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    • 专利摘要:
    1406085 Recovering sulphur from gase SHELL INTERNATIONALE RESEARCH MAATCHAPPIJ NV 15 Sept 1972 42920/72 Heading C1A Sulphur is recovered from H 2 S and SO 2 by partially combusting a H 2 S-containing gas with a free O 2 -containing gas in the presence of a SO 2 -containing gas, the S formed being separated and the remaining gas passed to a catalyst to form additional S, wherein the amount of SO 2 -containing gas is such that the mole per cent of SO 2 introduced externally to that formed during combustion is at least 25%. The mole ratio of H 2 S : SO 2 in the gases introduced may be between 10 : 1 and 2 : 1. A C 1 -C 5 gaseous hydrocarbon fuel may be mixed with the H 2 S- containing gas to maintain the temperature at 700-1400‹ C. in an amount of 1-25 mole per cent of the H 2 S contact. The catalyst may be activated bauxite. Prior to and after catalyst treatment the S may be removed by condensation. Further catalyst stages may be used.
    公开号:SU731888A3
    申请号:SU731961801
    申请日:1973-09-13
    公开日:1980-04-30
    发明作者:Гроенендаал Виллем (Нидерланды)；Макс Ленц Вальтер (Канада)；Луф Филлиппас (Нидерланды)
    申请人:Шелл Интернэшнл Рисерч Маатсхаппий Б.Ф. (Фирма)；
    IPC主号:
    专利说明:

    one
    The invention relates to the field of chemical technology and solves the problem of obtaining elemental sulfur from hydrogen sulfide and sulfur dioxide.
    The method of obtaining elemental sulfur from hydrogen sulfide-containing gases by conducting a Claus reaction is well known, and various methods based on the use of this reaction find wide industrial application. In accordance with one of these methods, the Claus reaction is carried out in a thermal reaction zone and one or more catalytic reaction zones, with sulfur being recovered from each zone by cooling the gases and condensing the formed sulfur vapor. In the thermal reaction zone, hydrogen sulphide is partially burned to form gases that contain hydrogen sulphide and sulfur dioxide in practically stoichiometric amounts, with sulfur being recovered by Claus reaction with the formation of a significant amount of sulfur vapor. When withdrawing from the thermal reaction zone, the gases are cooled and most of the sulfur vapor is condensed and recovered. Thereafter, the gases are again heated and passed through one or more catalytic reaction ZOIs, in which an additional amount of sulfur vapor is formed, followed by extraction of sulfur by condensation
     implementation of the Claus method, and in this way the stoichiometric amount of sulfur dioxide required for
    10, the reaction of the Claus reaction, partially or practically, is caused by the partial combustion of hydrogen sulfide. In those cases when a large quantity of sulfur dioxide is supplied by another source, the amount of sulfur dioxide, which is thus available, is not sufficient to significantly reduce the yield of sulfur vapor produced in the thermal reaction zone.
    20 Also known is a method for producing sulfur from hydrogen sulphide and gases containing sulfur dioxide, according to which process gases containing sulfur dioxide are treated with a liquid absorbent to obtain 2.5.5 sour (after desorption of the latter) gas enriched with sulfur dioxide, which is subjected to the latter by catalytic hydrogenation
    obtaining hydrogen sulfide gas, which can be used as a component of the hydrogen sulfide-containing feedstock from the Claus 2 process.
    The disadvantage of this method is its complexity, in that the gas containing sulfur dioxide must be reduced in the presence of a catalyst and then it can be used as a raw material component of the Claus process.
    The purpose of the invention is to simplify the process technology.
    To do this, a gas containing sulfur dioxide is introduced into the thermal reaction zone around the periphery of the flame of the burning hydrogen sulfide in an amount that ensures the molar ratio of the added sulfur dioxide and dioxide dioxide formed during the combustion of hydrogen sulfide to not less than 0.25, and to maintain the temperature thermal zone from 700 to 1400 ° C is additionally added to it.
