U.S. patent number 3,837,820 [Application Number 05/176,979] was granted by the patent office on 1974-09-24 for combustion control by additives introduced in both hot and cold zones.
This patent grant is currently assigned to Apollo Chemical Corporation. Invention is credited to Ira Kukin.
United States Patent |
3,837,820 |
Kukin |
September 24, 1974 |
**Please see images for:
( Certificate of Correction ) ** |
COMBUSTION CONTROL BY ADDITIVES INTRODUCED IN BOTH HOT AND COLD
ZONES
Abstract
By burning fuel in the presence of manganese and magnesium, and
by then additionally adding to the products of combustion at a
relatively low temperature zone an additional amount of magnesium,
noxious and undesirable emissions are greatly reduced and internal
boiler conditions are greatly improved.
Inventors: |
Kukin; Ira (West Orange,
NJ) |
Assignee: |
Apollo Chemical Corporation
(Clifton, NJ)
|
Family
ID: |
22646683 |
Appl.
No.: |
05/176,979 |
Filed: |
September 1, 1971 |
Current U.S.
Class: |
431/2; 44/354;
44/640; 110/343; 44/457; 44/641 |
Current CPC
Class: |
C10L
1/1233 (20130101); C10L 10/04 (20130101); C10L
10/02 (20130101); F23J 2215/20 (20130101) |
Current International
Class: |
C10L
1/10 (20060101); C10L 1/12 (20060101); C10l
009/00 () |
Field of
Search: |
;44/51,DIG.3,5 |
References Cited
[Referenced By]
U.S. Patent Documents
Foreign Patent Documents
|
|
|
|
|
|
|
1,189,356 |
|
Apr 1970 |
|
GB |
|
634,000 |
|
Jan 1962 |
|
CA |
|
740,062 |
|
Nov 1955 |
|
GB |
|
Primary Examiner: Wyman; Daniel E.
Assistant Examiner: Smith; Mrs. Y. H.
Claims
I claim:
1. The method of improving the effects of fuel combustion which
comprises:
a. Burning the fuel in the presence of a first effective amount of
an additive comprising a substance from the group consisting of
manganese, magnesium, compounds thereof, and combinations
thereof;
b. Conveying the combustion products to a relatively low
temperature station;
c. Adding to said combustion product at said station a second
amount of additive comprising a substance from the group consisting
of magnesium, magnesium compounds and combinations thereof; and
d. Conveying the resultant products to an exhaust station.
2. The method of claim 1, in which said fuel is burned in a boiler
and then conveyed through superheater means, said low temperature
station being located after said superheater means.
3. The method of claim 1, in which the temperature at said
relatively low temperature station is about 200.degree. to
1,000.degree. F.
4. The method of claim 1, in which said fuel is burned at the
combustion station and means are provided for recirculating a
substantial portion of said combustion products from said
relatively low temperature station to said combustion station, and
in which a member from a substance from the group consisting of
magnesium, magnesium compounds and combinations thereof is
physically added to said combustion products at said low
temperature station and in an amount at least equal to the sum of
said first and second amounts, said recirculation accomplishing the
step (a) addition of said substance.
5. The method of claim 1, in which said additive step (a) comprises
a manganese compound.
6. The method of claim 1, in which said additive of step (c)
comprises a substance selected from the group consisting of
magnesium oxide and magnesium hydroxide.
7. The method of claim 1, in which said second amount is at least
about 1.7 pounds of magnesium oxide or the equivalent thereof in
the case of other substances, per ton of sulphur in the fuel.
8. The method of claim 1, in which said second amount is from about
1.7 to 5.2 pounds of magnesium oxide, or the equivalent thereof in
the case of other substances, per ton of sulphur in the fuel.
9. The method of claim 1, in which said second amount is from about
1.7 to 17 pounds of magnesium oxide, or the equivalent thereof in
the case of other substances, per ton of sulphur in the fuel.
10. The method of claim 5, in which said additive of step (c)
comprises a substance selected from the group consisting of
magnesium oxide and magnesium hydroxide.
11. The method of claim 10, in which said second amount is at least
about 1.7 pounds of magnesium or magnesium compound, based on
magnesium oxide as said substance, per ton of sulphur in the
fuel.
12. The method of claim 10, in which said second amount is from
about 1.7 to 5.2 pounds of magnesium substance, based on magnesium
oxide as said substance, per ton of sulphur in the fuel.
13. The method of claim 3, in which said additive step (a)
comprises a manganese compound.
14. The method of claim 13, in which said additive of step (c)
comprises a substance selected from the group consisting of
magnesium oxide and magnesium hydroxide.
15. The method of claim 14, in which said second amount is at least
about 1.7 pounds of magnesium or magnesium compound, based on
magnesium oxide as said substance, per ton of sulphur in the
fuel.
16. The method of claim 14, in which said second amount is from
about 1.7 to 5.2 pounds of magnesium substance, based on magnesium
oxide as said substance, per ton of sulphur in the fuel.
17. The method of claim 3, in which said additive of step (c)
comprises a substance selected from the group consisting of
magnesium oxide and magnesium hydroxide.
18. The method of claim 17, in which said second amount is at least
about 1.7 pounds of magnesium or magnesium compound, based on
magnesium oxide as said substance, per ton of sulphur in the
fuel.
19. The method of claim 17, in which said second amount is from
about 1.7 to 5.2 pounds of magnesium substance, based on magnesium
oxide as said substance, per ton of sulphur in the fuel.
20. The method of claim 4, in which said additive of step (c)
comprises a substance selected from the group consisting of
magnesium oxide and magnesium hydroxide.
21. The method of claim 20, in which said second amount is at least
about 1.7 pounds of magnesium or magnesium compound, based on
magnesium oxide as said substance, per ton of sulphur in the
fuel.
