WO2001030691A1 - Procede pour faire bruler du gaz provenant du strippage d'eau corrosive - Google Patents

Procede pour faire bruler du gaz provenant du strippage d'eau corrosive Download PDF

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Publication number
WO2001030691A1
WO2001030691A1 PCT/EP2000/010575 EP0010575W WO0130691A1 WO 2001030691 A1 WO2001030691 A1 WO 2001030691A1 EP 0010575 W EP0010575 W EP 0010575W WO 0130691 A1 WO0130691 A1 WO 0130691A1
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WO
WIPO (PCT)
Prior art keywords
gas
oxygen
combustion
preheated
sour
Prior art date
Application number
PCT/EP2000/010575
Other languages
German (de)
English (en)
Inventor
Edwin Kniep
Rainer Kalthoff
Michael Bayertz
Christoph Sievering
Detlef Gorka
Original Assignee
Ruhr Oel Gmbh
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 Ruhr Oel Gmbh filed Critical Ruhr Oel Gmbh
Priority to AU12761/01A priority Critical patent/AU1276101A/en
Publication of WO2001030691A1 publication Critical patent/WO2001030691A1/fr

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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
    • C01B17/02—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
    • C01B17/0413—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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the invention relates to a method for the combustion of acid water stripping gas, the combustion taking place in a combustion chamber equipped with a burner with the supply of an oxygen-containing gas.
  • the invention further relates to an apparatus for performing the method.
  • Fossil fuels such as natural gas, coal, oil sands, oil shale and petroleum contain organic and inorganic sulfur compounds that are produced as gaseous, sulfur-containing products when processed. It is necessary to remove these sulfur compounds or to convert them into harmless sulfur compounds. Desulphurization takes place with the help of gaseous hydrogen (H 2 ). The organic sulfur compounds are converted into hydrogen sulfide. The gases containing hydrogen sulfide originating from such sources are separated from the hydrocarbons still present in a gas cleaning installation, a so-called "amine treater". The gas containing hydrogen sulfide (also called acid gas or Claus gas) coming from the amine scrubbers can contain up to 90% by volume of hydrogen sulfide.
  • amine treater gas containing hydrogen sulfide (also called acid gas or Claus gas) coming from the amine scrubbers can contain up to 90% by volume of hydrogen sulfide.
  • contaminated water which is referred to as "acid water” is another waste product of the oil refineries.
  • the “acidic water” contains, among other things, ammonia and hydrogen sulfide in dissolved form.
  • SWS gas sulfur dioxide
  • a process is used to remove the hydrogen sulfide, in which the hydrogen sulfide is converted into elemental sulfur.
  • the most frequently used direct conversion process is the Claus process, which was developed in 1883. This process relies on a dry one waited Claus procedure. This process is based on a dry oxidation process.
  • the various process variants developed are based on the same basic chemical reactions, using thermal and catalytic reactors.
  • the thermal reactor consists of a combustion chamber with a burner, a waste heat boiler.
  • the catalytic reaction part is carried out in two or three stages.
  • the individual stages each have a heater, a catalyst bed and a sulfur condenser.
  • reaction 2 The actual Claus reaction, in which elemental sulfur and water vapor are formed, is reaction 2.
  • the sulfur dioxide produced from the partial combustion of hydrogen sulfide reacts with the remaining hydrogen sulfide.
  • Elemental sulfur and water are also formed in the combustion chamber by thermal decomposition of hydrogen sulfide.
  • sour gas and SWS gas such as hydrogen, methane, higher hydrocarbons, ammonia, water vapor, carbon dioxide
  • gases which essentially only contain hydrogen sulfide a method is used in which a part of the amount of hydrogen sulfide is burned by the burner by means of combustion air to sulfur dioxide at a temperature of 900 to 1300 ° C. The remaining hydrogen sulfide is converted at temperatures between 180 ° C and 400 ° C in the catalytic reactors with the sulfur dioxide formed from the combustion to elemental sulfur and water.
  • the reaction is optimal when the hydrogen sulfide / sulfur dioxide ratio is 2: 1.
  • the elemental sulfur formed in the combustion chamber is separated in the waste heat boiler after the process gas has cooled.
  • the process gas is adjusted to the required reaction temperatures of the catalytic stages on the one hand by appropriate switching of the sulfur condenser or by upstream heaters.
  • the 5 sulfur formed by the Claus reaction is separated in sulfur condensers.
  • the feed gases contain different hydrogen sulfide concentrations
  • two main variants can be distinguished in the combustion process: the main flow operation for hydrogen sulfide concentrations greater than 50 vol.%
