EA022146B1 - Process for producing power from a sour gas - Google Patents

Process for producing power from a sour gas Download PDF

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Publication number
EA022146B1
EA022146B1 EA201201472A EA201201472A EA022146B1 EA 022146 B1 EA022146 B1 EA 022146B1 EA 201201472 A EA201201472 A EA 201201472A EA 201201472 A EA201201472 A EA 201201472A EA 022146 B1 EA022146 B1 EA 022146B1
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EA
Eurasian Patent Office
Prior art keywords
gas
sulfuric acid
stage
stream
steam
Prior art date
Application number
EA201201472A
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Russian (ru)
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EA201201472A1 (en
Inventor
Дьего Патрисио Валенсуэла
Рензе Вейнтье
Original Assignee
Шелл Интернэшнл Рисерч Маатсхаппий Б.В.
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Priority to EP10161374 priority Critical
Application filed by Шелл Интернэшнл Рисерч Маатсхаппий Б.В. filed Critical Шелл Интернэшнл Рисерч Маатсхаппий Б.В.
Priority to PCT/EP2011/056261 priority patent/WO2011134847A2/en
Publication of EA201201472A1 publication Critical patent/EA201201472A1/en
Publication of EA022146B1 publication Critical patent/EA022146B1/en

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Classifications

    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01KSTEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K23/00Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
    • F01K23/064Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle in combination with an industrial process, e.g. chemical, metallurgical
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/48Sulfur dioxide; Sulfurous acid
    • C01B17/50Preparation of sulfur dioxide
    • C01B17/508Preparation of sulfur dioxide by oxidation of sulfur compounds
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/69Sulfur trioxide; Sulfuric acid
    • C01B17/74Preparation
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/69Sulfur trioxide; Sulfuric acid
    • C01B17/74Preparation
    • C01B17/76Preparation by contact processes
    • C01B17/765Multi-stage SO3-conversion
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/69Sulfur trioxide; Sulfuric acid
    • C01B17/74Preparation
    • C01B17/76Preparation by contact processes
    • C01B17/78Preparation by contact processes characterised by the catalyst used
    • C01B17/79Preparation by contact processes characterised by the catalyst used containing vanadium
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01KSTEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K3/00Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
    • F01K3/18Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters
    • F01K3/24Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters with heating by separately-fired heaters
    • F01K3/247Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters with heating by separately-fired heaters one heater being an incinerator
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22STEAM GENERATION
    • F22BMETHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00Methods of steam generation characterised by form of heating method
    • F22B1/02Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/18Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
    • F22B1/1807Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines using the exhaust gases of combustion engines
    • F22B1/1815Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines using the exhaust gases of combustion engines using the exhaust gases of gas-turbines
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2257/00Components to be removed
    • B01D2257/30Sulfur compounds
    • B01D2257/304Hydrogen sulfide
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456Removing acid components
    • B01D53/1468Removing hydrogen sulfide
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00Combustion technologies with mitigation potential
    • Y02E20/12Heat utilisation in combustion or incineration of waste
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00Combustion technologies with mitigation potential
    • Y02E20/16Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/10Process efficiency
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/10Process efficiency
    • Y02P20/129Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Abstract

A process for producing power from a sour gas comprising HS, the process comprising the steps of: (a) providing a sour gas stream comprising natural gas and HS to an acid gas removal unit, resulting in a cleaned natural gas and a acid gas comprising HS; (b) combusting the cleaned natural gas stream with an oxygen containing gas in a gas turbine to produce power and a hot flue gas; (c) sending the hot flue gas to a first heat recovery steam generator to generate steam and a clean flue gas; (d) combusting at least part of the HS in the acid gas comprising HS in the presence of an oxygen containing gas to obtain a hot gas effluent comprising SO; (e) sending the hot gas effluent comprising SOto a second heat recovery steam generator to generate steam and a cooled gas effluent comprising SO; (f) leading the cooled gas effluent comprising SOto a sulfuric acid unit to produce sulfuric acid, steam and a cleaned flue gas stream.

Description

The invention relates to a method for producing energy from sour gas containing H 2 3, in particular a gas stream containing hydrogen sulfide, obtained from natural gas. The method is particularly useful in combination with the installation of receiving sulfuric acid.

Sour gas containing H 2 3 can be obtained from various sources. For example, numerous natural gas wells produce high-sulfur natural gas, i.e. natural gas containing H 2 3 and optionally other pollutants. Natural gas is a generic term applied to a mixture of light hydrocarbons and optionally other gases (nitrogen, carbon dioxide, helium) obtained from natural gas wells. The main component of natural gas is methane. In addition, other hydrocarbons are often present, such as ethane, propane, butane or higher hydrocarbons.

