Process for increasing the reactivity of sulfur compound scavenging agents

A process is provided for removing sulfur compounds, such as hydrogen sulfide, sulfur oxides and thiols, out of fluids, such as natural gas or natural gas liquids, by contacting the fluid with a physical mixture of iron oxide, zinc oxide or mixtures thereof and an activator, such as platinum oxide, gold oxide, silver oxide, copper oxide, copper metal, copper carbonate, copper alloy, cadmium oxide, nickel oxide, palladium oxide, lead oxide, mercury oxide, tin oxide and cobalt oxide, preferably copper oxide wherein the activator is present in an amount equal to 0.125% by wt. to 5% by wt. of the total physical mixture. The contacting is conducted at a temperature of 300.degree. C. or less.

FIELD OF THE INVENTION
 This invention relates to the activation of oxide products that are
 reactant with sulfur compounds, wherein the activated oxide products
 sweeten fluids, both gases and liquids, polluted with sulfur-bearing
 compounds such as hydrogen sulfide and thiols (mercaptans). Preferably,
 this invention relates to improving the removal of sulfur compounds from
 hydrocarbon streams by adding an activator to an iron oxide product which
 increases the rate of reactivity of the iron oxide product with the sulfur
 compounds found in hydrocarbon streams.
 BACKGROUND OF THE INVENTION
 Oxides, particularly iron oxides, supported on inert particulate matter
 have long been used in flow-through packed-bed processes to react with and
 scavenge hydrogen sulfide and thiols (mercaptans) present in natural gases
 and liquid hydrocarbons. The reactions between oxides and sulfides
 traditionally have been relatively slow, as compared to other sulfur
 removal or gas sweetening systems. Because of the slow rate of reaction,
 large iron oxide beds contained in large reactor vessels have been
 required in order to adequately remove hydrogen sulfide and thiols from
 the hydrocarbon fluids. The larger reaction vessels allow for longer
 contact times between the oxides and the sulfur compounds, with the longer
 contact times being necessary to adequately remove the sulfur compounds. A
 somewhat offsetting advantage to the slowness and size requirements of the
 iron oxide beds is that the reacted iron oxide bed material may be
 disposed of as non-toxic waste, unlike some other sulfur removal processes
 which require toxic waste disposal systems.
 Current iron oxide based products designed to remove sulfur compounds from
 gas or vapor streams have performance limitations. An example of such a
 performance limitation relates to the minimum hydrocarbon fluid or gas
 residence time in a reactor vessel, as the residence time required for the
 gas in the vessel limits the space and practical vessel size in some
 cases. Minimum gas exposure or retention time in low pressure iron oxide
 beds typically ranges between about 1 to about 1.3 minutes based on the
 amount of unoccupied bed space and actual gas volume. Thus, large diameter
 vessels and beds are typically required for efficient design common in low
 pressure iron oxide bed applications. Large diameter vessels are also
 required in high pressure oxide processes, and, like low pressure iron
 oxide beds, are very expensive. Because of the lengthy gas retention time,
 it is difficult to fit vessel sizes into "small foot print" applications
 like offshore drilling or limited space plant facilities. Consequently, a
 problem exists because small vessel sizes cannot be used to sweeten
 hydrocarbon fluids, meaning certain facilities do not have access to
 packed bed iron oxide processes. Because of the space limitation, it would
 be desirable to have an iron oxide bed that required less space,
 preferably about half of the cross sectional area normally required, and
 was still capable of sweetening hydrocarbon fluids.
 Unplanned increases in gas volumes and inlet hydrogen sulfide levels,
 beyond the design capacity of normal iron oxide beds, cause
 under-utilization of the iron oxide product and excessive costs. Iron
 oxide systems that are properly designed initially can experience
 increased gas flow and/or higher levels of hydrogen sulfide that
 significantly exceed normal design conditions resulting in inefficient
 utilization of iron oxide type products and substantially higher operating
 costs. Because unplanned increases in volume frequently occur, it is
 desirable to have a product and process that can handle increases in
 volume without wasting the iron oxide product.
 An additional problem involves hydrocarbon fluids, gas and liquid, that are
 less than totally water saturated, as the unsaturated hydrocarbon fluids
 require long contact times to effectively remove hydrogen sulfide. Also,
 systems designed for water saturated conditions operate inefficiently when
 the fluid is not water saturated. Natural gas and vapor, and liquid
 hydrocarbon streams that are less than totally water saturated will result
 in the decreased removal efficiency of hydrogen sulfide by the iron oxide
 product and higher operating costs. Thus, a problem exists because current
 iron oxide products are commercially efficient only in the removal of
 dissolved hydrogen sulfide or other sulfur compounds in hydrocarbon fluids
 if there is sufficient contact time and the hydrocarbon fluids are
 saturated. Often, however, it is not practical to inject water to fully
 saturate the hydrocarbon fluid to achieve normal hydrogen sulfide removal.
 Consequently, it is desirable to have a system for sweetening hydrocarbon
 fluids that does not require the hydrocarbon fluids to be totally water
 saturated.
