[go: up one dir, main page]

WO2010075027A1 - Production d'acide sulfurique et de bisulfite de sodium sans émissions à partir d'un gaz acide de gazéification pour le dessalement - Google Patents

Production d'acide sulfurique et de bisulfite de sodium sans émissions à partir d'un gaz acide de gazéification pour le dessalement Download PDF

Info

Publication number
WO2010075027A1
WO2010075027A1 PCT/US2009/067866 US2009067866W WO2010075027A1 WO 2010075027 A1 WO2010075027 A1 WO 2010075027A1 US 2009067866 W US2009067866 W US 2009067866W WO 2010075027 A1 WO2010075027 A1 WO 2010075027A1
Authority
WO
WIPO (PCT)
Prior art keywords
stream
wsa
sulfuric acid
tail gas
condenser
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/US2009/067866
Other languages
English (en)
Inventor
Paul Steven Wallace
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.)
Katana Energy LLC
Original Assignee
Katana Energy LLC
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 Katana Energy LLC filed Critical Katana Energy LLC
Publication of WO2010075027A1 publication Critical patent/WO2010075027A1/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
    • C01B17/765—Multi-stage SO3-conversion
    • C01B17/7655—Multi-stage SO3-conversion with intermediate absorption
    • 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
    • C01B17/48—Sulfur dioxide; Sulfurous acid
    • C01B17/50—Preparation of sulfur dioxide
    • C01B17/508—Preparation of sulfur dioxide by oxidation of sulfur compounds

