US2939769A - Sulfur recovery apparatus - Google Patents

Sulfur recovery apparatus Download PDF

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Publication number
US2939769A
US2939769A US587738A US58773856A US2939769A US 2939769 A US2939769 A US 2939769A US 587738 A US587738 A US 587738A US 58773856 A US58773856 A US 58773856A US 2939769 A US2939769 A US 2939769A
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Prior art keywords
chamber
vessel
wall
tube sheet
gas
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US587738A
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Webb Maurice
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Pan American Petroleum Corp
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Pan American Petroleum Corp
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Priority to US587738A priority Critical patent/US2939769A/en
Priority to GB738558A priority patent/GB890793A/en
Priority to DEP20438A priority patent/DE1198333B/de
Priority to FR1204504D priority patent/FR1204504A/fr
Application granted granted Critical
Publication of US2939769A publication Critical patent/US2939769A/en
Priority to BE645837A priority patent/BE645837A/xx
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
    • C01B17/0413—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process characterised by the combustion step
    • C01B17/0417—Combustion reactors
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
    • C01B17/0426—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process characterised by the catalytic conversion
    • C01B17/043—Catalytic converters

Definitions

  • FIG. 1 A first figure.
  • the gaseous products then usually sent through an economizer or condenser and thereafter introduced into aliquid sulfur scrubbing unit.
  • the unreacted gases taken off the scrubber overhead line are then adjusted to a temperature of from about 400 to 450 F. and sent to a second reaction zone.
  • the products from this reactor are then led to a second scrubber to recover free sulfur therefrom.
  • Still another object of my invention is to provide an overall plant layout based primarily on the aforesaid novel boiler design whereby it is possible to eliminate all boiler feed water preparation facilities.
  • this latter object can be accomplished by using the produced steam in an elevated amine l'eboiler of the type employed in Girbotol sour gas sweetening units.
  • Figure 1 is a front end elevational view of a sulfur recovery plant embodying my invention illustrating a particular arrangement of piping and equipment.
  • Figure 2 is a side elevational view of the arrangement shown in Figure l.
  • Figure 3 is a side elevational view of the novel boiler design.
  • Figure 4 is an end view of the boiler shown in Figure 3, illustrating in further detail the position of the two principal sections of the furnace, i.e. the boiler section and the condensing sections.
  • Figure 5 is a sectional view of the boiler shown in Figure '3.
  • Figure 6 is a detailed drawing of the fire tube section shown in Figure 5.
  • Figure 7 is a fragmentary isometric end view principally in section of the boiler of my invention having the front cover removed.
  • Figure 8 is a front end view of the boiler tube sheet shown in Figure3 taken along line A--A.
  • Figure 9 is a rear view of the boiler tube sheet shown in Figure 3 taken along line B-B.
  • Figure 10 is a sectional view of Figure 6 taken along line C-C.
  • Figure 11 is an elevational view partly in section of a novel liquid sulfur separator and storage tank.
  • Figure 12 is a sectional view of Figure 1.0 taken along line D--D.
  • Figure 13 is a fragmentary end view partly in section of the combination separator and storage tank of my invention.
  • Figure 14 is a plan view in section taken along line E-E of Figure 11.
  • Figure 15 is a plan view of the liquid sulfur separator and storage tank showing in detail a piping arrangement employed for handling gaseous and liquid product flowing to the separator and for gaseous efiluent comingfrom the separator.
  • my invention contemplates use of a specially designed boiler in which substantially the lower half thereof comprises a main fire tube and steam tubes.
  • hydrogen sulfide is burned producing temperatures in the neighborhood of 2200* to about 2-500 F., by employing suificient air to produce a final mixture of hydrogen sulfide to sulfur dioxide in a mol ratio of about 2:1.
  • a gas tight metal plate at each end of the boiler divides the upper and lower inter ior portions of the structure on the gas side thereof only, i.e. steam tubes in :the upper half of the unit are in contactwitli the same water that contacts the steam tubes in the lowerha-lf thereof.
  • the gas side in the upper half of the structure at each end of the boiler is preferably divided in half by means of a gas tight metal plate or partition. This provides separate entrance areas or compartments for .the product gas from each of the two converters employed. Hot gaseous reactants are removed from the boiler sec- .tion, some produced sulfur recoveredtherefirom in a section of the liquid separator and storage tank and the remainder of said reactants sent to the first converter in accordance with the more detailed description appearing below; After reaction in the first converter the product gas is sent to that portion of the boiler designed as the condenser section to'handle said product gas from the first converter. The resulting condensate, together with uncondensed gases, is next sent to a separator.
  • the uncondensed reactants are sent to the second converter and the general procedure of condensation, sulfur separation, etc., repeated with the condensation step, this time occurring in a different and separate portion of the boiler from that in which product sulfur from the first converter was condensed.
  • Steam generated during the simultaneous oxidation of about one-third of the hydrogen sulfide to sulfur dioxide and the condensation of converter product gas as generally outlined above is withdrawn from the boiler, and, if desired, it may be sent to a unit in which steam is used as a heating medium or to a suitable elevated condenser after which the resulting condensate is returned to the water or liquid side of the boiler by gravity. In this manner boiler feed water is continuously supplied to the unit without further treatment.
  • Figures 1 and 2 are front end and side elevational views, respectively, of
  • A' preferred arrangement of piping and equipment embodying my invention in which air is brought in through line 2 and mixed with acid (H 8) gas entering furnace 4' through line 6.