 Systems designed to control odors in vapors from wastewater and oil tanker
 vent scrubber systems often utilize blowers and pressure boosters that
 create unsaturated gas or vapor streams by changing the physical
 properties of the hydrocarbon fluids. These operational practices can
 reduce the efficiency of iron oxide products in removing hydrogen sulfide
 and other sulfur compounds from fluids. Thus, it is desirable to have a
 system that can remove hydrogen sulfide and other sulfur compounds from
 gas and vapor streams that have constantly changing physical properties.
 Additionally, some systems may inject air into the hydrocarbon fluid. The
 injection of air, which includes oxygen, causes increased corrosion and
 safety concerns despite increased capacity for hydrogen sulfide removal.
 The intentional and unintentional inclusion of air, including oxygen, in
 natural gas or vapor streams has long been seen to increase the capacity
 of iron oxide impregnated wood chips and other oxide products to react
 with hydrogen sulfide. However, corrosion and safety concerns are greatly
 increased due to the presence of oxygen, which will react with the vessel
 containing the oxide product. Also, many natural gas contracts presently
 specifically limit the amount of oxygen in the gas and some contracts
 prohibit the intentional injection of air due to problems caused
 downstream in gas transportation systems. The inclusion of a
 "non-oxidizer" stimulant or activator in the iron oxide product that
 enhances the capacity of sulfur removal, without the associated problems
 of organic and inorganic oxidizers, like air, would enhance the use of
 oxide products in sulfur removal processes.
 Liquid hydrocarbons commonly include dissolved hydrogen sulfide and other
 sulfur compounds. In some cases, the hydrogen sulfide removal sufficiently
 meets the required product quality for sales to pipelines and
 transporters. Frequently, however, other sulfur compounds, such as
 mercaptans, carbonyl sulfides, and carbon disulfide need to be removed to
 meet required sulfur limits and product quality tests before the
 hydrocarbons can be sold. An improved iron oxide product that would
 efficiently remove hydrogen sulfide and other sulfur compounds to meet
 required sulfur limitations in hydrocarbon fluids would significantly
 increase the commercial utility of iron oxide sulfur removal processes.
 Thus, it is desirable to have an iron oxide bed process and composition
 that functions in a small reactor vessel, removes sulfur compounds in a
 short amount of time, removes sulfur compounds from unsaturated fluids,
 does not require the injection of air, and removes most if not all of the
 sulfur compounds in a fluid, particularly a hydrocarbon fluid. As will be
 seen, the present invention activates the oxide bed process and
 composition to meet the above listed criteria.
 SUMMARY OF THE INVENTION
 The present invention relates to the use of an activator in an oxide
 product reactant with sulfur compounds. The activator increases the rate
 of reactivity of the oxide product with sulfur compounds contained in
 fluids. Preferably, the activator will have a higher electro-potential
 than the oxide product so that when the activator is coupled with the
 oxide product the coupling will result in an increase in the reactivity of
 the oxide product with sulfur compounds contained in fluids. Importantly,
 the activator increases the rate of reactivity of the oxide product
 without requiring high temperatures to help increase the rate of
 reactivity or the addition of air, oxygen in particular. The activator
 causes increased reactivity at a temperature equal to or less than
 300.degree. C. Additionally, when the oxide product and the activator are
 coupled, the oxide product can remove sulfur compounds, including oxides
 of sulfur, hydrogen sulfide, and thiols, from fluids including saturated
 and unsaturated fluids, as well as, liquid, gas, or a combination thereof,
 and not just hydrocarbon fluids.
 Typically, the activator is a noble metal oxide and the oxide product is an
 iron oxide or zinc oxide product. Noble metals are metals which are not
 very reactive, such as silver, gold, and copper. One of the most preferred
 embodiments of the activator involves the use of small amounts of copper,
 including copper metal and copper oxide, either cuprous and/or cupric,
 added to a conventionally-made sulfide reactant oxide-bed, such as an iron
 oxide bed. An example of such an iron oxide bed used for hydrogen sulfide
 removal is found in U.S. Pat. No. 5,320,992. The copper activator reacts
 with the iron oxide product in the iron oxide bed to increase the rate of
 reactivity of the iron oxide product with sulfur compounds found in
 fluids, including hydrocarbon fluids. The increased reactivity of the iron
 oxide product caused by the copper activator results in the completion of
 the sulfur compound removal reaction in less than half the time of a
 normal sulfur removal reaction, making feasible the use of iron oxide beds
 equal to half, or less, the volume than conventional beds. This unexpected
 result is believed to be due to the substantially higher electro-potential
 of the copper as compared to the iron oxides. Additionally, the use of
 limited amounts of copper activator will prevent the exhausted bed from
 being rated as a hazardous waste by the current standards promulgated by
 the Environmental Protection Agency.
 Metal oxides, such as iron and zinc oxide, have an electronegative
 potential, meaning the potential is on the active or anodic end of the Emf
 series, with the active end relating to metals which tend to corrode.
 Noble metals, copper for example, have an electropositive potential,
 meaning the potential is on the noble or cathodic end of the Emf series.
 Cathodic metals do not readily corrode. The Emf series is a listing of
 elements according to their standard electrode potential. When two
 dissimilar metals, a noble metal and an active metal, are combined a
 galvanic cell is formed, which will result in galvanic corrosion.
