SCAVENGING HYDROGEN SULFIDE FROM HYDROCARBON GASES

Abstract: Scavenging hydrogen sulfide as present in gases. One problem, common to regenerative systems and to the wood chip process, is that the products of reaction cannot be disposed of without polluting the environment. In contrast, when the present process is used, reaction products are stable, and are readily disposed of safely. This process employs a liquid suspension of unique iron oxide particles comprise substantially of amorphous Fe<u2>uO<u3>u and crystalline Fe<u2>uO<u3>u, Fe<u3>uO<u4>u and combinations thereof, and having a surface area of at least 4 m<s2>s/g. When gas contaminated by hydrogen sulfide is bubbled through the liquid or otherwise intimately contacts the suspended particles, acid-stable products of reaction are formed. The invention is especially useful in sweetening natural gas at the well-head, utilizing relatively simple, low cost reaction vessels serviced with a minimum of down-time.

Description: SCAVENGING HYDROGEN SULFIDE FROM HYDROCARBON GASES Description Technical Field: This invention relates to scavenging hydrogen sulfide from hydrocarbon gases such as natural gas- Background Art: Hydrogen sulfide has been removed previously from hydrocarbon gases utilizing iron oxides. U.S. Patent No. 1,160,375 (Burkheiser) teaches that H_S may be re- moved from hydrocarbon gases containing ammonia by reac¬ tion with Fe_0_ and free sulfur. The reaction product, Fe~S_, is unstable in air, regenerating the Fe~0_ and liberating H„S which is reacted with ammonia in a second step to produce forms of ammonium sulfide. U.S. Patent No. 1,734,307 (Sperr) discloses a method of removing hydrogen sulfide by first reacting the H^S with an alkali such as sodium carbonate, and further reacting the result¬ ing hydrogen sulfide salt with Fe_0_ to form Fe-S_ Canadian Patent No. 495,690 (Meuser) teaches that an H-S-reactive iron oxide is produced during iron-mediated nitroaromatic reductions in the presence of both sulfuric acid and aluminum chloride. The iron oxide so produced is composed entirely of Fe 2 0 3 and in reaction with hydrogen sulfide, forms an unstable iron sulfide which regenerates H„S upon acidification. The foregoing methods appear to be effective only where the concentration of hydrogen sulfide is low, that is, not in excess of about 15 ppm. Further, all of these iron oxides in reaction with H 2 S produce unstable OMPI products upon exposure to air or acids. Disclosure of Invention: • The present invention provides a method of scaveng¬ ing hydrogen sulfide from hydrocarbon gas utilizing exceptionally H 2 S-reactive iron oxide particles. These particles generally comprise forms of iron oxide of large surface area having an amorphous (non-crystalline) moiety of e 2 0 3 together with an Fe^O. or Fe 2 0 3 crys¬ talline phase, and impurity levels in bulk of less than 10.0% with respect to any contaminating element. Upon reaction with hydrogen sulfide, the iron oxides are converted to products which do not regenerate hydrogen sulfide in the presence of strong acids. The principal object of the present invention is to provide a process for scavenging hydrogen sulfide from hydrocarbon gas, regardless of its concentration. A further purpose is to produce, in the reaction with hydrogen sulfide, reaction products which do not readily regenerate hydrogen sulfide gas in the presence of air or dissolved acids. A still further object is to provide a process in which H 2 S may be scavenged from hydrocarbon gas over a broad acidic-alkaline pH range and from any liquid in which the defined iron oxide particles may be suspended. Briefly summarizing, and without limitation, the method of the present invention comprises suspending the particles in a -liquid to form a slurry, contacting the particles so suspended with hydrocarbon gas containing hydrogen sulfide, conveniently by bubbling or otherwise mixing the gas into the slurry, and reacting the hydro¬ gen sulfide with the particles to form acid-stable products of reaction comprising principally FeS_, S°, Fe_S. and other stable, non-FeS iron sulfide species, as the purified gas escapes from the slurry ' . Simple apparatus serves to carry out the process, and includes conventional scrubbing columns, bubble chambers, and mixers such as static mixers. While the OMPI efficacy of H_S-scavenging will vary for different types of apparatus, generally any such apparatus will serve which brings a gaseous hydrocarbon phase containing H_S into intimate mixing contact with the liquid-suspended particles. The simplicity of the apparatus is partic¬ ularly advantageous in that it permits small inexpensive installations close to single gas wells. The amount of iron oxide particles required