  • the secondary flow operation for hydrogen sulfide concentrations between 30 and 50 vol.% can be distinguished in the combustion process: the main flow operation for hydrogen sulfide concentrations greater than 50 vol.%
  • the secondary flow operation for hydrogen sulfide concentrations between 30 and 50 vol.% can be distinguished in the combustion process: the main flow operation for hydrogen sulfide concentrations greater than 50 vol.%
  • the secondary flow operation for hydrogen sulfide concentrations between 30 and 50 vol.%.
  • the gas flow is split in the secondary flow mode since the hydrogen sulfide gas has only a low calorific value.
  • Part of the hydrogen sulfide gas is burned with the combustion air in the combustion chamber and the sulfur dioxide gas that is produced is mixed with the remaining hydrogen sulfide gas and converted into elemental sulfur and water in the reactor.
  • the catalytic part is constructed analogously to the main current operation.
  • the bypass operation can no longer be used due to the low calorific value.
  • the bypass operation requires an ammonia-free feed gas, since otherwise the catalysts would be contaminated with ammonium salts.
  • the combustion air can be partially or completely replaced by oxygen.
  • oxygen By using oxygen, the proportion of inert gas is reduced or eliminated entirely.
  • the throughput of acid water stripping gas and Claus gas can be increased.
  • low-hydrogen sulfide feed gases with a low calorific value and high ammonia content can also be processed in a mainstream reactor.
  • BESTATIGUNGSKOPIE DE 197 18 261 A1 describes how the throughput and the degree of conversion of hydrogen sulfide to elemental sulfur can be improved.
  • oxygen or oxygen-containing gas is blown into the combustion chamber at high speed, as a result of which the mixture between the oxygen, the combustion air and the hydrogen sulfide-containing process gas is increased due to the high turbulence.
  • oxygen is not only used as an oxidizing agent, but also to increase the mixing energy. By increasing the mixing energy, the combustion density and thus the throughput of hydrogen sulfide can be increased.
  • a typical incinerator is the Lurgi oxygen Claus burner.
  • the Claus gas and the ammonia-containing acid water stripping gas are processed in this burner via separate burner muffles.
  • the sour water stripper gas is burned with air in a central burner muffle.
  • the Claus gas is burned with oxygen and air as the oxidation medium with several double-concentric individual burners, which are arranged around the burner muffle.
  • a single burner consists of a central oxygen nozzle, a concentric Claus gas nozzle and a double-concentric air nozzle. This arrangement creates individual oxygen / hydrogen sulfide flames, which are enveloped by colder air / hydrogen sulfide flames. This allows the temperature in the combustion chamber to be controlled.
  • the sour gas / SWS gas ratio must be at least 3: 1 in order to ensure adequate cooling of the separate SWS gas burner muffle with the amount of air required to convert the sour gas. This results in a disadvantageous limitation of the capacity for processing SWS gas in the Claus plants. Another disadvantage of processes with additional O 2 addition is the high cost of oxygen, as well as the then higher minimum load of the Clausaniage compared to pure air operation.
  • the technical object of the invention was therefore to increase the throughput in the combustion of SWS gas without increasing the minimum load of the Claus plant.
  • the technical problem is solved by a method for the combustion of acid water stripping gas, the combustion taking place in a combustion chamber equipped with at least one burner with the supply of an oxygen-containing gas, and wherein at least one of the gas flows and / or partial gas flows and / or gas flows of gas mixtures of two or more gases are preheated before combustion.
  • a burner in the sense of the invention can be understood to mean a single nozzle, a burner with two or more nozzles, an arrangement of burners, a burner ring and variations thereof.
  • the acid water stripping gas is burned in a mixture with acid gas.
  • the sour gas is also preheated.
  • the ammonia with the oxygen-containing gas is completely burned to nitrogen and water.
  • the hydrogen sulfide gas is reacted as follows. Part of the hydrogen sulfide reacts with the gas containing oxygen to form sulfur dioxide. The remaining hydrogen sulfide is reacted with the sulfur dioxide formed in a molecular ratio of 2: 1 to form elemental sulfur and water.
  • the sour gas / SWS gas ratio can therefore now also be less than 3: 1. This increases the working window for sour water stripper gas processing. Another advantage results from the fact that preheating the feed gases is less expensive than feeding in O 2 to increase the combustion chamber temperature.
