the bath is
maintained at a temperature of at least about 50.degree.C. above
its melting point.
13. The process as described in claim 12 wherein the metal bath is
maintained at a temperature of at least about 100.degree.C. above
its melting point.
14. The process as described in claim 1 wherein feeding of the
compound to the bath is terminated so that the dissolved oxygen
content of the bath is reduced by the reductant before the metal is
recovered from the bath.
15. The process as described in claim 1 wherein a portion of the
oxygen-containing bath is teemed and then subjected to a
subatmospheric pressure treatment for final impurity
elimination.
16. The process as described in claim 15 wherein the teemed
oxygen-containing bath is subjected to a subatmospheric pressure of
less than about 0.1 atmosphere.
17. The process as described in claim 16 wherein the
oxygen-containing bath is subjected to a subatmospheric pressure of
less than about 0.01 atmosphere.
18. The process as described in claim 17 wherein the
oxygen-containing bath is subjected to a subatmospheric pressure of
less than about 0.001 atmosphere.
19. The process as described in claim 3 wherein the nickel compound
is nickel oxide.
20. The process as described in claim 3 wherein the nickel compound
is nickel hydroxide.
21. The process as described in claim 3 wherein the nickel compound
is basic nickel carbonate.
22. The process as described in claim 4 wherein the cobalt compound
is cobalt oxide.
23. The process as described in claim 4 wherein the cobalt compound
is cobalt hydroxide.
24. The process as described in claim 4 wherein the cobalt compound
is basic cobalt carbonate.
Description
This invention pertains to reducing metal oxides and more
particularly to reducing and refining metal oxides, including
nickel and nickel-containing materials, by pyrometallurgical and
vapometallurgical techniques.
Nickel oxide is frequently an intermediate product in the
commercial recovery of nickel from its ores, whether oxide or
sulfide. For example, in the treatment of lateritic ores by
selective reduction and ammoniacal ammonium carbonate leaching,
nickel oxide is obtained by calcining precipitated basic nickel
carbonate. In treating sulfide ores, nickel sulfide concentrate,
obtained by matte separation including slow cooling and subsequent
comminution, is roasted to nickel oxide. Nickel oxide produced by
either of these processes can be employed, if it is sufficiently
pure, for alloying purposes. Often, however, a more pure form of
nickel is required, and nickel oxide must be reduced for further
refining. Sulfur contamination problems are frequently encountered
during reduction of nickel oxide, unless more expensive fuels,
deficient in sulfur, are employed. If low sulfur fuels are not
employed, sulfur dissolved in molten nickel must be removed
therefrom, e.g., by treatment with a flux rich in lime. This latter
procedure is not entirely satisfactory since it involves an
additional treatment, additional fluxing materials, is time
consuming and may create furnace refractory problems. Although
attempts were made to overcome the foregoing difficulties and other
disadvantages, none, as far as we are aware, was entirely
successful when carried into practice commercially on an industrial
scale.
It has now been discovered that metal oxides, including nickel
oxides, cobalt oxides and compounds heat decomposable thereto, can
be directly and continuously melted and refined by a combination of
pyrometallurgical and vapometallurgical operations. The combination
of processes allows the use of fuels containing substantial amounts
of sulfur and also provides a process for lowering the content of
impurities such as lead, zinc, cadmium, bismuth, antimony and other
impurities which are volatile or have volatile oxides. The product
obtained by the process has a low content of dissolved gases and is
particularly suitable for continuous casting.
It is an object of the present invention to provide a combination
of pyrometallurgical and vapometallurgical operations for refining
nickel oxide and nickel-containing compounds heat decomposable to
nickel oxide.
A further object of the present invention is to provide a
pyrometallurgical process for the direct and continuous production
of metals, including nickel and cobalt from their oxides and
compounds heat decomposable to their oxides.
Other objects and advantages will become apparent from the
following description.