 Corrosion of a metal is increased because of the current caused in a
 galvanic cell, so that as the corrosion rate is increased so is the
 reactivity of the metal. In particular, when copper, for example, is added
 to iron oxide, for example, a galvanic cell is formed which causes the
 iron oxide to corrode faster and thus be more reactive with various sulfur
 species. What this means is that increasing the electro-potential relates
 to forming a galvonic cell so that corrosion is increased and reactivity
 with various sulfur species is increased. Most of this information, as
 well as, the Emf series were discussed and disclosed in the "Basic
 Corrosion Course" offered by the National Association of Corrosion
 Engineers in October of 1978.
 According to another aspect of the present invention, even when the
 hydrogen sulfide-tainted fluids include thiols, mercaptans in particular,
 offensive odors are completely eliminated along with a reduction of total
 sulfur content to levels acceptable to commercial purchasers. Another
 aspect of the invention is that hydrocarbon fluids do not have to be
 saturated in order to have the oxide product, coupled with an activator,
 adequately remove thiols (mercaptans).
 Because the inventive activator effectively raises the rate of reactivity
 of oxide products, this invention results in the improvement in the use of
 disposable oxide products for the removal of sulfur compounds from natural
 gas and vapors, and other hydrocarbon liquids. Thus, the present invention
 is desirable because it allows for an oxide product that can be contained
 in a small reactor vessel, results in the removal of sulfur compounds in a
 short amount of time, the removal of sulfur compounds from unsaturated
 hydrocarbon fluids, the non-inclusion air, and the thorough removal of the
 sulfur compounds from fluids.

DESCRIPTION OF THE INVENTION
 In accordance with the present invention an activation method and
 composition are provided for increasing the reactivity of oxide products,
 preferably iron oxide or zinc oxide products, with sulfur compounds in
 contaminated fluids, including gas, liquid, or a combination thereof,
 resulting in the removal of the sulfur compounds from the fluids. The
 oxide products that react with sulfur compounds are also know as sulfide
 reactant oxides. The process is initiated by adding an activator
 composition, preferably a noble metal oxide, to the iron oxide product,
 preferably a packed-bed iron oxide product. The noble metal oxide
 activator will react with the iron oxide product to increase the
 reactivity of the iron oxide product with sulfur compounds. The reaction
 between the activator and iron oxide product causes the iron oxide product
 to more readily react with sulfur compounds, such as thiols, oxides of
 sulfur, and hydrogen sulfide (H.sub.2 S), resulting in the removal of the
 sulfur compounds from various fluids. Preferably, the sulfur compounds are
 removed from the hydrocarbon fluids so that upon removal of the sulfur
 compounds the hydrocarbon fluids can be used for commercial purposes.
 The process, as stated, involves adding an activator to an iron oxide or
 zinc oxide product reactant with sulfur compounds, with the activator
 reacting with and activating the iron oxide product. The activator
 increases the reactivity of the iron oxide product with sulfur compounds
 which can be found in hydrocarbon fluids. The activator may be selected
 from the noble metal oxides, which includes, but is not limited to,
 platinum oxide, gold oxide, silver oxide, copper oxide, cadmium oxide,
 nickel oxide, palladium oxide, lead oxide, mercury oxide, tin oxide, and
 cobalt oxide. In addition to the noble metal oxides, alloys made of noble
 metals and some metals may also be used. The most preferred noble metal
 oxide, is copper oxide, either cuprous or cupric oxide. Also, a
 combination of cuprous and cupric oxide may be used. Not only may copper
 oxide be used, but copper metal is also suitable for use. In general, any
 copper species can be used as an activator including copper oxides, copper
 alloys, copper carbonate, and copper metal. Regardless of the noble metal
 oxide selected, the activator is designed to increase the efficiency of
 treatment of fluids with known iron oxide or zinc oxide products. The
 activator will generally be of a powder grade particle size; however, the
 activator can have a particle size ranging between a U.S. mesh size 8 and
 a U.S. mesh size 325.
 The activator causes increased reactivity in the iron oxide or zinc oxide
 product, referred to generally throughout as the iron oxide product,
 because it has a higher electro-potential than the iron oxide product,
 with the dissimilar electro-potential causing bi-metallic coupling between
 the activator, copper oxide for example, and the iron oxide product. This
 bi-metallic coupling results in an increased rate of reaction between the
 iron oxide product and the sulfur compounds found in fluids, in particular
 hydrocarbon fluids. The activator causes the iron oxide to be more
 reactive by increasing the corrosion rate of the iron oxide, which causes
 an increased reactivity between the iron oxide product and sulfur
 compounds. Essentially, the activator causes the iron oxide to react with
 the sulfur compounds before the activator reacts with the sulfur
 compounds. More specifically, while copper oxide is known to react quickly
 with hydrogen sulfide, the reaction between the copper oxide and the
 hydrogen sulfide essentially takes place after the reaction of the
 activated iron oxide with the hydrogen sulfide, with the reaction between
 the copper oxide and the hydrogen sulfide continuing longer than the
 concentration of the activator accounts for. This is demonstrated in FIG.
 1, which show the presence of copper oxide in an iron oxide bed after
 having sulfur compounds pass through and react with the iron oxide bed.