for effective H„S removal will vary with H 2 S concentration and the degree of liquid-gas mixing. For hydrocarbon gases containing high H_S residuals and for apparatus wherein liquid-gas mixing is relatively inefficient (as in a conventional scrubbing column) , the iron oxide content of slurries may be conveniently increased to provide an amount sufficient for effective scavenging. Alternatively, at low H 2 S residuals, iron oxides having lower rates of reaction, but which fix the sulfur under highly acidic conditions, may be preferable. Best Mode for Carrying Out the Invention: In the method of the present invention, iron oxide particles having unique physical and chemical properties are utilized in scavenging hydrogen sulfide from hydro¬ carbon gases. In contrast to those gas sweetening processes in which the gas passes through only slightly moistened beds of reactive material, and to those pro¬ cesses in which liquid bearing such material is sprayed downward within packed towers, in the present process the hydrocarbon gas polluted by hydrogen sulfide is bubbled through a liquid slurry of reactive particles under con- ditions hereafter more fully described which allow for full reaction; the hydrogen sulfide is reacted in the liquid slurry to a point that it is either completely eliminated or reduced to within the permissible limit of 4 ppm; and the purified gas is gathered from the upper surface of the liquid slurry. The reactive particles utilized in the present process may be derived from several sources and may be prepared under various conditions. One such particle WWIIPP (hereinafter referred to as compound A) is described in my U.S. Patent No. 4,008,775, and is prepared convention¬ ally by controlled low temperature oxidation of iron. Other particles are obtained as the iron oxide waste dusts from steelmaking, as disclosed in my co-pending application, Serial No. 963,797, entitled USE OF STEEL PLANT WASTE DUSTS FOR SCAVENGING HYDROGEN SULFIDE. These may be open hearth dust (hereinafter referred to as com¬ pound B) or basic oxygen furnace dust (hereinafter referred to as compound C) and are formed upon rapid solidification of iron droplets or vapor, as upon contact with furnace flue surfaces. Yet another useful particle (hereinafter referred to as compound D) is formed upon conventional high temperature oxidation of ferrous sulfate with rapid cooling. In general, I have found that any iron oxide will be effective in the defined process, " regardless of source or method of manufacture, provided that it has the physical and chemical properties as hereinafter more fully described. Table I lists representative iron oxides of the present invention (compounds A-D) together with certain control and prior art iron oxides, and summarizes those physical and chemical properties, hereafter explained, which are found to be significant. OMPI -5- TABLE I Fe X-ray Kinetic Acid Surface Iron ESCA/ Diffraction "K" Value Stability Area Oxide AUGER unreacted reacted m 2// A Fe 2 0 3 702 Fe 3°4 FeS 2' 86.6% 7.0 Fe 3 S 4' FeS° B Fe 2 0 3 / FeS 2 ,S° 12.7 Fe 2°3 73.7% 9.0 Fe 3°4 N .A. Fe 2°3 / FeS 2 ,S° 35.1 93.8% 4.0 Fe 3°4 D Fe 2°3 Fe 2°3 FeS 2 1404 85.0% 4.0 2 0* Fe 3°4 Fe 3°4 N.A. < 0.35 18.7% 1.0 P 3 N.A. <0.3 Fe 3°4 FeSx 5 20.0% 1.0 Q 4 Fe 0, Fe_0. FeS, 0.42 18.6% 14.0 ' 2 3 2 3 Fe 2 Sx R 5 N.A. N.A. N.A. 0.35 50.0% N.A. N.A. - not analyzed 2 = magnetite 3 = hematite 4 = iron oxide made according to the method of Meuser, Canadian Pat. No. 455,690 5 = millscale OMPI Samples of various effective particles were subjected to ESCA and AUGER analysis. In ESCA spectroscopy, a beam of monochromatic X-rays impinge upon the atoms at a sample surface, striking electrons and displacing them at energy levels characteristic for each valence state of element present. AUGER spectroscopy is similar to ESCA, except that the sample is bombarded with high-energy electrons instead of X-rays. AUGER electrons are emitted at char¬ acteristic energies for the various elements in particular valence states. These techniques analyze only the sample surface (less than 100 A° interior to the sample) in contrast to X-ray fluorescence which quantifies elements detected in bulk. X-ray diffraction analysis detects only the crystal- line phase of iron oxides; it will not yield a diffraction pattern for any iron oxide in which the Fe and 0 atoms are not organized into a crystalline lattice structure. It is concluded, from comparison of the ESCA/AUGΞR analysis and X-ray diffraction, that the e 2 0 3 detected at the surface of any particle must be at least partially non- crystalline (amorphous) . Referring to Table I, ESCA/AUGER analysis of the present compound classes A, C and D shows that the surface of the particles