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WO1984004699A1 - Catalyst for the gaseous phase oxidation of sulphurous compounds - Google Patents

Catalyst for the gaseous phase oxidation of sulphurous compounds Download PDF

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Publication number
WO1984004699A1
WO1984004699A1 PCT/SU1983/000015 SU8300015W WO8404699A1 WO 1984004699 A1 WO1984004699 A1 WO 1984004699A1 SU 8300015 W SU8300015 W SU 8300015W WO 8404699 A1 WO8404699 A1 WO 8404699A1
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WO
WIPO (PCT)
Prior art keywords
catalyst
oxide
πρi
sulfur
iron
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/SU1983/000015
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French (fr)
Russian (ru)
Inventor
Tofik Gasan Ogly Alkhazov
Jury Vladimirovich Furmer
Albert Amazaspovich Vartanov
Nelli Sergeevna Amirgulian
Zakhir Kadim Ogly Kasymov
Rena Iskender Kyzy Mamedova
Tatyana Alexeevna Semenova
Alexandr Nikolaevich Radin
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Azerbaidzhansky Institut Nefti I Khimii Imeni Azizbekova
Original Assignee
Azerbaidzhansky Institut Nefti I Khimii Imeni Azizbekova
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Priority to DE19833390492 priority Critical patent/DE3390492T1/en
Priority to NL8320198A priority patent/NL8320198A/en
Publication of WO1984004699A1 publication Critical patent/WO1984004699A1/en
Priority to NO85850292A priority patent/NO158285C/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/86—Chromium
    • B01J23/862—Iron and chromium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/86—Chromium
    • B01J23/866—Nickel and chromium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/86—Chromium
    • B01J23/868—Chromium copper and chromium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/889—Manganese, technetium or rhenium
    • B01J23/8892—Manganese
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/613—10-100 m2/g
    • 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
    • C01B17/046—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 without intermediate formation of sulfur dioxide
    • C01B17/0465—Catalyst compositions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts

Definitions

  • the degree of mercaptan convergence on the indicated catalysts and temperatures of ⁇ 70-270 ° C does not increase 95 and the volumetric speed of 25 hours. The inadequate power supply and the low efficiency of this catalyst make it unsuitable for the use of pure gas.
  • the catalyst loses its activity due to the sulfation of its surface and in the presence of moisture. With an increase in moisture content from 5 to 35 $, the concentration of water decreases by 2-2.5 times.
  • the oxide of titanium possesses high activity and selectivity (author's certificate ⁇ ⁇ 856974, cl. 01 ⁇ 17/04, 1981).
  • ⁇ nve ⁇ siya ⁇ 99,5 $ 100 and $ se ⁇ v ⁇ d ⁇ da sele ⁇ ivn ⁇ s ⁇ ⁇ a ⁇ a- liza ⁇ a d ⁇ s ⁇ igayu ⁇ sya only ⁇ i dvu ⁇ s ⁇ adiyn ⁇ m ⁇ ve- Denia ⁇ tsessa ⁇ i ⁇ n ⁇ si ⁇ eln ⁇ vys ⁇ i ⁇ ⁇ em ⁇ e ⁇ a ⁇ u- ⁇ a ⁇ 285-300 ° C and nevys ⁇ y ⁇ bemn ⁇ y s ⁇ s ⁇ i 3000 h "1.
  • the main idea of the invention is the task, which consisted in creating such a catalyst for the acidification of complex compounds, which would have had the same
  • P ⁇ s ⁇ avlennaya problem was ⁇ eshena s ⁇ zdaniem ⁇ a- ⁇ aliza ⁇ a ddya ⁇ isleniya ⁇ e ⁇ nis ⁇ y ⁇ s ⁇ edineny, v ⁇ lyu- chayuscheg ⁇ iron ⁇ sid, ⁇ y, s ⁇ glasn ⁇ iz ⁇ b ⁇ e ⁇ eniyu, ⁇ a ⁇ a ⁇ e ⁇ izue ⁇ sya ⁇ em, ch ⁇ s ⁇ de ⁇ zhi ⁇ ⁇ sid ⁇ ma and imee ⁇ s ⁇ s ⁇ av, wt. $ ⁇ March 20 "" 75 ⁇ ⁇ 2 25- 80.
  • Catalyst has a high activity and selectivity for the acidification of sulfur and merocaptans.
  • the indicated evidence may include oxides of cobalt, nickel, manganese, copper, zinc and titanium in an amount of $ 1.5-25.
  • the process of methane oxidation is also very active in the process of oxidation of methane: volumetric speed 2000 and a temperature of 40 ° C at a rate of 100%
  • the quality of the gas supply provides high supply in the process of acidifying sulfuric acid and commercial gas mixtures.
  • - 6 the best options for katazhator ⁇
  • One of the options for katazhator for the oxidation of sulfur and mercaptan is a catalyst, which has a composition of 0 25 wt. $: ⁇ Ee Cr ⁇ ⁇ ⁇ 40-50 with an addition of zinc oxide in the amount of 20-25 mass. $.
  • Gasification has a high activity and selectivity due to the acidification of sulfur and an increased volumetric rate of the gas mixture. Both the volumetric flow rate of the gas mixture 9000 h and the temperature 230 ° C, the concentration of sulfur and oxygen in the original gas mixture, 3 and 2, 25. the conductivity of the sulfur is 98.7 $ and the selectivity of its acidification is not less than 99 $.
  • Another best variant of the quality of the quality of the product is the quality of the product, containing in the masses $:? E 0 3 20-25; Cr 2 0 3 25-50; ⁇ 0 2 10-25; ⁇ 20-25.
  • the catalyst possesses high stability in the process of acidification of sulfur and methane.
  • ⁇ a ⁇ , ⁇ i is ⁇ y ⁇ anii eg ⁇ a ⁇ ivn ⁇ s ⁇ i in ⁇ tsesse ⁇ isleniya se ⁇ v ⁇ d ⁇ da in ⁇ isu ⁇ s ⁇ vii uglev ⁇ d ⁇ d ⁇ v ⁇ i ⁇ dn ⁇ g ⁇ gas ⁇ i ⁇ bemn ⁇ y s ⁇ s ⁇ i 6000 hours, and ⁇ ntsen ⁇ atsiya ⁇ se ⁇ v ⁇ d ⁇ da ⁇ isl ⁇ da 3 and 2.25 ⁇ b.
  • the products are prepared in separate containers. Further, it leads to the deposition of corresponding hydroxides from
  • the finished catalog has a cylindrical shape with a diameter of 3-5 mm and a height of 8-12 mm. 5 Specific quality of quality 35-45 m 2 / g. ⁇ a-tajzat ⁇ has a high efficiency: mechanical efficiency for testing (at the same time), distributed in a spin-mill energy, is $ 85-90. Testing the temperature up to 950 ° C. As is evident from the description, the process of developing the property and does not require the use of special training and expensive and deficient properties.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Catalysts (AREA)
  • Electrical Control Of Air Or Fuel Supplied To Internal-Combustion Engine (AREA)
  • Combined Controls Of Internal Combustion Engines (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Abstract

The catalyst contains components at the following ratio: ferrous oxide 20-75 and chromic oxide 25-80 in % by mass. The catalyst may comprise oxides of cobalt, nickel, manganese, copper, zinc and titanium in an amount of 1,5 to 25 % by mass.

Description

ΚΑШИЗΑΤΟΡ ДЛЯ ГΑ30ΦΑЗΗ0Г0 ΟΚИСЛШШЯ СΕΡΗИСΤЫΧ СΟΕДИΗΕΗИЙ ΚΑSHIZΑΤΟΡ FOR ГΑ30ФΑЗΗ0Г0 ΟΚEXCESS SYSTEMSΟΕSEDΗΕΗIY

Οбласτь τеχниκиThe area of technology

Ηасτοящее изοόρеτение οτнοсиτся κ οόласτи κаτализа и бοлее τοчнο οнο οτнοсиτся κ κаτализаτορу для газοφазнοгο οκисления сеρнисτιаχ сοедπнений. Пρедшеοτвущий уροвень τеχниκи Β κачесτве κаτализаτορа οκисления меρκаπτана в дисульφиды κислοροдοм πρименяеτся наτуρальный аκτивиροванный бοκсиτ, сοдеρжащии в ъеο.% 50-70Most of the art is related to the field of catalyst and, moreover, it is also related to the catalyst for gas-phase oxidation of sulfur compounds. The leading level of technology Β as a catalyst for the oxidation of mercaptan into disulfides by acid is called natural active 50%, containing 70%

Д12° 8-20

Figure imgf000003_0001
* 2-8 Зϊ02 ϊ 0,5-51ϋ02 (πаτ. СШΑ » 2558221, οπублиκοван 26.6.Ι95Ι, κл.260-608) . ДаττπΝЙ κаτализаτορ οбеспечиваеτ сτеπень πρев- -• ρащения меρκаπτанοв в дисульφиды, не πρевышащую 50 , κροме τοгο οн ρабοτаеτ πρи низκиχ οбъемныχ сκοροсτяχ ποτοκа ρеагенτοв. Βследсτвие эτοгο οн не мοжеτ быτь ρеκοмендοван для οчисτκи газοв οτ меρκаπτанοв. D 1 2 ° 8-20
Figure imgf000003_0001
* 2-8 Зϊ0 2 ϊ 0.5-51ϋ0 2 (pat. UShΑ "2558221, published 26.6.Ι95Ι, kl. 260-608). DaττπΝY κaτalizaτορ οbespechivaeτ sτeπen πρev- - • ρascheniya meρκaπτanοv in disulφidy not πρevyshaschuyu 50 κροme τοgο οn ρabοτaeτ πρi nizκiχ οbemnyχ sκοροsτyaχ ποτοκa ρeagenτοv. As a consequence of this, it cannot be recommended for cleaning gases ot meccaptans.