  • the furnace is supported by means of I beams 8 which in turn restfon concrete footings 10 set in concrete pad 12.
  • a second supporting structure holding vessel 14 comprises vertical I beams 16 resting on footings 18 also supported by concrete pad 12.
  • Vessel 14 has two gas-tight compartments each of which contains a catalyst bed.
  • Cross-beam 20 makes the supporting structure more rigid and transmits the weight of vessel 14 to the supporting column 16.
  • Boiler 4 is inclined at an angle of about so that free sulfur condensed therein or produced as a result of the oxidation of one-third of the hydrogen sulfide to sulfur dioxide is removed along with the process streams from the rear portion of said boiler, as hereinafter described in detail, by means of line 22 and sent to partially submerged gas-liquid separator and storage tank 24 set in a concrete support25.
  • tank 24 is maintained at a temperature in the neighborhood of from about 250 to about 300 F. by the produced sulfur and by the hot process gas streams in order that the liquid product sulfur is kept in a pumpable and free flowing condition.
  • the exposed portion of tank 24 may be covered with of the resulting mixture in line 30 subsequently going into the first catalyst chamber in vessel 14 is at the de sired initial temperature of about 450 F.
  • Product gas from the first catalyst chamber in vessel 14 is withdravm through line 38 and sent to the first condensing section of boiler 4 via entrance port 64.
  • Condensed product sulfur, together with unreacted product gas, is withdrawn through exit port 65 and line 42 andsent to the second separating section in tank 24.
  • Uncondensed reactants issue from the secondseparating section through line 44 and are mixed with hot bypass gas passing from furnace 4 through three-way valve 46.
  • the resulting mixture comprises the feed gas to the second catalyst chamber and is transmitted thereto through line 32.
  • Hot product gas is taken from the base of the second catalyst chamber in vessel 14 through line 40 and enters the second condensing section of the boiler 4 through inlet port 82.
  • sulfur vapors are condensed to liquid sulfur and the latter together with uncondensed gases are sent through exit port 66 ( Figure 3), directly opposite exit port'65, and line 48 to storage tank 24 where said gases are separated from product liquid sulfur and vented through a stack not shown.
  • Steam generated in both the lower and upper sections of boiler 4 is led off through steam outlet nozzle 49' and line 50 at a pressure of about 50 pounds (absolute).
  • This steam may be used for process heating or for a number of other purposes.
  • such steam may be conducted to a suitable condensing unit, shown diagrammatically as 51 and the resulting condensate returned to the boiler via line 53 and entrance port 80.
  • the overall plant structure as shown in Figures 1 and 2 with the particular equipment sizes given stands approximately 20 feet high and covers an area of about 330 square feet.
  • the furnace itself may be 15 to 20 feet in length by 5 to 8 feet in diameter.
  • the separator and storage tank may be .25 to 30 feet long by 6 to 8 feet in diameter.
  • the overall length of the vessel serving as the two reactors may be from 12 to 15 feet with a diameter range of 6 to 8 feet.
  • the capacity of a plant of this size may range from about 10 to about 25 tons of sulfur per day; I
  • Figures 3 and 4 are detailed elevational side and front end views, respectively, of boiler 4.
  • a manway 52 is provided for access to the steam section of the boiler.
  • Nozzle 54 serves as a fitting for the boiler pressure reliefvalve.
  • Hand holes 56 and 58 are provided at both ends of the base of the boiler for occasional cleaning.
  • An exit port 60 leading from a point near the front end of the lower half of the boiler carries hot bypass gas from the furnace fire tube for purposes previously explained.
  • An exit port 62 appears on the opposite side of furnace 4 and also handles hot bypass gas from the fire tube as previously explained.
  • Entrance port 82 receives product gas coming from the second catalyst chamber and supplies said gas to the second condensing section of the furnace.
  • FIG. 4 shows the front end of the furnace consisting principally of face plates 68 and 70. These plates may be secured to the boiler by bolting them to a flanged support member integral with the shell portion of said boiler.
  • Inlet port 80 receives condensate water and supplies it to 'the steam section of the boiler. Entrance ports 64 and 82 receive product gas from the first and second catalyst chambers, respectively, in accordance with the procedure generally set forth above and which will be described in greater detail below.
  • FIG. 5 is a sectional view of the novel boiler design of my invention comprising a cylindrical shell 83 containing fire tube 84 into which acid gas and air flow through entrance ports 6 and 2, respectively.
  • a castable refractory material 88 Surrounding the front portion of fire tube 84 is a castable refractory material 88.
  • Fire tube 84 has a rear metal cover plate 86 protected fromthe hot combustion products by means of castable refractory 89. Combustion occurs in fire tube 84. Hot process gases produced in said tube then pass through outlets near the end of fire tube 84, one of said outlets 102 beingshown herein. Thereafter, said gases enter tubes 108 where the final cooling in the boiler section is accomplished.
  • Portions of fire tube 84 drot waterieoolediby tthe-steamrside of the boiler .as well lsaother portionsroffsaid boiler, such as :chamber 106,
  • iFire brick refractory 105 protects "cover plate68 from liot combustion "gaSBSiHiZOIIC 106.
  • tubes 108 additional liquid sulfur may be formed and drainslinto chamber llfl along'with unreacted gases which eventually flow out oftthe boiler through exit port 92 as previously errp'lained.
  • 'Castable refractory 1'12 secure'd'by means of -tack welded anchors 4-13, also -placed -on the underneath sidetof steel plate 114 forming the base of chamber monaster protecting the latter from the high temperatlllCS prevailingiin lower'chamber3110.
  • Figure' I is a fragrnentaryiisometric end view of boiler H T-with the cover plate removed. This view indicates clearly'thestructure of.the gas'ti'ght sections at thefront ead of' the boiler. The gasttight'sections at the rearof the boiler-areformed-in-anidentical'fashion.
  • -In-this-view vertical plate 126 is shown to project from tubes 94 to the iifront edgeofhorizontaldivider plate 124 thereby making ,apossible -.-a 1 gas :tight barrier between condensing sections a120tandF122 and forming-chambers 121 and 123 which communicatewith saidisections 120 and 122, respectively.