    In addition, the sulfur dioxide-containing gas is fed to the thermal reaction zone in addition to maintaining the molar ratio of H2S: SO2 in the feed in the range from 5: 1 to 3: 1.
    Also, the amount of fuel introduced into the reaction zone is maintained in the range of 1-25 mol. % of the amount of hydrogen sulfide supplied.
    Thus, the invention relates to a method for recovering sulfur from hydrogen sulphide and sulfur dioxide, in which gases that contain hydrogen sulphide are partially burned using oxygen-containing gas in a thermal reaction zone, and gases containing sulfur dioxide are introduced into this thermal reaction room. in such a quantity that the amount of sulfur dioxide in mole percent introduced from the external source of sulfur dioxide produced by partial combustion is o less than 25%, and an additional amount of heat is introduced into the thermal reaction zone, the sulfur formed in the said thermal reaction zone is removed from the gas mixture leaving the thermal reaction zone, and the final gas mixture is then passed, at least through a single catalytic reaction zone, in which an additional amount of sulfur is formed, which is removed from it by the consequence.
    In this description, the expression thermal reaction zone is used to denote the zone in which the gas containing hydrogen sulfide is burned into particles to form a gaseous mixture of hydrogen sulfide with sulfur dioxide, and the residence time of such a mixture in this zone is sufficient to form
    significant amounts of sulfur according to the Claus reaction. The main reactions that take place in the thermal reaction zone of the Claus plant, mol-sio, are presented using the following equations:
     -124 kcal (1)
    , S + SO, -2U ,, - 11 kcal (2)
    3H, S + /, O ,, S, -113 kcal (3)
    The equilibrium state at the end is determined by reaction (2), which is endothermic at high temperatures. To achieve high sulfur yields, it is necessary to maintain a high temperature in the thermal reaction zone and ensure sufficient residence time of hydrogen sulfide and sulfur dioxide to establish equilibrium in accordance with equation (2). Under these conditions, it is possible to achieve a sulfur yield of about 70% of the sulfur present in the raw material fed to the thermal reaction zone.
    In the event that non-combustible material is introduced into the thermal reaction zone, the amount of hydrogen sulfide in gases that is required for the combustion process is reduced, resulting in a decrease in the temperature of the gases in the thermal reaction zone, since less hydrogen sulfide is required for szhgrann with a purpose of sulfur dioxide for sulfur formation, and therefore less heat comes from the high exothermic reaction of
    (1) In accordance with the invention, sulfur dioxide-containing gas is introduced into the thermal reaction zone from an external source in such an amount that the amount, expressed in mole percent, of sulfur dioxide thus added to the amount of sulfur dioxide resulting from the partial combustion of hydrogen sulfide is at least 25%. Since as a result of introducing large quantities of gas that contains sulfur dioxide, the temperature of the gases is reduced to such a low level that the formation of sulfur almost completely stops in accordance with equation (2) for a period of time in which the gases remain in the thermal reaction In the practical application of the invention, the supply of an additional amount of heat to the thermal reaction zone is prevented in order to maintain a high temperature in the zone. In this way, it is possible to achieve a high sulfur yield even though large amounts of sulfur dioxide are introduced into the thermal reaction zone.
    In order to achieve a high sulfur yield in the thermal reaction zone, the amount of additionally supplied heat should preferably be such that the temperature in the thermal reaction zone is maintained at a level of at least 700 ° C. More preferably, the additional heat should be supplied in such an amount that the temperature in the thermal reaction zone is in the range from 900 to 1400 ° C.
    Heat can be supplied to a thermal reaction zone in a number of different ways. One of the methods is that the gas containing sulfur dioxide is heated to a high temperature before it is fed to the thermal reaction zone. In addition, the gas containing hydrogen sulfide, or oxygen-containing gas can be heated before it is fed into the thermal reaction zone. According to various embodiments of this method, two out of three gases or all three gases are heated before they are fed to the reaction zone.