It is desirable to reduce the amount of hydrogen sulfide in sour gas for a number of reasons. Sulfur-containing compounds, such as hydrogen sulfide and sulfur oxides, are regulated by emission standards in many countries. In addition, hydrogen sulphide, in particular, can cause equipment erosion.

The Claus process is often used to process the hydrogen sulfide recovered from various gas streams, such as hydrocarbon streams, such as natural gas. The multistage process produces sulfur from hydrogen sulfide gas.

The Claus process involves two stages: the first stage of thermal transformation and the second stage of catalytic transformation. In the first thermal stage, part of the hydrogen sulfide in the gas is oxidized at temperatures above 850 ° C to produce sulfur dioxide and water

2 3 + ЗО 2 -> 28О 2 + 2Н 2 О (I)

In the second catalytic stage, sulfur dioxide obtained in the thermal stage reacts with hydrogen sulfide to produce sulfur and water.

8O 2 -g 4H 2 8 -> 68 + 4H 2 O (II)

The gaseous elemental sulfur obtained in stage (II) can be extracted in the refrigerator first as liquid sulfur before further cooling to obtain solid elemental sulfur. In some cases, the second catalytic stage and the stage of sulfur condensation can be repeated several times, usually up to three times, to improve the recovery of elemental sulfur.

In the second catalytic stage of the Claus process, sulfur dioxide is required, one of the products of reaction (I). However, hydrogen sulfide is also required. Usually about one-third of the hydrogen sulfide gas is oxidized to sulfur dioxide in reaction (I) to obtain the desired molar ratio of 1: 2 sulfur dioxide to hydrogen sulfide for the reaction to produce sulfur in the catalytic stage (reaction (II)). The residual off-gases of the Claus process may contain combustible components and sulfur-containing compounds, for example, when there is an excess or lack of oxygen (and the resulting overproduction or underproduction of sulfur dioxide). Such combustible components can be further processed accordingly in a Claus process off-gas treatment installation, for example in a Zäe 11 Claus off-gas treatment facility.

The overall reaction in the Claus process can thus be written as 2H 2 8 + O 2 23 + 2H 2 O (III)

Since conventional Claus process installations are costly, both in terms of capital costs and also in terms of operating costs, alternative processes have been proposed.

The aim of the invention is to create a method for more efficient production of electricity from high-sulfur gas containing hydrogen sulfide.

Another object of the invention is a process in which the generation of energy from sour gas is combined with the production of sulfuric acid.

To this end, the invention provides a method for producing energy from sour gas containing H 2 8, a method comprising the steps of: (a) directing the flow of sour gas containing natural gas and H 2 8 to an acid gas recovery plant, resulting in purified natural gas and acid gas a gas containing H 2 8, (b) burning a stream of purified natural gas with oxygen-containing gas in a gas turbine to produce electricity and hot flue gas; (c) directing hot flue gas to the first waste heat boiler to generate steam and clean flue gas; (6) burning at least part of H 2 8 in an acidic gas containing H 2 8 in the presence of oxygen-containing gas to produce hot exhaust gas containing 8О 2 ; (e) supplying hot exhaust gas containing 8O 2 to the second waste heat boiler for generating steam and cooled exhaust gas containing 8O 2 ; (ί) directing the cooled waste gas containing 8О 2 into the device for obtaining sulfuric acid to produce sulfuric acid, steam and a stream of purified flue gas.

The method in accordance with the invention uses thermal energy used to generate electricity more efficiently from heavily polluted sour gases. The invention is suitable for sour gases, in which sour gas preferably contains 1-50, more preferably 10-35 vol.% H 2 3. In addition, the invention allows to produce sulfuric acid without obtaining sulfur. This reduces the number of process steps and associated process equipment.

- 1,022146

In accordance with known methods, sour gas is processed to produce a stream of purified natural gas to generate electricity in the so-called combined-cycle cycle, which includes a gas turbine and a steam turbine. The resulting acid gas, containing most of the H 2 §, is sent to the sulfur recovery unit for the production of solid sulfur, which is then degassed, granulated, stored and shipped. The combustion energy of H 2 §, which can be up to 30% of the chemical energy of sour gas, is not used to generate electricity in the production line.

