WO2004022205A1 - Procede et dispositif pour eliminer et recuperer du so2 dans des fumees - Google Patents

Procede et dispositif pour eliminer et recuperer du so2 dans des fumees Download PDF

Info

Publication number
WO2004022205A1
WO2004022205A1 PCT/CN2002/000819 CN0200819W WO2004022205A1 WO 2004022205 A1 WO2004022205 A1 WO 2004022205A1 CN 0200819 W CN0200819 W CN 0200819W WO 2004022205 A1 WO2004022205 A1 WO 2004022205A1
Authority
WO
WIPO (PCT)
Prior art keywords
section
ammonium sulfate
ammonium
flue gas
solution
Prior art date
Application number
PCT/CN2002/000819
Other languages
English (en)
Chinese (zh)
Inventor
Wende Xiao
Original Assignee
East China University Of Science & Technology
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
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=4748812&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=WO2004022205(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by East China University Of Science & Technology filed Critical East China University Of Science & Technology
Priority to AU2002349435A priority Critical patent/AU2002349435A1/en
Publication of WO2004022205A1 publication Critical patent/WO2004022205A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/73—After-treatment of removed components
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/24—Sulfates of ammonium

Definitions

  • the invention relates to a method and a device for desorbing and recovering SO 2 in flue gas, in particular to a flue gas desulfurization method using ammonia as a raw material (including liquid ammonia, ammonia water and ammonium carbonate).
  • the exhaust gas contains so 2 .
  • the content of so 2 in the flue gas is usually low.
  • the principle of flue gas desulfurization is the chemical reaction between an alkaline desulfurizer and an acidic SO 2 gas.
  • Typical desulfurizing agents are limestone (CaC0 3 ) and ammonia (N3 ⁇ 4), forming two typical technology categories, which are called calcium method and ammonia method, respectively.
  • the calcium method generates a gypsum by-product, CaS0 4 .2H 2 0, at the same time as desulfurization, which can be used as a raw material for building materials, but it is generally not very useful and can only be discarded and stacked. Therefore, the calcium method is often called the abandonment method.
  • the ammonia method can co-produce a variety of products while desulfurizing, such as sulfuric acid and ammonium sulfate fertilizers.
  • desulfurizing such as sulfuric acid and ammonium sulfate fertilizers.
  • the desulfurization by-product of the ammonia method has greater application value than the calcium method.
  • the ammonia desulfurizing agent ammonia comes from chemical fertilizers, and its desulfurization products also serve as chemical fertilizers, which do not cause additional ecological and environmental problems to nature. Therefore, the ammonia method is called the recycling method.
  • the ammonia desulfurization process usually includes two steps:
  • H 4 HC0 3 + NH 4 HS0 3 (NH 4 ) 2 S0 3 + C0 2 + H 2 0)
  • the absorption solution contains NH 4 HS0 3 and (NH 4 ) 2 S0 3.
  • the ratio of the two salts is controlled by the H 3 / S0 2 ratio in the desulfurization process.
  • N3 ⁇ 4 / S0 2 1.2 — 1.4
  • the ratio of (NH 4 ) 2 S0 3 and N3 ⁇ 4HS03 in the solution is 1 / 4-2 / 3.
  • the mixed solution of ammonium sulfite is a semi-finished product produced as a by-product of the desulfurization process, and it can also be directly used, for example, by adding After the ammonia was neutralized, an ammonium sulfite solution was obtained and sold as a liquid nitrogen fertilizer.
  • ammonium sulfite needs to be processed into solid ammonium sulfide, which is convenient for storage, transportation and seasonal sales.
  • the above-disclosed technology is particularly suitable for boiler flue gas containing sulfur, such as flue gas burning high sulfur coal or sintering machine flue gas of non-ferrous metal smelting plant.
  • sulfur content for boiler flue gas such as flue gas SO 2 content is less than lOOOppmv