comprises exclusively Fe 2 0 3 , regardless of crystalline content revealed by X-ray diffraction, which may be Fe,0., Fe_0_ and combinations thereof. In the case of compound A, all of the Fe 2 0 3 present must be amorphous since the only crystalline phase detected by X- ray diffraction analysis is Fe 3 0.. The amorphous nature of the e-0- in compound D cannot be directly determined since all of the iron is present in its highest oxidation state as Fe ; however, the amorphous property may be inferred from the high kinetic K value of reaction with hydrogen sulfide; also, compound D appears to have a relatively low density compared to that of crystalline hematite (data not shown) . The amorphous Fe_0_ moiety of compound classes A, B and C was further identified by ion titration analysis. In ion titration, the amounts of iron in the Fe and Fe oxidation states are measured simultaneously and compared to corresponding values for pure Fe *_m0-_5 and Fe 3 °4 standards. If the particles were composed sub¬ stantially of Fe_0 Δ , as indicated by strong X-ray diffraction patterns, then the ferric (Fe +++) content ++ would approximate 47.7% of the total iron, and Fe iron would be present at approximately 27.6%. Ion titration performed on the present iron oxide +++ powders (compound classes. A, B and C) shows that Fe content is much higher than would be predicted by X-ray diffraction analysis; Fe ++ levels are correspondingly lower than for the pure Fe-0. standard (see Table II) . Ion Titration * Iron Oxide Fe ++ (%) Fe +++ (%) Total Fe A 11.3 57.0 68.3 B 3.6 24.7 28.3 Pure e 2 0 3 2.8 67.2 70.0 Pure Fe3_04, 27.6 47.7 72.3 * Method of Kolthoff and Sandell Thus, these particles have an Fe content intermediate to that for pure standards of Fe 0_ and Fe,0.. It is concluded that the excess of iron in the Fe valence state is present in non-crystalline form as an amorphous Fe 2 0 3 . The Fe 2 0 3 stoichiometry is confirmed by the ESCA and AUGER spectroscopy described hereinabove. Applicant knows of no technical literature in which such tests have been correlated or conclusions drawn there¬ from. As a possible explanation (but without limitation) , it may be theorized that each of the present particles consists of a core comprising crystalline Fe 0., Fe~0 3 and combinations thereof, surrounded by an amorphous (non-crystalline) Fe-O- layer. Reaction with hydrogen OMPI sulfide may initiate within the amorphous Fe^O layer and proceed into the crystalline core portion. Kinetic analysis, as hereinafter more fully described, indicates a substantially uniphasic reaction, i.e., reaction pro- ceeds uniformly through the core at substantially similar rates to the initial reaction within the amorphous portion, and obeys the same rate law. This suggests that initial reaction energetically primes a subsequent reaction within the crystalline phase. In contrast, in the absence of an amorphous layer, as in mineral magnetite and hematite, reaction proceeds very slowly since the crystal lattice bonding must be overcome before Fe atoms are displaced and made available for chemical reaction. The proportion of crystalline material (Fe 2 0 3 or Fe,0.) in the present particles does not appear to be critical. The Fe^O . crystalline portion of compound A is approximately 50% by weight of the total particle; whereas in compound B (open hearth dust) the crystalline phase constitutes only about 9% of the total weight. In the present process, a liquid slurry of iron oxide particles is contacted with hydrocarbon gas con¬ taining hydrogen sulfide. As indicated by the kinetic data hereinafter described, rates of reaction (of fast- reacting compounds A and D) at acidic pH may be 1,000- fold greater than at alkaline pH. However, such a rapid reaction rate is not the only parameter of effectiveness of H„S scavenging. In the aqueous dissociation of dissolved H_S to HS — and H+, increased acidity increases the partial pressure of H_S in water in accordance with Henry's law. This means that there will be H 2 S residuals in sweetened hydrocarbon gas, which may actually be greater at lower pH where the rate of reaction is faster than at pH greater than 7. Further, even at pH greater than 7, reaction products of the present iron oxides are acid- stable. Accordingly, in an aqueous suspension of the particles, overall H_S removal may be more efficient at pH greater than 7 even for compounds A and D; and the apparent sacrifice of reaction speed may be compensated OMPI by utilizing greater concentrations of the iron oxide. These factors will be important where hydrocarbon gas flow is relatively rapid and where H 2 S content is high. Iron oxide concentration, pH and flow rate can readily be adjusted in the present process to achieve