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WO1981003166A1 - Procede d'obtention d'anhydride sulfurique - Google Patents

Procede d'obtention d'anhydride sulfurique Download PDF

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Publication number
WO1981003166A1
WO1981003166A1 PCT/SU1980/000071 SU8000071W WO8103166A1 WO 1981003166 A1 WO1981003166 A1 WO 1981003166A1 SU 8000071 W SU8000071 W SU 8000071W WO 8103166 A1 WO8103166 A1 WO 8103166A1
Authority
WO
WIPO (PCT)
Prior art keywords
mixture
minutes
temperature
sulfur dioxide
reactive mixture
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/SU1980/000071
Other languages
English (en)
Russian (ru)
Inventor
V Lakhmostov
Y Matros
A Ivanov
G Boreskov
V Volkov
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.)
Boreskov Institute of Catalysis Siberian Branch of Russian Academy of Sciences
Original Assignee
Boreskov Institute of Catalysis Siberian Branch of Russian Academy of Sciences
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Boreskov Institute of Catalysis Siberian Branch of Russian Academy of Sciences filed Critical Boreskov Institute of Catalysis Siberian Branch of Russian Academy of Sciences
Priority to DE19803050368 priority Critical patent/DE3050368C2/de
Priority to PCT/SU1980/000071 priority patent/WO1981003166A1/fr
Priority to GB8138825A priority patent/GB2085421B/en
Priority to JP55501134A priority patent/JPS6018604B2/ja
Publication of WO1981003166A1 publication Critical patent/WO1981003166A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • C01B17/69—Sulfur trioxide; Sulfuric acid
    • C01B17/74—Preparation
    • C01B17/76—Preparation by contact processes
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • 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
    • C01B17/69—Sulfur trioxide; Sulfuric acid
    • C01B17/74—Preparation
    • C01B17/76—Preparation by contact processes
    • C01B17/80—Apparatus

