DRY BED SCAVENGING HYDROGEN SULFIDE FROM GAS

Abstract: Substantially dry iron oxide particles having a high surface area, a high kinetic 'K' value and composed of a crystalline phase of Fe<u3>uO<u4>u together with an amorphous Fe<u2>uO<u3>u moiety or portion and having a surface area of at least 4m<s2>s/g are used for scavenging hydrogen sulfide from other gases containing it. A cartridge type device (10) is provided containing such particles (21) intermixed with inert particulate matter (22), e.g. sand. The invention of special value in small quantity applications, for example, where the production of a small well is to be used to operate a power generator located near a well head.

Description: DRY BED SCAVENGING HYDROGEN SULFIDE FROM GAS Technical Field: This invention relates to the use of certain particulate iron oxides to scavenge hydrogen sulfide from a gas in a dry fluidized bed process. Background Art: In U.S. Patent No. 4,008,775, issued February 22, 1977, there is described a process in which porous iron oxide particles are used in drilling muds, primarily aqueous drilling muds, to scavenge hydrogen sulfide (r S) released from a well in the course of a drilling operati This iron oxide is described as having an ideal composition of substan¬ tially F " e 3 0 4 » a particle size of about 1.5 to 50 microns and a surface area at least ten times as great as magnetite particles of equal size. It has been determined that the iron oxide described in the aforesaid patent is also characterized by having- an amorphous (non-crystalline) moiety of Fe 2 0 3 together with an Fe^O. crystalline phase. U.S. Patent No. 4,089,809, issued May 16, 1978, discloses that r-S can be removed from producer gas by passing the gas (at very high tempe atures) through a bed of pellets composed of silica and Fe,-0, thereby forming the crystalline reaction products FeS and FeS 2 - This process i designed to remove hLS from the producer gas immediately after such gas is formed and, as noted, at high temperatures of the order of 1000°C- 180Q°C. } which is considerably higher than that of most gases, e.g. natural gas containing t-LS. U.S. Patent No. 4,201,751, issued May 6, 1980, describes a process of reducing the H-S content of noxious gases containing same by passing the gas through a bed of perlite, an alkaline agent and iron Ill-oxide in the form of dust developed during production of iron or steel. ' The reaction products formed are not specified and the process appears to b directed primarily to the ' use of alkaline agents and the treatment of gases at elevated temperatures. Disclosure of Invention: My present invention does not require such extremely high tempera- tures. It is a process for scavenging LS from gases using certain iro oxide particles which react with the fi-S to form reaction products whic for the most part are not crystalline, but are substantially amorphous; moreover, they are stable and do not release significant quantities of r S on contact with air. The present invention provides a method of scavenging hydrogen sulfide from gases by passing such gases into intimate contact with substantially dry particles of hydrogen-sulfide-reactive iron oxide preferably intermixed in a roughly equal quantity of inert part culate material such as sand. The oxide particles have a surface area of at "K" value in excess of 1000, and are composed substantially of a crysta line phase of Fe.,Q. together with an amorphou Fe 2 0 3 moiety or portion. By the term "substantially dry" particles, as used herein, it is meant that the particles are free flowing and are either bone dry or contain such free moisture as they may pick up on being exposed to air at ambient temperatures and under ambient air humidity conditions, in which case they normally will contain less than 8% by weight of water. Although some crystalline sulfur and/or FeS 2 ma be formed in the course of contacting if the hydrogen sulfide concentra tion is high and the contact time is prolonged, the bulk of the hLS reacts with the iron oxide to form substantially stable, amorphous reaction products. For purpose of this application, the rate constant , measured as -1 -1 -2 min ppm cm x liters/mole, is calculated for iron oxide concentra- 3 tions measured in kg/m , and is as appears in the following derived rat law: d[S t 3 - -K x [H÷] 1 ' 06 x [A] dt where: [S,] is sulfide concentration in ppm. t is time in minutes. d[.S.]