 The presence of copper oxide is shown in FIG. 1 by line 6, with FIG. 1
 being an X-ray diffraction reading taken after the activated iron oxide
 product had removed hydrogen sulfide from hydrocarbon gas. In particular,
 FIG. 1 shows that the copper oxide activated the iron oxide to react
 first, as the amount of hydrogen sulfide that was passed through the iron
 oxide bed was equal to eight (8) times more hydrogen sulfide than would be
 necessary to exhaust the copper oxide present in the iron oxide bed.
 Because the copper oxide did not completely react with the hydrogen
 sulfide this indicates that the iron oxide reacted with the hydrogen
 sulfide before the copper oxide. In addition to coupling with and
 activating iron oxides, the activator can be used to activate other
 oxides. The other oxides, besides iron oxide, are oxides having a lower
 electro-potential than the activator.
 An amount of activator equal to less than 1% by total weight of the iron
 oxide product is sufficient to increase the reactivity of the iron oxide
 product with the sulfur species. Thus, the addition of a small amount of
 the activator, such as copper oxide, in combination with an iron oxide
 product results in a faster reaction with hydrogen sulfide, thiols
 (mercaptans), and other sulfur compounds, including carbonyl sulfide and
 carbon disulfides. In addition to increasing the reactivity of the iron
 oxide product, the copper oxides are preferred because they are readily
 available and meet current envirorunental standards as promulgated by the
 Environmental Protection Agency. Finally, dependence upon filly water
 saturated gas or vapor streams for efficient sulfur removal is not
 necessary due to the higher reaction rates caused by the activator of this
 invention.
 Use of copper oxide as an activator is also desirable because it generally
 does not corrode the reactor vessel. When unprotected mild steel
 equipment, such as the reactor vessel that houses the iron oxide beds, is
 exposed to copper ions corrosion of the steel can result. However, because
 a relatively small amount of noble metal oxide, preferably copper oxide,
 is used, the reactor vessel is not significantly corroded. Reactor vessel
 corrosion rates are not significantly higher than current iron oxide
 products due to the minimal presence of copper ions that cause high
 corrosion rates.
 The oxide product that reacts with sulfur is also known as sulfide reactant
 oxide and is selected from a metal oxide group having a lower
 electro-potential then the activator. Typically, the oxide product is an
 iron oxide product of the formula Fe.sub.x O.sub.y, with "x" equal to
 between 1 and 3, and "y" equal to between 1 and 4. Also, hydroxides of
 iron oxides may be used. More particularly, the iron oxide is preferably
 either Fe.sub.2 O.sub.3, Fe.sub.3 O.sub.4, or a combination thereof. An
 alternative to the iron oxide product is a zinc oxide product. Normally,
 the iron oxide product is combined with an inert bed material to form an
 iron oxide bed that is housed in a reactor vessel; but, it is not
 necessary to combine the iron oxide product with a bed material, inert or
 otherwise. When the iron oxide bed is made of an inert carrier material,
 the iron oxide product attaches to the inert carrier material which holds
 the iron oxide product in place when contacted with hydrocarbon fluids.
 Preferably, the inert carrier is a calcinated montmnorillonite carrier
 which is desirable because it is non-hazardous, stable, reliable, and easy
 to clean. Instead of an inert carrier the iron oxide product can be
 combined with other carriers such as water. Once the iron oxide product
 and carrier have been reacted with sulfur compounds, the reactant iron
 oxide product remains stable and non-hazardous according to currently
 promulgated Environmental Protection Agency and state standards.
 When activated, the iron oxide product reacts with sulfur compounds to
 remove the sulfur compounds from fluids, including gases, liquids, vapors,
 and combinations thereof as well as non-fully saturated fluids. The
 activated iron oxide product can remove sulfur compounds from fluids
 including air streams, carbon dioxide streams, nitrogen gas, and
 hydrocarbon gases, liquids, and combinations thereof. The sulfur compounds
 that are removed from the fluids include, but are not limited to, C.sub.1
 to C.sub.3 thiols (mercaptans), hydrogen sulfide, carbon disulfides,
 carbonyl sulfide, and other oxides of sulfur.
 The preferred iron oxide bed composition containing the activator is
 comprised of a carrier equal to from about 0% to about 95% by weight of
 the total iron oxide bed composition, more preferably from 0% to about 77%
 by weight, and even more preferably from about 59% to about 76.8% by
 weight. An amount of iron oxide product is added to the iron oxide bed
 composition equal to from about 3% to about 30% by weight of the total
 iron oxide bed composition, and more preferably equal to from about 5% to
 about 22% by weight of the total iron oxide bed composition. An amount of
 water can be added to the iron oxide bed composition ranging from
 approximately 0% to approximately 80% by weight of the total iron oxide
 bed composition and more preferably approximately 18% by weight of the
 total iron oxide bed composition. Finally, an activator, preferably copper
 oxide, is added to the iron oxide bed composition in an amount equal to
 from about 0.125% to about 5% by weight of the total iron oxide bed
 composition. Preferably, the activator is used in an amount equal to from
 about 0.25% to about 2% by weight of the total iron oxide bed composition.
 Larger amounts of the activator, greater than 5% by weight, can be used;
 however, it is most preferred to use an amount of activator equal to
 approximately 1% by weight of the total iron oxide bed composition.