22. The method of claim 20, in which said second amount is from
about 1.7 to 5.2 pounds of magnesium substance, based on magnesium
oxide as said substance, per ton of sulphur in the fuel.
23. The method of claim 6, in which said second amount is at least
about 1.7 pounds of magnesium or magnesium compound, based on
magnesium oxide as said substance, per ton of sulphur in the
fuel.
24. The method of claim 6, in which said second amount is from
about 1.7 to 5.2 pounds of magnesium substance, based on magnesium
oxide as said substance, per ton of sulphur in the fuel.
Description
The present invention relates to a method for improving fuel
combustion in furnaces, thereby to greatly improve stack emission
problems and to minimize boiler fouling.
There are two general areas where fuel combustion presents
problems. One general area involves the nature and amount of
chemicals which are discharged into the environment. The substances
emitted are often corrosive or otherwise damaging to any surfaces
on which they fall. In many instances they are harmful to human or
plant life, and in many instances they contribute to the formation
of smog. These problems are today very generally recognized as
quite serious, and strenuous efforts are being made to reduce the
environmental pollution attendant upon combustion. The other
general area, boiler fouling as a result of the formation of
various substances in the boiler which coat the walls or the tubes
of the boiler, constitutes a direct economic problem, since it
reduces the efficiency of heat transfer and, when the build-up of
materials becomes too great within the boiler, necessitates that
the boiler be shut down from time to time for cleaning purposes, an
obviously uneconomical procedure.
In general, different fuels present different problems. With
sulphur-containing fuels, one of the major problems is the
concentration of sulphur dioxide and sulphur trioxide in the stack
gases. These compounds are extremely deleterious from a pollution
point of view. When fuels contain vanadium in addition to sulphur,
the production of undesired sulphur oxides is accentuated; the
vanadium, probably in combination with the exposed iron on the
tubes in the boiler, is able to catalyze the formation of
undesirable sulphur oxides. Since both sulphur and vanadium are
present in many of the commonly available industrial fuels, these
problems are very pressing from a pollution control standpoint.
One standard approach to minimizing pollution problems is to add
various substances to the fuel with a vew to having those
substances enter into chemical combination with the undesired
products of combustion in order to render them less undesirable or
more readily removable from the stack emissions. Many different
substances have been proposed to this end, including manganese and
magnesium, usually introduced into the fuel in the form of
compounds such as oxides and hydroxides. It is the manganese and
magnesium which are the active ingredients, the oxides ane
hydroxides being chosen as the addition media because they are more
readily available and handleable than the active metals
themselves.
With these additives, as with other additives, problems often
arise. In some instances the additives, while entering into the
expected reactions, also enter into side reactions the products of
which present their own individual problems, which sometimes
outweigh the problems which are intended to be cured. Also, in some
instances particular additives, especially when used in large
quantities, cause such fouling of the interior of the boilers as to
make them undesirable from an economic point of view. Moreover, all
additives are costly, and if especially large amounts of a
particular additive are required in order to produce a given
improvement the cost may be prohibitive from a commercial point of
view.
It is the prime object of the present invention to improve the
effects of fuel combustion, particularly with regard to emitting
sulphur trioxide in the stack gases and improving the condition of
the boilers where the combustion is carried out.
It is a further prime object of the present invention to achieve
that improvement through the use of a minimal amount of additive,
thereby reducing the expense of the fuel combustion improvement
process.
It is another object of the present invention to provide a fuel
combustion improvement process which is particularly adaptable for
use in conjunction with commercially available fuels, and which can
be carried out in existing combustion installations with a minimum
of difficulty.
It is a further object of the present invention to provide a
process for improving the effects of fuel combustion which inhibits
the formation of slag in the boiler and which minimizes the
emission of many acid substances in addition to sulphur
trioxide.
The process of the present invention, involving as it does the
presence of manganese or magnesium at the time of combustion, not
only inhibits the formation of hard slag within the boiler, thereby
to reduce boiler fouling, but also, by combining with vanadium in
the fuel to form a relatively soft coating on the iron tubes within
the boiler, reduces the production of sulphur trioxide by
minimizing the availability of iron and vanadium to catalyze the
formation of SO.sub.3. This is done by burning the fuel in the
presence of magnesium or manganese additives in minimal amounts.
This alone is known in the prior art; it produces a reduction of
SO.sub.3 by about 25-40 percent. It is important to note, however,
that this prior art approach only incompletely reduces the SO.sub.3
content of the stack emission, and still leaves that emission with
a very substantial SO.sub.3 content. Adding additional quantities
of manganese or magnesium to the fuel have been ineffective in
SO.sub.3 reduction, have caused fouling problems within the boiler
and have involved excessive cost.
I have discovered that if, in addition to the employment of
manganese or magnesium in the hot zone of the furnace where the
fuel is burned, one also adds magnesium to the combustion products
at a zone in the furnace which has low temperature relative to the
temperature of the combustion zone, several highly advantageous
results are achieved: the ash is made less acidic (its pH is
raised), the hygroscopic nature of the flue gas particulates is
reduced, acid smut is effectively eliminated, boiler fouling is
reduced because lesser amounts of additive need to be applied at
the combustion station, and, most importantly, the SO.sub.3 content
of the fuel gas is very radically reduced by as much as 80
percent.
The method in question can be used with many different types of
fuel and many different types of furnaces. It may be used in
oil-fired boilers such as those employed by utility companies,
refineries and large industrial plants, with the additive feed to
the relatively low temperature zone (hereinafter sometimes called
cold-end feed) occurring at the economizer outlet, for example. The
combustion of both residual fuel and crude oil is greatly improved
in that manner. The process may also be used with coal-fired and
waste gas-fired boilers with a cold end feed occurring at the
up-takes, for example. The process is also applicable for use in
steel mills burning waste gases, either alone or with Bunker C
fuels, by refineries burning waste gas in boilers, and in refinery
process heaters burning waste gas or waste gas in combination with
Bunker C fuel. This list of examples is not intended to be
all-inclusive.