    The main disadvantage of such methods of heat supply is that installation of heating equipment is required for gas supply pipelines, which can be too expensive. Another way of supplying heat is to supply fuel through a burner installed in the pipeline into the pipeline for supplying gas containing sulfur dioxide and its complete ignition in this burner installed in the pipeline and, as a result, the gases are hot when they enter the thermal reaction zone. The disadvantage of this method is that the burner installed in the pipeline is an expensive and cumbersome piece of equipment.
    A method of supplying heat to a thermal reaction zone, which is preferred in accordance with the invention, involves the burning of fuel within said zone. The advantage of this method is the absence of the need and the installation of additional heating equipment, as a result of which this method is more economical. In this case, the amount of oxygen-containing gas, which is introduced into the thermal reaction zone, should be regulated so that it is sufficient for complete burning of the fuel, as well as for burning the required amount of hydrogen sulfide.
    The burning of the entire amount of iron that is introduced into the thermal reaction zone is required in order to prevent the formation of soot, which can lead to undesirable formation and release of B as a product of black sulfur and contamination of the catalyst in
    catalytic reaction zone or zones.
    The amount of hydrogen sulfide that needs to be burned in the thermal reaction zone, and therefore the amount of oxygen that needs to be injected, depends on the type of psychosed fuel and the amount of sulfur dioxide that is supplied from an external source. Positive results
    is achieved when the total amount of sulfur dioxide produced during the combustion of hydrogen sulphide and supplied from the source should be such that the molar ratio between the amounts of hydrogen sulphide and sulfur dioxide in the gases in the thermal reaction zone should be approximately 2: 1 i.e., stoichiometric amounts for the reaction according to equation (2).
    Thus, a high sulfur yield can be achieved in the thermal reaction zone.
    Despite the fact that the flow rate of the source oxygen-containing gas fed to the thermal reaction zone is usually controlled in such a way that the molar ratio between the amounts of hydrogen sulfide and sulfur dioxide in the gases in the thermal reaction zone is
    about 2: 1, this does not mean a significant decrease. If, for example, it is planned to bypass the thermal reaction zone of any part of the gas containing hydrogen sulfide, or part of the gas,
    containing sulfur dioxide, or parts of both of these gases with direct transmission through the catalytic reaction zone, the molar ratio between the amounts of hydrogen sulfide and sulfur dioxide in the gases that are removed from the thermal reaction zone may differ from 2: 1 in order to equal to the relationship between the amounts of hydrogen sulfide and sulfur dioxide in gases, which
    passed through the catalytic reaction zone, i.e., in the gases that are withdrawn from the thermal reaction zone, plus the gases passing around, was almost 2: 1. The yield of sulfur, which is formed in the thermal reaction zone, is reduced when such a workaround is used, however, when the amount of material to be bypassed is small, its effect and the total amount of sulfur recovered by this method is insignificant.
    The fuel can be introduced into the thermal reaction zone separately from other gases. In this case, it is advantageous to introduce fuel directly behind or in the immediate vicinity of the flame, which is formed by the partial combustion of gas containing hydrogen sulfide. However it is
    it is not essential, so the fuel can be introduced in any part or parts of the thermal reaction zone. In addition, the fuel can be introduced into the thermal reaction zone as a mixture with one or several other gases. Accordingly, it can be mixed with a gas that contains sulfur dioxide, or even with an oxygen-containing gas, which is not supplied to the thermal reaction zone. However, it is especially preferable to introduce the injection material into the thermal reaction zone in the form of a mixture of gas that contains hydrogen sulfide. The advantage of this is that the flame is flamed, which forms at the pressure of the gaseous mixture, is very hot and retains its stability even in the presence of large amounts of sulfur dioxide.