Definitions

  • the source gas is supplied to the contact unit with a temperature of 20 -00 ° ⁇ and heated in the case of a gas exchange in the process
  • the most intense oxidation occurs in the first place, at a slower rate of conversion, it reaches 0.7–0.8 and the gas leaves the unit with a temperature of 600 ° C.
  • the computer operating mode of the appliance at all stages of the catalytic converter helps to keep it constant.
  • the aforementioned methods oxidize gases with a sulfur dioxide content of 7, 5-12. , is only obtained by burning an element of the furnace, or by burning off the waste ("The source of the acid" is published on March 27, 2007).
  • the implementation of such devices will require a sophisticated and efficient implementation of portable devices. Existing methods also make it possible to receive a series of waste from the environment.
  • the inactive process reacts with a mixture of gas at the entrance to the contact unit and at the entrance to the reaction zone, including the non-interrupted;
  • the reaction mixture gases containing both dioxide and sulfur, located in the region of the beginning and end of the chemical reaction;
  • the best practice of the invention is that of the following.
  • the catalyst is supplied with an initial reactive mixture with a sulfur dioxide content of 1, 0, or 10%. with a temperature of 20 ° ⁇ .
  • the mixture will be heated and, having reached the temperature of the beginning of the reaction 350 ° ⁇ , the reaction of oxidation will begin.
  • the catalyticism of the input of the original reactive mixture is slow, giving rise to the temperature of the mixture, which is very long.
  • ⁇ As a result of the mechanism of heat transfer, the length of the catalytic converter is affected by the moving process (the area of the vehicle is by parameters.
  • P ⁇ edlagaemy s ⁇ s ⁇ b ⁇ susches ⁇ vleniya ⁇ tsessa is ⁇ lyu- chae ⁇ us ⁇ an ⁇ v ⁇ u ⁇ e ⁇ l ⁇ bmenni ⁇ v or d ⁇ lni ⁇ elny ⁇ ⁇ chni ⁇ v ⁇ e ⁇ la used for ⁇ d ⁇ g ⁇ eva is ⁇ dn ⁇ i ⁇ ea ⁇ tsi ⁇ nn ⁇ y sme- si ⁇ a ⁇ ⁇ a ⁇ itself sl ⁇ y ⁇ a ⁇ aliza ⁇ a vy ⁇ lnyae ⁇ ⁇ l ⁇ ege- ne ⁇ a ⁇ ivny ⁇ ⁇ e ⁇ l ⁇ bmenni ⁇ v, ⁇ e ⁇ emenn ⁇ nag ⁇ evaya is ⁇ d- hydrochloric ⁇ ea ⁇ tsi ⁇ nnuyu ⁇ lazhdaya ⁇ eagi ⁇ vavshuyu mixture and blend.
  • the sulfur dioxide is set to a temperature that is similar to that which is in a dry condition and that the solution is in a low temperature condition.
  • We offer a second version of the process flow which may be a little faster if the temperature is mixed at a temperature of 200 ° C. If, at the entrance to the catalytic converter, the original ⁇ ⁇ active mixture with a high temperature is lost, for example. 420 ° C, that is, in the initial part of the catalytic converter, the temperature is converted, and, in the case of heat, it is absorbed. Lowering the temperature of the initial mixture to the minimum values, at best 20 ° C, cools the catalytic converter, which is suitable for the place of entry.
  • the next step is to move to a warm place, where there is a simple turnaround.
  • valves 2 are open and the valves 3 are closed.
  • the initial reaction mixture is heated until the reaction starts at 390 ° C.
  • Figure 2 shows the oxidation scheme that occurs when the temperature of the mixture is changed from 20-200 ° C to 390-600 ° C for 1 . 0-200 minutes.
  • the delivery of the original reactive mixture in the catalytic bed is carried out in the same direction.
  • valves 1, 3 and 5 are short-circuited, and the valves 2, 4 and 6 are short-circuited.
  • a reactive mixture with a temperature of 500 ° C is transferred to the unheated part of the ⁇ ⁇ layer.
  • ⁇ e ⁇ i ⁇ d v ⁇ emeni ⁇ e ⁇ l ⁇ vye ⁇ n ⁇ y zashyau ⁇ ⁇ l ⁇ zhenie minutes and $ 2 g ( ⁇ ig.Zb) ⁇ sle cheg ⁇ zadvizh ⁇ i za ⁇ yvayu ⁇ 2 and 3, and zadvizh ⁇ u I -..
  • the original reactive) mixture is formed by burning the sulfur and consisting of 10.5% of the total. sulfur dioxide, 10.5% by volume. Acid and 79% ob. nitrogen, it is supplied to the portable device with the addi- tional adiabatic layer of the catalyst (Fig. ⁇ ). Uses a catalytic system.
  • Composition (wt.%): V 2, 0 ⁇ 6-9 ⁇ ⁇ ⁇ ⁇ -16
  • the original reactive mixture which is processed and burned down, is recycled and consists of 7.5% of the total. two- -9- ssery, 10.5% oob. Acid and 82% oob. nitrogen, it is delivered to the compact device with a single adiabatic layer of the catalytic converter (Fig. ⁇ ). It uses catalysis with the same kind of system, just like in case of I.
  • the unit has an initial reactive mixture of ⁇ 50 ° ⁇ , the standard contact time is 5 sec. Before starting the initial reactive mixture, the layer is discharged to a temperature of 550 ° ⁇ .
  • the flow rate of the reaction mixture changes after 55 minutes, the duration of the single cycle is 110 minutes.
  • the average degree of conversion of sulfur dioxide to sulfur dioxide is 98.5. Examples 3
  • the original reactive mixture which is produced by burning the sulfur and consisting of 12% of the total. sulfur dioxide, 11% ob. Acid and 78% by volume. nitrogen, it is supplied to the compact device with the addi- tional adiabatic layer of the catalyst (fig. ⁇ ). They use the same system, as in the case of I.
  • the unit of the original reactive mixture is 20 ° ⁇ , the condition of contact is 6 sec. Before starting the initial reaction mixture with a catalyst layer, it is heated to 500 ° C. After 30 minutes, they change the direction of movement of the reactive mixture to an efficient, continuous cycle - 60 buses.
  • the average degree of conversion of sulfur dioxide to sulfur dioxide is 98.1%.
  • Example 4 is analogous to Example I, which is different from the fact that the condition of the contact is equal to 7 sec. and the durability of one cycle is 200 minutes. Average Cycle Degree of Consumption
  • Example 6 is analogous to Example I, which is different from the fact that the original reactive mixture, consisting of 0.6% of the two-part sulfuric acid, 5% of the total. Acid and 94.4% of total Nitrogen, is supplied to the compact unit with the on-line catalytic converter. -10- cycle 60 minutes, averaging over the cycle the degree of rotation of 99, 3 / b.
  • the original reaction mixture and the catalyst are the same as in I.
  • the thin catalyst is divided into two equal parts, the operating principle of the 2 process. In this case, there is a change in the process solution of the reactive mixture before the catalytic converter and its parts, and I (Fig. 2).
  • the total amount of catalytic converter in both parts meets the condition of contact time of 8 sec.
  • Part of the product is pre-heated to 500 ° ⁇ .
  • nachinayu ⁇ s ⁇ v ⁇ emeni ⁇ gda ⁇ e ⁇ l ⁇ v ⁇ y ⁇ n ⁇ ( ⁇ ⁇ zanimae ⁇ ⁇ l ⁇ zhenie in se ⁇ edine sl ⁇ ya ⁇ - * - and used ⁇ dnuyu ⁇ ea ⁇ tsi ⁇ nnuyu mixture ⁇ eshe ⁇ a ⁇ u ⁇ y 20 ° C in ⁇ dayu ⁇ na ⁇ avlenii, ⁇ azann ⁇ m s ⁇ l ⁇ shnymi s ⁇ ezhash ( ⁇ ig.2) ⁇ e ⁇ l ⁇ v ⁇ y.
  • Example 7 It is similar to Example 7, it is distinguished that the original reactive mixture, consisting of 0.6% by weight sulfur dioxide, is 15%. Acid and 84% by weight of nitrogen, are subsequently supplied in part with a layer of ⁇ réelle and ⁇ (Fig. 2) with a temperature of 200 ° ⁇ . Duration of the cycle is 75 minutes. The cycle to cycle at the inlet of the mixture, in part, and the temperature of the mixture changes smoothly from 200 ° C to 600 ° C and decreases to 200 ° C. The average degree of rotation is 99.4 for the cycle. Press) 10
  • Example II It is similar to Example II, it is distinguished by the fact that the original reactive mixture is supplied with a temperature of 200 ° ⁇ for catalyst. Run a cycle of 150 minutes. The average degree of conversion is 98.2. Fri 13
  • Example II It is similar to Example II, it is distinguished by the fact that the original reactive mixture is 1.5% by volume. dioxides of the sera, 15 ob. Acid and 83.5% ed. nitrogen reprocess ⁇ -13- Duration of one cycle 130 minutes. The average degree of conversion is 99.3%. Note) A 14% reactive mixture, which is produced by burning the sulfur and consisting of 15% of the total. sulfur dioxide, 11% ob. Acid and 74% ob.
  • the catalyst mixture Before starting the feed, the catalyst mixture is discharged to a temperature of 500 ° ⁇ .
  • the average degree of conversion of sulfur dioxide into the sulfur dioxide after the first stage is 94% with a cycle length of 110 cords. A good degree of conversion is relatively low and further oxidation of the remaining sulfur dioxide is required.
  • the resulting reacted mixture is directed to the first stage of absorption, after a direct reacted mixture having 0.75% by weight. sulfur dioxide, 3.6 vol. .. Oxygen and other nitrogen, with a temperature of 60 ° C and a conditional period of contact of 5 sec. .
  • the proposed invention may be used in the manufacture of sulfuric acid.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Catalysts (AREA)
  • Heterocyclic Carbon Compounds Containing A Hetero Ring Having Nitrogen And Oxygen As The Only Ring Hetero Atoms (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