When the magnesium-containing substance is added to the combustion
products at a relatively low temperature station, it reacts
directly and catalytically with the SO.sub.3 in the flue gas. It
dramatically reduces acid particulates, acid condensation and dew
point of the flue gas.
The cold zone supplemental treatment has been found to be more
effective in controlling acid conditions than the standard oil
treatment methods. One reason for this greater reactivity is that
the cold zone additive does not have to first pass through the
flame zone before combining with SO.sub.3 in the colder zones of
the boiler. In the flame, oil dispersed additives, such as MgO or
MgO:Al.sub.2 O.sub.3, do not react with SO.sub.3 at the high
temperatures involved. At high boiler temperatures the sulfate
complexes decompose, actually releasing SO.sub.3. The dryer and
less hygroscopic ash resulting from the cold-end feed reduces cold
end corrosion and at the same time will often eliminate acid smut
emission problems. Moreover, an improvement in the stack plume
appearance will often result from cold-end feed, with the
consequent elimination of nuisance and legal complaints,
particularly when the plant is in a residential area.
The most practical and least costly way of carrying out the method
here disclosed is by initial treatment of the fuel oil with a
manganese- or magnesium-containing substance in order to minimize
the amount of SO.sub.3 in the stack gases and thus to minimize the
amount of magnesium containing substance to be added at the cold
zone. When this is done, the amount of additive can be reduced
considerably, by 20 or 50 percent or more, over what was normally
thought to be required with a particular fuel, yet the overall
reduction in SO.sub.3 content in the exit gases is very greatly
improved over what had previously been possible through the use of
relatively large amounts of additive in the fuel oil.
In some boilers a portion of the combustion gases, after they leave
the combustion station and their temperature drops, is recirculated
back to the combustion station. In boilers of this type the method
of the present invention can be practiced by adding a
magnesium-containing substance to the combustion products in
advance of the point where recirculation takes place. This not only
constitutes the "cold-end feed," but also, by reason of the
recirculation of a portion of the combustion products back to the
combustion zone, serves in effect to add the magnesium-containing
substance to the fuel oil in the combustion chamber.
By combining the operative use of a magnesium- or
manganese-containing additive at the combustion station with a
magnesium-containing substance at a station having a relatively low
temperature, SO.sub.3 is very substantially removed from the flue
gas, the SO.sub.3 formerly in the gas forming a dry and
non-corrosive powder. Those materials entrained in the flue gas are
generally rendered non-acidic, thus preventing damage to paint
surfaces, equipment and other objects in areas surrounding the
combustion plant. The visible plume from the stacks is often
reduced, and the acridity of the odor from the stacks is minimized.
The effectiveness of soot blowers and stack collectors, when
employed, is enhanced, the overall fallout from stack gases is
localized and the possibility of plume "hang-up" in the effect of
an atmospheric inversion is minimized.
With many fuels it is preferred that the combustion chamber
additive be a manganese-containing substance. Such a substance
reduces the amount of carbon in the fly ash because manganese is
known to be a carbon-destroying catalyst. This in itself is an
advantage, since wet carbon leaving the boiler tends to absorb
SO.sub.3. Moreover, the presence of manganese tends to cause the
formation of SO.sub.2 rather than SO.sub.3. The addition of the
magnesium-containing substance thereafter in the low temperature
zone is effective to remove virtually all of the SO.sub.3 which
does form in the boiler.
To the accomplishment of the above, and to such other objects as
may hereinafter appear, the present invention relates to a method
of improving the effects of fuel combustion, as defined in the
appended claims and as described in this specification, taken
together with the accompanying drawings, in which
FIG. 1 is a schematic representation of an exemplary fuel-burning
boiler installation of the non-recirculating type; and
FIG. 2 is a schematic representation of an exemplary fuel-burning
boiler installation in which a portion of the products of
combustion are recirculated back to the combustion chamber.
The illustrations are provided simply for purposes of facilitating
explanation of the process of the present invention. The
illustrated boiler arrangements per se form no part of the present
invention, are not novel in and of themselves, and are merely
exemplary of many different types of constructions and arrangements
with which the process of the present invention can be practiced.
Since the process of the present invention involves introducing
additives at different stations in the boiler, and particularly at
a high temperature station such as the combustion chamber and at a
low temperature station downstream of the combustion chamber, some
appreciation of the general arrangement of boiler systems is of
assistance in understanding the process of the present invention
and the results achieved thereby, and it is for that reason that
FIGS. 1 and 2 are here presented.
FIG. 1 represents a particular boiler installation where no
recirculation of the products of combustion takes place. An
appropriate fuel, such as fuel oil, coal or combustible gas, is
introduced into the furnace 1 in any appropriate manner as through
burner guns 24 in the case of fuel oil. Air, preferably heated, is
supplied to the furnace in any appropriate manner to combine with
the fuel. Combustion of the fuel takes place in the furnace 1, the
portion of the heat energy produced by that combustion being
transmitted to the tubes (not shown) covering the furnace walls,
thus converting the water in those tubes to steam. Combustion of
the hot gas may be completed by means of the addition thereto of
secondary heated air from the heated air duct 21, air being
supplied to that duct by air inlet 16, blower 17, air duct 18, air
preheater 19 and air ducts 20 and 21. The products of combustion
then pass through the platen superheater 2 and reheater 3, pendant
superheater 4, and the horizontal superheater 5. When the
combustion products leave the horizontal superheater 5 their
temperature, which in the furnace 1 was about
2,400.degree.-2,800.degree. F, has been reduced to
800.degree.-900.degree. F. The products of combustion then flow
through the economizer 6 which preheats the water entering the
steam-producing tubes inside the furnace 1. The products of
combustion then flow into the gas duct 7 at a temperature of
650.degree.-700.degree. F. They then flow through duct 8 and air
heater 9, the air heater 9 tending to transfer the heat from the
exiting gases to the air preheater 19. At this point the
temperature of the products of combustion is approximately
300.degree. F. The products of combustion then flow through duct 10
and precipitators 11 where ash is removed from the stream of gas.