    Any suitable fuel can be burned in the thermal reaction zone. It may be gaseous, liquid or solid. Liquid fuel should be burned with a nozzle, and solid fuel should be tocored before burning in order to ensure that it can be completely combusted. Nonetheless, an ir / t, and gaseous fuel is desirable, since it is most convenient to handle and in practical use does not require the installation of special equipment for combustion. A particularly preferred fuel is gaseous hydrocarbon, which is characterized by a practically constant composition, so that the temperature control inside the thermal reaction zone is simplified. This is due to the fact that in the case of using gas, the composition of which varies spontaneously during the process, the degree of heating of the gases also changes, which causes a difficulty in the process order with which the temperature is controlled. For example, methane, ethane, ionia, pentane, or a mixture of one or more of these gases can be used with success in different ratios of components.
    The amount of fuel that is introduced into the thermal reaction zone depends, among other factors, on the amount of gas containing sulfur dioxide, which is introduced, the temperature at which it is desirable to carry out the process and the type of oil used. In the case of the use of gaseous hydrocarbon, its amount usually does not exceed 25 ml. % of the amount of hydrogen sulfide, which is part of the gas containing hydrogen sulfide, introduced into the thermal reaction zone. Preferably, the amount of gaseous hydrocarbon introduced into the thermal reaction zone is in the range from 1 to 10 mol. % of the amount of hydrogen sulfide contained in the gas containing hydrogen sulfide introduced into the thermal reaction zone.
    Sulfur dioxide-containing gas can be introduced into a thermal reaction with a separate gas or in a mixture with a gas that contains hydrogen sulfide, or with oxygen-containing gas. Nevertheless, irrespective of the means of removal, special attention should be paid to the fact that
    formed during the partial combustion of gas containing hydrogen sulphide, should not become unstable, and the flame temperature should be too low. This latter condition takes on additional significance when the fuel is introduced into the thermal reaction zone as a mixture with gas that contains hydrogen sulfide, because if the flame temperature turns out to be too low, zero combustion of carbon black is achieved and soot formation takes place.
    In accordance with the preferred application of the invention, a gas containing sulfur dioxide should be introduced into a thermal zone by distributing it around a gas flame that was burned as a result of partial combustion of gas containing hydrogen sulfide. PRN
    this results in positive results, and since the sludge remains stable and the temperature of the sludge is ionized to a low slush. The distribution of gas containing sulfur dioxide is around
    gas flame can be carried out using any suitable means. However, for this purpose, it is preferable to use a ring distributor with a nozzle.
    The invention is particularly applicable to the process of decomposing sulfur from a gas containing sulfur dioxide obtained during the process of desulfurization of flue gases. When resolved
    The problem of reducing the pollution of the atmosphere with industrial gases by far more and more important is the process of removing sulfur dioxide from the exhaust gases. According to one of the syosobiasis, which
    proposed for the implementation of remote sulfur dioxide processes, it is envisaged to produce a gas enriched in sulfur dioxide, the content of which is approximately GO vol. % then
    as the rest of the gas comes from the water. The proposed method is quite acceptable for the treatment of such a gas. In practice, the amount of gas, sulfur dioxide and sulfur dioxide that is fed into the thermal reaction zoo, relative to the amount of hydrogen sulfide gas, which is also introduced into this gas, is limited. The ratio of: :: shlyos gas content of sulfur containing sulfur is not
    it must be so small that the temperature inside the thermal reaction zone decreases slightly, since in this case adding more heat to the thermal reaction zone is not necessary. On the other hand, this amount should not normally be so large that it eliminates the need for any partial combustion of hydrogen sulphide for the purpose of sulfur dioxide, necessary for sulfur recovery. Thus, typically, the molar ratio between the amounts of hydrogen sulfide and sulfur dioxide in gases that are introduced into the thermal reaction zone is in the range from 10: 1 to 2: 1, preferably in the range from 5: 1 to 3: 1.