  • Figure 8 is a front end view of the boiler shown in Figure 3-.taken along line 'A-A with the'cover plates 68 iand lfl'rem'oved.
  • Figure 9 is: asectional rear view Of FigureB taken'along :line-B-BJ This view indicates the similarityi-in'structure of the gas side at the rear of the :boilersto that in the' front end thereofs'hown in Figure 8.
  • The. lower f-POI'tiOIl-Ofithfi "boiler containing the steam tubes 108 is shown to be insulated from the condensing sections 120 and 122 Eby .means of castable refractory 112.
  • Figure 10 is a sectional view of Figure 6 taken along .steel baflle plates 140, 142 and 175 ( Figure 12) welded,
  • the opposite end of the tank is equipped with a pump well 158, which is suspended from a collar at the top of the storage tank, and extends to a level generally 2 to 4 .inches above the base of the tank. Directly below the base of the pump well is a dished head sump 162.
  • Figure l2 is asectional viewof'the vessel shown-in .
  • Figure 11 taken along line.D-D illustratingtin greater detail the structure of separator compartments 138 :and 154 and therelationshipof said compartments to U bend .seal tubes1148and168. Between said U bend'tubes is a riser through which condensate is withdrawn from steam header 172.
  • Channel support'member 144spot Welde'd-to the sides of said cylindricakshell 132 'andto base plate-140 serves'as a stifiienerforithe latter.
  • Partition extends from plate 142 to end cover128'to'define gas' tightcompartments 138 and 154. having inletlport 13K andexit port 155, respectively.
  • Figure 13 is a fragmentary isometric view,'partly in section, of combination separator andstoragetank 24. This viewillustrate s the manner in which vertical plate 175 is aifixed to horizontal plate 140 to form separating compartments 138 and 154. This figure indicates particularly the manner in which a gas tight closure may be used to maintain proper temperature during periods when the plant is not operating and process gases are not entervented to the atmosphere.
  • Figure 15'' is'a plan view of separator andstorage tank 24showing the piping arrangement to and away from tank 24 when the latter is employed in combination with the boiler and reactors. shown in Figures 1 and 2. 'At the end opposite thatinto which the .productgases discharge a conduit 190 attached to exit or exhaust port 164 leads to stack 192 where unreacted product gases are Liquid product sulfur is removed from the tank through conduit 194 by means of pump 196. I
  • Compart- Compartment ing the tank to supply heat.
  • header 176 provided with steam inlet line 178, is aflixed to lines 180 and 182 which in turn divide their flow of steam into lines 184 and'186, respectively, all of said lines 180 to 186, in-
  • header 172 clusive, terminating in header 172.
  • These lines are sup- 7 ported and held free from the base of the tank by means of U rails 188.
  • the entire steam line assembly is slanted so that the included angle defined by the base of the tank and the steam lines themselves terminating in header 172 is about to thus allowing condensate to flow into header 172 and permitting subsequent withdrawal thereof through l e 1?"-
  • 33.75 mols per hour or 11.6 long tons of sulfur per day were obtained for a recovery of 93.5 percent.
  • a further fa ctor' of importance affording substantial e'conom'y in sulfur recovery plants of the type contemplated byni-y invention is-the fact that all process lines -a'ie 'sel f draining. In plants of conventional design it is necessary to steam jacket r all drain lines in order to pre- "went undesirable accumulation and subsequent solidifi- 'cation of sulfur. Such lines are expensive to install and, Tiff eourse,-are subject toplugging.
  • the use of self-draining process' lines together with an ordinary steel storage 'tank havingadequate"external insulation and being so --eonstructed to-function as a final separator of liquid :sdlfur *from"product gases serves to reduce materially initial plant investment.
  • an apparatus for producing elemental sulfur from a gas containing hydrogen sulfide comprising an elongated enclosed metal vessel having a combustion chamber therein, separate means for injection of air and said gas into said chamber, conduits 1) near the opposite end of said chamber communicating with the interior thereof running exteriorly of' said chamber and back to the inlet end thereof, afirst tube sheet extending from wall to wall of said vessel holding the open ends of conduits (l) and a portion ofs'aid chamber near the inlet end thereof, a second tube sheet holding said opposite end of said chamber extending from wall to wall of said vessel and parallel to said first tube sheet, conduits in said vessel substantially surrounding said combustion chamber and connecting said tube sheets, a first gas tight partition extending from said first tube sheet to the end of said vessel adjacent said first tube sheet and from wall to wall of said vessel thereby defining a first and second gas tight chamber, each of said c" anthers thus defined being in communication with separate groups of said connecting conduits held by said first tube sheet, the open ends of conduits (l) being
  • the combination which comprises an elongated enclosed metal vessel first tube sheet, conduits in said vessel substantially surrounding said combustion chamber and connecting said tube sheets, a first gas tight partition extending from said first tube sheet to the end of said vessel adjacent said first tube sheet and from wall to wall of said vessel thereby defining a first and a second gas tight chamber, each of said chambers thus defined being in communication with separate groups of said connecting conduits held by said first tube sheet, the open ends of conduits 1) being in communication with said second chamber, two outlet ports in said second chamber, a gas tight wall extending from said first partition to the vessel Wall facing said partition and from said first tube sheet to the end of said vessel adjacent thereto to divide said first chamber into two compartments, an inlet port in each of said compartments, a second gas tight partition extending from said second tube sheet to the end of said vessel ad- ,jacent thereto and from wall to wall of said vessel thereby defining a third and a fourth gas tight chamber,