The thus cleaned gas flows through duct 12 and induced draft fan 13
into breeching and then out through the stack 15.
One of the most important problems in connection with reducing air
pollution caused by products of combustion is the presence of
acidic SO.sub.3 in the combustion products. That compound is itself
deleterious, and in addition it tends to be taken up in the
particulate matter which escapes from the stack to produce an acid
smut often referred to as "green rain."
The conventional approach to minimize this situation is to
introduce into the furnace a suitable quantity of a magnesium
compound, such as magnesium oxide. This is done by mixing it with
the fuel or by applying it to the coil before the latter is burned
or by adding the substance to the furnace while combustion takes
place. Such an additive has several effects. It reacts with the
vanadium in the fuel to prevent high temperature corrosion and the
formation of hard slag inside the furnace. It acts itself to coat
the superheater tubes and thus insulate the products of combustion
from the iron surfaces of those tubes. Since iron catalyzes the
formation of SO.sub.3 from SO.sub.2, this results in a reduction in
the formation of SO.sub.3. In addition, the magnesium compound
reacts with vanadium, thus reducing the amount of vanadium oxide
which is formed, that vanadium oxide also tending to catalyze the
formation of SO.sub.3. For these purposes, the magnesium oxide can
be added to the fuel in any suitable form, such for example as a
pre-mix with the fuel, as a liquid slurry added to the fuel, or as
a powder injected into the furnace proper.
However, there is a limit to the amount of magnesium compound which
can be provided at the high temperature combustion zone in the
furnace. If too much such material is provided large amounts of ash
will result; this ash will build up in and eventually block the
furnace, requiring that it be shut down and cleaned. Moreover, the
greater the amount of ash, the greater the amount of inorganic
particulate matter emitted through the stack. In addition, the
mechanism by which magnesium reduces the amount of SO.sub.3 in the
products of combustion involves the formation of magnesium
sulphate. Magnesium sulphate decomposes at temperatures above
1,500.degree. F, and since the temperatures in the furnace are well
above that value the decomposition of magnesium sulphate undoes
what the added magnesium initially accomplishes. Indeed, the nature
of the reactions involving SO.sub.2 are such that the introduction
of massive amounts of magnesium oxide into the hot end of the
furnace may actually increase the production of SO.sub.3 rather
than decrease it.
It has been proposed in the past that certain substances be added
to the products of combustion at a relatively low temperature
station. However, insofar as magnesium-containing oxides and any
effect they may have in reducing SO.sub.3 are concerned, this
approach is ineffective, because the magnesium compounds by
themselves are too inert to produce the desired result. They are in
solid form and must react with gaseous products. Reaction rates in
such conditions are generally very low. To use a magnesium compound
such as magnesium oxide only in conjunction with cold end feed
would require so much magnesium oxide that particulate matter would
escape from the stack in tremendous volume, and a pollution problem
would be created rather than eliminated.
I have found that by combining a magnesium-containing substance
added at the cold end with a magnesium-containing or
manganese-containing substance added at the hot end, greatly
improved results are obtained insofar as SO.sub.3 reduction is
concerned. A normal amount of magnesium oxide when added to the
combustion zone, in accordance with known practice, results in an
SO.sub.3 reduction of 15-25 percent, and that reduction cannot be
increased to much more than 40 percent no matter how much magnesium
oxide is added to the furnace and no matter what the deleterious
effects of adding that magnesium oxide to the furnace may be. The
same amount of magnesium oxide added only to the cold end of the
furnace (for example, at the outlet of the economizer 6 in FIG. 1,
a preferred place for effecting the cold-end feed in accordance
with the present invention) will reduce the SO.sub.3 content by
35-40 percent. However, if the same total amount of magnesium oxide
is used, but with 25 percent thereof added to the combustion zone
and 75 percent added to the cold end (e.g. the outlet of the
economizer 6 of FIG. 1) 50-80 percent of the SO.sub.3 is
removed.
If the substance added to the combustion zone is a
manganese-containing substance such as manganese oxide, and if it
is added solely to the furnace, the total SO.sub.3 removed is 40
percent or better, under exceptional circumstances sometimes going
as high as 75 percent. If, in conjunction with the addition of such
manganese oxide to the combustion zone, a magnesium-containing
compound such as magnesium oxide is added at the cold end, the
total SO.sub.3 emitted is easily reduced by 80-95 percent. Thus it
is seen that the combination of hot-end feed and cold-end feed as
here disclosed results in greatly improved SO.sub.3 reduction, to a
degree not achievable through the use of hot-end addition alone or
cold-end addition alone, and through the use of moderate and
economically feasible amounts of the additive materials.
The active components of the additive materials here under
discussion are manganese and/or magnesium. However, the handling of
those metals is not particularly convenient, nor are they
commercially available in quantity at reasonable prices.
Accordingly, the preferred additives are compounds of magnesium
and/or manganese, usually the oxides or hydroxides thereof because
of their ready and economic availability and ease of handling.
I set forth below a number of specific examples illustrating the
manner in which my new method of improving the effects of fuel
combustion can be carried out and showing the advantages thereof
over that which had formerly been thought to be achievable. It will
be understood that these examples are in no way limiting, and that
the method in its broader application can be practiced in
specifically different ways and in different environments.
Bunker C fuel containing an average of 225 parts per million
vanadium, a sulfur content of an average of 2.05 percent and an ash
content of 0.07 to 0.10 percent was burned in a front fired boiler
with a 375 megawatt output and a superheat steam temperature of
1,050.degree. F.