 Further, the reactor bed will preferably be maintained at a temperature
 equal to or less than 300.degree. C.
 An alternative embodiment would include an amount of iron oxide product
 equal to from about 95% to about 99.875% by weight of the total iron oxide
 bed composition in combination with an amount of activator equal to from
 about 0.125% to about 2% by weight of the total iron oxide bed
 composition.
 Another embodiment would include the use of water as the primary carrier,
 with the water added in an amount equal to from about 50% to about 80% by
 weight of the total iron oxide bed composition, an amount of iron oxide
 product added to the water in an amount equal to from about 5% to about
 22% by weight of the iron oxide bed composition, and an activator added to
 the water and iron oxide product equal to from about 0.125% to about 5% by
 weight of the total iron oxide bed composition. The preferred combination
 of activator to iron oxide product is equal to about 1 part by weight of
 activator to about 10 to about 50 parts by weight of iron oxide product.
 It should be noted that the amount of activator required is comparatively
 small when analyzed in view of the oxide product. This is because it takes
 a comparatively small amount of activator to increase the reactivity of
 the iron oxide product, or other oxide products.
 It should be further noted that the presence of oxygen in the fluid
 containing sulfur compounds further increases the electro-potential
 differential between the oxide product and the activator. Thus, even
 smaller vessels with dramatically shorter contact times are possible for
 order control applications and hydrogen sulfide removal systems with
 vapors naturally containing, or with the deliberate addition of, air,
 which may include oxygen.
 In order to further illustrate the present invention, the following
 examples are given. However, it is to be understood that the examples are
 for illustrative purposes only and are not to be construed as limiting the
 scope of the subject invention.
 EXAMPLES
 Example 1
 As will be shown in the following example, smaller-sized reactor vessels
 can be used for hydrogen sulfide and other sulfur species removal,
 including thiols (mercaptans), from gaseous and liquid hydrocarbons by
 adding a small amount of copper oxide activator to an iron oxide based
 reaction bed contained in a steel reactor vessel.
 Hydrocarbon gas samples were filtered in a reactor vessel which was 8 feet
 in length and had a diameter of 2 inches. The vessel contained 10 pounds
 of an experimental iron oxide mix, which contained about 5.921 pounds of
 an inert carrier, with the carrier being a calcinated montmorillonite
 carrier, an amount of iron oxide powder equal to approximately 2.15
 pounds, and an amount of water equal to approximately 1.9 pounds. Five (5)
 batches were made of the iron oxide mix, so that five (5) different tests
 could be conducted in the reactor vessel. Each of the five tests were
 initiated by passing nitrogen/carbon dioxide gas contaminated with
 hydrogen sulfide, the amount of hydrogen sulfide contained in contaminated
 gas is listed below, through the iron oxide mix contained in the reactor
 vessel. In three of the tests copper oxide was added to the iron oxide
 mix, the amount of which is listed below. In two of the tests no copper
 oxide was added to the iron oxide mix. Also, the tests were conducted on
 different amounts of hydrogen sulfide (H.sub.2 S) contaminant contained in
 nitrogen/carbon dioxide gas. Additionally, some nitrogen/carbon dioxide
 gas samples contained oxygen, the amount of which is listed below. Thus,
 the nitrogen/carbon dioxide samples that were tested, included samples
 with oxygen and without oxygen.
 The amount of copper oxide activator added the iron oxide bed was equal to
 about 1% or less by weight of the total bed composition. The actual amount
 of copper oxide added was about 1% by weight or an amount equal to about
 0.1 pounds and about 0.25% by weight or about 0.025 pounds. The specific
 parameters for each test are listed in the table below. The conditions in
 the reactor vessel in which the tests were conducted are as follows:

Test Conditions:
 Temp 70.degree. F.
 Flow Rate of Natural Gas containing H.sub.2 S 5.41 liters/min.
 Pressure 0.5 psig.
 Bed Height 7.9 ft.
 Gas was water saturated
 Contact time for the gas in the test unit was about 50 seconds at the above
 listed pressure, temperature, and flow rate. The gas was filtered through
 the reactor vessel containing the iron oxide mix. As can be seen below, a
 comparison was made between the efficiency of removal of the iron oxide
 mix without an activator and the iron oxide mix with an activator, copper
 oxide. The tests were also broken into nigrogeD/carbon dioxide gas samples
 containing moderate amounts and extreme amounts of H.sub.2 S. The extreme
 H.sub.2 S Contaminated nitrogen/carbon dioxide gas was filtered through an
 iron oxide mix without an activator, an iron oxide mix containing 1.0% by
 weight of activator, and an iron oxide mix containing 0.25% by weight of
 an activator.

Moderate H.sub.2 S Contamination Extreme H.sub.2 S
 Contamination
 Gas H.sub.2 5 500 ppm in N.sub.2 H.sub.2 S 2200 ppm
 in N.sub.2
 Composition No Oxygen Oxygen 4% by
 volume
 Carbon Dioxide 14% by volume Carbon Dioxide 14% by
 volume
 Test Results Iron 1% by wt. Iron Copper
 Oxide
 Oxide Only Copper Oxide Oxide Only 1% by wt
 0.25% by wt
 Bed Depth Greater Than Less Than Greater Than Less Than
 Less Than
 for Complete 7.9 feet 4.7 feet 7.9 feet 2.7 feet
 3.7 feet
 H.sub.2 S Removal
 Measurements were taken by Sensidyne hydrogen sulfide and total mercaptan
 stain tubes manufactured by the Sensidyne company.