  • the sulfur content of coal-fired boilers corresponding to less than 1%, especially smaller boiler capacity, the total annual prolapse than S0 2 small. If a solution for producing sulfuric acid is used, the scale of the sulfuric acid plant is too small, the relative investment and energy consumption are high, and the economy is poor. Therefore, it is of great significance to develop and research the sulfur extraction and recycling in the flue gas with very low sulfur content.
  • the technical problem to be solved by the present invention is to disclose a method and device for extracting and recovering SO 2 in flue gas with low sulfur content, so as to overcome the defects existing in the prior art.
  • the technical idea of the present invention is as follows: from the mixed solution of ammonium sulfite from the absorption process, after neutralization with ammonia, an ammonium sulfite solution is obtained:
  • ammonium sulfite solution is oxidized directly, and ammonium sulfate can be obtained:
  • the upper limit of the concentration of ammonium sulfite mixed salt is not limited, and the normal operating concentration is 30-50% (wt), In this way, energy consumption is low and equipment investment is small.
  • this method is more suitable for high-sulfur coal and / or large power plants. Accordingly, the inventor has proposed the following:
  • the specific method includes the following steps:
  • the ammonia includes liquid ammonia, ammonia water or / and ammonium carbonate;
  • the ammonium sulfite solution is oxidized with air to obtain an ammonium sulfate solution.
  • the pressure of the compressed air is generally 0.05-0.2Mpa (gauge pressure).
  • the flow rate of the compressed air is 1 to 5 times the theoretical amount of ammonium sulfite oxidation. Commonly, it is 2 to 4 times.
  • the residence time of the oxidation reaction is generally 1 to Between 3 hours, preferably around 2 hours. Under these conditions, the oxidation rate can be greater than 95%.
  • the concentration of ammonium sulfate solution is generally 5-20% (wt).
  • step (3) The ammonium sulfate solution generated in step (2) is in contact with hot flue gas with a temperature of 100-160 ° C. Through the process of heat and mass transfer, the temperature of the hot flue gas is reduced to 50-55 ° C and the humidity is increased to Near saturation humidity. While the water in the ammonium sulfate solution evaporates, the ammonium sulfate concentration can be increased to 40-50% (wt), sent to the ammonium sulfate crystallizer, and processed into commercial ammonium sulfate fertilizer.
  • the flue gas is washed with water, eluting the absorption liquid entrained in the flue gas, in particular ammonium sulfate, etc., in order to reduce product loss, while preventing into the reheater.
  • the water flow of the washing is the flow required to maintain the water balance of the absorption system, which is related to the flue gas conditions, and is generally 5 to 20% of the absorption liquid flow.
  • the flue gas is basically a vapor saturated with water vapor. If it is not reheated and the temperature is increased, water dew will necessarily form on the flue and the inner wall of the chimney. Causes corrosion. In addition, the saturated smoke leaving the chimney will often form a "white dragon". Due to insufficient lifting degree, raindrops will be formed, which will cause acid rain pollution to the boiler plant area.
  • the flue gas temperature after desulfurization is 48-50 ° C
  • the saturated dew point is about 48 ° C. In order to solve the above problems, the flue gas temperature should be above 20 ° C above the dew point.
  • the reheated flue gas temperature should be greater than 70 ° C.
  • the reheating heat source can come from the original flue gas, whose temperature is between 130-160 ° C. After the reheating, the desulfurized flue gas is sent to the chimney and exhausted after being pressurized.
  • the device for implementing the above method includes at least one desulfurization tower including a SO 2 absorption section, an ammonium sulfite oxidation section, an ammonium sulfate solution concentration section, a water washing section and a defogging section;