At 2 percent excess oxygen, the SO.sub.3 content without any
treatment was 60 parts per million.
Example 1
A slurry of magnesium oxide was injected directly into the fuel oil
being burned at a treatment rate of 3.1 lbs, MgO/8,000 lbs. of fuel
oil. The temperature in the flame zone was in excess of
2,300.degree. F.
The reduction of the SO.sub.3 in the flue gas was from 60 to 50
parts per million.
Example 2
The MgO was aspirated into the economizer outlet of the boiler at a
temperature of 700.degree. F. rather than being injected into the
fuel oil. On a dry powder basis, 3.1 lbs. of magnesium oxide was
injected for each 8,000 lbs. of fuel oil burned in the above
boiler.
The SO.sub.3 was reduced from 60 to 45 parts per million.
Example 3
A slurry of the magnesium oxide was introduced into the boiler to
provide 1.5 lbs. of magnesium oxide for each 8.000 lbs. of fuel
burned. At the same time the dry, powdered, MgO was concurrently
aspirated into the economizer outlet, to provide 1.6 lbs. MgO for
each 8,000 lbs. of fuel in the same boiler. In other words,
although the same amount of MgO was used in Example 3 as in either
Example 1 or 2 above, the quantity was split up so that half of the
MgO was added to the boiler proper and the other half was added to
the outlet section of the boiler in the economizer region at
temperatures of 500.degree. to 600.degree. F.
Under these conditions, the SO.sub.3 was reduced from 60 to 30
parts per million.
Example 4
In this case, the slurry of MgO was added exactly as in Example 1
so as to provide 3.1 lbs. MgO for 8,000 lbs. of fuel oil. In
addition, 1.6 lbs. MgO as a dry powder was aspirated into the
economizer outlet.
The SO.sub.3 was reduced from 60 to 27 parts per million. In other
words, increasing the amount of MgO added to the fuel oil did not
significantly reduce the SO.sub.3 content of the flue gas. Stated
in another way, there was a limiting factor in how far one could
reduce the SO.sub.3 when injecting the magnesium oxide through the
furnace by direct addition to the fuel oil.
Example 5
The addition of 1.5 lbs. of MgO as a slurry to the fuel oil was
supplemented by the direct injection of dry powdered magnesium
oxide into the economizer outlet, to provide a total of 3 lbs. of
MgO aspirated directly into the flue gas through the economizer
outlet.
The SO.sub.3 was reduced from 60 to 21 parts per million. This
further shows that once a minimum amount of MgO is added to the
fuel oil to provide a coating within the boilers, then the further
addition of MgO as a dry powder into the flue gas has a much
greater effect in reducing SO.sub.3 than adding that equivalent
amount or adding that same amount of MgO to the fuel oil through
the burner. This could indicate that cold-end injection (at
temperatures of 200.degree. to 1,000.degree. F.) is more effective
than the addition of the MgO through the furnace where temperatures
reach 2,000.degree. to 3,300.degree. F. or thereabouts.
Example 6
In this example, and in subsequent ones, the magnesium oxide was
added to the fuel oil to provide 1.5 lbs./8,000 lbs. of fuel oil
resulting in a reduction of the SO.sub.3 from 60 to 55 parts per
million. In addition the fuel was further treated with a slurry of
a manganese oxide to provide 16.5 parts per million of manganese to
the fuel oil.
The SO.sub.3 in the flue gas was reduced from 60 to 47 parts per
million. This shows that the manganese is even more effective than
the magnesium for reducing SO.sub.3 when added to the fuel, but the
reduction of the SO.sub.3 in the flue gas is still insufficient to
prevent low temperature corrosion.
Example 7
The fuel was treated with both the magnesium and manganese as in
Example 6 above and magnesium oxide, as a cold dry powder, was
aspirated into the economizer outlet at 700.degree. F. to provide
an additional 1.6 lbs. of MgO for each 8,000 pounds of fuel oil.
The SO.sub.3 was reduced from 60 to 26 parts per million.
Example 8
The fuel was treated with a slurry of manganese oxide to provide 40
parts per million manganese to the fuel. The SO.sub.3 in the flue
gas was reduced from 60 to 48 parts per million.
Example 9
The fuel was treated with the manganese oxide slurry to provide 40
parts per million manganese to the fuel oil. At the same time,
magnesium oxide was aspirated as a dry powder into the economizer
outlet so that the flue gas was being treated with 1.6 lbs. of MgO
for each 8,000 lbs. of fuel burned. The SO.sub.3 was reduced from
60 to 23 parts per million. This shows that the combination of
manganese addition to the fuel oil with magnesium oxide powder
added to the flue gas is effective for substantially reducing the
SO.sub.3 and even more effective than the combination of magnesium
oxide addition to the fuel supplemented with magnesium oxide
addition to the flue gas.
Example 10
In this example, a slurry of manganese oxide was added to the fuel
oil as in Example 8. This then was supplemented by the injection of
a magnesium oxide powder into the economizer outlet. However
instead of adding the magnesium oxide on a continuous basis, the
total daily amount of magnesium oxide was split into two portions
and half of this quantity was injected at 12 hour intervals one
hour each time. A coating of the magnesium oxide was thus formed on
the air preheater section of the boiler.
The total amount of additive was equivalent to 0.32 lbs. of MnO
added to the fuel oil and 1.6 lbs. of MgO aspirated into the
economizer (per each 8,000 lbs. of fuel burned). The sulphur
trioxide in the flue gas when the MgO powder was not being fed
remained at 48 parts per million but during the period when the MgO
powder was being fed the SO.sub.3 reduced to 30 ppm.