  • the combustion takes place at a temperature above 1300 ° C., particularly preferably at 1,350 to 1,500 ° C.
  • the implementation Combustion in this temperature range ensures the complete decomposition of ammonia, whereby lower temperatures require longer dwell times.
  • the temperature of the preheated gas or the preheated gas mixture is at least 200 ° C.
  • the combustion temperature can be increased to the required values. Precise control of the combustion temperature can be achieved through the specific preheating of the individual gas flows.
  • air, oxygen-enriched air or pure oxygen is used as the oxygen-containing gas.
  • oxygen-containing gas air, oxygen-enriched air or pure oxygen is used as the oxygen-containing gas.
  • the combustion process can be additionally controlled via the concentration of oxygen in the oxygen-containing gas.
  • the combustion chamber temperature can be increased by adding an oxygen-containing gas if necessary above the temperature values achieved by preheating.
  • part of the sour water stripping gas is not preheated and burned with preheated air in a central burner muffle.
  • the remaining part of the sour water stripper gas is mixed with the sour gas and preheated to over 200 ° C, whereby this preheated sour gas / sour water stripper gas mixture is fed into the individual burners arranged concentrically around the central burner muffle and burned together with air, whereby these are fed to the individual burners Air is also preheated to over 200 ° C.
  • non-preheated oxygen gas can be fed into the individual burners.
  • the preheating is carried out using means selected from the group consisting of high-pressure steam, electric heaters, in-line burners and heat exchangers.
  • the technical problem is solved by means of a device for carrying out the method, the device containing at least one burner and / or a burner muffle, means for heating the gases being provided on at least one of the gas feed lines.
  • additional individual burners are arranged around the central burner muffle, which contain at least one nozzle for oxygen-containing gas and at least one nozzle for acid gas or an acid gas / acid water stripping gas mixture.
  • This device also contains means for heating the gases on at least one of the gas feed lines.
  • means for heating the gases are provided on all gas supply lines.
  • the means for heating the gases are high-pressure steam heating means, electric heaters, in-line burners or heat exchangers.
  • the combustion temperature during the combustion of the ammonia-containing SWS gas can be increased to above 1300 ° C, preferably to 1350 to 1500 ° C, by preheating the supplied gases to over 200 ° C, for example by means of high pressure steam ,
  • the high combustion temperatures when using this preheating have a positive effect on the thermal cracking and complete combustion of ammonia.
  • the method described above for the combustion of acid water stripping gas can be carried out, the thermal decomposition of ammonia with oxygen already taking place completely with the stoichiometric addition of air to the SWS gas.
  • the means for heating the feed gases enable the combustion chamber temperature to be increased for the complete thermal decomposition of ammonia. Due to the reduction in the amount of air required, an increase in the processing capacity of acid water stripping gas is achieved with the device according to the invention.
  • the sour gas / SWS gas ratio in the combustion carried out in the device is no longer dependent on the amount of sour gas due to the preheating of the feed gases.
  • Part of the SWS gas is burned with air in a central burner muffle.
  • This air flow which is fed to the central burner muffle, is a mixture of preheated air and non-preheated air.
  • the remaining part of the SWS gas is mixed with the sour gas and preheated to approx. 290 ° C.
  • This preheated sour gas / SWS gas mixture is fed into the individual burners arranged concentrically around the central burner muffle and burned together with air, which is preheated to 285 ° C and also fed to the individual burners.
  • non-preheated oxygen gas can also be supplied to the individual burners.
  • Table 1 lists the parameters of seven different modes of operation of the sour gas / SWS gas combustion method according to the invention.
  • the sour gas / SWS gas mixture is preheated to 290 ° C and the air destined for the individual burners to 285 ° C.
  • Columns A and B indicate which sour gas or SWS gas quantities are burned in total.
  • Column C shows the amounts of the gas stream that carry a sour gas / SWS gas mixture. This mixture is preheated to 290 ° C.
  • Column D shows the ammonia content of the sour gas / SWS gas mixture.
  • Column E shows the amounts of the non-preheated SWS gas component that is burned separately from the sour gas in the central burner muffle.
  • Column F shows the quantities of combustion air used. In some variants, pure oxygen is also added