 As can be seen, in the moderately contaminated gas the addition of a small
 amount of activator, copper oxide, substantially decreased the iron oxide
 bed depth required for complete hydrogen sulfide removal. The iron oxide
 bed with an activator required 3.2 fewer feet to remove the sulfur
 compounds than the iron oxide bed without an activator. In the extreme
 contaminated gas, the activated iron oxide bed required less than half the
 amount of material, 3.7 feet as compared to 7.9 feet, to remove the sulfur
 compounds. Furthermore, as can be seen, an increased amount of activator
 increases the reactivity of the iron oxide. The iron oxide mix having 1%
 by weight of an activator added thereto only required 2.7 feet to remove
 the hydrogen sulfide; whereas, the iron oxide mix containing 0.25% by
 weight of an activator added thereto required less then 3.7 feet to remove
 the hydrogen sulfide. A lesser amount of iron oxide mix was required to
 remove the hydrogen sulfide from gas extremely contaminated with H.sub.2 S
 as compared to gas moderately contaminated with H.sub.2 S. The reason
 there was better removal in the gas with extreme hydrogen sulfide
 contamination, as compared to the gas with moderate hydrogen sulfide
 contamination, was the addition of oxygen to the gas. This shows that
 oxygen further increases the reactivity of the iron oxide product when an
 activator is added thereto. It should be pointed out that the addition of
 the oxygen did not increase the reactivity of the iron oxide product
 without an activator.
 Thus, the above examples demonstrate that the use of an activator results
 in the ability to use a smaller bed and vessel. The examples also
 demonstrate that the iron oxide product has increased activity when
 exposed to an amount of oxygen in combination with an activator.
 Example 2
 The following experiment was conducted to determine the amount of dissolved
 hydrogen sulfide and mercaptans removed from natural gas liquids (NGL) by
 an iron oxide product composition containing an activator. The removal of
 hydrogen sulfide and mercaptans from natural gas liquids is indicated by
 the reduction of the hydrogen sulfide and mercaptan concentrations
 measured in the vapor or "headspace" adjacent to the liquid.
 Two tests were conducted in two (2) reactor vessels that were 4 feet high.
 For each test each reactor vessel contained approximately 40 pounds of
 reaction material, including about 23.684 pounds of solid inert carrier, a
 montmorillonite carrier, about 7.6 pounds of water, and about 8.6 pounds
 of iron oxide powder. In one test approximately 0.4 pounds of copper oxide
 was added to the reaction material, while the other test did not have any
 copper oxide added to the reaction material.
 The tests conditions were as follows:
 Natural Gas Liquids (NGL) 72 API (density) at 70.degree. F.
 Headspace H.sub.2 S Untreated=&gt;4,000 ppm.
 Headspace Mercaptans Untreated - The metcaptan content could not be
 determined due to high H.sub.2 S levels.
 Flow Rate set at 2" equivalent unoccupied bed rising velocity. Measurements
 were taken by Sensidyne hydrogen sulfide and total mercaptan stain tubes
 manufactured by the Sensidyne company. Test results, as indicated by
 headspace concentration measurements, were as follows:

Iron Oxide Iron Oxide With 1% by wt. Copper Oxide
 Only At 4 ft. level At 8 ft. level
 Hours In At 4 ft. level Total Total
 Test H.sub.2 S H.sub.2 S Mercaptans H.sub.2 S Mercaptans
 At Start 400 ppm* 0 ppm 0 ppm 0 ppm 0 ppm
 6 Hr. * 0 ppm 35 ppm 0 ppm 0 ppm
 of Flow
 21 Hr. * 0 ppm 40 ppm** 0 ppm 0 ppm
 of Flow
 *The test was terminated due to the high amount of hydrogen sulfide,
 greater than 400 ppm, remaining in the headspace of the liquid
 hydrocarbon.
 The liquid hydrocarbon quality was excellent (clear yellow NGL) coming out
 of the unit(s) loaded with the copper oxide activator and the iron oxide
 product without the need for further processing. Conversely, the iron
 oxide product that did not have an activator did not result in sufficient
 removal of the hydrogen sulfide or mercaptans. Additionally, it should be
 pointed out that the iron oxide bed at the 8 foot level did not contain
 any detectable sulfur compounds. This means that the sulfur compounds were
 removed from the hydrocarbon fluid prior to contacting the iron oxide
 product at the 8 foot level.
 Accordingly, use of the present invention affords at least these
 significant advantages: increased speed of reactivity permits the use of
 much smaller beds of reactive materials; and, when mercaptans and/or
 hydrogen sulfide are present in liquid hydrocarbons, the products of the
 reaction are odor-free and are no longer contaminated with these sulfur
 compounds.