Procede d'obtention d'anhydride sulfurique consistant a oxyder l'anhydride sulfureux dans une couche fixe d'un catalyseur soit en inversant periodiquement, apres toutes les 10-200 minutes, le sens d'ecoulement de la masse de reaction contenant l'anhydride sulfureux au travers de la couche de catalyseur, soit en changeant la temperature de cette masse de reaction, amenee sur la couche de catalyseur, de 20-200 C jusqu'a 350-600 C pendant 10-200 minutes.
PCT/SU1980/000071 1980-05-05 1980-05-05 Procede d'obtention d'anhydride sulfurique Ceased WO1981003166A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
DE19803050368 DE3050368C2 (de) 1980-05-05 1980-05-05 Verfahren zur Herstellung von Schwefeltrioxid
PCT/SU1980/000071 WO1981003166A1 (fr) 1980-05-05 1980-05-05 Procede d'obtention d'anhydride sulfurique
GB8138825A GB2085421B (en) 1980-05-05 1980-05-05 Method of obtaining sulphur trioxide
JP55501134A JPS6018604B2 (ja) 1980-05-05 1980-05-05 三酸化硫黄の製造方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
PCT/SU1980/000071 WO1981003166A1 (fr) 1980-05-05 1980-05-05 Procede d'obtention d'anhydride sulfurique
WOSU80/00071 1980-05-05