/dt is the instantaneous rate of change of dissolved sulfide concentrations. [H ] is hydrogen ion concentration. [A] is iron oxide concentration kg/ . Normally the process is practiced at moderate temperatures, for example, from about 15-100°C, although somewhat higher or lower temp atures may be used. The present invention also provides a device useful in practicin the above method, and which may provide for optimum reaction in a som what fluidized bed. This device comprises a shell or casing containin the aforementioned iron oxide particles in combination with inert soli particles, together with means for retaining such particles in the casing and inlet means for bringing a gas containing H 2 S into contact with such particles in the casing and outlet means for permitting the contacted gas to escape from the casing. The device may also have mea for heating and/or cooling the casing and its contents, as well as mea associated with the inlet and outlet means, inter alia, to measure and/or control gas pressure and gas temperature and analyze the gas composition. The Drawing: The drawing is a schematic view of a dry iron oxide particles-gas contacting device embodying the present invention, positioned between source of gas containing hydrogen sulfide and a delivery point for receiving the sweetened gas exiting from the device. Best Mode for Carrying Out the Invention: Before describing the method of the present invention in greater detail, the device which is preferably used in practicing the method will be described. In the device shown, a vertically arranged cylindrical, solid-gas contacting casing generally designated 10 has a vertical wall 11, a to wall 12 and a bottom wall 13. Surrounding the casing is a cylindrical heating/cooling jacket generally designated 14 having a vertical wall 1 spaced equidistant from vertical wall 11, and top and bottom walls 16 and 17, respectively, which are spaced equidistant from top wall 12 and bottom wall 13, respectively. The jacket 14 is also provided with an inlet/outlet pipe 18 and an inlet/outlet pipe 19, each of which may be provided with suitable valving (not shown) and connected to a heating o coolant source (not shown). The jacket 14 may be omitted if no heating or cooling of casing 10 or its contents is required, but if used for cooling, a fluid such as chilled water may be introduced from a source (not shown) into the space 20 through either pipe 18 or 19, as CMFI desired, and the fluid then exits from the jacket through the other pipe. Normally, in using the device, heat will be generated in casing 10 so that cooling fluid will ordinarily be circulated in the jacket to cool the casing and its contents. However, the casing may be heated, i similar fashion, by circulating a heated fluid, e.g. steam, through the jacket. Inside of casing 10 are substantially dry iron oxide particles 21 (shown merely for convenience as greatly enlarged spherical particles), and sand or other chemically inert solid particles 22 (shown merely for convenience as triangular particles). Actually, particles 21 and 22 ca be of the same or different configuration, but preferably are both of the same configuration, e.g. substantially or roughly spherical. In th preferred embodiment, a substantially homogenous mixture of roughly 50% by volume of sand particles and 50% by volume of iron oxide particles i employed, one purpose being to substantially eliminate or at least lessen the agglomeration of iron oxide particles 21 which tends to follow when such particles scavenge hydrogen sulfide in the casing. However, satisfactory results may be obtained by using a mixture of as little as 20% by volume of sand particles to 80% by volume of iron oxid particles. Preferably, the particles occupy about 70% of the inner volume of the casing, although they may occupy a somewhat larger or smaller volum Prior to use of the device, the particles will settle in casing 10 leaving a head space (that is, a free gas space above the particles) substantially equal to the remaining (for example, 30%) inner volume of the casing. Entering through top wall.12 of casing 10 is an inlet/outlet gas pipe 23 through which a gas may be introduced into or exhausted from th casing. Pipe 23 is provided with a gas pressure measuring means 24, a gas temperature measuring means 25, and a sampling pipe or port 26 provided w th valve means 27. Entering through bottom wall 13 of the casing is substantially the same kind of inlet/outlet pipe 28 provided with a gas pressure measuring means 29, a temperature measuring means 30, and a sampling line or port 31 having valve means 32. The inlet/ outlet pipes 23 and 28 may be provided with flowmeters (not shown) to measure the rate of flow of gases through the device and with analytical instruments (not shown) to measure the H 2 S content and other of the entering or exiting gases. Al hough the internal dimension of casing 10 between one side wal 11 of the casing and the other is shown as being larger than the inter nal diameters of pipes 23 and 28, they can be the same; that is, pipe 23 and 28 can be mere vertical extensions of