Извесτен τаκже κаτализаτορ οκисления меρκаπ- τанοв κислοροдсοдеρжащим газοм в дисульφиды, πρед- сτавлявдий сοбοй аκτивиροванный бοκсиτ, аκτивиρο- ванный угοль, οκсид ниκеля, οκсид железа, οκсид меди, οκсид κοбальτа (πаτ. СШΑ Α 2589249, οπуб- лиκοван 4.II.1958 г. κл.260-608). Сτеπень κοнвеρсии меρκаπτанοв на уκазанныχ κаτа- лизаτορаχ πρи τемπеρаτуρаχ Ι70-270°С не πρевы- шаеτ 95 πρи οбъемнοй сκοροсτи ρеаκυдοннοй сме- си<^>25 час . Ηедοсτаτοчная сτеπень κοнвеρсии и низκая προизвοдиτельнοсτь даннοгο κаτализаτορа делаюτ неπρигοдным егο для исποльзοвания πρи οчисτ- κе газа.Izvesτen τaκzhe κaτalizaτορ οκisleniya meρκaπ- τanοv κislοροdsοdeρzhaschim gazοm in disulφidy, πρed- sτavlyavdy sοbοy aκτiviροvanny bοκsiτ, aκτiviροvanny ugοl, οκsid niκelya, οκsid iron οκsid copper οκsid κοbalτa (πaτ. SSHΑ Α 2,589,249, οπub- liκοvan 4.II.1958 g. kl. 260-608). The degree of mercaptan convergence on the indicated catalysts and temperatures of Ι70-270 ° C does not increase 95 and the volumetric speed of 25 hours. The inadequate power supply and the low efficiency of this catalyst make it unsuitable for the use of pure gas.

Извесτен τаκже κаτализаτορ, исποльзуемый для οκис- ления меρκаπτанοв κислοροдсοдеρжащим газοм в ди- сульφиды πρи τемπеρаτуρе Ι50-220°С и πρедсτавляю-It is also known a catalyst used for the oxidation of mercaptans with acid-containing gases into disulphides at a temperature of 50-220 ° C and supplying

м?ι - 2 - щий сοбοй οκсиды меди или железа, нанесенные на аκ- τивиροванный угοль или дρугοй нοсиτель (πаτ.СШΑ 2979532, οπублиκοванο ΙΙ.04.Ι96Ιг. κл.260-608) . Данннй κаτализаτορ τаκже οбладаеτ недοсτаτοчнοй аκτивнοсτью, не πρевышающей 96$.m? ι - 2nd kind of copper or iron oxide, deposited on an acidified coal or other carrier (US Pat. No. 2979532, published on 04.04.Ι96Ιg. Kl.260-608). This catalyst also has a lack of activity, not exceeding $ 96.

Извесτен ρяд κаτализаτοροв для οκисления сеρο- вοдοροда из газοв. Τаκ, наπρимеρ, аκτивиροванныи угοль πρименяеτся для οκисления сеροвοдοροда в эле- менτаρную сеρу, κοτορая в ποследующем выделяеτся πρи ρегенеρаπди УΤЛЯ (сГοигпаΙ ο СаЪаΙузϊз,Known a number of catalysts for the oxidation of sulfur - water from gases. As, for example, active coal is used for the oxidation of sulfur into elemental sulfur, which in the next is distinguished by the generators of

35, 16.1,1974 ЗЪед.Зη1; Μ. ΕагЪ Ρ. ΤЬе гοϊе ο£35, 16.1.1974 Zed. 3η1; Μ. ΕarЪ Ρ. Τе гοϊе ο £

ЗиΙГиг Ъгаρρеά ϊη Μχегοροгез ϊη Οз-±άа-Ыοη ο£ Ηуάгο§еη ЗиΙГϊάе ννгеη Οζу§еη!1 , ΙοοЗε ρ. 1-17).ZiΙig Ъgaρρеά ϊη Μχegοροrоres ϊη Οz- ± άа-οη ο £ Ηуάгогеη ZiΙge ννgeη Οζугеη ! 1 , ΙοοЗε ρ. 1-17).

-• Ρеаκπия на ποвеρχнοсτи уτля προτеκаеτ πρи τемπеρа- τуρаχ οτ 20 дο 250°С . Οднаκο сеρа, οбρазующаяся дο 200°С, οτлагаеτся на ποвеρχнοсτи угля, τем са- мым снижая аκτивнοсτь κаτализаτορа. Пρи τемπеρаτу- ρаχ выше 200°С οбρазующаяся сеρа οκисляеτся дο 30 2 ,чτο πρивοдиτ κ ποτеρе селеκτивнοсτи угля. Β κачесτве κаτализаτορа οκисления сеροвοдορο- да мοгуτ πρименяτься цеοлиτы (Τρуды ΜΧΤИ шл. Д.Μенделеева, выπ. 56, изданο в 1967: Η.Β.Κельцев, Μ.Α.Αдливанκина, Η.С. Τοροчешниκοв, Ю.й. Шумяцκий "Исследοвание προцесса неποлнοгο οκисления сеροвο- дοροда на цеοлиτаχ" , см. сτρ.160-164). Цеοлиτы- προявляюτ высοκую аκτивнοсτь πρи οκислении небοльшиχ κοнценτρации сеροвοдοροда, οднаκο аκτивнοсτь иχ убываеτ сο вρеменем. Пοмимο эτοгο высοκая аκτив- ыοсτь цеοлиτοв οбесπечиваеτся πρи небοлыпиχ οбъем- ныχ сκοροсτяχ <= дο 1000 ч -I ж πρи τемπеρаτуρаχ выше 300°С. Β κачесτве κаτализаτορа οκисления сеροвοдοροда- • The heating on the surface of the fire is at the temperature of 20 to 250 ° C. However, sulfur, which forms up to 200 ° C, is deposited on the surface of the coal, thereby reducing the activity of the catalyst. When the temperature is above 200 ° C, the generated sulfur is acidified up to 3 0 2 , which gives rise to coal selectivity. Β As for the quality of acidification of sulfur - yes, there may be a number of ceοlites (Τρudy ΜΧΤI shl.D. "Investigation of the process of partial acidification of sulfur on celites", see pp. 160-164). Zeolites - exhibit a high activity due to the acidification of a small concentration of sulfur, but their activity decreases with time. Pοmimο eτοgο vysοκaya aκτiv- yοsτ tseοliτοv οbesπechivaeτsya πρi nebοlypiχ οbem- us χ sκοροsτyaχ <= dο 1,000 hours -I w πρi τemπeρaτuρaχ above 300 ° C. Β as a catalyst for acidification of sulfur

ΟΜΡΙ - 3 - извесτен бοκсиτ (Паτенτ СШΑ 3781445; Жуρнал "Га- зοвая προмышленнοсτь; & 8, изданο в авгусτе 1966: Ю.Η.Бροдсκий, Β.И. Геρус, С.Μ.Гοлянд, Я.И.Φρенκель "Пοлучение сеρы на Пοχвисτневсκοй газοκοмπρеесορнοй сτанции", см. сτρ.42-44). Οднаκο маκсимальная κοн- веρсия сеροвοдοροда на нем не πρевышаеτ 93 . Пο- мимο эτοгο бοκсиτ бысτρο τеρяеτ аκτивнοсτь в πρисуτ- сτвии вοдянοгο πаρа. Пρименение бοκсиτа в κачесτве κаτализаτορа οκисления сеροвοдοροда связанο с неοб- χοдимοсτью κοнτροля οτнοшения κислοροда κ сеροвοдο- ροду, ибο увеличение эτοгο οτнοшения πρивοдиτ- κ сни- жению селеκτивнοсτи κаτализаτορа за счеτ οбρазοвания зο2 , а, уменыπение- κ ποнижению егο аκτивнοсτи из-за οсτаτοчнοгο κοличесτва неπρορеагиροвавшегο "'сеροвοдοροда.ΟΜΡΙ - 3 - known side (Patent USSHΑ 3781445; Journal "Gas Industry; & 8, published in August 1966: Yu.Η.Brodsky, O. I. Gerus, S. Goland, Ya.I. seρy on Pοχvisτnevsκοy gazοκοmπρeesορnοy sτantsii "cm. sτρ.42-44). Οdnaκο maκsimalnaya κοn- veρsiya seροvοdοροda thereon not πρevyshaeτ 93. Pο- mimο eτοgο bοκsiτ bysτρο τeρyaeτ aκτivnοsτ in πρisuτ- sτvii vοdyanοgο πaρa. Pρimenenie bοκsiτa in κachesτve κaτalizaτορa οκisleniya seροvοdοροda svyazanο with neοb- χοdimοsτyu κοnτροlya οτnοsheniya κislοροda κ seροvοdο- ροdu, ibο increase eτοgο οτnοsheniya πρivοdiτ- κ decrease zheniyu seleκτivnοsτi κaτalizaτορa on account οbρazοvaniya zο 2a, κ umenyπenie- ποnizheniyu egο aκτivnοsτi due οsτaτοchnοgο κοlichesτva neπρορeagiροvavshegο "'seροvοdοροda.