Publications (1)

Publication Number Publication Date
WO1981003166A1 true WO1981003166A1 (fr) 1981-11-12

Family

ID=21616606

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/SU1980/000071 Ceased WO1981003166A1 (fr) 1980-05-05 1980-05-05 Procede d'obtention d'anhydride sulfurique

Country Status (4)

Country Link
JP (1) JPS6018604B2 (fr)
DE (1) DE3050368C2 (fr)
GB (1) GB2085421B (fr)
WO (1) WO1981003166A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2213045C1 (ru) * 2002-02-20 2003-09-27 Институт катализа им. Г.К.Борескова СО РАН Способ окисления диоксида серы
RU2277066C1 (ru) * 2005-02-01 2006-05-27 Государственное образовательное учреждение высшего профессионального образования Новгородский государственный университет имени Ярослава Мудрого Способ получения серной кислоты из дымовых газов
RU2351536C2 (ru) * 2004-04-27 2009-04-10 Альбермарл Корпорейшн Способ параллельного окисления диоксида серы и его применение в производстве тетрабромфталевого ангидрида

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BG61107B1 (bg) * 1994-08-29 1996-11-29 Институт По Инженерна Химия При Бан Метод за получаване на серен триокис
DE4443774A1 (de) 1994-12-08 1996-06-13 Basf Ag Vorrichtung und Verfahren zur Durchführung exothermer Reaktionen
RU2131397C1 (ru) * 1997-12-04 1999-06-10 Открытое акционерное общество "НИУИФ" Способ получения триоксида серы
USD843075S1 (en) * 2018-04-24 2019-03-12 Lilly Brush Company, Llc Handheld detailer
USD917891S1 (en) 2019-07-26 2021-05-04 Lilly Brush Co., LLC Detailing tool
US11517171B2 (en) 2019-07-26 2022-12-06 Lilly Brush Co., LLC Detailing tool

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU301985A1 (ru) * 1964-04-13 1975-05-15 Институт Катализа Сибирского Отделения Ан Ссср Способ получени трехокиси серы путем окислени двуокиси серы

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU301985A1 (ru) * 1964-04-13 1975-05-15 Институт Катализа Сибирского Отделения Ан Ссср Способ получени трехокиси серы путем окислени двуокиси серы

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
"Spravochnik sernokislotchika", pod red. K.M. Malina, published in 1971, "Khimiya", (Moscow), pages 559-570 *

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2213045C1 (ru) * 2002-02-20 2003-09-27 Институт катализа им. Г.К.Борескова СО РАН Способ окисления диоксида серы
RU2351536C2 (ru) * 2004-04-27 2009-04-10 Альбермарл Корпорейшн Способ параллельного окисления диоксида серы и его применение в производстве тетрабромфталевого ангидрида
RU2277066C1 (ru) * 2005-02-01 2006-05-27 Государственное образовательное учреждение высшего профессионального образования Новгородский государственный университет имени Ярослава Мудрого Способ получения серной кислоты из дымовых газов

Also Published As

Publication number Publication date
GB2085421A (en) 1982-04-28
JPS6018604B2 (ja) 1985-05-11
GB2085421B (en) 1984-03-07
DE3050368C2 (de) 1988-04-14
DE3050368T1 (de) 1980-05-05
JPS57500606A (fr) 1982-04-08

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