  • An ammonium sulfate crystallization tank connected to the outlet of the concentrated ammonium sulfate solution at the lower part of the concentration section through a pipeline; an ammonium sulfate liquid-solid separator connected to the ammonium sulfate crystallization tank through a pipeline;
  • An ammonium sulfate solution circulation tank connected to the dilute ammonium sulfate outlet of the oxidation section and the mother liquid outlet of the separator through a pipeline;
  • a circulation pump connected to the circulation tank through a pipeline, and the outlet of the circulation pump is connected to the dilute ammonium sulfate solution inlet provided on the upper part of the ammonium sulfate solution concentration section;
  • An absorption liquid circulation pump connected through a pipeline to an absorption liquid outlet provided at the bottom of the oxidation section and an absorption liquid inlet provided at the upper portion of the absorption section;
  • the flue gas containing so 2 is reacted in the desulfurization tower with the absorption solution (mixed solution of ammonium sulfite) entering the desulfurization tower, so that the S0 2 in the flue gas generates an ammonium sulfite solution with a concentration of 0.1 to 5% (wt),
  • the ammonium sulfite solution is then contacted with the air entering the desulfurization tower and is oxidized into an ammonium sulfate solution.
  • the ammonium sulfate solution is contacted with the high temperature flue gas entering the desulfurization tower.
  • the ammonium sulfate solution is concentrated by using the heat of the high temperature flue gas, and the concentrated sulfuric acid
  • the ammonium solution is sent to an ammonium sulfate liquid-solid separator, and the separated solid ammonium sulfate is dried in an ammonium sulfate dryer to obtain a finished ammonium sulfate, which can be used as a general chemical fertilizer;
  • the method and device of the present invention integrate the functions of SO 2 absorption in flue gas, oxidation of ammonium sulfite, concentration of ammonium sulfate solution, water washing and defogging ( ⁇ ), convenient operation, and the investment cost is the same as that of the prior art. Under the conditions of processing capacity, it can be reduced by 10 ⁇ 30%, and the energy consumption is low. The waste heat of high temperature flue gas is fully utilized, and the steam consumption can be reduced by 90%.
  • the desulfurization efficiency is very high, in which the concentration of SO 2 in the flue gas can be reduced to less than 10 to 100 ppm, and the quality of the obtained ammonium sulfate conforms to the national fertilizer grade standard, and the nitrogen content is 20.5 to 21%, which can be used as agricultural fertilizer .
  • FIG. 1 is a flowchart of the present invention.
  • Figure 2 shows the structure of the desulfurization tower.
  • FIG. 3 is a schematic diagram of a vertical partition plate and a horizontal partition plate.
  • the device of the present invention includes:
  • a desulfurization tower 6 including an S0 2 absorption section 63, an ammonium sulfite oxidation section 61, an ammonium sulfate solution concentration section 62, a water washing section 64 and a demister section 65;
  • An ammonium sulfate crystallization tank 9 connected to the concentrated ammonium sulfate solution outlet 6201 provided at the lower portion of the liquid concentration section 62 through a pipeline 9;
  • An ammonium sulfate liquid-solid separator 13 connected to the ammonium sulfate crystallization tank 9 through a pipeline, and a centrifuge may be preferred;
  • An ammonium sulfate solution circulation tank 12 is connected to the dilute ammonium sulfate outlet 6101 of the oxidation section 61 and the mother liquid outlet 1301 of the separator 13 through pipelines, respectively;
  • a circulation pump 10 connected to the circulation tank 12 through a pipeline, and the outlet of the circulation pump 10 is connected to the dilute ammonium sulfate solution inlet 6202 provided on the upper part of the ammonium sulfate solution concentration section 62;
  • An absorption solution outlet 6301 provided at the lower portion of the absorption section 63 and an ammonium sulfite solution inlet 6102 of the oxidation section 61 are connected to the ammonium sulfite delivery line 5;