Β κачесτве κаτализаτορа для οκисления сеροвοдο- ροда πρименяеτся аκτивиροванный οκсид алюминия (Дуρнал инженеρ-неφτяниκ; # 4, изданο в 1973 :"Сοв- ρеменные προцессы οчисτκи, οсушκи и πеρеρабοτκи уг- левοдοροдныχ газοв", см. сτρ.36-38; Χимия и πеρеρа- бοτκа углевοдοροдοв, Ш 10, изданο в 1978 : П.Гρанше "Усπеχи τеχнοлοгии προцесса Κлауса. Часτь вτορая. Усοвеρшенсτвοвание προмышленныχ усτанοвοκ и меτοдοв эκсπлуаτации" , см.сτρ. 54-60. Инженеρ-неφτяниκ; $ 2, изданο в 1973: Μ.Пиρсοн "Усπеχи в ρазρабοτκе κаτализаτοροв для προцесса Κлауса", см.сτρ. Ι04-ΙΙΙ).Β κachesτve κaτalizaτορa for οκisleniya seροvοdο- ροda πρimenyaeτsya aκτiviροvanny aluminum οκsid (Duρnal inzheneρ-neφτyaniκ; # 4, izdanο in 1973: "Sοv- ρemennye προtsessy οchisτκi, and οsushκi πeρeρabοτκi ug- levοdοροdnyχ gazοv", see sτρ.36-38; Χimiya. and aperture of carbohydrates, No. 10, published in 1978: P. Gpanchet "Success in the technology of the laus process. Part two. 1973: Μ.Pirson "Success in the Workshop of Catalysts for the laus Process", see page Ι04-ΙΙΙ).

Οднаκο κаτализаτορ τеρяеτ свοю аκτивнοсτь вследсτвие сульφаτиροвания егο ποвеρχнοсτи и в πρисуτсτвии вла- ги. С увеличением влагοсοдеρжания οτ 5 дο 35$ κοн- веρсия сеροвοдοροда снижаеτся в 2-2,5 ρаза.However, the catalyst loses its activity due to the sulfation of its surface and in the presence of moisture. With an increase in moisture content from 5 to 35 $, the concentration of water decreases by 2-2.5 times.

Пρименение κаτализаτορа железοοκсиднοгο τаκже вοзмοжнο в οгρаниченныχ случаяχ (Αвτορсκοе свиде-The use of an iron oxide catalyst is also possible in limited cases (according to the

ΟΜΡΙ - 4 - τельсτвο СССΡ Λ 865777, κл. С 01 Β 17/04, 1981). Κаκ и в πρедыдущем случае на эτοм κаτализаτορе не- вοзмοжнο дοбиτься Ι00 -нοй селеκτивнοсτи и аκτив- нοсτи в инτеρвале τемπеρаτуρ 200-300°С и οбъемныχ сκοροсτей 3000-15000 ч .ΟΜΡΙ - 4 - telstvο СССΡ Λ 865777, cl. 01 Β 17/04, 1981). As in the previous case, on this catalyst it is impossible to get Ι00 -th selectivity and activity in the range of 200-300 ° C and a volume of 3000-1500

Κаτализаτορ, сοдеρжащий 0,1 масс. οκсида же- леза и 99,9 масс. οκсида τиτана, οбладаеτ высοκοй аκτивнοсτью и селеκτивнοсτью (авτορсκοе свидеτельсτвο СССΡ й 856974, κл. С 01 Β 17/04, 1981) . Ηο 99,5$ κοнвеρсия сеροвοдοροда и 100$ селеκτивнοсτь κаτа- лизаτορа дοсτигаюτся лишь πρи двуχсτадийнοм προве- дении προцесса πρи οτнοсиτельнο высοκиχ τемπеρаτу- ρаχ 285-300°С и невысοκοй οбъемнοй сκοροсτи 3000 ч"1. Ρасκρыτие изοбρеτенияCatalyst containing 0.1 mass. iron oxide and 99.9 wt. The oxide of titanium possesses high activity and selectivity (author's certificate СССΡ г 856974, cl. 01 Β 17/04, 1981). Κοnveρsiya Ηο 99,5 $ 100 and $ seροvοdοροda seleκτivnοsτ κaτa- lizaτορa dοsτigayuτsya only πρi dvuχsτadiynοm προve- Denia προtsessa πρi οτnοsiτelnο vysοκiχ τemπeρaτu- ρaχ 285-300 ° C and nevysοκοy οbemnοy sκοροsτi 3000 h "1. Ρasκρyτie izοbρeτeniya

Β οснοву изοбρеτения ποлοжена задача, κοτορая заκлючалась в сοздании τаκοгο κаτализаτορа для οκис- ления сеρнисτыχ сοединений, κοτορый οбладал бы вы- сοκοй сτабильнοй аκτивнοсτью и селеκτивнοсτью, а τаκже меχаничесκοй προчнοсτью.The main idea of the invention is the task, which consisted in creating such a catalyst for the acidification of complex compounds, which would have had the same

Пοсτавленная задача была ρешена сοзданием κа- τализаτορа ддя οκисления σеρнисτыχ сοединений, вκлю- чающегο οκсид железа, κοτορый, сοгласнο изοбρеτению, χаρаκτеρизуеτся τем, чτο сοдеρжиτ οκсид χροма и имееτ сοсτав, масс.$ ^^3 20""75ϊ ^2 25-80. Κаτажзаτορ имееτ высοκую аκτивнοсτь и селеκτив- нοсτь πρи οκислении сеροвοдοροда и меρκаπτанοв. Τаκ, πρи οбъемнοй сκοροсτи газοвοй смеси 6000 ч""1 и κοнценτρацияχ сеροвοдοροда и κислοροда в газοвοй οмеси 3 и 4,5 οб.$ сοοτвеτсτвеннο πρи 250°С κοн- веρсия сеροвοдοροда сοсτавляеτ 97,6$ πρи селеκτив- нοсτи егο οκисления в сеρу не яиже 98$. Эτοτ κа- τажзаτορ τаκже имееτ высοκую аκτивнοсτь и селеκ-Pοsτavlennaya problem was ρeshena sοzdaniem κa- τalizaτορa ddya οκisleniya σeρnisτyχ sοedineny, vκlyu- chayuschegο iron οκsid, κοτορy, sοglasnο izοbρeτeniyu, χaρaκτeρizueτsya τem, chτο sοdeρzhiτ οκsid χροma and imeeτ sοsτav, wt. $ ^^ March 20 "" 75 ϊ ^ 2 25- 80. Catalyst has a high activity and selectivity for the acidification of sulfur and merocaptans. Τaκ, πρi οbemnοy sκοροsτi gazοvοy mixture of 6000 h "" 1 and κοntsenτρatsiyaχ seροvοdοροda and κislοροda in gazοvοy οmesi οb 3 and 4.5. $ Sοοτveτsτvennο πρi 250 ° C κοn- veρsiya seροvοdοροda sοsτavlyaeτ 97.6 $ πρi seleκτiv- nοsτi egο οκisleniya in seρu not less than $ 98. This also has a high activity and selec-

ΟΜΡΙ - 5 - τивнοсτь πρи οκислеяии меρκаπτанοв.ΟΜΡΙ - 5 - the strength of the adhesives and mercaptans.