Definitions

  • This hi venison relates generally to methods and sysietrss for treating an acid gas stream in a sul furic acid plain and, more particularly, to methods and systems for treating an acid, gas stream in a sulfuric acid plant ami producing a sulfuric acid stream and a sodium bisulfite stream from the acid gas stream.
  • Conventional desalination facilities typically require chemical ehlorination and subsequent dechlorination of the seavater.
  • the seawater is initially chlorinated as a bioeide treatment to prevent biological growth in the inlet treatment section.
  • the .seawater or reject brine is then dechforinated to protect the downstream membranes and to protect, marine life if the brine from the conventional desalination facility is rejected back to the ocean.
  • Dechlorination of the seawater or reject brine typically uses at least one of sodium bisulfite ("NaMSO,;' * ), sodium sulfite ("Na-SO;”), and sodium mcUibi sulfite to neutralize the chlorine.
  • sodium sulfite is typically not cost competitive when compared to sodium bisulfite or sodium metabisulfite.
  • Sodium metabisidfite is typically shipped as a dry powder ami is the least expensive purchased dechlorination chemical
  • sodium mefabssuifite releases sodium dioxide when mixed with water vapor or water.
  • the sodium meiabis ⁇ Hite must be kept dry and mixed in a cloyed storage tank with a vapor control system. This vapor control .system increases the cost for using sodium melabisuHite as a dechlorination compound.
  • the acid gas stream includes hydrogen sulfide ("H 2 S:"; and carbon dioxide vV ( €CK ' ).
  • the conventional commercial sulfuric acid plant uses the air stream arsd the acid gas stream from the conventional gasification faci lity to produce a tail gas stream, which is typically released as stack gas to the atmosphere, and a dry sul furic acid stream.
  • the tail gas stream consists mainly nitrogen and carbon dioxide; however, the tail gas stream also contains sulfur oxides ("SO ⁇ " ) and sulfuric acid mist.
  • This tail gas stream is not suitable for recycle to the conventional gas ⁇ fier facility because it consists of significant amounts of nitrogen and corrosive sulfuric acid mist particles.
  • the nitrogen is an inert gas and reduces gasif ⁇ er syngas capacity.
  • the sulfuric acid mist particles require compression and expensive metallurgy in the piping if transported.
  • This tail gas stream also is nut useabie within the desalination facility,
  • the sulfuric acid stream is used as sulfuric acid addition in the desalination plants.
  • the problems associated with shipping and handling of sulfuric acid for a conventional desalination facility that is integrated with a conventional sulfuric acid plant and a conventional gasification facility become mule, [0007]
  • the conventional seawater desalination facilities are commercially operated in conjunction with the conventional gasification facilities since gasifiers produce large amounts of iow level heat that are required for thermal desalination.
  • gasifiers require significant amounts of makeup water since water is chemically consumed in the gasiiler to produce hydrogen.
  • a sulfuric acid plant includes a wet sulfuric acid (WSA) condenser and a caustic scrubber fluidly coupled to the WSA condenser.
  • WSA wet sulfuric acid
  • a SO S rich condenser feed stream enters the WSA condenser.
  • the condenser oroduces a WSA overheads stream and a WSA bottoms stream from the
  • the WSA overheads stream feeds into the caustic scrubber.
  • the eausJie scrubber produces ⁇ tail gas stream and a caustic bottoms stream from the WSA overheads stream.
  • the caustic scrubber bottoms .stream includes sodiujvi bisulfite
  • the tail gas stream includes carbon dioxide and oxygen
  • the WSA bottoms stream includes concentrated sulfuric acid.
  • a method for operating a sulfuric acid piani includes providing a wet sulfuric acid (WSA) condenser and fli ⁇ diy coupling a caustic scrubber to the WSA condenser.
  • a SOi rich condenser feed stream enters the WSA condenser.
  • the condenser produces a WSA overheads stream and a WS.A bottoms stream from the SO* rich condenser feed stream.
  • the WSA overheads stream feeds into the caustic scrubber.
  • the caustic scrubber produces a tail gas stream and a caustic bottoms stream from the WSA overheads stream.
  • the caustic scrubber bottoms stream includes sodium bisulfite
  • the tail gas stream includes carbon dioxide and oxygen
  • the WSA bottoms stream includes concentrated sulfuric acid.
  • Figure 1 shows a flowchart depicting a sulfuric acid plant in accordance with an exemplary embodiment.
  • the application is directed to methods and systems fbr treating an acid gas stream in a sulfuric acid plant.