  • An absorption liquid circulation pump 7 connected to the absorption liquid outlet 6103 provided at the bottom of the oxidation section 61 and the absorption liquid inlet 6302 provided at the upper portion of the absorption section 63 through a pipeline, respectively; 7
  • An ammonium sulfate dryer 14 connected to the liquid-solid separator 13 through a pipeline may be preferably a fluidized bed dryer
  • the present invention further includes:
  • a reheater 2 connected to the desulfurization tower 6 through a pipeline for raising the temperature of the purified flue gas; a filter 4 connected to the bottom of the desulfurization tower 6 through a pipeline for filtering ammonium sulfate;
  • the drying fan 15 at the rear end of the dryer 14 and the outlet of the drying fan 15 are connected to the crystallization tank 9 so that the dryer 14 can be operated under negative pressure.
  • the dried hot air enters the crystallization tank 9 and the fine ammonium sulfate particles entrained in the hot air are removed. Then enter the desulfurization tower 6. In this way, the present invention will not generate additional exhaust gas.
  • the desulfurization tower 6 mentioned above is a vertical tower, which includes an ammonium sulfite oxidation section 61, an ammonium sulfate concentration section 62, a S0 2 absorption section 63, a water washing section 64, and a demister from the bottom to the top.
  • a flue gas inlet 66 is provided at the lower part of the desulfurization tower 6, a purge gas outlet 67 is provided at the top of the desulfurization tower 6, an air inlet 68 for oxidation is provided at the side of the oxidation section 61, and a process water inlet 69 is provided at The upper part of the water washing section 64; the mentioned oxidation section 61 is provided with a vertical partition plate 6104 and a horizontal partition plate 6105, as shown in FIG.
  • the transverse partition plate 6105 is a sieve hole plate, the sieve holes are evenly distributed, and the sieve hole diameter d.
  • one end of the vertical partition plate 6104 is provided with a channel hole 6106, so that the liquid flow path is 3 ⁇ 4 serpentine, and the ammonium sulfite inlet 6102 is set on one side of the oxidation section 61, The dilute ammonium sulfate outlet 6101 is set on the other side.
  • the ammonium sulfite enters the oxidation section 61 from one end, and leaves the tritium oxidation section 61 from the opposite end, so that the unoxidized ammonium sulfite solution and the oxidized ammonium sulfate solution are separated as much as possible. Back to mix.
  • the flue gas inlet 66 is provided above the vertical partition plate 6104 and the horizontal partition plate 6105, and the oxidation air inlet 68 is provided below the horizontal partition plate 6105 of the oxidation section 61.
  • a first partition plate 6203 with a gas distribution device and a liquid collector is provided between the ammonium sulfate concentration section 62 and the oxidation section 61, and a dilute ammonium sulfate solution inlet 6202 is provided in the upper part of the concentration section 62.
  • An outlet 6201 is provided in the lower part of the concentration section 62, and an ammonia gas inlet 6204 is provided above the concentration section 62.
  • a gas distribution device and a liquid are provided between the above-mentioned S0 2 absorption section 63 and the ammonium sulfate concentration section 62.
  • the second partition plate 6303 of the collector and the absorption section 63 are filled with a vapor-liquid contact element 6304.
  • the vapor-liquid contact element 6304 can be preferably a sieve plate type or a packing type.
  • a large-pore sieve plate is disclosed with a hole diameter of 10-25 mm and an opening ratio of 15-25%, which is particularly suitable for the situation of the present invention.
  • structured packing with a specification of 50-150m 2 / m 3.
  • the filling height of the packing is generally 2-5m, and a suitable height is 3-4m.
  • a large-pore screen is used, generally 2-5 pieces, suitably 3-4 pieces.