    In the case where the molar ratio between hydrogen sulfide and sulfur dioxide in gases that are introduced into the thermal reaction zone is less than 2: 1, the fuel is partially burned to produce hydrogen to restore some sulfur dioxide and to achieve stoichiometric proportions hydrogen sulfide and sulfur dioxide to supply heat, but also to generate hydrogen to reduce sulfur dioxide.
    The invention also relates to a device that can be used to carry out the proposed method. This device includes a reaction apparatus with one or more inlets for a gas containing hydrogen sulfide, a gas containing sulfur dioxide, oxygen-containing gas and fuel, the reaction apparatus being provided with means for burning hydrogen sulfide and fuel; a sulfur condenser and one or more catalytic reaction apparatus, each of which is followed by a sulfur condenser.
    In accordance with a particularly preferred embodiment, the inlet device for a gas containing sulfur dioxide is an annular distributor with nozzles arranged in such a way that the gas is distributed around the flame resulting from the partial combustion of the gas containing hydrogen sulfide. Any suitable burner can be used as a means for burning hydrogen sulphide and fuel, in particular, a very high intensity vortex chamber burner.
    The process in which the method and apparatus according to the invention is applied to extract sulfur from hydrogen sulphide and sulfur dioxide is described in the following part of this detailed description with reference to the accompanying drawings. These figures do not show auxiliary equipment, in particular valves, pumps, instrumentation and the like.
    FIG. 1 shows a flowchart of the process for the recovery of sulfur from hydrogen sulfide and sulfur dioxide; FIG. 2, 3 and 4 are schematic views of three possible variants of isoleny of the reaction apparatus, which can be used to implement the proposed method. In accordance with the technological scheme presented in FIG. 1, a mixture of gas containing hydrogen sulfide and gaseous fuel is fed via line I to the reaction apparatus 2, in which this mixture is burned. The oxygen-containing gas is fed to the reaction apparatus 2 via line 3, and the gas containing sulfur dioxide is introduced into the reaction apparatus 2 via line 4 and through the ring distributor 5. The ring distributor 5 serves to evenly distribute the gas containing dioxide
    sulfur, around the flame produced by burning gas containing hydrogen sulfide and gaseous fuels. Hot gases are removed from the reaction apparatus 2 through line 6 to the heat exchanger 7. Cooling agent
    is fed to heat-transfer agent 7 via line 8 and removed from its ionium 9. Sulfur is condensed from these gases in heat exchanger 7, and it is withdrawn to lithium 10. The cooled gases are further heated and fed through the lip.
    through two catalytic reactionary annauts installed in series 12. After passing through the first catalytic reaction apparatus, the gases are cooled in the refrigerator (in the drawing and shown) to condense the sulfur formed in it, after which they are heated and then passed through the second reaction apparatus, the gases are cooled again in a condenser (not shown in the figure) for the purpose of condensing sulfur in it. The sulfur is removed via line 13. The gases leaving the catalytic reaction apparatus are fed via line 14 to the calcination furnace (not shown in the figure) and then released into the atmosphere.
    FIG. 2-4 equivalent units and parts of the three representative reaction aiarats are denoted by the same elements and contain inlet means 15 for supplying hydrogen sulfide and fuel to the reaction apparatus, refractory lining 16 of the reaction apparatus, means 17 for supplying oxygen-containing gas to the reaction unit, means 18 for supplying Sulfur dioxide-containing gas reaction apparatus, distribution tools 19 used to distribute sulfur dioxide-containing gas inside the reaction apparatus, distribution nozzles 20 and 21 itelnyh means, means 22 for discharging the products from the reaction vessel.