  • the application is directed to methods sn ⁇ systems for treating an acid gas stream in a sulfuric acid plant and producing a sulfuric acid stream and a sodium bisulfite stream from the acid gas stream.
  • the invention may be belter understood by reading the following description of non- Hmiting, exemplary embodiments with reference to the attached drawing, and which is briefly described as follows.
  • FIG. 1 shows a flowchart depicting a sulfuric acid plant 100 irs accordance with an exemplary embodiment.
  • the sulfuric acid plant 100 includes an mclnerator 1 10, an SO> converter 125, a wet sulfuric acid (“'WSA' " ) condenser 130, and a caustic scrubber 155.
  • an acid gas stream 102 enters the incinerator 1 10.
  • the acid gas stream 102 includes hydrogen sulfide r ⁇ H;S N" ). ranging from about thirty percent to about seventy percent, and carbon dioxide "(CO/ ' '), ranging from about thirty percent to about seventy percent.
  • (he acid gas stream 102 originates ironi a gasification facility (not shown), and more specifically from an acid gas removal ("AGR") unit (not shown).
  • a high purity oxygen stream 104 and a recycle tail gas incinerator blower discharge stream 1 52 are combined prior to entering the incinerator 1 10.
  • the recycle tail gas incinerator blower discharge stream 1.52 originates from a tail gas stream S 58, which is further described below.
  • the high purity oxygen stream 104 includes approximately ninety-five percent or greater oxygen composition.
  • the recycle tail gas incinerator blower discharge stream 1 52 includes approximately ninety-five percent carbon dioxide and approximately live percent oxygen.
  • the combined high purity oxygen stream 104 and the recycle tail gas incinerator blower discharge stream 1 52 result in a stream comprising approximately twenty percent oxygen and approximately eighty percent carbon dioxide.
  • the combined high purity oxygen stream 104 and the recycle tail gas incinerator blower discharge stream 152 have combustion properties similar to air, but do not contain any amounts of nitrogen.
  • each of the high purity- oxygen stream 104 and the recycle- tail gas incinerator blower discharge stream 152 enter the incinerator I H) independently from one another, but are mixed thoroughly within the incinerator 1 10.
  • the acid gas stream 102 is combusted to produce an incinerator discharge stream 1 12.
  • the hydrogen sulfide gas within the acid gas stream 102 is converted into sulfur dioxide ("S(K').
  • the incinerator discharge stream 1 12 is routed to an SO : ; cooler 1 15 where the incinerator discharge stream 1 12 is cooled and forms a SO? cooler discharge stream i 17.
  • an exemplary temperature range is provided for the incinerator discharge stream 1 12, the incinerator discharge stream ⁇ ⁇ 2 can be at other temperatures outside of this provided range without departing from the scope and spirit of the exemplary embodiment.
  • the SO;> cooler discharge stream 1 17 is routed to a SOn converter 125 where the SO; present within the SC> cooler discharge stream U ? is converted into SO . ;.
  • a portion of the SO? cooler discharge stream 1 17 is routed to the lower portion. of the caustic scrubber 155 via a SO? cooler discharge slip stream H S, which is diseased in further deUul below.
  • the SOj converter According to some of the exemplary embodiments, the SOj converter
  • the SO? convener 125 includes three stages of catalyst beds and three stages of intercooiers, where each inlereooler is positioned below a catalyst bed.
  • the SO? convener 125 is described as having three stages of catalyst beds and three stages of iniereooiers, the SO;; converter 125 can .have more or less stages of catalyst beds and/or stages of int ⁇ rcooSers without departing from the scope and spirit of the exemplary embodiment.
  • Bach of the catalyst beds is made of catalysts capable of converting SO> to SCK. These eataiys ⁇ types are known to people having ordinary skill in the art.
  • heal is generated ⁇ uc to the exothermic reaction of the S(> to SO .? conversion.
  • the intercooiers svUhsrs the SO-? converter [25 are used to remove the heat generated by this exothermic reaction.
  • the SO 2 cooler discharge stream ) 17 enters the SO 2 converter 125 above the first stage of catalyst bed and flows through each of the catalyst beds and each of the intercooiers until n reaches the bottom of the SO; converter 125, A SCb converter discharge stream.
  • 127 which is rich in S(>; gas, exits the SO 3 converter 125 and is routed to ihe WSA condenser 130, l ' 0019 ' l According to some exemplary embodiments, a heat recovery system