  • an apparatus for producing elemental sulfur from a gas containing hydrogen sulfide comprising an elongated enclosed metal vessel having a combustion chamber therein, means for injection of air and said gas into said chamber, conduits (1) near the opposite end of said chamber communicating with the interior thereof running exteniorly of said chamber and back toward the inlet end thereof, a first tube sheet extending from wall to wall of said vessel holding the open ends of conduits (1) and a portion of said chamber near the inlet end thereof, a second tube sheet holding said opposite end of said chamber extending from wall to wall of said vessel and parallel to said first tube sheet, conduits in said vessel substantially surrounding said combustion chamber and connecting said tube sheets, a
  • first gas tight partition extending from said first tube sheet to the end of said vessel adjacent said first tube fining a first and a second gas tight chamber
  • each of said chambers thus defined being in communication with separate groups of said connecting conduits held by said first tube sheet, the open ends'of conduits (1) being in communication with said second chamber, two outlet ports in said second chamber, a gas tight wall extending from said first partition to the vessel wall facing said partition and from said first tube sheet to the end of said vessel adjacent thereto to divide said first chamber into two compartments, an inlet port in each of said oompar-tments, a second gas tight partition extending from said second tube sheet to the end of said vessel adjacent thereto and from wall to wall of said vessel thereby defining a third and a fourth gas tight chamber,.each of said chambers thus defined being in communication with separate groups of said connecting conduits adjacent said second tube sheet, an outlet port in said fourth chamber, a gas tight wall extending from said second partition to the vessel wall facing said partition and from said second tube sheet to the end of said vessel adjacent said second
  • a separator and storage vessel for recovering elemental sulfur from a gaseous mixture containing sulfur vapors
  • the combination comprising an elongated enclosed shell having a plurality of contiguous fluid tight gas separation chambers within a portion ofvsaid shell for handling liquids and vaporscontaining free sulfur, the length and diameter of each of said chambers being less than the respective dimensions of said shell, an individual inlet and outlet port in each of said chambers communicating directly with the exterior of said vessel, and a separate conduit leading from each of said chambers into a common portion of said shell, each of said conduits lying within said shell.
  • a separator and storage vessel for recovering elemental sulfur from a gaseous mixture containing sulfur vapors, the combination comprising an elongated enclosed shell having a fluid tight gas separation chamber within a portion of said shell for handling liquids and vapors containing free sulfur, the length and diameter of said chamber being less than the respective dimensions of said shell, an individual inlet and outlet port in said chamber communicating directly with the exterior of said vessel, and a separate conduit ieading from said chamber into a common portion of said shell, said conduit lying within said shell.
  • a separator and storage vessel for recovering elemental sulfur from a gaseous mixture containing sulfur vapors
  • the combination comprising an elongated'enclosed shell having two fluid tight gas separation chambers within a portion of said shell for handling liquids and vapors containing free sulfur, the length and diam eter of each of said chambers being less than the respective dimensions of said shell, an individual inlet and outlet port in each of said chambers communicating directly with the exterior of said vessel, and a separate conduit leading from each of said chambers into a common por tion of said shell, each of said conduits lying within said shell.
  • an apparatus for producing elemental sulfur from a gas containing hydrogen sulfide comprising an enclosed metal vessel having a combustion chamber therein, means for injection of air and said gas into said chamber, an exit port in said chamber opposite said injection means, a first heat exchange means communicating with both said exit port and the exterior of said vessel, and a second heat exchange means within said vessel superimposed on and spaced apart from said first heat exchange means and said combustion chamber, said second heat exchange means having individual inlet and outlet means communicating with the exterior of said vessel and in non-communicating relationship with said combustion chamber and said first heat exchange means, said combustion chamber and said first and second heat exchange means all being enclosed in a common heat exchange section.
  • an apparatus for producing elemental sulfur from a gas containing hydrogen sulfide comprising an enclosed metal vessel having a combustion chamber therein, means for injection of air and said gas into said chamber, an exit port in said chamber opposite said injection means, a first heat exchange means communicating with both said exit port and the exterior of said vessel, and a second heat exchange means within said vessel and spaced apart from said first heat exchange means and said combustion chamber, said second heat exchange means having individual inlet and outlet means communicating with the exterior of said vessel and in non-communicating relationship with said combustion chamber and said first heat exchange means, said combustion chamber and said first and second heat exchange means all being enclosed in a common heat exchange section.
  • an apparatus for producing elemental sulfur from a gas containing hydrogen sulfide comprising an enclosed metalvessel, said vessel having a first series of tubes arranged therein to define a boiler section, a second series of tubes in said vessel defining a separate condensing section therein having individual inlet and outlet means communicating with the exterior of said vessel but not communicating within said vessel with said first series of tubes, said condensing and boiler sections being enclosed in a common heat exchange section.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Treating Waste Gases (AREA)
US587738A 1956-05-28 1956-05-28 Sulfur recovery apparatus Expired - Lifetime US2939769A (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
US587738A US2939769A (en) 1956-05-28 1956-05-28 Sulfur recovery apparatus
GB738558A GB890793A (en) 1956-05-28 1958-03-07 Apparatus for producing elemental sulfur from hydrogen sulfide containing cases
DEP20438A DE1198333B (de) 1956-05-28 1958-04-01 Einrichtung zur Gewinnung von elementarem Schwefel
FR1204504D FR1204504A (fr) 1956-05-28 1958-04-03 Appareil pour obtenir du soufre élémentaire
BE645837A BE645837A (en:Method) 1956-05-28 1964-03-27