    FIG. 2 is a depiction of the usual city-sector, which means for
    权利要求:
    Claims (2)
    [1]
    Sulfur dioxide containing gas distributions are an annular distributor enclosed in a jacket with means for injecting oxygen-containing gas. Sulfur dioxide-containing gas is introduced by means of nozzles around a flame formed during the combustion of hydrogen sulphide and fuel. FIG. 3, the gas containing sulfur dioxide is introduced into the reaction apparatus through nozzles located in the direction of the central part of the reaction apparatus. These nozzles can be installed perpendicular to the walls of the reaction apparatus, by analogy with nozzle 20 or at an acute angle along the nozzle 21. FIG. 4 shows the image of the reaction apparatus, inside which a high-intensity burner is installed. Sulfur dioxide-containing gas is introduced through a nonstop distribution chamber 19 through nozzles that can be installed either perpendicular to the walls of the reaction apparatus, by analogy with nozzle 20, at an acute angle to them along the lines of nozzle 21. Example. The mixture of gas containing hydrogen sulphide with a mixture of butane and peptan is burned at atmospheric pressure in the main reaction apparatus. The hydrogen sulfide content in the gas, which contains hydrogen sulfide, is 88.0 mol. %, and the amount of the mixture of butane with pentane, which is shifted with a gas containing hydrogen sulfide, is 4.6 mol. % The flow rate of this mixture fed to the main reaction apparatus is 27.2. The flow rate of air that is supplied to the main reaction apparatus is 69.5, while the flow rate of gas containing sulfur dioxide, the content of sulfur dioxide in which is equal to 91.5 mol. % fed to the main reaction apparatus through the ring distributor, equal to 4.8. The average temperature of the gases inside the main reaction apparatus is 1 255 ° C, and the residence time of the gases inside the main reaction apparatus is 0.5 s. The molar ratio between hydrogen sulfide and sulfur dioxide in gases is approximately 2: 1. These gases are fed from the main reaction apparatus to a heat exchanger, in which lh is cooled to a temperature of 205 ° C. Sulfur is condensed from gases at a rate of 24.5 kg / min. The amount of sulfur that is recovered, of the total sulfur content in the initial gas streams supplied to the main reaction apparatus, is 68.07 °. These gases are then fed to two successively installed catalytic reaction apparatus. Before being fed into each of the reaction apparatus, they are heated to a temperature of 2GO-220 ° C, and after passing through each catalytic 5 10 15 20 23 30 35 40 45 50 55 60 65 the reaction apparatus is cooled to a temperature of 150-140 ° C in order to condense of them are sulfur. The catalyst is activated nrnorodny bauxite. The total amount of sulfur condensed from gases passed through two catalytic reaction vessels is 12.0 kg / mpn. The amount of sulfur recovered in the catalytic reaction apparatus, of the total sulfur content in the initial gas streams that are fed to the main reaction apparatus, is 30.9%. The gases leaving from the last reaction catalytic apparatus contain 0.8 mol. % hydrogen sulfide and 0.4 mol. % sulfur dioxide. These gases are passed through an incineration furnace, resulting in gases containing hydrogen sulfide equal to less than 20 parts / 1000000 parts, after which these gases are vented to the atmosphere. As an example, the total amount of recovered sulfur is 93.9% of the total amount of sulfur contained in the source gases entering the main reaction unit, and 63.0% of this sulfur is recovered in the heat exchanger and the remaining 80.9% recovered from gases discharged from the catalytic reaction apparatus. Claim 1. The method is obtained by elemental hydrogen sulfide and sulfur dioxide, including the interaction of hydrogen sulfide with oxygen-containing gas in the thermal reaction zone under conditions of incomplete combustion of hydrogen sulfide in the flare mode, resulting from a mixture of sulfur dioxide and hydrogen sulfide, coming out of the thermal train, coming from the heat source and the hydrogen source, coming out of the heat. measure, in one catalytic reaction zone and extraction of elemental sulfur from the products of each reaction zone, is also distinguished by the fact that, in order to simplify the technology of nroces, Thermal reaction zone at the periphery of the flame of the burning hydrogen sulfide is injected gas containing sulfur dioxide in an amount equal to the curing molar ratio of the additionally introduced sulfur dioxide and sulfur dioxide produced during the combustion of hydrogen sulfide, not less than 0.25, and to maintain the temperature in the thermal zone from 700 to 1,400 ° C, fuel is additionally introduced into the fuel bed. 2. A method according to claim 1, characterized in that the gas containing sulfur biconoxide is supplied to the thermal reaction zone in an amount which removes the support of the molar ratio H2S: SO2 in the feedstock in the range from 5: 1 to 3: 1. 3. Method according to paragraphs. 1 and 2, characterized in that the amount of fuel introduced into the reaction zone is maintained in the range of 1-25 mol. % of the amount of hydrogen sulfide supplied. Sources of information taken into account in examining 1. "Ullmans Encyklopadie der technischen 31888 chemie," Urbans Schwarzenberg, Munchen - Berlin - Wien, 1964, B 15, p. 519 +.