casing 10. Detachably mounted in casing 10 and covering the entrance of pipe 23 and 28 into it are particle retaining, gas porous members 33 which can be very fine wire mesh screens or fritted ceramic or sintered stai less steel discs or their equivalent which have passages or pores of smaller size than particles 21 and 22. These members ser e to retain the particles in casing 10 while permitting the scavenged gas to escape from the casing through the outlet pipe. They are held by brackets 34. In the preferred mode of operation of the device, a gas containing H-S is introduced into casing 10 through pipe 28 and flows upwardly through the iron oxide and sand particles 21 and 22, thereby contacting the iron oxide particles 21 which scavenge or remove H 2 S from the gas. The resultant sweetened gas then exits from the casing through outlet pipe 23. As the gas passes up through these particles, the particles become somewhat fluidized (that is, they separate from each other in th gas and rise to some extent into the head space) thereby effecting more complete contact between oxide particles 21 and the H 2 S in the gas. However the sand particles 22 themselves serve, without such fluidizing to assure distribution of the gas to the oxide particles 21. Therefore if channeling of the gas through the particles is a problem, the gas ca be fed downward into the casing through pipe 23 and thence downward through the particles, in which case the particles become a fixed bed (thus minimizing channeling), and the sweetened gas exits the casing through pipe 28. A disadvantage of such downflow operation exists wher the material is used to exhaustion; caking of the particles tends to occur in the bed after the H 2 S breaks through the bed unscavenged and the pressure necessary to force the gas through the bed increases con¬ siderably. This effect of downflow operation is explained further in the specific examples. The process of the invention is preferably practiced, as previously noted, by passing a gas containing the H 2 S upward through a bed of the iron oxide particles intimately mixed with inert particulate matter, preferably sand particles. In this mode of operation it is possible to scavenge H ? S from the gas without substantial caking of the particles until the particles have exhausted their capacity to Preferably, the iron oxide particles should contain some "free" water (absorbed from the atmosphere during storage) in addition to "bound" water, that is, water as is present in the particles after drying at a temperature of 100-110°C. for 48 hours. If the particles do not conta some "free" water they will generate water rapidly on contact with the H 2 S and will tend to cake, causing considerable resistance to gas flow through the bed. Preferably, the particles contain at least 0.015%, a as high as 1 to 2% by weight of water, most desirably from about 0.05% to about 0.5% . The inert part culate matter employed with the particles may be sand or any other siliceous material or any inert material which sep¬ arates the iron oxide particles from each other and hence tends to prevent the iron oxide particles from agglomerating or caking. The particle size of the inert particles may be chosen to be somewhat si i lar to that of the iron oxide particles so that the two types of parti cles do not materially segregate during passage of the gas through the bed, but inert particles one hundred times as large as the oxide parti cles functioned as seen in the example which follows. The gas contaminated with H 2 S employed in the process is preferabl any gas which contains little if any oxygen, and can be a natural gas any hydrocarbon gas exiting from a producing well, or a flue gas, pro¬ ducer gas, coke oven gas or the like. The present process is particu¬ larly suitable for scavenging H 2 S from natural gas. The H 2 S content o the gas is not critical and can be as high as 50% by volume. In the case of natural gas, the H 2 S concentration may be in the range of abou 0.1 to about 5% by volume. By use of the present process, it is possi to reduce the H.