  • this heat recovery system 120 is used t ⁇ provide a cooling medium to the SO; cooler 1 15 and 10 each of the lmercoolers within the SO; converter 125.
  • the heat recovery system 120 provides a SOj cooler supply stream J 22a Jo the SO?, cooler 1 15.
  • the SO;$ cooler supply strt-am 122s removes heal from the Incinerator discharge stream 1 1 2 and returns back to the heat recovery system 120 via a SO; cooler return stream 122b,
  • the heat recovery system 120 provides a SOj converter supply stream 523a to each of She intercooiers within the SO?
  • Each of the SC>> converter supply streams 123a removes heat from the SO; cooler discharge stream 1 17 as it Hows through the $(>> converter 125 and returns back Vo the heat recovery system 120 via a eorrespt Hiding SO : > converter return stream S 23b.
  • a .steam discharge stream 12 I exits the heat recovery system 120.
  • the heat recovery system 120 provides a cooling medium to the SO ?
  • cooler 1 15 and to each of the ⁇ ntercooters within the SO; converter 125 one or more heat recovery systems can be used to provide cooling medium to the S(> cooler 1 15 and to each of the ⁇ itereoolers within the SO; converter 125 without departing from the scope and spins, of the exemplary embodiment
  • a heat recovery system is shown in some of the exemplary embodiments, any other type of cooling system can be used thai is known to people having ordinary skill in the art.
  • the water vapor present within the SO;; converter discharge stream 12? is condensed within the WSA condenser 1 30, thereby converting the SO .? gas into commercial grade concentrated sulfuric acid which is suitable for use in a desalination facility (not shown).
  • the commercial grade concentrated sulfuric acid is about ninety-eight percent concentration arid, exits the WSA condenser 130 at its bottom portion via a WSA condenser bottoms stream 1 32.
  • the portion of the SO 2 converter discharge stream 12? that remains uncondensed exits the top portion of the WSA condenser 130 via a WSA condenser overheads stream 131 and is routed to the middle portion of the caustic scrubber 155.
  • the WSA condenser bottoms stream 132 is routed to a mixer 135 where it is combined with an acid cooler recycle stream 148, thereby lowering the temperature of the WSA condenser bottoms stream ⁇ 32 and preventing cavitation of an acid pump 140.
  • the mixed WSA condenser buttoms stream 132 and the acid cooler recycle stream 148 is fouled to the acid pump HO.
  • the acid pump 140 discharges an acid pump discharge stream 142, which is at a higher pressure than the mixed VVSA condenser bottoms stream 132 and the acid cooler recycle stream 148.
  • the acid pump discharge stream 142 is routed to an acid cooler 145, which eoois the acid pump discharge stream 142 and forms an acid cooler discharge stream 147.
  • the acid cooler 145 has an acid cooler supply stream 143a which removes heat from the acid pump discharge stream 142. Upon removing heat from the acid cooler 145, the acid cooler supply stream 143a exits the acid cooler 145 via an ack; cooler return stream 343b. According to some exemplary embodiments, cooling water is used to provide cooling to the acid cooler 145.
  • the acid cooler discharge stream 147 which has about a ninety-eight percent sulfuric acid concentration, is routed to a desalination facility according to some exemplary embodiments so that sulfuric acid can he added to certain streams to prevent calcium carbonate scale formation within membranes.
  • the sulfuric acid is used to adjust pH levels within the desalination facility.
  • the sulfuric acid reacts, with the bicarbonatcs and forms sulfates, which are more easily removed .hi membranes than the bicarbonates.
  • a portion of She acid cooler discharge stream 147 is routed to the mixer 135 via the acid cooler recycle stream 148.
  • the recycle tail gas WSA blower discharge stream 172 originates from the tail gas stream 158 and enters the WSA condenser 130 near its top portion, The recycle tail gas WSA blower discharge stream 172 removes heat from within the WSA condenser 130 and forms a recycle tail gas WSA condenser discharge stream 134.
  • recycle ttsil gas WSA condenser discharge stream 134 is combined with the WSA condenser overheads stream 13 1 and is routed to the middle portion of the caustic scrubber 155. However, a portion of the recycle tail gas WSA condenser discharge stream 134 is routed to at) incinerator blower 150 via a recycle tail gas incinerator blower feed stream 1 33. The incinerator blower 150 then discharges the recycle tail gas incinerator blower discharge stream 152 into the incinerator 1 10, as previously mentioned.
  • sonic exemplary embodiment provide condensing within the WSA condenser 130 using eou ⁇ tedlow methods