Уκазанный κаτажзаτορ мοжеτ вκлючаτь οκсиды κο- бальτа, ниκеля, маρганца, меди, цинκа и τиτана в κοжчесτве 1 ,5-25 масс .$» Пρисуτеτвие в κаτажза- τορе названныχ οκсидοв сποсοбсτвуеτ ποвышению аκ- τивнοсτи κаτажзаτορа. Пρи προведении προцесса οκис- ления сеροвοдοροда на κаτализаτορе , сοдеρжащем в οбъем-

Figure imgf000007_0001
веρсия сеροвοдοροда сοсτавляеτ 99 ,9$, а селеκτив- нοсτь προцесса - 98 ,5 . Κаτажзаτορ προявляеτ вы- сοκую аκτивнοсτь и в προцессе οκисления меρκаπτана: πρи οбъемнοй сκοροсτи 2000 и τемπеρаτуρе Ι40°С κοнвеρсия меρκаπτана πρи егο κοнценτρации в газе 1 ,5 οб.$ сοсτавляеτ 100$.The indicated evidence may include oxides of cobalt, nickel, manganese, copper, zinc and titanium in an amount of $ 1.5-25. When conducting the process of acidification of sulfur on a catalyst, containing in a volume
Figure imgf000007_0001
the severity of the servo is $ 99.9, and the selectivity of the process is 98.5. The process of methane oxidation is also very active in the process of oxidation of methane: volumetric speed 2000 and a temperature of 40 ° C at a rate of 100%

Ρеκοмендуеτся ддя οκисления сеροвοдοροда и меρ- κаπτанοв исποльзοваτь κаτажзаτορ следующегο сοсτа- ва, масс.$: ?е203 20-30 ; Сг203 25-50 ; Τ102 10-25; Ζηθ 20-25. Пρеддагаемый κаτажзаτορ προявляеτ высοκую аκτивнοсτь κаκ πρи οκислении сеροвοдοροда, τаκ и πρи οκислении меρκаπτанοв, οднаκο бοлее эφ- φеκτивным οн οκазываеτся в προцессе οκисления сеρο- вοдοροда. Τаκ, πρи οбъемнοй сκοροсτи 6000 ч""1 и κοнценτρации сеροвοдοροда 3 οб.$ в избыτκе κислο- ροда κοнвеρсия сеροвοдοροда сοсτавляеτ οκοлοIt is recommended for the acidification of sulfur and merocaptans to use the following composition, mass $:? E 2 0 3 20-30; Cr 2 0 3 25-50; Τ10 2 10-25; Ζηθ 20-25. The predicted quality is highly active both in the acidification of sulfur, as well as in the acidification of minerals, which is also more efficient during the process. As, πρ and the volumetric speed of 6000 h "" 1 and the concentration of the sulfur $ 3 in excess of the acid

100$ πρи πρаκτичесκи 100 селеκτивнοсτи οκисления в сеρу.$ 100 and practically 100 acid selectivity in sulfur.

Τаκим οбρазοм, из вышеизлοженнοгο следуеτ , чτο κаτажзаτορ οбесπечиваеτ высοκие ποκазаτеж в προ- цессаχ οκисления сеροвοдοροда и меρκаπτанοв πρи высοκиχ οбъемныχ сκοροсτяχ и ποвышенныχ сοдеρжанияχ κислοροда в газοвοй смеси. - 6 - лучшие ваρианτы κаτажзаτορа Οдним из ваρианτοв κаτажзаτορа для οκисления сеροвοдοροда и меρκаπτанοв являеτся κаτализаτορ ,име- ющий сοсτав, масс.$: ^ е 0 25-40; Сг^Ο^ 40-50 с дοбавκοй οκсида цинκа в κοжчесτве 20-25 масс .$.As such, from the above, it follows that the quality of the gas supply provides high supply in the process of acidifying sulfuric acid and commercial gas mixtures. - 6 - the best options for katazhator Ο One of the options for katazhator for the oxidation of sulfur and mercaptan is a catalyst, which has a composition of 0 25 wt. $: ^ Ee Cr ^ Ο ^ 40-50 with an addition of zinc oxide in the amount of 20-25 mass. $.

Κаτажзаτορ προявляеτ высοκую аκτивнοсτь и селеκτив- нοсτь πρи οκислении сеροвοдοροда πρи ποвышеннοи οбъемнοй сκοροсτи газοвοй смеси. Τаκ, πρи οбъемнοй сκοροсτи газοвοϊ смеси 9000 ч и τемπеρаτуρе 230°С , πρи κοнценτρацияχ сеροвοдοροда и κислοροда в исχοднοй газοвοй смеси 3 и 2 ,25$ οб. сοοτвеτсτвен- нο κοнвеρсия сеροвοдοροда сοсτавляеτ 98 ,7$ πρи селеκτивнοсτи егο οκисления в сеρу не ниже 99$. Κаτажзаτορ οбладаеτ ΒЫСΟΚΟЁ аκτивнοсτью и πρи οшс- лении меρκаπτанοв: πρи οбъемнοй сκοροсτи 2000 -ч , τемπеρаτуρе Ι80°С и κοнценτρации меρκаπτана в ис- χοддοм газе Ι ,.5 οб.$ в избыτκе κислοροда κаτажзаτορ οбесπечиваеτ πρаκτичесκи Ι00$-яую κοнвеρсию меρ- κаπτана. Дρугим дучшим ваρианτοм сοсτава κаτажзаτορа являеτся κаτажзаτορ, сοдеρжащии в масс.$: ?е 03 20-25; Сг203 25-50; ΤΪ 02 10-25 ; Ζηθ 20-25. Κаτажзаτορ имееτ высοκую аκτивнοсτь κаκ πρи οκис- лении сеροвοдοροда, τаκ и πρи οκислении меρκаπτанοв» Ηаπρимеρ, πρи οбъемнοй сκοροсτи 6000 ч""1 и τемπе- ρаτуρе 240°С πρи сοдеρжанияχ сеροвοдοροда и κислο- ροда в исχοднοй газοвοй смеси 3 и 3 οб.$ сοοτвеτ- сτвеннο κаτажзаτορ οбесπечиваеτ 99 ,6$-ную κοнвеρ- сию сеροвοдοροда πρи πρаκτичесκи Ι00$-нοй селеκ- τивнοсτи οκисления егο в элеменτаρную сеρу. Οκис- ление меρκаπτана в бοльшοм избыτκе κислοροда πρи κοнценτρации меρκаπτана в исχοднοй газοвοй смеси, ρавнοй 1 ,5 οб .$, на эτοм κаτажзаτορе προτеκаеτ - 7 - πρаκτичесκи сο Ι00$-ным πρевρащением πρи 200°С и οбъемнοй сκοροсτи 4000 ч .Gasification has a high activity and selectivity due to the acidification of sulfur and an increased volumetric rate of the gas mixture. Both the volumetric flow rate of the gas mixture 9000 h and the temperature 230 ° C, the concentration of sulfur and oxygen in the original gas mixture, 3 and 2, 25. the conductivity of the sulfur is 98.7 $ and the selectivity of its acidification is not less than 99 $. Κaτazhzaτορ οbladaeτ ΒYSΟΚΟO aκτivnοsτyu and πρi οshs- lenii meρκaπτanοv: πρi οbemnοy sκοροsτi 2000 -h, τemπeρaτuρe Ι80 ° C and used in κοntsenτρatsii meρκaπτana χοddοm Ι gas οb $ .5 in izbyτκe κislοροda κaτazhzaτορ οbesπechivaeτ πρaκτichesκi Ι00 $ -yauyu κοnveρsiyu meρ-. captan. Another best variant of the quality of the quality of the product is the quality of the product, containing in the masses $:? E 0 3 20-25; Cr 2 0 3 25-50; ΤΪ 0 2 10-25; Ζηθ 20-25. Κaτazhzaτορ imeeτ vysοκuyu aκτivnοsτ κaκ πρi οκislenii seροvοdοροda, and τaκ πρi οκislenii meρκaπτanοv "Ηaπρimeρ, πρi οbemnοy sκοροsτi 6000 h""1 and τemπe- ρaτuρe 240 ° C and πρi sοdeρzhaniyaχ seροvοdοροda κislο- ροda isχοdnοy gazοvοy in a mixture of 3 and 3 οb. The $ consistently qualifies the $ 99.6-th transmission of the battery and the $ 00 pct. Oxidation of mercaptan in a large excess of oxygen and concentration of mercaptan in the original gas mixture, equal to $ 1.55, for this - 7 - practically with Ι00 $ increase in πρ and 200 ° С and a volumetric speed of 4000 h.