  • An absorption liquid inlet 6302 is provided in the upper part of the absorption section 63, and an absorption liquid outlet 6301 containing ammonium sulfite is provided in the lower part of the absorption section 63. It is connected to the ammonium sulfite inlet 6102 of the oxidation section 61 through a connection line 5.
  • the washing section 64 is filled with polypropylene plate corrugated structured packing.
  • the model can be 125 or 250m 2 / m 3 , and the filling height is 0.3-0.6m.
  • the defogging section 65 is filled with 250-500m 2 / m 3 structured corrugated packing with a degree of 0.3-0.6m.
  • the low sulfur-containing flue gas enters the desulfurization tower 6 from the flue gas inlet 66, passes through the first partition plate 6203, and enters the concentration section 62, and performs heat and mass exchange with the dilute ammonium sulfate solution from the ammonium sulfate solution circulation tank 12, The flue gas is cooled and humidified, and the dilute ammonium sulfate solution is concentrated. Then the flue gas passes through the second partition plate 6303 and enters the absorption section 63, and comes into countercurrent contact with the absorption liquid sprayed down from the top of the absorption section 63. S0 in the flue gas 2 is absorbed, and ammonium sulfite is generated.
  • the purified flue gas passes through the water washing section 64 and the defogging section 65, and then exits the desulfurization tower 6 and exchanges heat with the high temperature flue gas in the reheater 2. Empty by chimney;
  • ammonium sulfite solution mentioned above enters the oxidation section 61 through the connection line 5 and undergoes an oxidation reaction with the air entering the oxidation section 61 to generate ammonium sulfate, which flows into the circulation tank 12 and is sent by the pump 10 to the concentration section 62.
  • a 220T / h coal-fired thermoelectric boiler has a flue gas flow of 250,000 Nm 3 / hr, a S0 2 content of 1500mg / Nm 3 , a flue gas dust content of 80mg / Nm 3 , and a flue gas temperature of 140 ° C.
  • the desulfurization tower 6 has a diameter of 6 m and a height of 28 m.
  • the reheater 2 is of a heat pipe type. After the flue gas passes through the reheater 2, the temperature drops to 110 ° F. and enters the desulfurization tower 6. When Depart from the desulfurization tower, desulfurizing tail gas S0 2 content of 20mg / Nm 3, H 3 content lmg / Nm 3, the water content through droplets of 96mg / Nm 3.
  • the absorption section uses 100m 2 / m 3 polypropylene structured porous plate corrugated packing, the absorption liquid flow rate is 100m 3 / hr, and the ammonium sulfate content is 7.5% (wt).
  • the ammonium sulfite concentration is 0.6% (wt ).
  • the ammonia feed rate is 1.45 according to N / S, and the BP is 145 kg / hr.
  • the amount of water added was 11.75 m 3 / r.
  • the ammonium sulfate production was 780 kg / hr, of which the ammonium sulfate content was 97.8%, which was equivalent to a nitrogen content of 20.8%.
  • a 670T / h thermal power unit namely 200MW, burns coal with a sulfur content between 1.5-2.0%.
  • the flue gas flow is 800,000 Nm 3 / hr, and the S0 2 content is 4200mg / Nm 3 .
  • the device has 3 electric fields, the dust content of the flue gas is 200mg / Nm 3 , and the flue gas temperature is 145 ° F.
  • the desulfurization tower 6 has a diameter of 10 m and ⁇ is 30 m.
  • the reheater 2 is a rotary heat storage type. After the flue gas passes through the reheater, the temperature drops to 116 ° C and enters the desulfurization tower. Leaving the desulfurization tower, desulfurizing tail gas S0 2 content of 34mg / Nm 3, NH 3 content of lmg / Nm 3, Shuimo content of 125mg / Nm
  • the absorption section was filled with 125m 2 / m 3 polypropylene structured porous plate corrugated packing, the absorption liquid flow was 400m 3 / hr, and the ammonium sulfate content was 17.3% (wt). When leaving the absorption section, the ammonium sulfite concentration was 1.6% ( wt).
  • the amount of water added was controlled at 39.5 m 3 / hr.
  • the output of ammonium sulfate is 7070 kg / hr, and the ammonium sulfate content is 98.0%, which is equivalent to the nitrogen content of 21.0%.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Treating Waste Gases (AREA)