Generally speaking, the present invention contemplates a process
for reducing metal oxides. A turbulent bath of at least one metal
selected from the group consisting of nickel and cobalt is
established, which bath contains at least about 0.01 percent
dissolved oxygen but not saturated therewith. At least one compound
selected from the group consisting of nickel oxide, cobalt oxide
and compounds heat decomposable thereto and a carbonaceous
reductant are fed to the turbulent bath while the dissolved oxygen
content of the bath is maintained at at least 0.01 percent but less
than saturation whereby the carbonaceous reductant reacts with the
dissolved oxygen in the bath to generate carbon monoxide. The
generated carbon monoxide and a fuel are burnt above the bath with
a free-oxygen-containing gas to produce heat for maintaining the
bath at operating temperatures. When it is desired to teem at least
a portion of reduced metal from the bath, feeding of the compound
to the bath is terminated so that the dissolved oxygen content of
the bath is reduced by the carbonaceous reductant. Alternatively, a
portion of the oxygen-containing bath can be teemed from the
furnace and then subjected to a subatmospheric pressure treatment
for final impurity elimination.
When the metal oxide or the reductant fuel contain impurities that
are oxidizable to volatile oxides, the oxygen-containing bath can
be directly subjected to a subatmospheric pressure treatment so
that the oxidized impurities are more effectively volatized from
the bath. Alternatively, dissolved oxygen can be incorporated into
the bath by surface blowing the bath with a free-oxygen-containing
gas before the subatmospheric pressure treatment or by passing a
free-oxygen-containing gas through the metal bath during the
subatmospheric pressure treatment.
Oxides, compounds heat decomposable to the oxides of nickel and
cobalt, and materials containing these compounds can be treated in
accordance with the process of the present invention. Compounds
heat decomposable to the oxides include, but are not limited
thereto, hydroxides, carbonates, basic carbonates and nitrates of
nickel and cobalt. These compounds are often produced by
hydrometallurgical techniques and are contaminated by various
impurities, most of which can be eliminated by practice of the
process in accordance with the present invention. Impurities which
can be volatilized or oxidized and volatilized include antimony,
bismuth, cadmium, lead, sulfur and zinc. The total content of the
aforementioned metallic impurities can amount to as much as about
0.5 percent while sulfur can amount to as much as about 3 percent,
e.g, about 2 percent. Compounds produced by hydrometallurgical
techniques frequently contain nuisance amounts of gangue such as
alumina, calcium, magnesia and silica and the process of the
present invention provides a highly effective mode for separating
these constituents from nickel and/or cobalt.
A highly important feature of the present invention is the
exceptionally high production rates that are achieved by
maintaining the oxygen content of the turbulent bath at at least
about 0.01 percent, or about 0.02 percent and even higher, when the
metal oxide and the reductant are being added to the bath. In fact,
when this technique is employed, commercial production rates are
approached with only pilot-plant-sized apparatus. High
temperatures, e.g., about 50.degree.C. or even 100.degree.C. above
the melting point of the metal bath, and turbulence of the metal
bath are the two factors that are most important in controlling the
oxygen content in the metal bath. Advantageously, the metal bath is
established in a top blown rotary furnace in which the bath can be
independently agitated and maintained at high temperatures. Use of
a top blown rotary furnace has many advantages with the foremost
being the independent control of temperature, atmosphere and
agitation. Further advantages flowing from the use of top blown
rotary converters include high thermal and chemical efficiencies
provided by the rotating refractories and by the turbulence of the
bath.
A carbonaceous reductant, such as coal, coke, charcoal or even
liquid hydrocarbons, is added to the oxygen-containing metal bath
to reduce the dissolved oxygen. The reduction reaction is so
extremely rapid, particularly when conducted in a top blown rotary
converter, that nickel oxide or cobalt oxide and the carbonaceous
reductant can be added to the bath in a continuous or
semicontinuous manner. The reduction reaction is so rapid and
energetic that a carbon monoxide boil can be observed. Not only is
the carbon monoxide boil important as a measure of the rate of the
reaction; but, even more importantly, the boil agitates the metal
so vigorously that the formation of a quiescent refractory oxide
layer is avoided whereby briquetted nickel oxide and compounds heat
decomposable thereto are rapidly wetted by and dissolved in the
metal bath and do not merely float on a quiescent refractory layer.