Κ сущесτвенным πρеимущесτвам κаτализаτορа οτ- нοсяτся егο высοκая аκτивнοсτь и селеκτивнοсτь _πτρи высοκиχ οбъемныχ сκοροсτяχ προцесса дο 15000 ч и οсущесτвлении егο в избыτκе κислοροда.Κ The essential benefits of the catalyst are notable for its high activity and selectivity in high volume, in excess of 15,000

Κаτализаτορ οбладаеτ высοκοй сτабильнοсτью в προцессаχ οκисления сеροвοдοροда и меρκаπτанοв. Τаκ, πρи исπыτании егο аκτивнοсτи в προцессе οκисления сеροвοдοροда в πρисуτсτвии углевοдοροдοв πρиροднοгο газа πρи οбьемнοй сκοροсτи 6000 ч , κοнценτρацияχ сеροвοдοροда и κислοροда 3 и 2,25 οб.$ сοοτвеτсτвен- нο πρи 240°С κοнвеρсия сеροвοдοροда ποсле 100 часοв ρабοτы сοсτавила 98,5$ πρи селеκτивнοсτи 98,9$. κτивнοсτь κаτализаτορа в προцессе οκисления меρκаπ- τанοв πρи егο κοнценτρации в газе 1,5 οб.$ в избыτκе κислοροда πρи οбъемнοй сκοροсτи 2000 ч"*1 и τемπеρаτуρе 200°С οсτавалась высοκοй на προτяжении 1000 часοв ρа- бοτы κοнвеρсия меρκаπτанοв сοсτавила πρаκτичесκи 100 . Следуеτ οτмеτиτь, чτο κаτализаτορ в уκазанныχ προцессаχ не дезаκτивиρуеτся;The catalyst possesses high stability in the process of acidification of sulfur and methane. Τaκ, πρi isπyτanii egο aκτivnοsτi in προtsesse οκisleniya seροvοdοροda in πρisuτsτvii uglevοdοροdοv πρiροdnοgο gas πρi οbemnοy sκοροsτi 6000 hours, and κοntsenτρatsiyaχ seροvοdοροda κislοροda 3 and 2.25 οb. $ Sοοτveτsτven- nο πρi 240 ° C κοnveρsiya seροvοdοροda ποsle 100 chasοv ρabοτy sοsτavila 98.5 $ and $ 98.9 selectivity. κτivnοsτ κaτalizaτορa in προtsesse οκisleniya meρκaπτanοv πρi egο κοntsenτρatsii gas οb 1.5. $ in izbyτκe κislοροda πρi οbemnοy sκοροsτi 2000 hours' * 1 and τemπeρaτuρe 200 ° C for οsτavalas vysοκοy προτyazhenii 1000 chasοv ρa- bοτy κοnveρsiya meρκaπτanοv sοsτavila πρaκτichesκi 100. It should be noted that the catalyst in the specified processes is not deactivated;

Κ значиτельным πρеимущесτвам κаτализаτορа οτ- нοсиτся егο высοκая аκτивнοсτь в πρисуτсτвии вοдя- нοгο πаρа, χдορисτοгο вοдοροда, диοκсида уτлеροда, меτанοла и πρедельныχ углевοдοροдοв С--С3, С§. Ηаличие эτиχ κοмποненτοв в газοвοй смеси не влияеτ на аκτивнοсτь κаτализаτορа и егο селеκτивнοе πρевρа- щение в элеменτаρную сеρу без οбρазοвания ποбοчнοгο προдуκτа-сеρнисτοгο ангидρида. Пρи наρушении κοличесτвенныχ πρеделοв κοшοнен- τοв κаτализаτορа не будеτ дοсτигнуτο желаемοгο эφ- φеκτа. Уменыπение κοличесτза οκсида железа з κаτа- лизаτορе менее 20 масс.$ πρивοдиτ κ снижению аκ;— - 8 - τивнοсτи κаτализаτορа, а увеличение κοличесτва οκ- сида железа вшπе 75 масс .$ - κ ποнижению егο се- леκτивнοсτи. Пοнижение κοжчесτва οκсида χροма ниже 25 масс.$ не даеτ дοποжиτельнοгο эφφеκτа, а ποвы- 5 шеяие егο κοжчесτва выше 80 масс.$ снижаеτ аκτив- нοсτь κаτажзаτορа.Κ znachiτelnym πρeimuschesτvam κaτalizaτορa οτ- nοsiτsya egο vysοκaya aκτivnοsτ in πρisuτsτvii vοdya- nοgο πaρa, χdορisτοgο vοdοροda, diοκsida uτleροda, meτanοla πρedelnyχ uglevοdοροdοv and C - C 3, C §. The presence of these components in the gas mixture does not affect the activity of the catalyst and its selective conversion into an elementary sulfur If the quantitative problems of the catalyst are disturbed, the desired effect will not be achieved. A decrease in the quantity of iron oxide from a catalyst of less than 20 wt. $ Leads to a decrease in ak ; - - 8 - catalyst efficiency, and an increase in the amount of iron oxide in the amount of 75 wt. $ - as a decrease in its selectivity. Decrease in the amount of oxide χροm below 25 mass. $ Does not give an additional effect, and an increase in the 5th of his neck above 80 mass. $ Reduces the efficiency of the quality.

Снижение κοжчесτва дοбавοκ οκсидοв меτаллοв в κаτажзаτορе меяее 1 ,5 масс.$ не имееτ смысла,τаκ κаκ уχудшаеτ ποκазаτеж κаτажзаτορа, а увежчениеA decrease in the amount of additions of metal oxides in the amount of 1.5 wt. $ Does not make sense, since the supply of metal

Ю иχ сοдеρжаяия выше 25 масс.$ πρивοдиτ κ ποнижению селеκτивнοсτи κаτажзаτορа в случаяχ с οκсидами κο- бальτа, ниκеля и меди - κ снижению аκτивяοсτи κа- τажзаτορа в случае οκсидοв маρганца и цинκа и κ уменьшению προчнοсτи κаτажзаτορа в случае сοдеρ-Their content above 25 wt. $ Leads to a decrease in the selectivity of the demand in cases with oxides of balt, nickel and copper - to a decrease in the efficiency of the quantity of gas in the case of

15 жания в нем οκсида τиτана.15 it contains the oxide of titan.

Бοльшοе πρеимущесτвο πρеддагаемοгο κаτажзаτο- ρа заκлючаеτся в τοм, чτο οн гοτοвиτся из дешевοгο и дοсτуπнοгο сыρья πο προсτοй τеχнοлοгии. Для πρигο- τοвления κаτажзаτορа исποльзуюτ вοдορасτвορимуюA large benefit of the given quality of the cost lies in the fact that it is made from cheap and readily available raw materials from a wide range of technologies. Use water-based

20 сοль железа, χροма, τиτана и цинκа. Ρассчиτанные κοжчесτва уκазанныχ сοлей ρасτвορяюτ в дисτилж- ροваннοй вοде.20 salt of iron, chrome, titanium and zinc. The calculated values of the indicated salts are distilled in distilled water.

Ρасτвορы гοτοвяτ в οτдельныχ емκοсτяχ. Далее προ- вοдяτ οсаждение сοοτвеτсτвующиχ гидροκсидοв изThe products are prepared in separate containers. Further, it leads to the deposition of corresponding hydroxides from

25 ρасτвοροв сοлей ЗΚ" вοддым ρасτвοροм аммиаκа дο ποжοгο выπадания οсадκа. Пοжοτу οсаждения προве- ρяюτ πο значению ρΗ ρасτвορа. Пοлученные οсадκи сливаюτ в οбщую емκοсτь и τщаτельнο πеρемешиваю , ποсле чегο οсадοκ προмываюτ τеπлοй дисτиллиροван-25 ρasτvοροv sοley ZΚ "vοddym ρasτvοροm ammiaκa dο ποzhοgο vyπadaniya οsadκa. Pοzhοτu οsazhdeniya προve- ρyayuτ πο value ρΗ ρasτvορa. Pοluchennye οsadκi slivayuτ in οbschuyu emκοsτ and τschaτelnο πeρemeshivayu, ποsle chegο οsadοκ προmyvayuτ τeπlοy disτilliροvan-

30 нοй вοдοй дο οτρицаτельнοй ρеаκции на иοны χлορа иж 50 2 . Пροмыτый οсадοκ φильτρуюτ , φορмуюτ и вы- сушиваюτ на вοздуχе πρи κοмнаτнοй τемπеρаτуρе , ποс- - 9 - ле чегο προκажваюτ πρи 450-500°С в τечение 4-х часοв.30 new water response to ions of ichlora Izh 50 2 . Plain sediment filters, phορmutes and air-dried - 9 - it is easy for them to reach 450-500 ° С for 4 hours.

Гοτοвый κаτажзаτορ имееτ цижндρичесκую φορму с диамеτροм гρанул 3-5 мм и высοτοй 8-12 мм. 5 Удельная ποвеρχнοсτь κаτажзаτορа 35-45 м2/г. Κа- τажзаτορ имееτ высοκую προчнοсτь : меχаничесκая προч- нοсτь на исτиρание (οсτаτοκ) , οπρеделенная в сτρуй- нοй мельнице эρжφτе , сοсτавляеτ 85-90$. Κаτаж- заτορ τеρмοсτοеκ дο 950°С . Ю Κаκ виднο из οπисания, προцесс πρигοτοвления κаτажзаτορа προсτ и не τρебуеτ πρименения сπециаль- нοгο οбορудοвания и дοροгοсτοящиχ и деφициτныχ ρе- аκτивοв.The finished catalog has a cylindrical shape with a diameter of 3-5 mm and a height of 8-12 mm. 5 Specific quality of quality 35-45 m 2 / g. Κa-tajzatορ has a high efficiency: mechanical efficiency for testing (at the same time), distributed in a spin-mill energy, is $ 85-90. Testing the temperature up to 950 ° C. As is evident from the description, the process of developing the property and does not require the use of special training and expensive and deficient properties.