Abstract

L'invention concerne un procédé et un dispositif pour éliminer et récupérer du SO2 dans des fumées, ledit procédé comprenant les étapes suivantes: 1) les fumées à faible teneur en soufre réagissent tout d'abord avec une solution aqueuse d'ammoniaque, produisant ainsi une solution de sulfite d'ammoniaque, le rapport molaire ammoniaque/soufre étant compris entre 1,3 et 1,8, et le rapport en volume gaz/liquide étant compris entre 2000 et 5000; 2) la réaction d'oxydation entre le sulfite d'ammoniaque et l'air produit une solution de sulfate d'ammoniaque; 3) la solution de sulfate d'ammoniaque est mise en contact avec les fumées chaudes puis la solution de sulfate d'ammoniaque dont l'eau s'est évaporée est acheminée à un cristalliseur pour être traitée dans un organe de fertilisation de sulfate d'ammoniaque. Le dispositif selon invention comprend une tour de désulfuration qui présente une section d'adsorption de SO2, une section d'oxydation de sulfite d'ammoniaque, une section de condensation de solution de sulfate d'ammoniaque, une section de lavage et une section de déshumidification. Ledit dispositif est facile à utiliser et ses coûts sont réduits de 10 à 30 %. La consommation de vapeur peut être réduite de 90 % et la concentration de SO2 dans les fumées peut être réduite à une valeur inférieure à 10-100 ppm. La qualité du sulfate d'ammoniaque obtenu répond aux normes nationales.
PCT/CN2002/000819 2002-09-09 2002-11-18 Procede et dispositif pour eliminer et recuperer du so2 dans des fumees WO2004022205A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU2002349435A AU2002349435A1 (en) 2002-09-09 2002-11-18 Method and apparatus for eliminating and recovering s02 from fume

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CNB021369062A CN1178735C (zh) 2002-09-09 2002-09-09 烟气中so2的脱出和回收方法及装置
CN02136906.2 2002-09-09

Publications (1)

Publication Number Publication Date
WO2004022205A1 true WO2004022205A1 (fr) 2004-03-18

Family

ID=4748812

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2002/000819 WO2004022205A1 (fr) 2002-09-09 2002-11-18 Procede et dispositif pour eliminer et recuperer du so2 dans des fumees

Country Status (3)

Country Link
CN (1) CN1178735C (fr)
AU (1) AU2002349435A1 (fr)
WO (1) WO2004022205A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101429070B (zh) * 2008-12-05 2011-05-04 聊城鲁西化工第四化肥厂 利用锅炉烟气及硫酸尾气生产氮磷钾复合肥的方法
CN105771607A (zh) * 2016-05-14 2016-07-20 张波 一种氨法脱硫超低排放系统和工艺
US10207220B2 (en) * 2017-03-15 2019-02-19 Jiangnan Environmental Protection Group Inc. Method and apparatus for removing sulfur oxides from gas