    [2]
    2. Patented application of the Netherlands No. 7102211, cl. From 07C 17/60, 08.22.72 (pro5 totype).
    N, 13
    类似技术:
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    同族专利:
    公开号 | 公开日
    AU474293B2|1976-07-15|
    ES418724A1|1976-10-01|
    ATA792473A|1975-04-15|
    NO137542B|1977-12-05|
    FR2200192A1|1974-04-19|
    SE396586B|1977-09-26|
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    AU6030473A|1975-03-13|
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    MY7600116A|1976-12-31|
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    CS164798B2|1975-11-28|
    GB1406085A|1975-09-10|
    DK135228B|1977-03-21|
    BE804461A|1974-03-05|
    DK135228C|1977-09-19|
    US3851050A|1974-11-26|
    NO137542C|1978-03-15|
    CA987073A|1976-04-13|
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    AT327225B|1976-01-26|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
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    DE3212279C2|1982-04-02|1985-11-28|Davy McKee AG, 6000 Frankfurt|Method and device for the combustion of H 2 S-containing gases|
    US4632043A|1985-01-09|1986-12-30|Amoco Corporation|Method of treating low-quality acid gas and furnace therefor|
    US4798716A|1986-04-29|1989-01-17|Amoco Corporation|Sulfur recovery plant and process using oxygen|
    US4849203A|1987-12-07|1989-07-18|Amoco Corporation|Sulfur recovery plant and process using oxygen|
    DE3642858A1|1986-12-16|1988-06-30|Davy Mckee Ag|METHOD FOR THE SIMULTANEOUS PRODUCTION OF ELEMENTAL SULFUR FROM H2S-CONTAINING GASES AND SOGAS|
    US4798530A|1987-04-21|1989-01-17|Sestrap Arvo M|Nozzle assembly for hot air torch|
    DE3735002A1|1987-10-16|1989-04-27|Metallgesellschaft Ag|PROCESS FOR REMOVING SULFUR HYDROGEN FROM EXHAUST GAS|
    US4830838A|1988-11-01|1989-05-16|The Dow Chemical Company|Removal of hydrogen sulfide from fluid streams with minimum production of solids|
    US5508013A|1991-04-25|1996-04-16|Elf Aquitaine Production|Process for the production of sulphur from at least one sour gas containing hydrogen sulphide and a fuel effluent and thermal reactor|
    DE4121290A1|1991-06-27|1993-01-07|Linde Ag|PROCESS FOR THE THERMAL IMPLEMENTATION OF SULFUR HYDROGEN TO ELEMENTARY SULFUR|
    US7888381B2|2005-06-14|2011-02-15|Bristol-Myers Squibb Company|Modulators of glucocorticoid receptor, AP-1, and/or NF-κB activity, and use thereof|
    US8795625B2|2012-09-27|2014-08-05|Strom W. Smith|Sulfur recovery process|
    US8617509B1|2013-03-31|2013-12-31|Mahin Rameshni|Thermal reduction of sulfur dioxide to sulfur in a single reaction furnace|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB4292072A|GB1406085A|1972-09-15|1972-09-15|Process for the recovery of sulphur from hydrogen sulphide and sulphur dioxide|
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