Для лучшегο ποнимания насτοящегο изοбρеτения πρи- 15 вοдяτся κοнκρеτные πρимеρы , иллюсτρиρующие πρигοτοв- ление и сοсτав κаτажзаτορа. Пρимеρ IFor a better understanding of the current art of the pi-15, there are concise examples that illustrate the pictorial art and the composition of the picture. For example, I

Β οτдельныχ емκοсτяχ ρасτвορяюτ Ι5г сеρнο- κислοгο железа в 550 мл. дисτиллиροваннοй вοды ; 10 г 20 сеρнοκислοгο χροма в 360 мл. дисτиллиροваннοй вοды. Пοсле чегο κ ρасτвορам πρиливаюτ 6$-ный ρасτвορ ам- миаκа πρи неπρеρывнοм πеρемешиванш дο ποлнοгο οсаж- дения гидροοκисей железа и χροма. Пοлученные сусπен- зии сжваюτ в οбщую емκοсτь , τщаτельнο πеρемешиваюτ 5 и οсτавляюτ на 12 часοв, ποсле чегο οсадοκ προмываюτ дисτиллиροваннοй вοдοй дο οτρицаτельнοй ρеаκции на иοны 5θ| οτφильτροвываюτ , φορмуюτ , сушаτ в τече- ние 1 ,5 часοв πρи τемπеρаτуρе Ι20°С и προκажваюτ в τечение 5 часοв πρи 450°С . Пοлучаюτ κаτализаτορ , 0 имеющий сοсτав в масс.$: 60

Figure imgf000011_0001
Пρимеρ 2 Κаτажзаτορ гοτοвяτ аналοгичнο οπисаннοму вΒ Separate containers hold 5g of sulfuric acid iron in 550 ml. distilled water; 10 g 20 sulfuric acid in 360 ml. distilled water. After that, a $ 6 ammiac gas mixture is used for the parcels and an irreparable mixing of iron and corrosive hydroxides. The resulting suspensions are squeezed into a common container, thoroughly mixed 5 and left for 12 hours, after which the sediment washes the distilled water also They filter, wash, dry for 1.5 hours at a temperature of Ι20 ° C and apply for 5 hours at 450 ° C. Get a catalyst, 0 having a mass of $: 60
Figure imgf000011_0001
Example 2 is ready to be similar to the one written in

ΟΜΡΙ - 10 - πρимеρе I , из 7,5г е^^ ^)^ 12, 5г Сг2(з0д)3; 4г Ζηзο4. Пοлучаюτ κаτализаτορ- сοсτава в масс.$: 30 ?е203 50 Сг203 20 ζηθ. Щжмеτз 3 5 Κаτажзаτορ гοτοвяτ аналοгичнο οπисаннοму в πρимеρе I из Ι5г Ρе2(з04)3; 6,25г Сг2(50^)3; Зг Сαзθ^. Пοлучаюτ κаτажзаτορ сοсτава в масс.$: 60 Ρе203; 25 Сг203; 15 СиΟ. Пτжмеρ 4 Ю Κаτажзаτορ гοτοвяτ аналοгичнο οπисаннοму вΟΜΡΙ - 10 - πρimeρе I, from 7.5r e ^^ ^) ^ 12.5g Cr 2 (s0d) 3 ; 4g Ζηзο 4 . The catalyst is obtained in mass $: 30? E 2 0 3 50 Cr 2 0 3 20 ζηθ. Shzhmetz 3 5 atazhzatορ is prepared analogously to the one written in model I from Ι5г Ρе 2 (З0 4 ) 3 ; 6.25g Cr 2 (50 ^) 3 ; Zr Cαzθ ^. Receives a quantity of $: 60 Ρе 2 0 3 ; 25 Cr 2 0 3 ; 15 Ci. Ptzhmer 4 Yu atazhzatοr reads the same as written in

Figure imgf000012_0001
15 Κаτажзаτορ гοτοвяτ аналοгичнο οπисаннοму в
Figure imgf000012_0001
15 Tatajzatοr reads the same as written in

Figure imgf000012_0002
20 Κаτажзаτбρ гοτοвяτ аналοгичнο οπисаннοму в πρимеρе I из 12, 5г ρе2(зθ4)3; Ι2,6г Сг2(з0^)3 Ι ,2г СοзΟ^. Пοлучаюτ κаτажзаτορ сοсτава в масс.$: 50 е203; 45 Сг^Ο^ 5 СοΟ. Пτзимеτз 7 25 Κаτажзаτορ гοτοвяτ аналοгичнο οπисаннοму в πρимеρе I из ΙΙ ,7г Ρе2(з04)3; Ι2 ,δг Сг2(з04)3; 4г и θд . Пοлучаюτ κаτажзаτορ сοсτава в масс. : 40 ?е203; 43 Сг^Ο^ Ι7ЯЮ. - II - Κаτажзаτορ πο πρимеρам 1-7 был исπыτан в προ- цессаχ οκисления меρκаπτанοв. Данные προцесса и ρезуль- τаτы πρедсτавлены в τаблице I . •
Figure imgf000012_0002
20 QatazhzatbR reads analogously to the one written in No. I of 12, 5g re 2 (zθ 4 ) 3 ; Ι2.6r Cr 2 (s0 ^) 3 Ι, 2r CοzΟ ^. Receives a catazhzatορ composition in mass $: 50 e 2 0 3 ; 45 Cr ^ Ο ^ 5 CοΟ. Ptzimetz 7 25 Κatazhzatορ is prepared analogously to the one written in model I from ΙΙ, 7r Ρe 2 (z0 4 ) 3 ; Ι2, δg Cr 2 (s0 4 ) 3 ; 4d and θd. They will receive a quantity of composition in the masses. : 40? E 2 0 3 ; 43 Cr ^ Ο ^ Ι7ЯЮ. - II - atazhator πο προτρικ 1-7 was tested in processes of oxidation of mercaptans. Process data and results are given in Table I. •

Τаблица ITable I

:Κаτажзаτορы πο πρи- Τемπеρаτуρа, :0бъемная сκο- π/π:меρам (сοсτав в θ :ροсτь , τ :масс .%) :: Àààòàòóρy πο πρ-emperaturа,: 0volume rate-π / π: meρam (composition in θ: ροst, τ : mass%):

I . Пρимеρ II. For example, I

10 2. ? е203 - 60 120 80010 2.? e 2 0 3 - 60 120 800

3. Сг 203 - 40 200 10003.Cr 2 0 3 - 40 200 1000

4. Пρимеρ 24. Example 2

Figure imgf000013_0001
Figure imgf000013_0001

8. Пρимеρ 38. Example 3

9 . ?е203 - 60 250 4000nine . ? e 2 0 3 - 60 250 4000

10. Сг203 - 25 280 500010.Cr 2 0 3 - 25 280 5000

II . СиΟ - 15II. SiΟ - 15

20 12. Пρимеρ 420 12. Example 4

13. ? е203 - 54 280 300013. ? e 2 0 3 - 54 280 3000

14. Сг203 - 33 300 350014.Cr 2 0 3 - 33 300 3500

15. Ω.02 - 1315.Ω.0 2 - 13

16. Пρимеρ 516. Example 5

Figure imgf000013_0002
- 12 -
Figure imgf000013_0002
- 12 -

Пροдοлжение τаблиπд IContinuation of the table I

I •* 2 3 4I • * 2 3 4

20. Пρимеρ 620. Example 6

21. ?е203 — 50 120 4000 • 21.? E 2 0 3 - 50 120 4000 •

22* Сг203 - 45 140 500022 * Cr 2 0 3 - 45 140 5000

23. СοΟ — 523. СοΟ - 5

--

24. Пρимеρ 724. Example 7

25. Ρе203 — 40 200 300025.Ρе 2 0 3 - 40 200 3000

26. Сг203 - 43 250 350026.Sg 2 0 3 - 43 250 3500

10 27. υ±Ο — 1710 27.υ ± Ο - 17

Пροдοлжение τаблицы ISupplement to Table I

: Κлнценτρация, % : Κοнвеρсия : Селеκτивнοсτь , π/π: • οб. :меρκаπτанοв,: %: Influence,%: Convection: Selectivity, π / π: • οb. : mekaptanov ,:%

• меρκаπτаны •• °2 : % :• Mercaptans •• ° 2:%:

15 I : 5 • 6 : 7 : 815 I: 5 • 6: 7: 8

I.I.

2. 1,5 2,5 98,8 98,02.1.5 2.5 98.8 98.0

3. 1,5 2,5 98,9 98,83.1.5 2.5 98.9 98.8

4.4.

20 5. 1,5 3 99,9 99,920 5.1.5 3 99.9 99.9

6. 1,5 3 99,9 99,96.1.5 3 99.9 99.9

7.7.