Although the intermittent use of MgO was not sufficient to prevent
the SO.sub.3 completely, the use of the MgO in this fashion did
almost completely protect preheaters against corrosion. This is
quite significant because it shows how to prevent low temperature
corrosion of the exit sections of the boiler, where there are no
other problems such as acid smut emissions and for other reasons
where it would not be desirable to continuously treat the flue gas
with the neutralizing powder. It also shows the possibility of
reducing the amount of neutralizing powder required by aspirating
it intermittently into the zone in cases where it is only necessary
to lay down a coating on the furnace surfaces.
Example 11
This is similar to Example 10 above except that the additive is
added directly to the fuel oil was a magnesium oxide slurry. Again
the intermittent use of the magnesium oxide powder protected the
air heaters from corrosion to a greater extent than use of
magnesium oxide slurry added only to the fuel oil.
TABLE 1
__________________________________________________________________________
COLD END FEED vs ADDITION TO FUEL OIL FURNACE CHAMBER
__________________________________________________________________________
Fuel = Bunker C of 225 ppm V, 2.05% S and 0.085% Ash Addition of:
Injection Sulfur Acidity Condition Appearance Total Lbs. of Mg:V
Ex- Agent of: Point Trioxide of Ash of of Stack Lbs. of Additive
Weight ample in Flue Deposits Air Additive Ton of Ratio Gas on Air
Heater (on dry Sulfur (parts Heater basis) per Outlet per million)
8,000 lbs. of fuel Equal to Lbs. Addi- tive/1,000 Gals. Fuel
__________________________________________________________________________
-- None None 60 1.9 Heavily Distinct -- -- -- Corroded Blue Plume 1
Magnesium Fuel Oil 50 2.4 Corroded Distinct 3.1(as 37.8 1:1 Oxide
Blue Plume MgO) Slurry 2 MgO Economizer 45 3.0 Fair, Blue Plume,
3.1 37.8 1:1 Powder Outlet only slightly trace of reduced in
Corrosion intensity 3Gi a) Magnesium Fuel Oil ) 1.5 18.3) 0.5:1
Oxide ) Slurry ) 30 4.0 Negligible Slight ) Plus ) Corrosion Blue
Plume ) 37.8 (b) Mgo Economi- 19.5) 0.5:1 Powder zer Out- 1.6 let
4(a ) Mgo Fuel Oil ) 3.1 37.8 1:1 Slurry Plus ) 27 4.0 Negligible
White-grey, ) 57.3 (b ) Mgo Economi- ) Dense Plume 1.6 19.5) 0.5:1
Powder zer Out- ) let ) 5(a ) Mgo Fuel Oil ) 1.5 18.3) 0.5:1 Slurry
) White-- Plus ) 21 4.5 Good --slightly ) 54.9 (b) MgO Economi- )
grey cast 3.0 36.6) Powder zer Out- ) let 6( a) Mgo Fuel Oil ) 1.5
18.3 0.5:1 Slurry ) ) Plus ) 47 2.9 Slight Slight ) 19.9 (b)
Mangasese ) Corrosion Blue Plume 0.132 lbs 1.6) -- Oxide ) MnO
Slurry 7( a) Slurry of Fuel Oil ) 1.5 18.3) 0.5:1 Mgo ) Plus ) )
(b) Slurry of Fuel Oil ) 26 4.2 Good,only Almost 0.132 lbs 1.6)
39.4 -- Manganese trace of clear Oxide Plus Corrosion ) (c) Mgo
Economi- ) 1.6 19.5) 0.5:1 Powder zer Out- ) let ) 8 Slurry of Fuel
Oil 48 2.7 Slightly Slight 40 ppm Mn Manganese Corroded Blue Plume
(0.32 lbs. 3.9 -- Oxide MnO) 9( a) Slurry of Fuel Oil ) 40 ppm Mn
Manganese ) (0.32 lbs 3.9) -- Oxide ) 23 4.6 Negligible Almost MnO)
) 23.4 Plus ) Clear ) (b) MgO Economi- ) 1.6 ) 0.5:1 Powder zer
Out- ) 19.5) let ) 10( a) Slurry of Fuel Oil ) 40 ppm Mn 3.9) --
Manganese ) (0.32 lbs ) 23.4 Oxide ) MnO) ) Plus ) 48 3.8
Negligible Slight ) (b) Mgo Inter- ) (except Blue Plume 1.6 ) 0.5:1
Powder mittently ) during 19.5 into econo- ) MgO mizer outlet feed
(at 12 hr cycle, intervals) when it dropped to 30 ppm) 11(a)
Magnesium Fuel Oil ) 1.5 18.3 0.5:1 Oxide ) ) Slurry ) ) 15.1 Plus
) 55 3.8 Satis- Slight ) (b) Mgo Inter- ) (except factory Blue
Plume 1.6 19.5) 0.5:1 Powder mittently ) during into econo- ) the
Mgo mizer outlet ) feed (as in cycle, 13b) when it dropped to 30
ppm)
Example 12
A novel feature of the present invention is the adding of a
magnesium oxide powder into a furnace in such a way that we get
complete control and arresting of corrosion of the air heaters,
complete elimination of acid smut emissions, the capabilities of
reducing the exit gas temperature by 50.degree. to 100.degree. F.
(which is a fuel savings of 2.5 percent for each 100.degree. drop
in exit temperature), as well as a means of keeping the furnace
clean. As previously shown, using an equal weight of magnesium
oxide added to the fuel oil itself, or injected with the primary
air going to the furnace, or direct addition of MgO powder or an
MgO containing slurry to the hot furnace box, does not give this
benefit of keeping the superheater tubes clean in the furnace,
because (1) any MgSO.sub.4 that forms decomposes in the hot furnace
zones, and (2) the MgO, as it goes through the flame, is exposed to
temperatures of 3,000.degree. F. This causes the MgO to melt and
accordingly it becomes fluxed and is not available as a dry powder
on the surface tubes in the superheaters.