One of the applications of manufactured sulfur granules is the production of sulfuric acid. For example, υδ-Ά-20090077944 describes the use of elemental sulfur, with solid sulfur being burned. The sulfur combustion chamber produces hot sulfur dioxide, while the ejector mixes hot combustion gases with a cooling gas (such as compressed air) compressed Ν 2 or circulating sulfur dioxide to form a mixed working gas with a temperature below the maximum allowable temperature (metallurgical limit) for turbine blades . The resulting sulfur dioxide is sent to the plant for the production of sulfuric acid.

Thus, one of the main differences between the present invention and prior art processes is that elemental sulfur is produced in prior art processes, which can be used in a second process for the production of sulfuric acid at another site, while the present invention preferably completely transforms all H 2 § in δθ 2 in one stage, followed by conversion to sulfuric acid. The method in accordance with the present invention, therefore, is much more energy efficient.

Sour gas streams are typically hydrocarbon streams, such as natural gas. Natural gas consists mainly of methane, usually more than 50 mol.%, Usually more than 70 mol.% Of methane. Depending on the source, natural gas may contain different amounts of hydrocarbons heavier than methane, such as ethane, propane, butane, and pentanes, as well as a certain amount of aromatic hydrocarbons. Natural gas may also contain different amounts of hydrogen sulfide. For example, some natural gas fields contain natural gas with 15-30% hydrogen sulfide by volume. The gas may also contain other non-hydrocarbon impurities, such as H 2 O, 2 , CO 2, and the like.

The content of impurities in the produced natural gas gradually increases over time due to a decrease in the availability of good quality natural gas. In addition, environmental legislation is becoming increasingly stringent to the conditions of impurities in the combusted gas. As a result, there is an increasing need for processing natural gas to remove impurity gases from it in order to produce the final gas with the required specifications. In the process according to the invention, the high sulfur gas is first treated in an acid gas removal unit.

There are known methods for separating a gas stream containing hydrogen sulfide from a hydrocarbon gas stream in an acid gas removal installation, such as natural gas, to produce a gas stream containing hydrogen sulfide and purified natural gas.

In step b) of the process of the invention, the purified natural gas stream is combusted with oxygen-containing gas. Oxygenated gas can be pure oxygen or air or air enriched with oxygen. To eliminate the need for air separation to obtain oxygen-enriched air or pure oxygen, it is preferable to use air for burning hydrogen sulfide. There are known methods and devices for the operation of a gas turbine. The temperature of the resulting hot flue gases ranges from 400 to 700 ° C.

Step (c) of the method described in the invention uses the heat of the hot flue gases to produce steam in the recovery boiler. Thus, the resulting steam is used to drive one or more steam turbines. The steam streams used to drive steam turbines may be saturated steam streams or may be superheated steam streams.

Steam turbines can be selected from the group consisting of backpressure turbines, condensing turbines, backpressure / condensing turbines, condensing / heating turbines, condensing / withdrawing turbines and condensing / heating / withdrawing turbines. In another embodiment, steam turbines may be used to drive one or more devices from a group consisting of electric generators, pumps, and compressors.

In another embodiment, heat may be produced in conjunction with energy by taking steam from steam turbines. Steam can be retracted at a pressure of 5 bar and can be fed to any steam consumer (such as reboilers, steam feed, conventional heat exchangers). The pressure level during selection is usually dictated by customer requirements.

At stage 6) of the process, a hot waste gas containing O 2 is obtained by burning at least a part of the H 2 g that is present in the sour gas. Preferably, at least 50% of the H 2 § of the acid gas containing H 2 is burned, more preferably at least 70% of the H 2 is burned, more preferably at least 90% of the H 2 is burned. The temperature of the hot exhaust gas containing δθ 2 is preferably from 400 to 700 ° C. This heat is used in stage f)

- 2 022146 second recovery boiler. The reason for using the second steam generator, and not the same steam generator of stage c), is that the flue gases obtained in stage b) are already cleaned flue gases that do not require additional treatment prior to discharge into the exhaust pipe. Thus, in accordance with the invention, the waste gas containing §O 2 remains as concentrated as possible, while keeping the volume of the stream requiring additional treatment to a minimum.

At stage ί), the exhaust gas is fed to a device for producing sulfuric acid, which removes sulfur dioxide from the exhaust gases and uses it to produce sulfuric acid. A device for producing sulfuric acid can produce sulfuric acid from sulfur dioxide in the exhaust gas by the method of the prior art. For example, sulfur dioxide can first be oxidized to sulfur trioxide §O 3 by oxygenating an oxygen-containing stream, such as air. A catalyst may be present, such as a vanadium oxide (V) based catalyst.