-S concentration of the sweetened gas to a commercially acceptable predetermined level of 4 ppm or less. Preferably, the scav¬ enging process is practiced on gases at ambient atmospheric temperature or on natural gases exiting from operating gas wells or earth formation and it has been found that the iron oxide particles used have a high H scavenging capacity under such conditions. The temperature of gases en countered under such conditions is usually in the range of about -10°C. to about 50°C. The preferred iron oxide particles employed herein have a particl size such that 90% of the particles are in the range of from about l.Q to about 70 microns, a surface area of at least 4.0 m / , a kinetic "K value in excess of 1500 and an ideal composition of substantially Ee-,0. . - -y - '■ ^ " -v composed of a crystalline phase of ^0. and an amorphous e 2 0 3 moiet A particularly suitable form of such iron oxide particles is describe in U. S. Patent No. 4,008,775. Such particles may also contain trace amounts of minerals as described in said patent. Unlike the crystal- line reaction products, obtained when such iron oxides are employed to scavenge H 2 S in liquid (aqueous or anhydrous liquid) systems, the re¬ action products obtained by the use of such iron oxides in the present process are substantially amorphous, believed to be substantially composed of amorphous sulfur and amorphous iron sulfides. The following specific example is intended to illustrate the use the device and the practice of the processes described herein, but is not to be construed as limiting the scope of the present invention. EXAMPLE A. Equipment Used: (1) The equipment used was essentially as illustrated in the accompanying drawing except that the inner diameter of the cylindrical casing 10. was the same as that of the inlet and outlet pipes 23 and 28 and the particle retaining discs 33 were composed of sintered stainles steel. The casing portion, which was 40.64 cm high and had an interna diameter of 2.22 cm, was wrapped in a 2.54 cm wide and 0.32 cm thick insulation material and placed vertically in an insulation chamber. Seventy per cent of the casing volume was filled with an intimate mix¬ ture of iron oxide particles (6-8 micron particle size) and dry sand (700 micron particle size) in equal weight ratios and obtained by mixi these ingredients on a roll mixer for one hour at 200 rpm, which mix¬ ture gave a settled bed depth of 28 cm. The head space above the mixtur occupied about 30% of the volume of the casing. (2) A mixture of nitrogen and H 2 S was supplied to the casing through pipes 23 or 28, depending on whether downward or upward flow through the mixture was used. The inlet and outlet flow rates were monitored with flowmeters. The pressure drop was measured with the aid of pressure gauges in the inlet and outlet lines. Gas sampling ports 26 and 31 consisted of Teflon® coated septu s. The gaseous effluent from casing 10 was bubbled through two caustic scrub traps (about 10% by weight aqueous NaOH) before venting. (3) Variations in H~S gas concentration were determined by the Draeger sampling method - National Draeger, Inc., "Gas Samples Method, _QMPI I A - ._ • .-_-..-. Bulletin No. ND103, 1980. This technique requires a fixed-volume pump (100 ml) and direct reading sample tubes for monitoring specific atmos pheres. Once a gas sample was collected, it was drawn through a Draeg tube by the pump. The sampling procedure required the collection of 1.0 ml gas sampl using a gas-tight syringe (Pressure-Lok Series "A" Gas Vol. 0-10 ml, Precision Sampling Corp., Baton Rouge, LA). The feed gas was analyzed using a high capacity, H<-S-sensitive Draeger tube (100/s), (Vallen Corp New Orleans, LA) with a range of 10,000-200,000 ppm (1.0-20%). The product gas was analyzed by a more sensitive H 2 S Draeger tube (the 1/c), with a range of 100-20,000 ppm (0.01-2.0%). If the concen¬ tration exceeded the range of one tube, two or more tubes were employed in series. After the infusion of H 2 S- was completed and the reactor disassem- bled, the 1/c Draeger tube was used to analyze the atmosphere above the sample for H 2 S, using the recommended sampling technique. (4) After the process was carried out in the device, the mixture in the casing was sieved to separate the sand particles from the re¬ action products and any unreacted iron oxide, and the latter were groun to 200 mesh (74 microns) and dried in vacuum for 24 hours. X-ray spec¬ tra were run at 40 V, 20 Ma, 500 cps using Cu-Ka. The reaction pro¬ ducts were also subjected to analyses to determine the total amount of sulfur therein. B. Materials Used: (1) Hydrogen Sulfide of a minimum purity of 99.5%. (2) Sand dried at 110-n0°C. for 24 hours prior to use. (3) Nitrogen — ultra high purity with less than 0.01% contamin¬ ation. (4) Compound A is composed of iron oxide particles having 98% of the particles of a size of 6-8 microns, a surface area of 10 m2/ , a kinetic "K" value (as hereinafter defined) of 2000 and consisting essentially of a crystalline phase of Ee.,0. and an amorphous Ee 2 Q., moiety and traces of minerals in amounts less than 5% by weight. This material under ordinary ambient temperature and pressure conditions had a water content of about 0.3% by weight. These iron oxide particles are described in the aforesaid U. S. Patent No. 4,008,775. (5) Dry Compound A is the same as Compound A except it has been _ E CMPI dried in a circulation oven at 100-110°C. for a minimum of 48 hours an has a water content of 0.006% by weight. This material was dessicated after drying to avoid rehydration. TABLE 1, which follows, shows the conditions used in the equipmen for scavenging H 2 S from nitrogen gas employing Compound A containing about 0.3% by weight of water, and the H«S reactive capacity of this Compound under these conditions. On the first run, gas upflow was employed to fluidize the bed; in the other runs the gas was flowed downward. TABLE 1 Run Iron Breakthrough H 2 S Feed Fee Id Rate Weight No. Oxide Capacity Concentration I Compoun Used (g H 2 S/g % (.cm /miη) (g/hour) (cfd) (g) Cpd A) 1* Compound A 0.17 16.3 260 3.84 • 13.2 • 107 " . 