Families Citing this family (31)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1321723C (zh) * 2003-09-17 2007-06-20 镇江市江南环保设备研究所 氨法脱除回收烟气中二氧化硫的方法
CN100428979C (zh) * 2005-06-28 2008-10-29 江苏世纪江南环保有限公司 塔内结晶氨法脱硫工艺及装置
CN100395006C (zh) * 2005-06-28 2008-06-18 江苏世纪江南环保有限公司 空塔型氨法脱硫工艺及装置
CN1310699C (zh) * 2005-08-16 2007-04-18 孙克勤 平流吸收塔集成式烟气脱硫装置
CN100486676C (zh) * 2005-11-23 2009-05-13 中国石油天然气股份有限公司 一种烟气氨法脱硫并副产亚硫酸铵的方法
CN101157004B (zh) * 2007-08-02 2010-08-18 武汉凯迪电力环保有限公司 湿式氨法烟气脱硫产物的喷雾干燥和多级冷却工艺及其系统
CN101433804B (zh) * 2008-12-02 2011-04-20 中冶焦耐工程技术有限公司 气体再循环式的湿式氧化法脱硫液再生工艺及装置
CN101601964B (zh) * 2009-06-03 2012-01-11 李鹏举 一种氨法烟气脱硫装置
CN101698134B (zh) * 2009-10-27 2012-05-02 德阳市南邡再生资源有限公司 一种二氧化硫高温尾气的处理方法
CN102211762B (zh) * 2010-04-06 2012-11-21 山东三维石化工程股份有限公司 用亚硫酸氢铵做中间体的制硫及尾气处理方法
CN101879379B (zh) * 2010-07-12 2012-05-23 西安交通大学 一种溴化锂循环回收脱硫系统排气含水的系统及方法
CN102343211A (zh) * 2011-10-08 2012-02-08 湖北双环科技股份有限公司 燃烧锅炉烟气脱硫方法
CN102614735A (zh) * 2012-04-13 2012-08-01 大连华氏流体设备有限公司 一种烟气脱硫与废弃物回收再利用的装置和方法
CN103537108B (zh) * 2013-10-23 2015-07-29 中冶长天国际工程有限责任公司 一种蒸发含亚硫酸铵的硫酸铵溶液的方法及其系统
CN105749716B (zh) * 2013-12-03 2018-06-19 张波 一种脱硫脱硝系统的脱硫脱硝方法
CN103585874B (zh) * 2013-12-03 2016-05-04 张波 脱硫脱硝系统及其脱硫脱硝方法
CN105771597A (zh) * 2016-04-05 2016-07-20 石家庄市正定金石化工有限公司 一种大炉尾气进行氨法脱硫的工艺
CN105833704A (zh) * 2016-05-14 2016-08-10 张波 一种氨法脱硫抑制亚硫酸铵氧化的系统及工艺
CN106178859A (zh) * 2016-08-22 2016-12-07 江苏中圣高科技产业有限公司 用于硫磺回收尾气焚烧炉的烟气脱硫消雾霾系统及方法
CN106925078A (zh) * 2017-03-15 2017-07-07 上海交通大学 一种脱硫超净再热排放系统及基于该系统的方法
CN107213785B (zh) 2017-05-25 2020-08-07 江苏新世纪江南环保股份有限公司 一种fcc尾气氨法脱硝脱硫除尘的方法及装置
CN107213769B (zh) 2017-05-25 2019-09-20 江苏新世纪江南环保股份有限公司 一种分室加氨的氨法脱硫方法及装置
JP6582286B2 (ja) 2017-06-14 2019-10-02 ジァンナン・エンバイロメンタル・プロテクション・グループ・インコーポレイテッドＪｉａｎｇｎａｎ Ｅｎｖｉｒｏｎｍｅｎｔａｌ Ｐｒｏｔｅｃｔｉｏｎ Ｇｒｏｕｐ Ｉｎｃ． アンモニアに基づく脱硫装置のための自動アンモニア添加システム及び方法
CN107485994A (zh) * 2017-08-22 2017-12-19 张波 炭素行业脱硫除尘超低排放一体化装置
CN108722163B (zh) 2017-09-07 2019-06-07 江苏新世纪江南环保股份有限公司 一种氨法脱硫控制吸收过程气溶胶产生的方法
CL2018002442A1 (es) 2018-04-13 2018-10-12 Jiangnan Environmental Prot Group Inc Método y dispositivo para oxidar una solución para desulfuración de amoníaco.
CN116510513A (zh) 2018-04-13 2023-08-01 江苏新世纪江南环保股份有限公司 氨法脱硫溶液的氧化方法及装置
CN110732227B (zh) 2018-07-20 2023-02-21 江南环保集团股份有限公司 一种酸性气处理的方法和装置
CN109499289A (zh) * 2018-11-07 2019-03-22 襄阳泽东化工集团有限公司 一种脱硫尾气的处理方法及装置
CN109647163B (zh) * 2018-12-21 2021-10-19 大田县伊鑫新型材料有限公司 一种干法水泥窑氨法半干法脱硫装置
CN111957183A (zh) 2019-12-26 2020-11-20 江苏新世纪江南环保股份有限公司 一种改进的氨法脱硫控制吸收过程气溶胶产生的方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS4930290A (fr) * 1972-07-14 1974-03-18
JPS51121955A (en) * 1975-04-16 1976-10-25 Nippon Kokan Kk <Nkk> Method of liquid type oxidation treatment of exhaust liquid mixture
CN1194176A (zh) * 1997-03-21 1998-09-30 沈阳环境科学研究所 一种利用化学方法吸收清除烟气中二氧化硫的新工艺
CN1359742A (zh) * 2001-12-07 2002-07-24 罗经宇 采用斜孔板塔处理烟气的方法及装置