The gaseous sulfur trioxide can then be treated with water to produce sulfuric acid in an exothermic reaction. To control the heat generated during the treatment of sulfur trioxide, it is preferable to use 97-98 wt.% Sulfuric acid containing 2-3% water to obtain concentrated 98-99 wt.% Sulfuric acid.

In an alternative embodiment, sulfur trioxide can be treated with oleum, H 2 § 2 O 7 , to form concentrated sulfuric acid. Such processes, along with other methods of producing sulfuric acid from sulfur dioxide, are well known to those skilled in the art. Concentrated sulfuric acid can then be added to water to produce aqueous sulfuric acid.

The resulting product of the combustion stage e) - cooled exhaust gas containing §O 2 , is a gaseous mixture, mainly containing sulfur dioxide, nitrogen, carbon dioxide and optionally residual oxygen. This gas mixture may be partially separated or partially concentrated to increase the content of sulfur dioxide, for example, by removing nitrogen. Preferably expose at least a portion of cooled exhaust gas containing 2 gD, gD 2 concentration step between the step (e) and step (ί), thereby creating a gas stream containing at least 70% gD 2 in terms of dry matter .

The advantage of having a stage of concentration of sulfur dioxide between stage (e) and (ί) is that the size of the device for obtaining sulfuric acid can be reduced in the preferred case, when the gas stream containing at least 70% §O 2 in terms of dry matter, is fed in the device for producing sulfuric acid. In addition, by adjusting the composition of the cooled waste gas containing §O 2 , the choice of device that is used to produce sulfuric acid becomes more flexible. A device for producing sulfuric acid may include a dry process for producing sulfuric acid, or a contact process for obtaining H 2 §O 4 , or a wet process for obtaining sulfuric acid, or both, following each other. Preferably, the adjustment of the composition of the cooled waste gas containing §O 2 can be accomplished by combining a gas stream containing at least 70% of §O 2 in terms of dry matter with the untreated part of the cooled exhaust gas containing 8О 2 to stage () .

Sulfur dioxide can be concentrated by any method of the prior art, such as, for example, liquid adsorption, for example, the Saigon process, adsorption, membrane separation or condensation of sulfur dioxide. Sulfur dioxide condenses at higher temperatures, i.e. about -10 ° C, than, for example, nitrogen. Due to the high condensation temperature of sulfur dioxide, the separation after burning sulfur dioxide and nitrogen is preferable to the separation of oxygen and nitrogen before burning.

The most preferred method for concentrating sulfur dioxide is to contact sulfur dioxide containing gas (i.e., a mixture comprising sulfur dioxide and nitrogen) with sulfur dioxide absorbing liquid in the sulfur dioxide absorption zone to selectively transfer sulfur dioxide from the burnt off gas to absorbing liquid to obtain absorbing liquid enriched in sulfur dioxide, and subsequent desorption of sulfur dioxide from absorbing liquid enriched to sulfur dioxide to obtain a lean absorber containing liquid and gas containing sulfur dioxide. One preferred sulfur dioxide absorbent fluid includes at least one substantially water-immiscible organic diester phosphonate.

Another preferred sulfur dioxide absorbent liquid includes tetraethylene glycol dimethyl ether.

Another preferred sulfur dioxide absorbing liquid includes diamines with a molecular weight of less than 300 in the form of a free base and a pKa value of a free nitrogen atom of from about 3.0 to about 5.5, containing at least 1 mole of water for each mole of sulfur dioxide absorbed.

The desorption of sulfur dioxide from an absorbing liquid enriched in sulfur dioxide is usually carried out at elevated temperatures. To ensure a more energy efficient process, the steam generated in the recovery boiler can be used to provide at least some of the heat needed to desorb sulfur dioxide from absorbing liquid enriched in sulfur dioxide. Preferably, the steam obtained in steps (c), (e) or (ί) can be used to concentrate the sulfur dioxide.

- 3 022146

In the preferred embodiment of the invention, the pairs obtained in step (c), (e) and (ί) are collected in one collection of steam. Steam can be distributed at various points in the process where heat or energy is required.

In another preferred embodiment of the invention, the clean flue gas from step (c) and the flow of cleaned flue gas from step (ί) are combined and fed into one common exhaust pipe.