the desired H_S residual. By commercial standard, a residual of 4 ppm H 2 S is tolerated. Compounds B and C, having a combination of e 2 0 3 and Fe_0. crystalline phases, demonstrate lower reaction efficiency (Table I, kinetic K values) than either com¬ pounds A or D whose respective Fe_0. or F 2 0 3 crystalline phases are substantially pure; but both compounds B and C have unusually stable reaction products. Therefore these compounds are adequately useful in the method of the present invention wherein hydrogen sulfide residuals are present in hydrocarbon gases in low concentrations; in such situations, it is important merely that dissolved sulfides be removed as acid insoluble products of reac¬ tion, so as to avoid the regeneration of H 2 S gas. Reaction kinetics of various iron oxides in reaction with hydrogen sulfide were compared to kinetic results reported in the literature. In the pH range 8-10, the derived rate law for compound A is as follows: d[S. ] = -K x [H + ] 1,06 x [A] wherein [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 3 concentration and [A] is iron oxide concentration kg/ . K is the rate constant in min -1 ppm-1 cm-2 x liters/mole and equal to approximately 1,052. At pH 8-10, the derived rate law agrees closely with Richard's analysis of the reaction of hydrated iron oxide (ferric hydroxide) and hydrogen sulfide [Am. J. Sci. , 274:941 (1974)]. Substitution of observed [S ] and [H ] values at low pH into the rate law equation hereinabove, yields apparent K values which define relative differences in reaction rates among different compounds. In general, OMPI it is found that any iron oxide particle attaining a maximum K value greater than 20 when [S ] and [H ] are measured intermittently during the course of continuous acidic reaction, will be satisfactorily effective in the defined process. The kinetic K values for each of the present iron oxides and control materials are summarized in TABLE I. Only the compounds of classes A-D have kinetic K values greater than 7.0 and so would be of sufficient practical reactivity with hydrogen sulfide over both an alkaline and acidic pH range. In contrast, all of the prior art iron oxides give maximum K values of approximately 0.4 or less when measured at acidic pH. In scavenging hydrogen sulfide from hydrocarbon gases, iron oxides have heretofore been known to form chiefly unstable products of reaction such as e 2 S- 3 (ferric sulfide) and FeS (ferrous sulfide) , together with lesser amounts of stable species such as FeS_ and S°. The unstable products rapidly regenerate H^S upon acidification. Even if the " reaction with hydrogen sulfide itself is conducted under alkaline conditions so as to fix the sulfides in solution (as taught by Sperr, U.S. Patent No. 1,734,307), there is substantial danger of H-,S release from the consumed par¬ ticles upon acidification through later contact with atmospheric C0_. The iron oxide particles used in the present process produce unexpectedly stable reaction products even in the presence of strong inorganic acids. In my prior co-pending application Serial No. 939,441, these products for compound A were identified as FeS 2 , S° and Fe 3 S. by X-ray diffraction. Since X-ray diffraction is essentially semi-quantitative, revealing only materials having a defined crystalline structure, a more functional test of reaction product stability was developed. In this assay, ferrous sulfide (FeS) was prepared by the reaction of Fe(NH.) 2 (SO 2 and Na 2 S in water; a black FeS precipitate was recovered and washed to remove un¬ reacted sulfides. In water solution (200 mis.), the FeS fUK-EA OMP precipitate (2400 total ppm sulfide) rapidly regenerates H_S upon addition of strong acid (10 mis. concentrated HC1) . The liberated H 2 S is bubbled into a ZnC0 3 trap and assayed. In the test series, the iron oxides of Table I were introduced individually into the 200 ml. slurry prior to acidification. Strong acid was then added and the amount of H_S recovered in a zinc carbonate trap measured after one-half hour. The rationale of these experiments is as follows: if the H_S liberated from the FeS precipitate upon acidification reacts with the iron oxide to produce FeS or other species of iron sulfide unstable in the presence of acid, these unstable reaction products will regenerate sulfide as H 2 S gas which bubbles into the zinc carbonate trap. However, if the liberated H_S reacts with the test iron oxide to produce an acid- stable product of reaction, it will be fixed in the reaction vessel and will not pass into the zinc carbonate trap. For purpose of this application and its claims, products of reaction are to " be deemed to be acid-stable if they ' are at least 70% stable in the presence of