Carbonaceous reductant is added to the oxygen-containing metal bath
in amounts necessary to substantially satisfy the reduction
stoichiometry and to provide carbon monoxide to at least partially
satisfy the heat requirements. Greater amounts of reductant can be
added to insure complete reduction and to act as a source of fuel
which can be burned by reaction with free-oxygen-containing
gases.
In order to minimize metal losses and other problems associated
with dusting, finely divided nickel oxides and compounds heat
decomposable thereto are briquetted or otherwise put into an
agglomerated state. During agglomeration reductant and fuel, either
liquid or solid, can be incorporated in the briquettes or pellets.
A highly advantageous embodiment is to incorporate into the pellets
liquid hydrocarbons, such as Bunker C fuel oil during briquetting,
so that at least part of the reductant and/or fuel can be added via
the pellets. In addition to providing reductant and fuel, the
incorporation of liquid hydrocarbons during the briquetting
operation has the further addition of lowering, or even
eliminating, the use of water as a binder, thereby lowering fuel
costs attributable to drying and vaporizing such water. Moreover,
liquid hydrocarbon, such as Bunker C oil, are particularly
kinetically active reductants. The amount of reductant incorporated
in the pellets can vary within wide limits. Less than
stoichiometric amounts of reductant can be incorporated in the
briquettes with difference being made up by the addition of coke or
other solid reductant to the bath. If more than stoichiometric
amounts of reductant are incorporated in the briquetted nickel
oxide or other compounds heat decomposable thereto, the oxygen
content of the molten nickel bath can be maintained above about
0.01 percent by surface blowing the bath with a
free-oxygen-containing gas to burn the excess reductant and to
incorporate oxygen in the bath, or by the addition of
reductant-free briquetted oxide. The presence of excess reductant
is readily ascertained since the vigor of the carbon monoxide boil
rapidly diminishes.
Since the overall process is endothermic heat must be supplied to
the metal bath to maintain it in a molten state. Heat can be
supplied by burning above the bath carbon monoxide generated in
situ or the carbonaceous reductant with a free-oxygen-containing
gas and/or by burning a fuel with a free-oxygen-containing gas in a
burner provided for this purpose. The fuel can be the same as the
reductant or can be gaseous (e.g., natural gas) and does not have
to be sulfur free. Sufficient heat is generated by any or all of
these methods to maintain the metal bath at a temperature of at
least about 50.degree.C. or even 100.degree.C. above its melting
point to promote dissolution of the oxide and to increase reduction
kinetics.
An important feature of the present invention is the subatmospheric
pressure treatment for final impurity elimination. A bath
containing the requisite amounts of dissolved oxygen can be
produced in the vacuum unit and is advantageously so done during
final impurity elimination. However, when the starting material
contains large quantities, e.g., about 4 percent, of impurities
which are volatile or oxidized to volatile species, the demands
placed on the vacuum unit render such a procedure commercially
impractical. Therefore, it is preferred, in most instances, to
incorporate oxygen into the molten bath by other means. From the
standpoint of economy, efficiency in operation and controllability,
the oxygen content of the bath can be controlled by terminating the
addition of carbonaceous reductant to the bath while continuing the
addition of oxides or by surface blowing the surface of the bath
with a free-oxygen-containing gas.