Depending on the concentration of Η 2 δ sour gas and the stage of concentration O 2, you can choose the method of obtaining sulfuric acid. Preferably, when the high-sulfur gas contains 120, more preferably 10-20, even more preferably 15-20% by volume 2 δ, the sulfuric acid production device of stage (ί) includes a wet process for the production of sulfuric acid. In another preferred embodiment, when the high-sulfur gas comprises more than 15, more preferably 20-50, even more preferably 20-35% 2 δ, the sulfuric acid production device of stage (ί) includes a contact process for the production of sulfuric acid.

Claims (11)

  1. CLAIM
    1. The method of obtaining energy from sour gas containing Η 2 δ, comprising the following stages:
    (a) directing the stream of sour gas containing natural gas and Η 2 δ to the acid gas recovery unit, resulting in purified natural gas and acid gas containing 2§;
    (b) burning a stream of purified natural gas with oxygen-containing gas in a gas turbine to produce electricity and hot flue gas;
    (c) directing the hot flue gas to the first waste heat boiler to generate steam and clean flue gas;
    (6) at least a part of Η 2 δ is burned in an acidic gas containing 2 δ in the presence of oxygen-containing gas to produce hot exhaust gas containing 8О 2 ;
    (e) supplying hot exhaust gas containing §O 2 to the second waste heat boiler for generating steam and cooled exhaust gas containing 8О 2 ;
    (ί) direct cooled waste gas containing §O 2 into the device for producing sulfuric acid to produce sulfuric acid, steam and a stream of purified flue gas.
  2. 2. The method according to claim 1, in which between stage (e) and stage (ί) at least part of the cooled exhaust gas containing 8O 2 is subjected to the concentration stage §O 2 , thereby obtaining a gas stream containing at least 70 % §O 2 in terms of dry substance.
  3. 3. The method according to claim 2, in which the gas stream containing at least 70% §O 2 in terms of dry matter, is sent to the device for producing sulfuric acid to produce sulfuric acid, steam and a stream of purified flue gas.
  4. 4. The method according to claim 3, wherein a dry process for producing sulfuric acid is performed in the device for producing sulfuric acid.
  5. 5. The method according to claim 2, wherein the gas stream containing at least 70% of §O 2 in terms of dry matter, is combined with the untreated part of the cooled waste gas containing §O 2 , up to stage ().
  6. 6. The method according to any one of claims 1 to 5, wherein in step (6) at least 50% Η 2 δ is burned in an acid gas containing Η 2 δ, preferably at least 70% Η 2 δ is burned, more preferably burn at least 90% Η 2 δ.
  7. 7. The method according to any one of claims 1 to 6, in which the steam produced in step (c) and the steam generated in step (e) are collected in one collection of steam.
  8. 8. A method according to any one of claims 1 to 7, in which the clean flue gas of stage (c) and the flow of purified flue gas of stage (ί) are combined and sent to a single exhaust pipe.
  9. 9. The method according to any one of claims 1 to 8, in which in step (a) a stream of sour gas containing natural gas and 1-50% by volume 2 δ is directed to an acid gas recovery unit.
  10. 10. The method according to any one of claims 1 to 3, 5-8, in which sour gas contains 10-20% by volume 2 δ and in the device for producing sulfuric acid of stage (ί) the wet process of obtaining sulfuric acid is carried out.
  11. 11. A method according to any one of claims. 1-8, in which sour gas contains 20-35% об 2 δ and in the device for producing sulfuric acid stage (ί) carry out the dry process of obtaining sulfuric acid.
EA201201472A 2010-04-28 2011-04-19 Process for producing power from a sour gas EA022146B1 (en)

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EP10161374 2010-04-28
PCT/EP2011/056261 WO2011134847A2 (en) 2010-04-28 2011-04-19 Process for producing power from a sour gas

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EA022146B1 true EA022146B1 (en) 2015-11-30

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Families Citing this family (5)

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Publication number Priority date Publication date Assignee Title
AU2012339842A1 (en) * 2011-11-15 2014-05-15 Shell Internationale Research Maatschappij B.V. Method of producing sulfur dioxide
CA2855808A1 (en) * 2011-11-15 2013-05-23 Shell International Research Maatschappij B.V. Method of processing feed streams containing hydrogen sulfide
CA2855815A1 (en) * 2011-11-15 2013-05-23 Shell Internationale Research Maatschappij B.V. Method of processing feed streams containing hydrogen sulfide
WO2013098329A1 (en) 2011-12-27 2013-07-04 Shell Internationale Research Maatschappij B.V. Method for producing sulphuric acid
WO2013150081A2 (en) 2012-04-04 2013-10-10 Shell Internationale Research Maatschappij B.V. Process for producing power from a sour gas

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