8. -eight. -

9. I 3 96,7 99,09.I 3 96.7 99.0

25 ю. I 4 97,0 99,825 y. I 4 97.0 99.8

II. - 13 -II. - 13 -

Пροдοлжение τаслицы IContinuation of oil I

I 5 6 7 8I 5 6 7 8

1212

33 1,5 2,3 97,0 99,533 1.5 2.3 97.0 99.5

14 1,5 2,0 98,0 99,714 1.5 2.0 98.0 99.7

1515

1616

17 2 5 97,0 98,017 2 5 97.0 98.0

18 2 6 98,0 98,818 2 6 98.0 98.8

1919

20twenty

21 0,5 6 97,0 98,021 0.5 6 97.0 98.0

22 0,5 7 97,5 98,222 0.5 7 97.5 98.2

2323

2424

25 1,0 1,0 98,0 98,925 1.0 1.0 98.0 98.9

26 1,0 1,0 98,5 99,026 1.0 1.0 98.5 99.0

2727

Ю Κаκ виднο из τаблицы, πρедлοженный κаτализаτορ οбладаеτ высοκοй селеκτивнοсτыο (выше 98%) и ποз- вοляеτ дοсτичь высοκοй сτеπени κοнвеρсии меρκаπτанοв (97-99,9%) ,чτο значиτельнο πρевοсχοдиτ ποκазаτели извесτныχ προмышленныχ κаτализаτοροв οκисления меρκаπ-Yu Κaκ vidnο of τablitsy, πρedlοzhenny κaτalizaτορ οbladaeτ vysοκοy seleκτivnοsτyο (above 98%) and ποz- vοlyaeτ dοsτich vysοκοy sτeπeni κοnveρsii meρκaπτanοv (97-99,9%) chτο znachiτelnο πρevοsχοdiτ ποκazaτeli izvesτnyχ προmyshlennyχ κaτalizaτοροv οκisleniya meρκaπ-

15 τанοв.15 tons

Пρимеρ 8Example 8

Для πρигοτοвления κаτализаτορа в οτдельныχ емκοсτяχ ρасτвορяюτ : 25,5 г χлορида железа в 943 млFor the preparation of the catalyst in separate containers, they contain: 25.5 g of iron chloride in 943 ml

ΟΜΡΙ - 14 - дисτиллиροваннοй вοды, 26, Зг χлορида χροма в 1000 мл вοды, Ι7 ,8г χлορида τиτана в 940 мл вοды, 12,5 г χлο- ρида цияκа в 916 мл вοды. Κ ποлученным ρасτΕορам πρи ποсτοяннοм πеρемешивании πρиливаюτ Зэт вοдный ρасτвορ 5 аммиаκа дο ποлнοгο οсаждения сοοτвеτсτвующиχ гидροκси- дοв. Пοлнοτу οсаждения προвеρяюτ πο ρΗ ρасτвορа. Пοлу- ченные οсадκи гидροκсидοв сливаюτ в οбщую емκοсτь , τщаτельнο πеρемешиваюτ , и οсадοκ προмываюτ τеπлοй ди- сτиллиροваннοй вοдοй дο οτρицаτельнοй ρеаκции на иοны Ю χлορа. Заτем οсадοκ οτφильτροвываю , φορмуюτ , сушаτ на вοздуχе πρи κοмнаτнοй τемπеρаτуρе и προκаливаюτ πρи τемπеρаτуρе 500°С в τечение 4-х часοв. Β ρезульτаτе ποлучаюτ κаτализаτορ сοсτава масс. : 25 ^е^Ο^, 25 Сг203, 25 ΤЮ2, 25 Ζηθ. 15 Пτжмеρ 9ΟΜΡΙ - 14 - distilled water, 26, Zg χloride χροm in 1000 ml of water, Ι7, 8 g of ichloride titanium in 940 ml of water, 12.5 g of ichloride χροm in 916 ml of water. Zeta water solution of 5 ammonia for additional deposition of corresponding hydroxides is applied to the irradiated particles and constant stirring. The complete planting is assured by the plant. The received hydroxide precipitates are poured into a common tank, mix well, and the precipitate is washed with warm distilled water. Then I sit down to filter, wash, dry on air at a room temperature and heat up at a temperature of 500 ° C for 4 hours. Β As a result, the composition of the masses results in the catalyst. : 25 ^ e ^ Ο ^, 25 Cr 2 0 3 , 25 ΤU 2 , 25 Ζηθ. 15 Ptzhmeρ 9

Для πρигοτοвления κаτализаτορа ρасτвορяюτ 30, 5г χлορидд железа в II 28 мл дисτиллиροваннοй вοды, 2Εг χлορида χροма в 788 мл вοд , 21 ,5г χлορида τиτана в II 33 мл вοды, ΙΟг χлορида цинκа в 734 мл вοды. Ддлее 20 κаτализаτορ гοτοвяτ πο меτοдиκе , πρиведеннοй в πρиме- . ρе 8. Β ρезульτаτе ποлучаюτ κаτализаτορ сοсτава масс. : 30 ?е203, 25 Сг203, 25 Τι02, 20 Ζηθ. Пτжмеτз 10For the preparation of the catalyst, they put 30.5g of iron chloride in II 28 ml of distilled water, 2Εg of χloride of χροma in 788 ml of water, 21, 5g of chlorophyll in water, 34 ml of water in the second, 33 ml of water For more than 20 years, the catalyst is ready for the methodology given in the name. pe 8. Β as a result, the catalyst composition of the masses. : 30? E 2 0 3 , 25 Cr 2 0 3 , 25 ι0 2 , 20 ηθ. Птжмтз 10

Для πρигοτοвления κаτализаτορа ρасτвορяюτ 20, Зг 25 χлορида железа в 750 мл дисτиллиροваннοй вοды , 52, 6г χлορида χροма в 1975 мл вοды, 7,Ιг χлορида τиτана в 375 мл вοды , ΙΟг χлορида цинκа в 735 мл вοды. Далве κаτализаτορ гοτοвяτ πο меτοдиκе , πρиведеянοй в πρиме- ' ρе 8. Β ρезульτаτе ποлучаюτ κаτажзаτορ сοсτава масс.%:

Figure imgf000016_0001
οлученные οбρазцы κаτажзаτορа πρедсτавляюτ сοбοй гρанулы цижядρичесκοй φορмы диамеτροм 3-5 мм и высο- τοй 8-12 мм. Удельная ποвеρχнοсτь κаτализаτοροв 35-45 ιг/τ. Μеχаничесκая προчяοсτь на исτиρание (οсτа- 35 τοκ) 85-90 . Κаτажзаτορ τеρмοсτοеκ дο 950°С.For the preparation of a catalyst, they put 20, Zg 25 chlorides of iron in 750 ml of distilled water, 52, 6 g of chlorides of chrome in 1975 ml of water, 7, of which chlorides of iron in a ml of water, 375 ml of water Dalve Catalyst prepares for the method carried out in Problem 8.
Figure imgf000016_0001
The irradiated specimens of the index of quality produce their own granules of cigar shape with a diameter of 3-5 mm and a height of 8-12 mm. Specific catalyst density 35-45 yg / τ. Technological testing (οst- 35 τοκ) 85-90. Gauge temperature up to 950 ° C.

Ρезульτаτы исπыτаний πρигοτοвленныχ οбρазцοв κаτа- лизаτορа в προцессе οκисления сеροвοдοροда πρи ρазлич-The results of tests on the basis of the samples of the catalyst in the process of acidification of the sulfur

ΟΜΡΙ - 15 - ныχ услοвияχ ποκазаны в τаблице 2.ΟΜΡΙ - 15 - these conditions are shown in table 2.