strong acid when tested by the foregoing assay. The results of tests are given in Table I and are expressed as the percent of total sulfides derived from FeS which remain fixed in the reaction vessel upon acidi- fication and are not released as H 2 S into the zinc carbonate trap. From the data of Table I, each of the classes of compounds A-D, effective in the present process, forms reaction products at least 70% stable in the presence of strong acids. In contrast, all the prior art compounds and control materials yield reaction products only about 10% to 20% stable in the presence of acid. Such reaction products, even if formed under alkaline conditions, pose a future danger of regenerating hydrogen sulfide upon contact with acidic compounds in the environment. Where very rapid reaction rates are desired, impurity levels of various elements in bulk may significantly affect scavenging efficiency. Even compounds having large 2 surface area (greater than 4 m / ) and the characteristliiec g OMPI Fe_0_ or Fe.,0. crystalline phase as hereinabove described, are presently deemed to be unsatisfactory in the present process if any free element of impurity exceeds about 10% by weight. For example, all the control prior art iron oxides designated Q and R of Table I have greater than 10% by weight of at least one such element; all of them have correspondingly low kinetic K values of reaction during the course of continuous flow reaction at acidic pH. In contrast, compounds A-D are found to have low levels of such bulk impurities (less than about 5% by weight) as measured by X-ray fluorescence, these compounds attain a kinetic K value of at least7.0 at acidic pH during the course of continuous flow reaction. The surface area of iron oxides is correlated with their chemical reactivity. Highly dense crystalline com¬ pounds such as magnetite or hematite have very low surface 2 area, generally less than 1.0 /g, and corresponding low reactivity with hydrogen sulfide. Low reactivity thus reflects both the smaller effective surface area available for reaction and the relatively low free energy of these substances due to crystalline lattice bonding. The present iron oxides, useful in the present process, may therefore be characterized or defined by the presence of substantial amorphous iron oxide content, or alternatively by their effective surface area and low density. Reactive compounds will generally have a surface area of greater 2 than 4 m /g and have a lesser density than that of crystalline hematite or magnetite; or reveal a substantial amorphous portion together with a crystalline iron oxide phase upon the more elaborate analysis by ESCA/AUGER, X-ray diffraction, and ion titration analysis hereinabove described. In the method of the present invention, iron oxide particles are added to a liquid to form a slurry or sus¬ pension. Hydrocarbon gas is contacted with the slurry so as to react any hydrogen sulfide present with the particles. Any apparatus adapted to bring a liquid phase into intimate contact with the gas phase will be effective in this method, as scrubbing columns, static mixers, bubble vessels, and the like. The sweetened hydrocarl gas then passes from the liquid slurry and is collected conventionally as it escapes from the slurry. Contrary to prior art teachings, the slurry of the present process may utilize any liquid capable of prac- tical use with the aforementioned apparatus. In experi¬ ments utilizing a Parr pressure bomb apparatus, recovery of sulfur-containing solids was fully as efficient where anhydrous diesel fuel was substituted for water in forming a test slurry of dessicated iron oxide of the type des- ignated compounds A-D, residual water content of dessicated samples was less than 0.2%. These results were not to be expected, in view of Simon and Reichelt [2. Anerg. Allg. Chem. 319:962 (1964)] which teaches that iron oxide reacts with hydrogen sulfide by being first hydrated to FeOOH; that the hydrogen sulfide becomes ionized to form HS and H +; and the reaction proceeds between the FeOOH and the HS , at an optimum water content of 18.0%. Industrial Applicability: Benefits of the present invention, as compared with Conventional regenerative processes (amine type) include the following: the reactive vessel design is of far greater simplicity and less cost, and may accommodate long intervals between change-out of the reactant material, as when gas wells are remote from servicing personnel. At each change-out the down-time will be substantially less. The reacted material being inert, it is easily disposed of; while the regenerative pro¬ cesses produce concentrated hydrogen sulfide which, if flared off, pollutes the atmosphere with sulfur dioxide; otherwise it must be converted into sulfur. As compared with the iron sponge process, the present process will remove far greater concentrations of hydro¬ gen sulfide, change-out is faster and more simple; and the reaction products may be simply disposed of; whereas in the iron sponge process unstable forms of iron sulfide are generated. OMPI Definition: In the claims, the rate constant K, measured as min -1 ppm-1 cm-2 x liters/mole, is calculated for iron 3 oxide concentrations measured in kg/m , and is as appears in the following derived rate law: d[S ]_ -K x [H*] 1*06 x [A] d 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 co .nncceennttrraattiioonn.. [A] is iron oxide concentration kg/m"