  • the condensing can occur using other methods including, but not limited to, concurrent How methods without departing from the scope and spirit of the exemplary embodiment.
  • the caustic scrubber 155 includes an upper portion having an upper packed portion and a leaver portion having a lower packed ponion. The upper packed portion, and the lower packed portion provides a space therebetween. Although some exemplary embodiments provide two packed sections within the caustic scrubber 155, greater or less packed sections can be provided within the caustic scrubber without departing from ihe scope sn ⁇ spirit of the exemplary embodiment.
  • the caustic scrubber 155 is fabricated using fiberglass reinforced plastic. ("FRP' * ), a plastic coated material such as steel, stainless steel or any other suitable materiel capable of withstanding corrosion that is known to people having ordinary skill in the art.
  • the SQ; cooler discbarge slip stream 1 18 is quenched with a sodium bisulfite cooler lower recycle stream 16? so- that die resulting temperature is about 220 0 F.
  • die sodium bisulfite cooler lower recycle stream 16? has & pi! of about five and a temperature about 90 0 F.
  • the SO 2 cooler discharge slip stream I I S and the sodium bisulfite cooler lower recycle stream 16? are mixed together within an acid resistant alumina lined spool J 80 prior to both streams 1 18 and 167 entering the bottom portion of the caustic scrubber 155.
  • a caustic and water stream 169 and a sodium bisulfite cooler upper recycle stream 168 enter the top portion of the caustic scrubber 155 near the top of the upper packed portion.
  • the sodium bisulfite cooler upper recycle stream 168 has a pli of about five and a temperature of about 90 "V.
  • the caustic and water stream S 69 and the sodium bisulfite cooler upper recycle stream 168 are mixed together prior Io entering the caustic scrubber 1 55.
  • the combined caustic and water stream ⁇ 69 and the sodium bisulfite cooler upper recycle stream 168 also referred to as eausiie solution, have a pH of about eight and a temperature at or below about 90 1 T,
  • the caustic solution 169 and 168 first absorbs the residual SO 2 and SO* and a portion of the carbon dioxide that are present wiih ⁇ Ti the WSA condenser overheads stream KM and the recycle tail gas WSA condenser discharge stream 134. This absorption occurs in the upper packing section of ihe caustic scrubber 1.55.
  • the temperature at the top portion of the caustic scrubber 155 is about H)O T,
  • the solution from the upper packing section is routed to the lower packing section where SO 1 ; is absorbed, from the SCX; cooler discharge slip stream 1 I S and carbon dioxide is stripped out.
  • the temperature ai the bottom portion of the caustic scrubber 155 is about 150 T.
  • NaHSO/' Sodium bisulfite
  • the tail gas stream 158 exits the upper portion of the caustic scrubber
  • the tail gas stream 158 has a temperature of 120 0 F or less, a PH of about 5.5 to about six, and includes of carbon dioxide and oxygen.
  • This tali g&s stream 158 Is compressed and routed to a gasifkr according in some of the exemplary embodiments. Since the tail gas stream 158 includes carbon dioxide, the carbon dioxide act as a moderator within the gasifier to reduce the temperature within the gassiler. Additionally, the carbon dioxide within the tail gas stream 158 increases the conversion from carbon to carbon monoxide ("CO”) within the gasifier.
  • the tail gas stream 158 is routed to a sulfur recovery unit (not shown) that can operate in parallel with the sulfuric acid plant. 100.
  • This sulfur recovery unit can use a portion oi "the acid gas. stream 102, which comes from an acid gas removal unit (not shown) located within She gasifter facility * to produce sulfur. This converts any residual SC>> or SC>; gases io sulfur and produces an oxygen free CX>> tail gas stream 158 thai can be used for enhanced oii recovery.
  • Most of the tail gas stream 158 is recycled back to the WSA condenser 130 via a recycle tail gas WSA blower supply stream 159 and the recycle fail gas WSA blower discharge stream 172.
  • the recycle Tail gas WSA blower supply stream 159 enters a WSA blower 170 and is thereafter routed to the WSA condenser 130 via the recycle tail gas WSA blower discharge stream 172, as previously mentioned.
  • a caustic scrubber bottoms stream 1 57 is discharged from the bottom portion of the caustic scrubber 155 and is routed a sodium bisulfite pump 160.
  • the caustic scrubber bottoms stream 15? is acidic having a pH of about 4,5, has a dilute sodium bisulfite concentration at about Ci ve to ten percent and is at a temperature of about 150 T.