2 0.12 21.4 158 3.06 8.02 93.5 3 0.13 23.7 105 2.28 5.33 96.6 4** » 0.15 43.7 220 8.76 11.2 94.6 * indicates upflow of feed ** indicated feed [H 2 S] = 43.7% The above results indicate that Compound A has a greater capacity for H 2 S scavenging when the gas is passed upward through the Compound A sand bed than when the gas is passed downward through the bed. TABLE 2, which follows, shows the H 2 S reactive capacity of Compoun A at the breakthrough capacity and also at various capacities of Compou A when H 2 S is continued to be infused through the bed up to 50% of its total H 2 S reactive capacity. The last column shows the extrapolated H 2 S reactive capacity at 100% completion. The breakthrough capacity is the capacity of the iron oxide to scavenge H„S from the gas in grams of.H-S scavenged per gram of Compoun A at the time at which detectable quantities of H 2 S first appear in the gas stream after passage through the Compound A-sand bed. TABLE 2 Run No. Iron Breakthrough .10 Capacity .15 Capacity .50 Capacity 1.0 Capacity Oxide Capacity Completion Used lg Cpb A ) C H p2b S A . lg Cpb A ) lg Cpb A ) lg Cpb A ) (extrapolated) 1* Compound A 0.17 0.18 ' 0.18 0.31 0.50 2 II 0.12 0.13 0.16 3 II 0.13 0.14 0.15 0.22 0.40 4** II 0.15 0.19 0.20 0.24 0.30 * indicates upflow of feed ** indicates feed [H 2 S] = 43.7% - These results indicate that Compound A continues to scavenge H 2 S from the gas even after the breakthrough capacity is reached and that such potential capacity can be almost double or triple the breakthrough capacity. TABLE 3, which follows, shows the x-ray crystallographic analyses data and total sulfur analyses of amorphous sulfur and amorphous iron sulfide reaction products plus crystalline reaction products such as crystalline sulfur, FeS 2 and Fe-S. obtained in Runs 1-4 of TABLE 1. The results in this table indicate that some crystalline reaction products are obtained when the gas contains higher H 2 S concentrations (Runs 2, 3 and 4), and that the reaction products contain substantial amounts of stable amorphous materials. These materials are believed to be essentially amorphous sulfur and amorphous iron sulfides. TABLE 3 Run No. Iron Reaction Crystalline FeS 2 F 3 S 4 Total Sulfur Oxide Extent S in Reaction Used Product (%) (%) (%) (%) + + + Standard Compound A N.D. N.D. + N.D. N.D. (as is) 1* Compound A Completion N.D. N.D. N.D. 22.5 (after reac¬ tion) 2 II Breakthrough 3.2 N.D. N.D. 18.25 3 II Completion N.D. 9.0 N.D. 13.04 4** II Completion 9 6 <1 22.39 * indicates upflow of feed ** indicates feed [l_ 2 S] = 43.7% N. D. none detected As indicated previously in the description, there is a tendency f the iron oxide particles to cake or agglomerate over a period of time a result of continued passage of the H 2 S containing gas through the Compound A-sand bed. This phenomenon is illustrated by the data in TABLE 4, which follows, and is based on the Runs of TABLE 1, TABLE 4 Run Iron Reacti on Backpressure Temperature Caking No . Oxide Extent Range Used (psiq ) (°C. ) 1* Compound Compl etion 1 .5-3.0 20.3-23.4 Minimal A 2 Breakthrough 0-1 .5 N/A Minimal 3 Completion 6.0-10.5 21 .8-26.1 Extreme ** Completion 1 .0-3.5 N/A Extreme Caking is a physical phenomenon of the packed solids which prevent the removal of the products. Two types were observed and are briefly defined here: Minimal - some clumping; nothing more radical than minor tapping on the exterior of the reactor removed the product. Extreme - required driving product out of tubular reactor.with a hammer and a steel rod. indicates upflow of feed ** indicates feed [H 2 S] = 43.7% N/A not available It will be noted from TABLE 4 that caking of the bed is minimal when the H 2 S concentration of the gas is lower (Runs 1 and 2) and the upflow mode is used (Run 1), whereas caking and higher back pressures are encountered when the H„S concentration of the gas is higher and the gas flow through the bed is continued past the breakthrough point. It should also be noted if Compound A is used in the dry " state tha is, without "free" water as defined in the description, the