In practice, a turbulent bath of at least one metal selected from
the group consisting of nickel and cobalt and having at least 0.01
percent oxygen but not saturated therewith is established in a
rotary converter that is provided with means for partially
combusting hydrocarbon fuel above the bath to generate heat and
means for surface blowing the metal bath with a gas containing free
oxygen. The rotary converter is rotated to maintain the metal bath
in a turbulent state and briquetted oxides, or compounds heat
decomposable to oxides, of nickel and cobalt are fed to the
turbulent metal bath to maintain the dissolved oxygen in the bath
at the aforedescribed levels. Carbonaceous reductants are added to
the oxygen-containing metal bath to rapidly and energetically
reduce the oxide fed to the bath. The amounts of oxide and
reductant added to the bath are proportioned to insure that the
bath contains at least about 0.01 percent oxygen and does not reach
saturation levels. Precautions need not be taken to insure that the
fuel has a low sulfur content since sulfur absorbed by the bath
will be subsequently removed by the subatmospheric pressure
treatment. Carbon monoxide generated by the reduction reactions,
the carbonaceous reductant and fuel introduced via the burner are
burned with an excess of free oxygen to maintain the bath at a
temperature at least about 50.degree.C. above its melting point.
The additions of agglomerated oxide and solid reductants can be
simultaneous or can be repeatedly alternated until the furnace
capacity is approached. When the capacity of the furnace is
approached, the oxygen content of the bath can be adjusted so that
the metal can be cast into product form. Alternatively, the oxygen
content of the bath can be adjusted for final impurity elimination
during a subatmospheric pressure treatment.
When it is desirable to further purify the metal bath, the bath is
subjected to a vacuum treatment for final impurity elimination. It
is advantageous for thermodynamic and kinetic reasons to subject
the metal bath to a vacuum of less than about 0.1 atmosphere and
advantageously to a pressure less than about 0.01 atmosphere or
even less than about 0.001 atmosphere. If the bath is deficient in
oxygen, additional oxygen can be added thereto. Advantageously,
gaseous oxygen is introduced into the molten bath to overcome any
oxygen deficiencies. The addition of oxygen during the low pressure
treatment is advantageous in that it lessens the need to
incorporate all the oxygen required for final impurity elimination
by surface blowing during the smelting operation and thereof avoids
the problems associated with possible formation of undesirable and
inactive metal oxide dross. Gaseous oxygen can be added as air,
oxygen-enriched air, preheated air or commercial oxygen.
Maintenance of the metal bath in a turbulent state during the
vacuum treatment is highly desirable since independently induced
turbulence is generally of such intensity that the bath is
sufficiently mixed such that approach to equilibrium is materially
increased. Furthermore, constant mixing continually provides fresh
surfaces from which volatilization can occur without overcoming the
pressure head of the metal bath. During the vacuum treatment, the
bath can be maintained in a turbulent state by pneumatic means
(e.g., by the addition of a free-oxygen-containing gas), as well as
by mechanical agitation, magnetic means or electromagnetic
stirring.
For kinetic reasons and to insure more complete impurity
elimination, the metal bath is maintained at a temperature of at
least about 50.degree.C. above its melting point during the vacuum
treatment. Even better results are obtained by maintaining the
metal bath at a temperature of about 100.degree.C. above its
melting point. Higher temperatures provide better results by
increasing the vapor pressure of the volatile impurities, by
thermodynamically insuring more complete reactions when impurities
are being eliminated as volatile oxides and by the amount of
dissolved oxygen to thereby increase the driving force of this
oxidizing reaction. In addition to rapid sulfur elimination down to
about 0.5 percent and advantageously below about 0.01 percent
sulfur, impurities such as bismuth and lead can be eliminated to
almost undetectable amounts. The subatmospheric pressure treatment
is advantageously continued after elimination of impurities without
further oxygen additions to degas the metal.
After the refining and deoxidation operations, the metal bath can
be finally deoxidized by the addition of carbon, silicon, aluminum,
or calcium silicon. Deoxidation can also be effected by lancing the
turbulent bath with methane or other gaseous hydrocarbons or by
passing a reducing gas containing carbon monoxide, hydrogen or
methane through the molten bath or by surface blowing the bath with
such reducing gases. Advantageously, after both final impurity
elimination and deoxidation, the melt is degassed under
subatmospheric pressures to provide a final metal product that has
a low content of dissolved gases which product is particularly
suitable for continuous casting.