  • the sodium bisulfite pump 160 discharges a sodium bisulfite pump discharge stream 162, which is at a higher pressure than the caustic scrubber bottoms stream 1 57.
  • a caustic stream 163 is added to the sodium bisulfite pump discharge stream 162 to neutralize a small portion nf the sodium bisulfite, about ten to twenty percent of the total sodium bisulfite concentration, to sodium sulfite.
  • the resulting pH of the combined sodium bisulfite pump discharge stream 162 ami the caustic stream S 63 is about five.
  • the combined sodium bisulfite pump discharge stream 162 &n ⁇ the cau.s ⁇ e stream 163 are Orientd to a sodium bisulfite cooler 165, which cools streams 162 and 163 and forms a sodUrm bisulfite cooler discharge stream 166.
  • the excess caustic, dilute solution, and cooler temperature present within the sodium bisulfite cooler discharge stream 166 prevent S(>- emissions from the sodium bisulfite cooler discharge stress 166.
  • the sodium bisulfite cooler 165 has a sodium bisulfite cooler supply stream 164a which removes heat from the combined sodium bisulfite pump discharge stream 162 and the caustic stream 163. Upon removing heat from the sodium bisulfite cooler 165, the sodium bisulfite cooler supply stream 164a exits the sodium bisulfite cooler 165 via a sodium bisulfite cooler return stream 164b.
  • cooling water is used to provide cooling to die sodium bisulfite cooler 165.
  • the sodium bisulfite cooler discharge stream 166 is at a temperature of about 90 °F and is routed to a desalination facility so that certain .streams within the desalination facility cars be deehlortnated. ⁇ portion of the sodium bisulfite cooler discharge stream 166 is used to quench the SO; cooler discharge slip stream I I 8 via the sodium bisulfite cooler lower recycle stream 167, as previously mentioned.
  • Another portion of the sodium bisulfite cooler discharge stream 166 is recycled back to the upper portion of the caustic- scrubber 155 via the sodium bisulfite cooler upper recycle stream 168, as previously mentioned.
  • the sodium bisulfite cooler upper recycle stream 168 Is combined with the caustic and water stream 169 prior to entering the caustic scrubber 155.
  • the costs of purchasing, handling and storing sodium bisulfite and sulfuric acid, and the SO;; emissions associated with the shipment and transfer of sodium bisulfite and sulfuric acid to the desalination facility are eliminated.
  • the norma! atmospheric emissions point, for example, the WSA condenser overheads stream, from the conventional sulfuric acid plants also is eliminated.
  • the corrosion and emission issues associated with concentrated sodium bisulfite solution are eliminated.
  • sulfuric acid corrosion due to water and water vapor contamination is avoided.
  • the carbon conversion in the gasifser is increased because a recycle stream including mainly carbon dioxide and oxygen, and insignificant amounts of nitrogen, is recycled back into the gasiiser from the caustic scrubber.
  • a wider compositional range uf carbon dioxide within the gasification acid gas stream can be used as feed to the improved sulfuric acid plant section. Since an oxygen stream and a recycle tail gas stream is used to feed the incinerator, instead of an air stream, the oxygen content and inert content can be adjusted independently to compensate .for changes in the carbon dioxide concentration in the gasification acid gas feed stream.
  • one feature includes an integrated gasification facility, sulfuric acid plant, and a desalination facility that does not have a sulfuric acid tail gas stack emitted to the environment and also docs not require third party supply of sulfuric acid and/or sulfites. Additionally, according to some exemplars' embodiments., one feature includes a caustic scrubber that simultaneously produces a sodium bisulfite and s ⁇ dlurn sulfite stream that is optima! for dechlorination of seawater in a desalination facility and a tail gas stream that is optimal for recycle to a gasifler.
  • the sodium bisulfite mv ⁇ sodium sulfite stream is dilute, cool has a pH of about 5, has low bicarbonate composition, and lias low SO? : emissions.
  • the tail gas stream is composed of essentially carbon dioxide and oxygen and has a near neutral pH at about six.. Additionally, the tail gas stream has low moisture content, is at about 100 T or cooler, and has low SO x concentrations.
  • one feature includes an alumina lined quenching spool that is nsed for the Sl>> cooler discharge slip stream H S.
  • one feature includes a caustic scrubber imbricated from PRP or any other corrosion resistant material.
  • one feature includes using a recycle tail gas stream, which is composed essentially of carbon dioxide and oxygen, and an oxygen stream, instead of air, to feed Into the incinerator, [0033]