 Example 3
 Two reactor vessels were prepared that was 15 feet in length and each
 reactor vessel contained approximately 30 pounds of iron oxide mix. The
 iron oxide mix contained about 17.763 pounds of carrier, about 5.7 pounds
 of water, about 6.45 pounds of iron oxide product, and about 0.087 pounds
 of copper oxide. The reactor vessel was connected to a carbon dioxide gas
 source. The carbon dioxide gas, before passage into the reactor, was water
 saturated through a bubbler and filtered in the reactor under the
 following conditions:

Flow Rate (ft.sup.3 /hr) 30
 Temperature (.degree. F.) 70
 Pressure (psig) 400
 Bed Height (ft.) 30
 Inlet H.sub.2 S (ppm) 25
 Inlet Mercaptans (ppm) 20
 The inlet gas contained a number of other sulfur species, in addition to
 mercaptans and hydrogen sulfide, the most abundant sulfur compounds being
 methyl and ethyl sulfides and disulfides. Three carbon dioxide gas samples
 were tested, one sample per day for three consecutive days, with each
 sample passing through the iron oxide mix in the same reactor. The sulfur
 components, other than hydrogen sulfide and mercaptans, were not removed
 by the iron oxide mix. The hydrogen sulfide (H.sub.2 S) and Mercaptans
 were removed by about 5 ft. of the iron oxide mix, out of a possible 30
 feet. The following table shows the amount of hydrogen sulfide and
 mercaptans entering the reactor as well as the conditions in the reactor
 vessel. The following table shows the data that was collected and
 formulated with measurements taken by Sensidyne hydrogen sulfide and total
 mercaptan stain tubes manufactured by the Sensidyne company and test
 trailer meters.

Sample 1 Sample 2 Sample 3
 Inlet H.sub.2 S (ppm) 25 22 24
 Inlet Mercaptans (ppm) 20 20 20
 First Port H.sub.2 S (ppm) 0 0 0
 First Port Mercaptans (ppm) 0 0.5 0.75
 Column 1 temp (.degree. F.) 85 68 84
 Column 1 press (psig) 410 410 400
 Flow (ft.sup.3 /hr.), actual 30 30 30
 The tested samples revealed that the activated iron oxide mix removed the
 contaminants with 5 feet of iron oxide mix from the contaminated carbon
 dioxide streams. Specifically, it should be noted that no contaminants
 were detected at the second port or 10 foot mark. The tests showed that no
 hydrogen sulfide (H.sub.2 S) or mercaptans passed the first 15 feet of the
 reactor. Thus, the iron oxide mix with an activator was able to remove
 hydrogen sulfide and mercaptans from water saturated carbon dioxide
 streams.
 Example 4
 Two reactor vessels were prepared that were each 15 feet in length and each
 reactor vessel contained approximately 30 pounds of iron oxide mix. The
 iron oxide mix contained about 17.763 pounds of carrier, about 5.7 pounds
 of water, about 6.45 pounds of iron oxide product, and about 0.087 pounds
 of copper oxide. The reactor vessel was connected to a carbon dioxide gas
 well. The carbon dioxide gas was 20% water saturated and was run in the
 reactor under the following conditions:

Flow Rate (ft.sup.3 /hr) 30
 Temperature (.degree. F.) 70
 Pressure (psig) 400
 Bed Height (ft.) 32
 Inlet H.sub.2 S (ppm) 25
 Inlet Mercaptans (ppm) 20
 Inlet Carbonyl Sulfide (ppm) .025
 The inlet gas contained a number of other sulfur species, in addition to
 mercaptans, hydrogen sulfide, and carbonyl sulfide, the most abundant
 sulfur compounds being methyl and ethyl sulfides and disulfides. Three
 carbon dioxide gas samples were tested, one sample tested per day for
 three consecutive days, with each sample passing through the iron oxide
 mix in the same reactor. Hydrogen sulfide and mercaptans were tested for,
 in addition to carbonyl sulfide. Other sulfur compounds were not removed
 by the iron oxide mix, nor were they tested for. The following table shows
 the amount of hydrogen sulfide, mercaptans, and carbonyl sulfide entering
 the reactor as well as the conditions in the reactor vessel. The following
 table shows the data that was collected and formulated with measurements
 taken by Sensidyne hydrogen sulfide and total mercaptan stain tubes
 manufactured by the Sensidyne company and test trailer meters.

Sample 1 Sample 2 Sample 3
 Inlet H.sub.2 S (ppm) 25 22 24
 Inlet Mercaptans (ppm) 20 20 20
 Inlet Carbonyl Sulfide 0.025 0.025 0.025
 First port H.sub.2 S (ppm) 0 Broke through Broke through
 port 3 (15 ft) port 3 (15 ft)
 First port Mercaptans (ppm) 0 Broke through Broke through
 port 3 (15 ft) port 3 (15 ft)
 First port Carbonyl sulfide 0 Broke through Broke through
 port 2 (10 ft) port 3 (15 ft)
 Column 1 temp (.degree. F.) 54
 Column 1 press (psig.) 410
 Flow (ft.sup.3 /hr), actual 30
 As can be seen, the activated iron oxide product did not remove the sulfur
 compounds from the water unsaturated carbon dioxide gas as effectively as
 it did the sulfur compounds from the water saturated carbon dioxide gas.
 But, the activated iron oxide product still removed sulfur compounds from
 the unsaturated carbon dioxide gas.