The method described in this Example is a unique one because the
SO.sub.3 is contacted with fresh, dry and unfluxed (active) MgO;
then residual MgO that is recirculated through the furnace is in
direct contact with the superheater tubes so that it is never
exposed to surface temperatures in excess of 2,000.degree. F.
Reference to FIG. 2, which shows an exemplary furnace with
recirculation of a portion of the products of combustion, will be
helpful in understanding this example. Fuel, fuel oil or coal is
injected into the furnace 1' through burner guns 19'. Heated air
from heated air duct 18' combines with the fuel and helps to
atomize it, that heated air being sucked in from the atmosphere at
air inlet 14', blown through duct 16' by fan 15', passing through
air heater 17' and then flowing through duct 18' into the furnace
1'. Combustion of the fuel takes place in the furnace at a high
temperature, and the heat produced thereby is transmitted to the
tubes (not shown) covering the walls of the furnace, coverting the
water in those tubes to steam. The products of combustion pass
through a secondary superheater 2', a reheater 3', a primary
superheater 4', a duct 5', an economizer 6' and a duct 7' into
heater 8' which transmits some of the heat from the exhaust
products to the heater 17'. The exhaust products then flow through
duct 10' to a point where duct 11' and induced draft fan 12' are
located. There some of the products of combustion are forced
through the duct 11' back into the furnace 1' (this being the
recirculated portion of the products of combustion) while the bulk
of those products of combustion pass through duct 13' to a
collection device and thence to the stack.
With a furnace of the type shown in FIG. 2, the
magnesium-containing additive, such as magnesium oxide or magnesium
hydroxide may be added completely at a relatively low temperature
zone, such as the outlet of the economizer 6'. The bulk of the
material thus added remains with low temperature combustion
products, but that portion of the additive entrained with the
recirculated combustion products passing through duct 11' are
returned to the furnace or combustion zone 1', where they are
subjected to the high temperatures of combustion. Thus, although
the magnesium additive is introduced into the system only at a
single location, in fact some of that additive finds its way to the
combustion station, while another portion of the additive remains
in contact with the low temperature combustion products, and hence
in effect some of the additive is introduced at a high temperature
zone and another portion of the additive is subjected only to low
temperature conditions.
The following Table 2 discloses the results obtained in connection
with a furnace of the type disclosed in FIG. 2 in which fuel oil
was burned, the fuel oil containing 0.97 percent sulphur and having
a vanadium content of 100 parts per million and an ash content of
0.035 percent.
TABLE 2 ______________________________________ MgO MgO lbs./8000
Condition of Addition lbs. of Fuel Superheater Tubes
______________________________________ 1) Added as a 50/50 slurry
directly to the fuel oil. 1.75 Furnace walls heavily slagged and
superheater tubes completely bridged over with a heavy coating but
porous and removable with manual lancing. 2) Added as a 50/50
slurry directly to the fuel oil. 1 Some fouling of furnace box, but
not a continuous sheet. Hard deposits on superheater tubes.
Impossible to remove by manual cleaning. 3) MgO added as a powder
into economizer outlet and recirculated back into furnace. 2
Furnace walls have only a minimum of deposit buildup. Superheater
tubes show soft white deposits that are easily removed by manual or
air lancing. Completely cleaned to bare metal by air lancing. 4)
MgO added as a powder into economizer outlet and recirculated back
into furnaces. 1 No deposits on furnace walls. Superheater tubes
show a lightly crusted slag, removable by air lancing.
______________________________________
Example 13
This example, like Example 12, involves cold-end feed of magnesium
oxide and recirculation of a portion of the additive back to the
furnace through the gas recirculation duct 11'.
A coal to oil converted boiler with a mechanical cyclone collector,
a 20 megawatt design unit, was experiencing difficulties following
conversion when fired with Bunker C fuel. The stack emissions had a
low pH of 1.5 and when the particles descended onto the cars in the
employees' parking lot, as well as on adjoining homes near the
utility generating plant, greenish-black, wet, corrosive, deposits
penetrated the paint surfaces of the cars and homes. The surface of
the cars were covered with black-greenish dots or splotches.
The superheat temperature within the furnace was 900.degree. F. and
particularly when burning fuel oils having a sulfur content of 2 to
2.5 percent and vanadium contents of 100 to 400 ppm, there was a
further problem of hard deposits formed on the superheater tubes,
which were difficult to clean off.
As a first attempt to solve this problem, the plant tried the use
of oil slurried additives consisting of 50:50 weight ratio of MgO
in the fuel oil. Using quantities as high as 1 gallon of this 50:50
ratio for each 500 gallons of fuel oil, the persistent acid
emissions were not materially reduced. Moreover, at these high
rates, the plant experienced serious operating difficulties because
of blockage by the magnesium-containing deposits that had built up
between the tubes.
Reverting to a blend of oil additive containing various ratios of
aluminum oxide with the magnesium oxide of 1:10, 1:6, 1:3 and 1:1
and continuing with rates as high as 1 gallon/500 gallons of fuel
did not alleviate the acid emission problem but resulted in even
harder and more tenacious deposits on the superheater tubes.
Using combinations of manganese oxide slurries added to the fuel
oil, as well as mixtures of manganese oxide with magnesium oxide of
various weight ratios from 1:5 to 1:10 of Mn:Mg likewise did not
reduce the emissions problem or the blockage problem within the
boiler.
Since the boilers were equipped with gas recirculation, a blend of
the additive of this invention was added to the economizer outlet
with approximately 50 percent of the powder being recirculated
through the boiler into the superheat cavity. The additive blend
consisted of 70 percent magnesium oxide, 20 percent calcium oxide,
5 percent manganous oxide and 5 percent urea. The addition rate was
14 lbs./hour at a steam level of 300,000 lbs./hour. Utilizing this
cold-end feed, the pH of the deposits collected in the mechanical
hoppers as well as on the surrounding plant was 4.2 and the
deposits were light and fluffy with a whitish appearance. They did
not adhere to the paint surface of the cars or homes.