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Treating Waste Gases (AREA)

Abstract

L'invention concerne une installation de production d'acide sulfurique qui comprend un condenseur d'acide sulfurique humide (ASH) et un épurateur caustique couplé en relation fluidique au condenseur d'ASH. L'installation de production d'acide sulfurique reçoit un courant d'alimentation en gaz acide et produit un courant d'acide sulfurique concentré par le condenseur, un courant de bisulfite de sodium par l'épurateur et un courant de gaz de queue par l'épurateur. Le courant d'alimentation en gaz acide peut être fourni par un équipement de gazéification. Le courant d'acide sulfurique peut être utilisé dans un équipement de dessalement destiné à neutraliser les carbonates dans un courant d'eau de mer. Le courant de bisulfite de sodium peut être utilisé dans l'équipement de dessalement pour déchlorer l'eau de mer. Le courant de gaz de queue comprend essentiellement du dioxyde de carbone et de l'oxygène et est recyclé dans l'équipement de gazéification. Ainsi, l'installation de production de gaz sulfurique n'émet aucune émission. L'installation de production d'acide sulfurique comprend également un incinérateur qui est alimenté par un courant d'oxygène et une partie du courant de gaz de queue.
PCT/US2009/067866 2008-12-15 2009-12-14 Production d'acide sulfurique et de bisulfite de sodium sans émissions à partir d'un gaz acide de gazéification pour le dessalement Ceased WO2010075027A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US12267108P 2008-12-15 2008-12-15
US61/122,671 2008-12-15

Publications (1)

Publication Number Publication Date
WO2010075027A1 true WO2010075027A1 (fr) 2010-07-01

Family

ID=42288080

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2009/067866 Ceased WO2010075027A1 (fr) 2008-12-15 2009-12-14 Production d'acide sulfurique et de bisulfite de sodium sans émissions à partir d'un gaz acide de gazéification pour le dessalement

Country Status (1)

Country Link
WO (1) WO2010075027A1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010114679A1 (fr) * 2009-04-03 2010-10-07 General Electric Company Procédé et appareil de recyclage de gaz résiduaire
WO2015006873A1 (fr) * 2013-07-18 2015-01-22 Cansolv Technology Inc. Procédés de production d'acide sulfurique à partir d'un champ de gaz naturel résiduaire acide
CN105003826A (zh) * 2015-07-02 2015-10-28 广东韶钢松山股份有限公司 一种用于酸汽输送的环形管网
CN111362233A (zh) * 2020-04-14 2020-07-03 长沙有色冶金设计研究院有限公司 一种处理高浓度so2冶炼烟气的预转化工艺及其装置
CN111689477A (zh) * 2020-07-21 2020-09-22 株洲宏大高分子材料有限公司 高含烃酸性气湿法制硫酸工艺与装置

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050011832A1 (en) * 1999-08-20 2005-01-20 Leon Awerbuch Water desalination process using ion selective membranes
US20060233687A1 (en) * 2005-04-15 2006-10-19 Hojlund Nielsen Poul E Process for cleaning gases form gasification units
US20080169098A1 (en) * 2004-05-28 2008-07-17 Bp Exploration Operating Company Limited Desalination Method
US20080175777A1 (en) * 2007-01-23 2008-07-24 Naresh Suchak Process for removing contaminants from gas streams
US20080196587A1 (en) * 2007-02-16 2008-08-21 Bao Ha Co2 separation apparatus and process for oxy-combustion coal power plants

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050011832A1 (en) * 1999-08-20 2005-01-20 Leon Awerbuch Water desalination process using ion selective membranes
US20080169098A1 (en) * 2004-05-28 2008-07-17 Bp Exploration Operating Company Limited Desalination Method
US20060233687A1 (en) * 2005-04-15 2006-10-19 Hojlund Nielsen Poul E Process for cleaning gases form gasification units
US20080175777A1 (en) * 2007-01-23 2008-07-24 Naresh Suchak Process for removing contaminants from gas streams
US20080196587A1 (en) * 2007-02-16 2008-08-21 Bao Ha Co2 separation apparatus and process for oxy-combustion coal power plants