Claims: Claims The embodiments of the invention in which an exclusive property or privilege is claimed are defined as follows: 1. In scavenging hydrogen sulfide from hydro¬ carbon gas the process characterized by and comprising the following steps: (a) forming a liquid slurry of iron oxide particles having a surface area of at least 2 4 m /g comprising a crystalline phase portion selected from the group consisting of Fe-O-, Fe_0., and combinations thereof, together with an amorphous e 2 0 3 portion, (b) contacting with said slurry, hydrocarbon gas containing hydrogen sulfide, (c) reacting such hydrogen sulfide with said particles to form substantially acid-stable products of reaction, and (d) collecting the hydrocarbon gas es¬ caping from said slurry. 2. In scavenging hydrogen sulfide from hydrocarbon gas the process characterized by and comprising the steps of (a) contacting hydrogen sulfide contained in such hydro- carbon gas with a liquid slurry of iron oxide particles comprising substantially a crystalline phase of Fe 2 0 3 , Fe_>0., and combinations thereof, said particles having a surface area of at least 4 2/g, and having impurity levels of any free element in bulk of less than 10.0% by weight, (b) reacting said particles with such hydrogen sulfide in a reaction which, if measured intermittently during the course of continuous flow reaction, attains a kinetic K value greater than7.0, and (c)collecting the hydrocarbon gas escaping from said slurry. 3. n scavenging hydrogen sulfide from hydrocarbon gas the process characterized by and comprising the following steps: (a) forming a liquid slurry of iron oxide particles having an Fe +++ content intermediate to that for pure standards of e 2 0 3 and Fe,0., said particles having a surface area of at least 4 m /g, (b) contacting with said slurry hydrocarbon gas containing hydrogen sulfide, (c) reacting such hydrogen sulfide with said particles to form acid-stable products of reaction, and (d) collecting the hydrocarbon gas escaping from said slurry. 4. The process of Claim 1, wherein said iron oxide particles comprise substantially a crystalline Fe_0. core together with an amorphous Fe_0 3 portion. 5. In scavenging hydrogen sulfide from hydrocarbon gas, the process characterized by and comprising the following steps: (a) forming a liquid suspension of iron oxide particles having an Fe content intermediate to that for pure standards of Fe 2 0-. and Fe 3 0., said particles having a crystalline phase comprised substan¬ tially of Fe.,0 with lesser amounts of Fe_0_, and having - a surface area of at least 4 m /g, (b) contacting hydrogen sulfide contained in such hydrocarbon gas with said suspension, (c) reacting said particles with such hydrogen sulfide to form acid-stable products of reaction, and (d) collecting the hydrocarbon gas escaping from said suspension. 6. In scavenging hydrogen sulfide from hydrocarbon gas, the process characterized and comprising the follow- ing steps: (a) forming a liquid slurry of iron oxide particles having an Fe +++ content intermediate to that for pure standards of e 2 0 3 and Fe.,0-, said particles having a surface area of at least 4 m /g and having impurity levels of free elements in bulk of less than 10.0% by weight, (b) contacting hydrogen sulfide con¬ tained in such hydrocarbon gas with said slurry, (c) reacting said particles with such hydrogen sulfide in a reaction attaining a kinetic K value of at least 7.0 during the course of continuous acidic reaction, and (d) collecting the hydrocarbon gases escaping from said slurry. 7. The process of Claims 1, 2, 3, 5 or 6 wherein -Said liquid .is water. 8. The process of Claims 1, 2, 3, 5 or 6 wherein said liquid is a hydrocarbon-based oil. 9. The process of Claims 1, 2, 3, 5 or 6 wherein said iron oxide is basic oxygen furnace dust. 10. The process of Claims 1, 2, 3 , 5 or 6 wherein said iron oxide particles are open hearth dust. OM

Inventors: FOX IRWIN
Applicants: GAS SWEETENER INC
Application year: 1980
Main classification: B01D53
IPC codes: B01D53, C01G49, C07C7