reaction with H 2 S is so rapid that water is formed almost instantaneously on the surface of the iron oxide particles causing them to agglomerate and cak O PI so that gas flow through the bed becomes difficul to sustain due to very high back pressure. This occurs, for example, when Compound A has been dried at a temperature of 10Q o -110°C. for 48 hours and has a water content of 60 g per Kg of iron oxide or 0.006% by weight. To avoid such caking the iron oxide should contain some "free" water, preferably a water content of at least 0.015% by weight. In contrast to the results obtained using the method of this in¬ vention, I have found that some other iron oxides give entirely differe results, even contrary to those reported in the patent literature. Thus, I have found that a different iron oxide which I refer to as Com¬ pound D, Serial No. 44,026,when used in the method described in the above example, does scavenge H 2 S but when the resulting reaction produc is exposed to air, sulfur dioxide is evolved and in some instances the reaction product ignites when exposed to a humid atmosphere. This result is contrary to that.reported for ferric oxide in U. S. Patent No 4,089,809. Compound D is characterized as being iron, oxide particles 2 having a surface area of 4 / , a kinetic "K." value of 4000 and com¬ posed of a crystalline phase of e 2 0 3 and an amorphous e 2 0- moiety; these particles were prepared by the conventional high temperature oxidation of ferrous sulfate. Also, I have found that still another iron oxide which I refer to as Compound C, when used in the method described in the above example, is essentially incapable of scavenging H 2 S from a nitrogen-H 2 S gas mixture in that the H 2 S breaks through the bed of Compound C and sand shortly after the gas flow through the bed is started. This result is contrary to that reported in U. S. Patent No. 4,201,751 although it should be noted that this patent requires the use of an alkaline agent with the basic oxygen furnace iron oxide material described therein. Compound C is characterized as being iron oxide particles having a 2 surface area of 4 / , a kinetic "K" value of 100, a crystalline phase of Fe^O-, and Fe.,0, and an amorphous Fe 2 Q 3 moiety. These iron oxide particles are iron oxide waste dusts from open hearth or basic oxygen furnace steel making operations. ^n_addi lon, I have found that when magnetite is employed in the method of the above example the magnetite is essentially incapable of scavenging H 2 S from a nitrogen-HpS gas mixture in that the H 2 S breaks through the bed of magnetite and sand shortly after the flow of the gas y/λ through the bed is started. The magnetite used is characterized as having a surface area of 1 m / , a kinetic "K" value of <1.0 and as being composed substantially of Fe.-! , of which the predominent part i believed to be a crystalline phase of Fe.,0,. In regard to the Fe 3 0 4 crystalline phase of magnetite this is the primary similarity to Com¬ pound A employed in the above example. However, the other characteris tics of magnetite are quite different from those of Compound A. As to the kinetic "K" value, referred to in the foregoing descrip tion, in the pH range 8-10, the derived rate law for Compound A is as follows: J l - -K x CS 2 x [H*] 1 - 06 x [A] d τ wherein [S t ] is sulfide concentration in ppm, t is time in minutes, d[S.]/dt is the instantaneous rate of change of dissolved sulfide conc trations, [H ] is hydrogen ion concentration and [A] is iron oxide -1 -1 2 concentration (Ib./bbl.). K is the rate constant -in min. ppm cm x 1/mole and equal to approximately 2000. At pH 8-10, the derived rate law agrees closely with Rikard's analysis of the reaction of hydrated iron oxide (ferric hydroxide) and hydrogen sulfide [Am. J. Sci . , 274:94 (1974)]. When [S.] and [H ] are measured intermittently during the t course of continuous acid reaction the substitution of observed [S ] an [H ] values into the rate law equation above yields apparent K values which define relative differences in reaction rates among different iro oxides. A second such device as illustrated in.the drawing may be connecte in series with the first for assured efficiency. However, this appears to be unnecessary and in actual practice it is preferred to connect two such devices in parallel and employ only one of them to sweeten the gas until it loses its ability to do so, after which the gas is sweetened i the second device while the first device is prepared for further gas sweetening service. While the device illustrated in the drawing is substantially as utilized in the laboratory tests reported, with up-flow of the gas for maximum fluidization, horizontal flow will fluidize the bed while avoid ing caking and back