 Example 5
 To test whether copper metal powder and copper oxide increase the
 reactivity of iron oxide with sulfur compounds three (3) towers were set
 up in a side-by-side arrangement. The three (3) towers were each six (6)
 inches in diameter and five (5) feet tall and contained approximately 70
 pounds of material reactive with sulfur compounds. The three (3) towers
 each had an inlet where jet fuel entered the towers. The jet fuel passed
 into the towers from a common source. An amount of jet fuel stream
 contaminated with 126 parts per million by weight of mercaptans was passed
 through each of the reactor towers, so that three (3) separate streams of
 jet fuel, in an amount equal to 400 milliliters per minute, was passed
 through each of the three (3) reactor towers. The jet fuel passed through
 the reactor towers under atmospheric pressure and a temperature of
 80.degree. F. After passage through the reactor towers it was determined
 at the outlet how much of the mercaptans remained in the jet fuel after
 passage through the three (3) different reactor towers. The mercaptan
 levels were determined 48 hours after initiation of the tests, so that the
 jet fuel passed through the reactor vessels for 48 hours with a reading
 then taken at the 48 hour mark.
 Reactor No. 1, which was non-activated material, contained 70 pounds of
 material comprised of 59% by weight montmorillonite, an amount of iron
 oxide (Fe.sub.2 O.sub.3) equal to 21.75% by weight, and an amount of water
 equal to 19.25% by weight. At the end of 48 hours it was found that the
 jet fuel contained an amount of mercaptans equal to 78 parts per million
 by weight, meaning approximately 48 ppm by weight had been removed by the
 non-activated material.
 In the second reactor, the clay or montmorillonite, and water were added in
 the same amount as in the first reactor and the iron oxide was added in an
 amount equal to 21.25%. Additionally, an amount of copper powder was added
 in an amount equal to 0.5% by weight of the reactor materials. It was
 found that after 48 hours the jet fuel contained approximately 15.8 parts
 per million by weight of mercaptans after passage through the iron oxide
 activated with copper powder.
 In a third reactor, the reactor contents were prepared the same as in the
 reactor containing the copper metal powder, however, an amount of copper
 oxide equal to the same amount of copper powder was added thereto. As
 such, the copper oxide was added in an amount equal to 0.5% by weight of
 the contents of the reactor. The mercaptans in the jet fuel were measured
 after passage through the reactor contents and at the end of 48 hours. It
 was found that 8.5 parts per million by weight of mercaptans remained in
 the jet fuel after passage through the iron oxide activated with copper
 oxide.
 As can be seen, both the copper metal and the copper oxide provided for
 suitable removal of sulfur compounds and in particular mercaptans from the
 hydrocarbon stream.
 Example 6
 A test was conducted to show that zinc oxide could be activated to more
 readily remove sulfur compounds from fluids than non-activated zinc oxide.
 As such, two (2) side-by-side tests were conducted to compare activated
 zinc oxide with non-activated zinc oxide.
 The activated zinc oxide was formed by mixing 240 grams of inert base, with
 80 grams of water, 77 grams of zinc oxide, and 3 grams of cupric oxide.
 The total weight of the mixture was 400 grams. After formation, the
 activated zinc oxide was placed in a test reactor having a one (1) inch
 diameter and a twelve (12) inch length. The activated zinc oxide was
 placed in the reactor at a depth of 10.5 inches.
 A non-activated zinc oxide composition was formed by mixing 240 grams of
 inert base with 80 grams of water and 80 grams of zinc oxide. Again the
 total weight of the mixture was 400 grams. The non-activated zinc oxide
 mixture was then placed in a test reactor having the same dimensions as
 the test reactor used for the activated zinc oxide, with the non-activated
 zinc oxide present in the same depth as the activated zinc oxide.
 Each of the reactors had an amount of water saturated nitrogen containing
 3000 ppm of hydrogen sulfide passed therethrough. The nitrogen gas had a
 flow rate of 3000 ml/min. through each of the reactor vessels and the
 reactor vessels were each at a temperature of 80 F. and a pressure of 3
 psig. The nitrogen gas was passed through each of the zinc oxide
 compositions in the reactor vessels for three (3) hours. At the end of the
 three (3) hours the amount of hydrogen sulfide in the nitrogen gas was
 measured, at the outlet of non-activated zinc oxide reactor vessel 525 ppm
 of hydrogen sulfide was measured in the treated nitrogen gas. At the
 outlet of the activated zinc oxide reactor vessel 0 ppm of hydrogen
 sulfide was measured in the treated nitrogen gas. As can be seen from
 these results, the activated zinc oxide demonstrated superior results,
 with the activated zinc oxide removing a greater amount of hydrogen
 sulfide than the non-activated zinc oxide.
 Thus, there has been shown and described a novel method and composition for
 activating oxides reactant with sulfur compounds to remove sulfur
 compounds from fluids which fulfill all the objects and advantages sought
 therefore. It is be apparent to those skilled in the art, however, that
 many changes, variation, modification, and other uses and applications for
 the subject method and composition are possible, and also such changes,
 variations, modifications, and other uses and applications which do not
 depart from the spirit and scope of the invention are deemed to be covered
 by the invention which is limited only by the claims which follow.