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US587738A US2939769A (en) 1956-05-28 1956-05-28 Sulfur recovery apparatus
BE645837A BE645837A (en:Method) 1956-05-28 1964-03-27

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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3057698A (en) * 1958-12-04 1962-10-09 Pan American Petroleum Corp Sulfur recovery apparatus
US3607132A (en) * 1969-09-05 1971-09-21 Amoco Prod Co Vertical sulfur recovery plant
US4042340A (en) * 1974-05-06 1977-08-16 Amoco Production Company Apparatus for using reheat gas in sulfur recovery systems
US4641607A (en) * 1984-06-04 1987-02-10 Energiagazdalkodasi Intezet Multistage evaporation boiling equipment
US20040265213A1 (en) * 2003-06-25 2004-12-30 Mahin Rameshni Water wall boiler for air and oxygen fired claus sulfur recovery units
US20100012051A1 (en) * 2008-07-15 2010-01-21 Sidney Leroy Born Compact, Tiered Sulfur Recovery Unit
DE102010013052A1 (de) * 2010-03-22 2011-09-22 Uhde Gmbh Vorrichtung und Verfahren zur Kondensation, Abscheidung und Lagerung von flüssigem Schwefel in einer Claus-Anlage
US20150291421A1 (en) * 2014-04-09 2015-10-15 P. Scott Northrop Generating Elemental Sulfur