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010114679A1 (fr) * 2009-04-03 2010-10-07 General Electric Company Procédé et appareil de recyclage de gaz résiduaire
US8551199B2 (en) 2009-04-03 2013-10-08 General Electric Company Method and apparatus to recycle tail gas
WO2015006873A1 (fr) * 2013-07-18 2015-01-22 Cansolv Technology Inc. Procédés de production d'acide sulfurique à partir d'un champ de gaz naturel résiduaire acide
US9815693B2 (en) 2013-07-18 2017-11-14 Shell Oil Company Processes for producing sulfuric acid from sour tail gas field
EA033099B1 (ru) * 2013-07-18 2019-08-30 Кэнсолв Текнолоджи Инк. Способ производства серной кислоты из источника кислого хвостового газа
CN105003826A (zh) * 2015-07-02 2015-10-28 广东韶钢松山股份有限公司 一种用于酸汽输送的环形管网
CN111362233A (zh) * 2020-04-14 2020-07-03 长沙有色冶金设计研究院有限公司 一种处理高浓度so2冶炼烟气的预转化工艺及其装置
CN111362233B (zh) * 2020-04-14 2021-07-02 长沙有色冶金设计研究院有限公司 一种处理高浓度so2冶炼烟气的预转化工艺及其装置
CN111689477A (zh) * 2020-07-21 2020-09-22 株洲宏大高分子材料有限公司 高含烃酸性气湿法制硫酸工艺与装置
CN111689477B (zh) * 2020-07-21 2024-04-26 株洲宏大高分子材料有限公司 高含烃酸性气湿法制硫酸工艺与装置

Similar Documents

Publication Publication Date Title
KR100464840B1 (ko) 산소 함유 혼합물로부터 이산화탄소를 회수하는 방법
US20070269358A1 (en) Processes for absorbing chlorine from a gas containing chlorine and carbon dioxide
WO2010075027A1 (fr) Production d'acide sulfurique et de bisulfite de sodium sans émissions à partir d'un gaz acide de gazéification pour le dessalement
US10246330B2 (en) Systems and processes for removing hydrogen sulfide from gas streams
JPH0134114B2 (fr)
US20210354084A1 (en) Method for carbon dioxide capture and sequestration using alkaline industrial wastes
EP1962992B1 (fr) Epurateur de refroidissement rapide a deux etages
US7927576B2 (en) ATS tail gas treating process for SRU and SWS off gases
KR101998682B1 (ko) 탈황 가스의 재순환을 갖는 황산 제조
SA519402395B1 (ar) تحسين معالجة الغازات المتخلفة في وحدة كلاوس بواسطة تقنية الأغشية الانتقائية لثاني أكسيد الكبريت
CA3021202A1 (fr) Usine d'acide sulfurique
US20020159938A1 (en) Method for treating hydrogen sulfide-containing waste gases
CN103130682B (zh) 制备异氰酸酯的方法
KR20070118032A (ko) 황산의 회수 방법
WO2013098329A1 (fr) Procédé de production d'acide sulfurique
JPH02237620A (ja) 硫化水素除去方法
NO854541L (no) Oksydativ fjerning av hydrogensulfid fra gasstroemmer.
US9504984B2 (en) Generating elemental sulfur
EP0151010B1 (fr) Dispositif et procédé de concentration d'acide sulfurique
EP2374752A1 (fr) Procédé pour la fabrication de chlore
JP2006219369A (ja) 塩素の製造方法
AU2022374973A1 (en) Production of sulfuric acid employing an o2 rich stream
US20250313468A1 (en) Tail gas treatment system and method for a sulfuric acid production plant
CA2920747C (fr) Procede et appareil pour le traitement de gaz comprenant le sulfure d'hydrogene
EP4211073B1 (fr) Système et procédé de production de dioxyde de soufre et installation d'acide sulfurique associée

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 09835552

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 09835552

Country of ref document: EP

Kind code of ref document: A1