Refining and degassing can be conducted in a suitable vacuum
chamber in which low pressures are maintained by mechanical pumps,
steam ejector systems, or any other system capable of pumping large
volumes of gas at low pressures. The vacuum chamber is equipped
with means for controlling the temperature of the molten bath. For
instance, the vacuum unit can be heated by induction or by carbon
arc or by other means. The molten bath can be maintained in a state
of turbulence while undergoing vacuum treatment by electromagnetic
stirring or by pneumatic or mechanical means.
For the purpose of giving those skilled in the art a better
understanding of the invention, the following illustrative examples
are given:
EXAMPLE I
A charge consisting of 1.5 inches .times. 1 inch .times. 1 inch
briquettes of basic nickel carbonate analyzing approximately 54
percent nickel plus cobalt on a dry basis, and containing about 20
percent moisture was fed into a rotary converter operating at 20
revolutions per minute. The converter contained a bath of molten
nickel maintained at about 2,950.degree.F. and containing
approximately 0.1 percent dissolved oxygen. The carbonate was added
at 80 pounds per minute, and metallurgical coke at the rate of 9.6
pounds per minute. A very vigorous boil was maintained, and the
carbonate and coke was almost immediately reacted. The converter
was maintained at between 2,900.degree.F. and 2,980.degree.F. by
burning natural gas within excess of the stoichiometric requirement
of oxygen. The amount of oxygen was such that the gas exiting from
the converter was contained between about 0 and 3 percent carbon
monoxide. The carbon monoxide from the reduction of nickel oxide by
carbon was threfore being largely burned to carbon dioxide in the
converter, supplying a significant portion of the heat requirements
for the process. Dust losses to the converter stock were
negligible.
After teeming a portion of the heat, a further test on this heat
was continued at a higher smelting rate. At 100 pounds per minute
carbonate, the reaction of the carbonate and coke was still much
faster than the rate of addition. The gas velocity out of this
small converter was higher than the available gas handling
capabilities of the flue system. Thus, even higher smelting rates
may be possible with equipment engineered for this application.
EXAMPLE II
A heat of nickel similar to that obtained in the previous example
containing 0.8 percent sulfur and just saturated with oxygen at
2,900.degree.F. was held in a 750 kilowatt, 180 cycle vacuum
induction furnace. The furnace was gradually evacuated to a fine
vacuum of about 0.1 mm. of mercury using up to 6 stages of a
7-stage steam ejector. A vigorous boil occurred as the vacuum was
taken below 100 mm. mercury because of the rapid withdrawal of
SO.sub.2. After a total evacuation time of approximately 2 hours,
the sulfur was analyzed at 0.003 percent. The heat was then
deoxidized using graphite as the reductant to produce a final metal
having an analysis of 0.003 percent sulfur and about 0.01 percent
carbon.
It will be observed that the present invention provides a process
for reducing metal compound. The process comprises establishing a
bath of at least one metal selected from the group consisting of
nickel and cobalt, which bath contains at least about 0.1 percent
dissolved oxygen (and advantageously at least about 0.1 percent
dissolved oxygen). At least one compound selected from the group
consisting of nickel oxide, cobalt oxide, and compounds heat
decomposable thereto and a carbonaceous reductant are fed to the
bath while the dissolved oxygen content of the bath is maintained
at at least 0.01 percent (and advantageously at least about 0.1
percent) whereby the carbonaceous reductant reacts with the
dissolved oxygen in the bath to generate carbon monoxide. The
generated carbon monoxide and a fuel are burned above the bath with
free-oxygen-containing gas to heat the bath to operating
temperatures. A portion of reduced metal is recovered from the
bath.
Although the present invention has been described in conjunction
with preferred embodiments it is to be understood that
modifications and variations may be resorted to without departing
from the spirit and scope of the invention as those skilled in the
art will readily understand. Such modifications and variations are
considered to be within the purview and scope of the invention and
appended claims.
* * * * *