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Treating Waste Gases (AREA)
  • Incineration Of Waste (AREA)

Abstract

L'invention concerne un procédé pour faire brûler du gaz provenant du strippage d'eau corrosive, la combustion s'effectuant dans une chambre de combustion équipée d'au moins un brûleur, avec apport d'un gaz contenant de l'oxygène. Au moins un des flux gazeux et/ou des flux gazeux partiels et/ou des flux gazeux de mélanges contenant au moins deux gaz est préchauffé avant la combustion. L'invention concerne en outre un dispositif pour mettre en oeuvre ledit procédé, comportant au moins un brûleur et/ou un moufle de brûleur, des moyens pour chauffer les gaz étant placés au niveau d'au moins une des conduites d'amenée de gaz.
PCT/EP2000/010575 1999-10-28 2000-10-27 Procede pour faire bruler du gaz provenant du strippage d'eau corrosive WO2001030691A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU12761/01A AU1276101A (en) 1999-10-28 2000-10-27 Method for incinerating sour water stripper gas

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19951909A DE19951909C2 (de) 1999-10-28 1999-10-28 Verfahren zur Verbrennung von Sauerwasserstrippergas
DE19951909.9 1999-10-28

Publications (1)

Publication Number Publication Date
WO2001030691A1 true WO2001030691A1 (fr) 2001-05-03

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ID=7927150

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2000/010575 WO2001030691A1 (fr) 1999-10-28 2000-10-27 Procede pour faire bruler du gaz provenant du strippage d'eau corrosive

Country Status (3)

Country Link
AU (1) AU1276101A (fr)
DE (1) DE19951909C2 (fr)
WO (1) WO2001030691A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004024622A1 (fr) * 2002-09-12 2004-03-25 Amer Sarssam Procede pour recuperer du soufre dans des flux gazeux contenant du sulfure d'hydrogene
US20220194794A1 (en) * 2020-12-18 2022-06-23 Uop Llc Process for managing hydrogen sulfide in a refinery

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3860697A (en) * 1973-04-23 1975-01-14 Amoco Prod Co Method for recovery of elemental sulfur from low hydrogen sulfide sulfur plant feed gas
US4075310A (en) * 1975-03-08 1978-02-21 Metallgesellschaft Aktiengesellschaft Production of sulfur by the Claus process
GB2114106A (en) * 1982-02-02 1983-08-17 Shell Int Research Process for the production of elemental sulphur
WO1989012023A1 (fr) * 1988-06-08 1989-12-14 American Combustion, Inc. Procede et appareil de recuperation de soufre a partir de gaz contenant du sulfure d'hydrogene
US4988287A (en) * 1989-06-20 1991-01-29 Phillips Petroleum Company Combustion apparatus and method
US5508013A (en) * 1991-04-25 1996-04-16 Elf Aquitaine Production Process for the production of sulphur from at least one sour gas containing hydrogen sulphide and a fuel effluent and thermal reactor

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3842599A1 (de) * 1988-12-17 1990-06-21 Linde Ag Verfahren zur behandlung eines sauergase enthaltenden abwassers
DE19718261A1 (de) * 1997-04-30 1998-11-05 Messer Griesheim Gmbh Verfahren und Vorrichtung zur Umwandlung von Schwefelwasserstoff in elementaren Schwefel

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3860697A (en) * 1973-04-23 1975-01-14 Amoco Prod Co Method for recovery of elemental sulfur from low hydrogen sulfide sulfur plant feed gas
US4075310A (en) * 1975-03-08 1978-02-21 Metallgesellschaft Aktiengesellschaft Production of sulfur by the Claus process
GB2114106A (en) * 1982-02-02 1983-08-17 Shell Int Research Process for the production of elemental sulphur
WO1989012023A1 (fr) * 1988-06-08 1989-12-14 American Combustion, Inc. Procede et appareil de recuperation de soufre a partir de gaz contenant du sulfure d'hydrogene
US4988287A (en) * 1989-06-20 1991-01-29 Phillips Petroleum Company Combustion apparatus and method
US5508013A (en) * 1991-04-25 1996-04-16 Elf Aquitaine Production Process for the production of sulphur from at least one sour gas containing hydrogen sulphide and a fuel effluent and thermal reactor

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004024622A1 (fr) * 2002-09-12 2004-03-25 Amer Sarssam Procede pour recuperer du soufre dans des flux gazeux contenant du sulfure d'hydrogene
US20220194794A1 (en) * 2020-12-18 2022-06-23 Uop Llc Process for managing hydrogen sulfide in a refinery
US11708267B2 (en) * 2020-12-18 2023-07-25 Uop Llc Process for managing hydrogen sulfide in a refinery

Also Published As

Publication number Publication date
AU1276101A (en) 2001-05-08
DE19951909A1 (de) 2001-05-23
DE19951909C2 (de) 2002-01-24

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