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2393763A1 (fr) * 1977-06-06 1979-01-05 Zink Co John Appareil destine a bruler un jet de gaz acide et un autre jet d'hydrogene sulfure en un produit permettant de recuperer du soufre

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1751534A (en) * 1929-05-22 1930-03-25 Taylor Huston Boiler
US1790828A (en) * 1931-02-03 Heating apparatus
US2589730A (en) * 1949-09-20 1952-03-18 Gas Machinery Co Heat exchanger
US2834655A (en) * 1955-09-09 1958-05-13 Parsons Co Ralph M Production of elemental sulfur

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1790828A (en) * 1931-02-03 Heating apparatus
US1751534A (en) * 1929-05-22 1930-03-25 Taylor Huston Boiler
US2589730A (en) * 1949-09-20 1952-03-18 Gas Machinery Co Heat exchanger
US2834655A (en) * 1955-09-09 1958-05-13 Parsons Co Ralph M Production of elemental sulfur

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3057698A (en) * 1958-12-04 1962-10-09 Pan American Petroleum Corp Sulfur recovery apparatus
US3607132A (en) * 1969-09-05 1971-09-21 Amoco Prod Co Vertical sulfur recovery plant
US4042340A (en) * 1974-05-06 1977-08-16 Amoco Production Company Apparatus for using reheat gas in sulfur recovery systems
US4641607A (en) * 1984-06-04 1987-02-10 Energiagazdalkodasi Intezet Multistage evaporation boiling equipment
US20040265213A1 (en) * 2003-06-25 2004-12-30 Mahin Rameshni Water wall boiler for air and oxygen fired claus sulfur recovery units
US7067101B2 (en) * 2003-06-25 2006-06-27 Worleyparsons Group Inc. Water wall boiler for air and oxygen fired Claus sulfur recovery units
US20100012051A1 (en) * 2008-07-15 2010-01-21 Sidney Leroy Born Compact, Tiered Sulfur Recovery Unit
US7867459B2 (en) 2008-07-15 2011-01-11 Sidney Leroy Born Compact, tiered sulfur recovery unit
DE102010013052A1 (de) * 2010-03-22 2011-09-22 Uhde Gmbh Vorrichtung und Verfahren zur Kondensation, Abscheidung und Lagerung von flüssigem Schwefel in einer Claus-Anlage
US20150291421A1 (en) * 2014-04-09 2015-10-15 P. Scott Northrop Generating Elemental Sulfur
US9504984B2 (en) * 2014-04-09 2016-11-29 Exxonmobil Upstream Research Company Generating elemental sulfur

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BE645837A (en:Method) 1964-07-16
FR1204504A (fr) 1960-01-26

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