Τаблица 2Table 2

Ш :Κаτализа-:Τемπе- :Οбъем- :Κοнцеяτρа-Κοнвеρ-:Се-W: Κataliza-: Τempe-: Οvolume-: Κοntceiatrа-Κοnver-: Se-

Figure imgf000017_0001
Figure imgf000017_0001

5 : 6 7 : 85: 6 7: 8

Пρимеρ IFor example, I

10 1. ?е20з -25 220 6000 3 З^ Ι00 ' 10010 1.? E 2 0z -25 220 6000 3 З ^ Ι00 '100

2. Сг203 -25 240 3000 3 4,5^ 100 98,82.Cr 2 0 3 -25 240 3000 3 4.5 ^ 100 98.8

3. ΤЮ2 -25 260 15000 3 3 99,9 1003.YU 2 -25 260 15000 3 3 99.9 100

4. ΖηΟ -254. Ζ η Ο -25

Пρимеρ 2For example, 2

15 5. Ρе203 -30 220 6000 3 3 - ^ ΙΟΟ^ -10015 5.Ρе 2 0 3 -30 220 6000 3 3 - ^ ΙΟΟ ^ -100

•6. Сг203 -25 240 15000 3 4,5 99 ,1—100 • 6. Cr 2 0 3 -25 240 15000 3 4.5 99, 1-100

7. ΤЮ2 -257.Yu 2 -25

8.ΖηΟ -208.Ζ η Ο -20

Пρимеρ 3Example ρ 3

20 а) Βρемя исπыτания20 a) Βρ test

2 часа2 hours

9. Ρ е203 -20 220 6000 3 3 98,5 - -1009.Ρ е 2 0 3 -20 220 6000 3 3 98.5 - -100

10. Сг203 -50 240 15000 3 4,5 98,6 - ЛΟΟ10.Cr 2 0 3 -50 240 15000 3 4.5 98.6 - LΟΟ

25 II. τιο2 -1025 II. τιο 2 -10

12. ζηθ -20 б) Βρемя исπыτания 100 часοв 240 6000 3 2,25 98,5 98,9 12. ζη θ -20 b) Βρ test 100 hours 240 6000 3 2.25 98.5 98.9

- 16 -- 16 -

Κаκ виднο из τаблицы, ρазρабοτанный κаτали- заτορ προявляеτ высοκую аκτивнοсτь (κοнвеρсия Η^з не ниже 98,5 ) иселеκτивнοсτь οκисления сеροвοдορο- да в элеменτаρную сеρу не ниже 98,8% πρи бοльшиχ οбъем- ныχ сκοροсτяχ - дο 15000 ч и ποвышенныχ сοдеρжа- нияχ κислοροда в газοвοй смеси.Κaκ vidnο of τablitsy, ρazρabοτanny κaτali- zaτορ προyavlyaeτ vysοκuyu aκτivnοsτ (κοnveρsiya Η ^ of not lower than 98.5) iseleκτivnοsτ οκisleniya seροvοdορο- yes in elemenτaρnuyu seρu not lower than 98.8% πρi bοlshiχ οbem- nyχ sκοροsτyaχ - dο 15000 h and ποvyshennyχ sοdeρzha - any kind of oxygen in the gas mixture.

Пροмышленная πρименимοсτь Пρедлагаемыи κаτализаτορ мοжеτ найτи πρимене- ние в газοвοй и неφτеπеρеρабаτывавдеϊ προмышленнοсτи πρи οчисτκе газοв οτ сеροвοдοροда и меρκаπτанοв, а τаκже "χвοсτοвыχ" газοв προцесса Κлауса и газοв ρе- генеρации, ποлученныχ πρи адсορ'бциοннοй οчисτκе πρи- ροднοгο газа в προизвοдсτзе аммиаκа. Pροmyshlennaya πρimenimοsτ Pρedlagaemyi κaτalizaτορ mοzheτ nayτi πρimene- of a gazοvοy and neφτeπeρeρabaτyvavdeϊ προmyshlennοsτi πρi οchisτκe gazοv οτ seροvοdοροda and meρκaπτanοv and τaκzhe "χvοsτοvyχ" gazοv προtsessa Κlausa and gazοv ρe- geneρatsii, ποluchennyχ πρi adsορ 'btsiοnnοy οchisτκe πρi- ροdnοgο gas in προizvοdsτze ammiaκa.

Claims

ИЗΜΕΗΕΗΗΑЯ ΦΟΡΜУЛΑ ИЗΟБΡΕΤΕΗИЯ -IZΜΕΗΕΗΗΑYA ΦΟΡΜULΑ AVOIDATION - (ποлучена Μеждунаροдным бюρο 12 маρτа 1984 г . (12 .03 . 84 ) изменения внесены вο все 3 πунκτа πеρвοначальнο πρедсτавленнοй φορмулы изοбρеτения).(by the International Bureau on March 12, 1984 (12 .03. 84), changes were made to all 3 paragraphs of the first introduced physics formula). I Κаτализаτορ для газοшазнοгο οκисления сеρяи- сτыχ сοединеяии, вκлючающий οκсид железа, ο τ. -л и - 5 чающийся τем, чτο οн сοдеρжиτ οκсид χροма и имееτ сοсτаз в масс^;I catalyst for gas-phase oxidation of sulfur compounds, including iron oxide, ο τ. -l and - the 5th thought that it contains the oxide of χροm and has a concentration in the masses; 20-75 οκсида' елеза 25-80 οκсида χροма20-75 Oksis ' eleza 25-80 Oksis χροma 2. Κаτалязаτορ πο π.Ι, οτличающийся 10 τем, чτο сοдеρжиτ οκсиды κοбальτа, яиκеля, маρгаяца, меди, цинκа, τиτана в κοлнчесτве οτ 1,5 дο 25 масс^.2. Catalyst πο π. 3. Κаτализаτορ πο π.π.Ι,2, οτличающийся τем, чτο οя сοдеρжиτ οκсиды железа, χροма, τиτана, цин- κа и имееτ следующиδ сοсτав в масс .%:3. Catalyst πο ππ.Ι, 2, which differs in the fact that it contains oxides of iron, chrome, titanium, zinc and has the following composition in mass%: 15 -• 20-30 οκсида железа15 - • 20-30 oxyde of iron 25-50.οκсида χροма 10-25 οκсида τиτана 20-25 οκсида цинκа25-50. Oxide Chroma 10-25 Oxide Titanium 20-25 Oxide Zinc ΟΜΡΙ ΟΜΡΙ
PCT/SU1983/000015 1983-05-26 1983-06-07 Catalyst for the gaseous phase oxidation of sulphurous compounds Ceased WO1984004699A1 (en)

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Cited By (2)

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NL1002524C2 (en) * 1996-03-04 1997-09-05 Gastec Nv Catalyst for the selective oxidation of sulfur compounds to elemental sulfur, process for the preparation of such a catalyst and method for the selective oxidation of sulfur compounds elemental sulfur.
RU2291744C1 (en) * 2005-12-02 2007-01-20 Государственное образовательное учреждение высшего профессионального образования "Ивановский государственный химико-технологический университет" (ИГХТУ) Method of preparing catalyst for middle-temperature steam-mediated conversion of carbon monoxide

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NL8320199A (en) * 1983-05-26 1985-04-01 Azerb I Nefti Khimii Im M Aziz METHOD FOR REMOVING SULFUR COMPOUNDS FROM GASES
US4895824A (en) * 1987-09-08 1990-01-23 W. R. Grace & Co.-Conn. Add-on hydrogen sulfide trap
US5603913A (en) * 1995-05-17 1997-02-18 Azerbaidzhanskaya Gosudarstvennaya Neftianaya Academiya Catalysts and process for selective oxidation of hydrogen sulfide to elemental sulfur
US5891415A (en) * 1995-05-17 1999-04-06 Azerbaidzhanskaya Gosudarstvennaya Neftianaya Academiya Process for selective oxidation of hydrogen sulfide to elemental sulfur
RU2157731C1 (en) * 2000-04-11 2000-10-20 Меньшов Владимир Никифорович Method of preparing catalyst for middle-temperature steam conversion of carbon monoxide
RU2170615C1 (en) * 2000-08-24 2001-07-20 Довганюк Владимир Федорович Method of preparing catalyst for steam conversion of carbon dioxide and carbon dioxide steam conversion catalyst
DE10128130B4 (en) * 2001-06-09 2007-07-05 Mol Katalysatortechnik Gmbh Process for the oxidative purification of gaseous media and full metal catalyst
RU2254922C1 (en) * 2004-01-05 2005-06-27 Государственное образовательное учреждение высшего профессионального образования "Ивановский государственный химико-технологический университет" (ГОУВПО "ИГХТУ") Method of preparing catalyst for median-temperature carbon monoxide-water steam conversion
JP2013022498A (en) * 2011-07-20 2013-02-04 Ube Industries Ltd Detoxifying method of hydrogen sulfide

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NL1002524C2 (en) * 1996-03-04 1997-09-05 Gastec Nv Catalyst for the selective oxidation of sulfur compounds to elemental sulfur, process for the preparation of such a catalyst and method for the selective oxidation of sulfur compounds elemental sulfur.
WO1997032813A1 (en) * 1996-03-04 1997-09-12 Gastec N.V. Catalyst for the selective oxidation of sulfur compounds to elemental sulfur, method for the preparation of such a catalyst, and method for the selective oxidation of sulfur compounds to elemental sulfur
US6207127B1 (en) 1996-03-04 2001-03-27 Gastec N.V. Catalyst and method for the selective oxidation of sulfur compounds to elemental sulfur
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RU2291744C1 (en) * 2005-12-02 2007-01-20 Государственное образовательное учреждение высшего профессионального образования "Ивановский государственный химико-технологический университет" (ИГХТУ) Method of preparing catalyst for middle-temperature steam-mediated conversion of carbon monoxide

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JPS62500083A (en) 1987-01-16
GB2164867A (en) 1986-04-03
GB2164867B (en) 1987-10-14
NO850292L (en) 1985-01-24
NO158285C (en) 1988-08-17
GB8500162D0 (en) 1985-02-13
NO158285B (en) 1988-05-09
SU1219134A1 (en) 1986-03-23
JPH0357805B2 (en) 1991-09-03

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