pressures. Accordingly, especially where no heating or cooling is required, in an alternate form of device the casing has a • annular configuration about a vertical axis, with an inner or central gas stream inlet (or outlet) port, a radially inner, preferably fibrous particle retaining annular filter, and, thence outwardly, a fill of the two types of particles as described, a radially outer annular fibrous filter, and a radially outer gas stream outlet Cor inlet) port in the casing radially outer wall. Gas flow may be in either direction. The fill of the two types of particles, between the two fibrous annular fil ers, is loose, to a static level well above mid-level but somewhat below the upper wall of the casing, to leave a small head space; while the inlet and outlet ports are located below this static particle level As the gas flows through the particles, they separate from each other and fluidize in the casing, effecting more complete reaction; while the location of the inlet and outlet gas ports below the static level of th particles avoids channeling of gas flow. Industrial Applicability: The present invention affords a simple and inexpensive process and apparatus for sweetening (that is, removing hydrogen sulfide from) gas through the simplest of dry bed agents. It is of special value in small quantity applications, for example, where the production of a small well is to be used to operate a power generator located near a wel l head. _OM?I VvT- O ■

Claims: Cl ai s The embodiments of the invention in which an exclusive property o privilege is claimed are defined as follows: 1. A method of scavenging hydrogen sulfide from a gas containin the same which comprises (a) contacting said gas with substantially dr part cles of a hydrogen sulfide-reactive iron oxide having a surface 2 area of at least 4.0 / , a kinetic "K" value in excess of 1000 and composed substantially of a crystalline phase of Fe-0. and an amorphous Fe 2 Q, moiety, (b) continuing said contacting until the hydrogen sulfide has reacted with said particles and its concentration in said gas has been reduced to a predetermined level, and (c) separating the gas so scavenged from said particles. 2. A method in accordance with that of Claim 1, in which the gas to be contacted is substantially free of oxygen. 3. A method in accordance with that of Claim 1, in which the gas to be contacted is substantially a hydrocarbon gas containing hydrogen sulfide and said gas is contacted with a substantially uniform mixture of from about 50 to 80% by weight of said iron oxide particles and from about 50 to 20% by weight of inert solid particles. 4. A method in accordance with that of Claim 1, together with an intermediate step between step (a) and step (b) thereof, comprising in the course of such contacting, causing the gas to pass upward through said particles and the particles to separate from each other and flui- dize in the gas, whereby to achieve more intimate contacting. 5. A device useful for scavenging H„S from a gas containing same comprising (a) a casing for containing and retaining solid particles an having a gas inlet post entering said casing and a gas outlet post exiting from said casing, (b) said casing containing an intimate mixtur of 20 to 50% by volume of inert solid particles and of 80 to 50% by volume of dry particles of iron oxide having a surface area of at least 2 4.0 m / , a kinetic "K" value in excess of 1000 and composed substan¬ tially of a crystalline phase of Fe^O * and an amorphous e 2 0-. moiety, and (c) solid particle retaining, gas porous members covering the en¬ trance and exit posts of said casing and having openings or pores there- in smaller in size than said solid particles. - Tj?.__ OMPI 6. A device as defined in Claim 5 , said mixture of particles bei further characterized in that they occupy the greater part but not all of the inner volume of said casing, whereby to provide a headspace suff cient to permit the particles to separate from each other and fluidize in the gas, for more complete reaction, and heating or cooling means su rounding said casing. 7. A device as defined in Claim 5, wherein said gas inlet pipe enters the bottom of said casing and the gas outlet pipe exits from the top thereof. 8. A device as defined in Claim 5, wherein the casing has a gen¬ erally annular configuration about a vertical axis, one of said posts being at its radially inner side and having a particle retaining filter the other of said posts being at its radially outer side and having a fibrous filter. 9. A device as defined in Claim 8, the said posts being at a level below that of said mixture of particles in the casing. OMPI

Inventors: FOX IRWIN
Applicants: GAS SWEETENER INC
Application year: 1981
Main classification: B01D53
IPC codes: B01D53