Quite unexpectedly, the boiler tubes remained extremely clean when
treated in this manner. The boilers remained on the line for a
period of 6 months as compared to 3 months prior to the use of the
additive either when the fuel was untreated or treated with any of
the magnesium oxide, aluminum oxide or manganese containing oxide
slurries described above.
Repeating this test, but using MgO, resulted in a considerably
improved emitted deposit with a pH of 3.8, and the boilers showed
considerably cleaner boiler tubes, without any hard deposits on the
tubes.
Further, it has been found that even in furnaces that do not have a
serious acid emissions problem, this combination of aspiration of
MgO with gas (and powder) recirculation back to the furnace is a
considerably improved way to prevent hard, tenacious and corrosive
vanadium deposits from fouling the superheater tubes and passages.
The same amount of MgO added to the fuel does not produce these
dramatic results, and instead will often require a more frequent
shutdown of the furnace for clean-down.
Example 14
This example illustrates the use of the method of the present
invention in connection with a furnace which had been converted
from coal firing to oil firing, utilizing Bunker C fuel oil with an
80 megawatt rating.
It was experiencing great difficulty in utilizing the electrostatic
precipitators when burning the liquid fuel. Fouling of the air
heater elements occurred and sticky adherent deposits were present,
which resulted in frequent shutdowns. Further, the pH of the
deposits collected on the precipitators, as well as the deposits
collected 100 feet from the stack, showed a value of 1.5 to
1.9.
An intimate mixture consisting of 60 percent magnesium oxide, 15
percent sodium bicarbonate, 10 percent calcium oxide and 15 percent
manganous oxide was injected into the economizer outlet of the
furnace before the electrostatic precipitators.
The particle size of the powder mixture averaged 25 to 40 microns.
The addition rate of the powder was 7.5 lbs./8,000 lbs. of fuel
burned, the fuel having a sulphur content of 2.7 percent, a
vanadium content of 375 parts per million and an ash of 0.14
percent.
With this dry powder addition, the pH of the deposits collected 100
feet from the stack was found to be 4.1. There was negligible
sticky deposits on the electrostatic precipitators which
functioned, virtually uninterruptedly, as long as the powder blend
was fed continuously into the economizer outlet at temperatures of
400.degree. to 850 F., the normal temperature of the flue gas at
the economizer outlet.
The addition of this powder, or the same amount of MgO of 7.5
lbs./8,000 lbs. of fuel, directly to the fuel or to the furnace did
not raise the pH of the stack deposits above 2.5 to 3.0, an
ineffective result.
Where, as is optimally the case, the cold-end additive is used to
minimize the presence of SO.sub.3 in the flue gas, at least enough
additive should be used to accomplish the maximum neutralization of
SO.sub.3. This will, of course, depend upon the amount of sulphur
in the fuel to begin with, the percent of conversion of that
sulphur (as SO.sub.2) to SO.sub.3 in the course of combustion
(generally ranging from 1 to 10 percent depending upon the
particular combustion conditions and hot-end additives used) and
also the amount of excess air present. This if a fuel oil contains
0.25 percent sulphur, for optimum minimum use of a 1:1 equivalent
neutralizing mole ratio of additive to SO.sub.3, then 0.2 lbs. of
cold-end additive in the form of MgO per 8,000 lbs. of fuel oil
would be required if the conversion of SO.sub.2 to SO.sub.3
amounted to 1 percent, and 2.0 lbs. of that additive would be
required if the conversion figure were 10 percent. Stated in terms
of ratio of additive per tons of sulphur in the fuel oil, 1.7 lbs.
of MgO additive per ton of sulphur would be required where the
conversion figure is 1 percent and 17 lbs. of that additive would
be required where the conversion figure was 17 percent. If the fuel
oil contained a greater proportion of sulphur, then the amounts of
additive would increase but the ratio of additive would remain the
same.
If it is desired to remove SO.sub.2 from the flue gases, then
additional amounts of cold-end additives will be required, with a
lower limit of perhaps 2.5 lbs. of MgO additive per 100 lbs. of
fuel for each 1 percent of sulphur content in the fuel.
Of course, there is nothing to prevent the use of lesser amounts of
cold-end additive than those set forth above in order to obtain
some benefit from the method of the present invention, even though
that benefit is not maximally obtained. Comparably, additional
amounts of cold-end additive may be used than those here set forth,
although it is not believed that any additional benefit can be
obtained thereby, except perhaps by way of a safety factor to
compensate for variations in the sulphur content of the fuel, for
inaccuracies in determining the magnitude of that sulphur content,
or for changes which may occur in the combustion conditions which
in turn may give rise to variations in the percentage conversion to
SO.sub.3. In other words, there is nothing critical in the amounts
of magnesium-containing material employed for cold-end feed, and in
a given installation the determination of the optimal amount of
additive to be used may well be arrived at empirically, by varying
the amount of additive, analyzing the content of the stack gases,
and selecting that amount of additive which gives the best
results.
The cold-end feed additive may be introduced into the system
continuously or intermittently, depending upon economic and
environmental needs and operating conditions to which the plant in
question is subject, but in general it is preferred that the
cold-end addition occur continuously, since only in that way will
the undesirable SO.sub.3 emissions from the plant be fully
minimized.
The additives used in accordance with the present invention may
contain substances other than the manganese- and
magnesium-containing substances here specified, those other
substances sometimes adding combustion control effects of their own
and sometimes enhancing the effect of the manganese and/or
magnesium here involved.
The additives may be introduced into the cold end in any convenient
form e.g., as a dry powder, as a liquid slurry, either aqueous or
non-aqueous, or as a solution.
While only a limited number of embodiments of the present invention
have been here specifically described, it will be apparent that
many variations may be made therein, all without departing from the
spirit of the invention as defined in the following claims.
* * * * *