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS4930290A (fr) * 1972-07-14 1974-03-18
JPS51121955A (en) * 1975-04-16 1976-10-25 Nippon Kokan Kk <Nkk> Method of liquid type oxidation treatment of exhaust liquid mixture
CN1194176A (zh) * 1997-03-21 1998-09-30 沈阳环境科学研究所 一种利用化学方法吸收清除烟气中二氧化硫的新工艺
CN1359742A (zh) * 2001-12-07 2002-07-24 罗经宇 采用斜孔板塔处理烟气的方法及装置

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101429070B (zh) * 2008-12-05 2011-05-04 聊城鲁西化工第四化肥厂 利用锅炉烟气及硫酸尾气生产氮磷钾复合肥的方法
CN105771607A (zh) * 2016-05-14 2016-07-20 张波 一种氨法脱硫超低排放系统和工艺
US10207220B2 (en) * 2017-03-15 2019-02-19 Jiangnan Environmental Protection Group Inc. Method and apparatus for removing sulfur oxides from gas

Also Published As

Publication number Publication date
AU2002349435A1 (en) 2004-03-29
CN1408464A (zh) 2003-04-09
CN1178735C (zh) 2004-12-08

Similar Documents

Publication Publication Date Title
WO2004022205A1 (fr) Procede et dispositif pour eliminer et recuperer du so2 dans des fumees
CN200998639Y (zh) 浓缩结晶和吸收氧化组合式氨法脱硫塔
AU2020413277B2 (en) Controlling aerosol production during absorption in ammonia-based desulfurization
CN101579602B (zh) 一种节能高品质硫酸铵回收的氨法脱硫工艺
CN103303877B (zh) 多气源低浓度so2烟气综合回收制酸工艺流程
CN100460045C (zh) 一种处理废气中SOx的方法
CA2629987C (fr) Procede de desulfurisation des gaz de combustion faisant appel au peroxyde d&#39;hydrogene
CN102850092B (zh) 一种氨法烟气脱硫生产硫铵化肥的工艺及装置
WO2014172860A1 (fr) Procédé et appareil de traitement de gaz résiduaire acide à l&#39;aide de gaz de combustion par traitement à l&#39;ammoniac
CN101085410A (zh) 一种逆流烟气二氧化硫回收方法和装置
CN100534583C (zh) 以氨为原料回收烟气中so2的方法和装置
CN100506351C (zh) 一种回收烟气中二氧化硫生产硫铵的方法和装置
CN201026440Y (zh) 一种吸收、氧化和浓缩组合式脱硫塔
CN101757844B (zh) 一种氨法烟气脱硫方法及其设备
CN103977689B (zh) 两步加碱再生亚硫酸钠法脱除烟气中二氧化硫装置与方法
CN110314505B (zh) 一种碱行业干铵工段含氨尾气处理装置及其处理方法
CN106621768A (zh) 酸性气体硫回收尾气的氨法脱硫一体化净化装置及方法
CN101433798A (zh) 塔外氧化提浓的高效湿式氨回收法脱硫方法及其装置
CN107789965A (zh) 一种氨‑镁组合烟气脱硫及副产鸟粪石的方法
CN105271132A (zh) Swsr-6硫磺回收工艺及装置
US3172725A (en) Production of sulfuric acid
CN108686478A (zh) 一种烟气脱硫及脱硫废水的处理方法与装置
CN102887529A (zh) 一种硫酸铵生产系统及其制备方法
CN206549426U (zh) 一种氯酸氧化烟气脱硫、脱硝一体化装置
CN205948622U (zh) 新型烟气脱硫消雾霾系统工艺装置

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NO NZ OM PH PL PT RO RU SC SD SE SG SI SK SL TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR IE IT LU MC NL PT SE SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
122 Ep: pct application non-entry in european phase
NENP Non-entry into the national phase

Ref country code: JP

WWW Wipo information: withdrawn in national office

Country of ref document: JP