WO2002018270A1 - Procede de decomposition du gypse en dioxyde de soufre - Google Patents

Procede de decomposition du gypse en dioxyde de soufre Download PDF

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Publication number
WO2002018270A1
WO2002018270A1 PCT/CN2001/000811 CN0100811W WO0218270A1 WO 2002018270 A1 WO2002018270 A1 WO 2002018270A1 CN 0100811 W CN0100811 W CN 0100811W WO 0218270 A1 WO0218270 A1 WO 0218270A1
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WO
WIPO (PCT)
Prior art keywords
preheater
stage
stage cyclone
cyclone preheater
gas
Prior art date
Application number
PCT/CN2001/000811
Other languages
English (en)
French (fr)
Inventor
Yisheng Feng
Jiutian Feng
Xigang Liu
Yurui Wang
Tianbao Lu
Original Assignee
Shandong Lubei Enterprise Group Company
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 Shandong Lubei Enterprise Group Company filed Critical Shandong Lubei Enterprise Group Company
Priority to EA200300328A priority Critical patent/EA007885B1/ru
Priority to AU2001273807A priority patent/AU2001273807A1/en
Priority to US10/363,435 priority patent/US20050100503A1/en
Publication of WO2002018270A1 publication Critical patent/WO2002018270A1/zh

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/02—Oxides or hydroxides
    • C01F11/08—Oxides or hydroxides by reduction of sulfates
    • 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
    • C01B17/501—Preparation of sulfur dioxide by reduction of sulfur compounds
    • C01B17/506—Preparation of sulfur dioxide by reduction of sulfur compounds of calcium sulfates
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/02—Rotary-drum furnaces, i.e. horizontal or slightly inclined of multiple-chamber or multiple-drum type
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
    • F27B7/2016—Arrangements of preheating devices for the charge
    • F27B7/2025—Arrangements of preheating devices for the charge consisting of a single string of cyclones
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D2017/009—Cyclone for separating fines from gas
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • the invention relates to a method and a device for producing sulfur dioxide, and particularly to a method and a device for producing sulfur dioxide by gypsum decomposition. Background technique
  • the CN106598B patent disclosed that 600-750 "C flue gas was used to preheat and dry the gypsum to a total water content of 4-6%, and then compounded, decomposed, and calcined to prepare sulfur dioxide and cement clinker.
  • the Linz chemical plant in Austria has proposed to install a four-stage vertical cylinder preheater at the end of the rotary kiln.
  • the device dehydrates and cleans the washed phosphogypsum (addition amount of 70%) to 6-8% water content, and prepares it with natural anhydrous gypsum, sand, coke, etc. which are separately dried and ground.
  • the four-stage vertical cylinder preheater preheats the material at a temperature of 650-700 ° C, and enters the rotary kiln for decomposition and calcination.
  • the temperature of the gas entering the preheater at the end of the kiln is 800-850 ° C, and the temperature of the gas discharged from the preheater is 425-430%.
  • this preheater reduces the heat energy consumption to a certain extent, it still has the disadvantages of low heat exchange efficiency of the vertical tube preheater, easy crusting and clogging in the tube, low heat utilization of the rotary kiln, and low unit volume production of the kiln; It is used for the low concentration of SO 2 in acid gas. Generally, only one rotation and one suction process can be used at about 7-9% (volume concentration), which causes defects such as large sulfur gas system gas treatment capacity and low production capacity. Disclosure of invention
  • the purpose of the present invention is to provide a method for decomposing and producing sulfur dioxide by gypsum with high utilization rate of thermal energy, more simplified process flow, and capable of obtaining higher concentration of sulfur dioxide;
  • Another object of the present invention is to provide an apparatus for decomposing gypsum to produce sulfur dioxide.
  • the invention relates to a method for producing sulfur dioxide by decomposition of gypsum
  • the method includes: directly mixing the newly input gypsum raw material with the gas discharged from the second-stage cyclone preheater, entering the first-stage cyclone preheater, and discharging sulfur dioxide gas from the top;
  • the solid materials are moved down by gravity, mixed with the gas discharged from the third-stage cyclone preheater, and then entered into the second-stage cyclone preheater for preheating separation; the separated solid materials are discharged from the fourth-stage preheater.
  • the gas After the gas is mixed, it enters the third-stage cyclone preheater for preheating separation; the solid materials separated by the third-stage cyclone preheater enter the first-stage preheater, and the exhaust gas discharged from the tail of the rotary kiln is in the fourth-stage preheater. After the medium preheating, it enters the rotary kiln for decomposition and calcination.
  • the temperature of the gas entering the fourth-stage preheater from the kiln tail is 800-900 ° C, and the raw material feed after preheating by the fourth-stage preheater.
  • the temperature of the kiln is 600-720 ° C; among them, the temperature of the exhaust gas from the first stage cyclone preheater is 260-400 ° C, the sulfur dioxide is on a dry basis, and the volume content is 11-14%.
  • the invention also relates to a device for decomposing and producing sulfur dioxide by gypsum.
  • the device comprises a set of four-stage cyclone preheater and a decomposing and calcining rotary kiln.
  • the connection method of the device is as follows: The gas discharged from the second stage cyclone preheater is directly mixed into the first stage cyclone preheater, and the sulfur dioxide gas is discharged from the top. The separated solid material is moved downward by gravity, and then the gas discharged from the third stage cyclone preheater.
  • the separated solid material is mixed with the gas discharged from the fourth-stage preheater and enters the third-stage cyclone preheater for preheating separation;
  • the solid material separated by the first-stage cyclone preheater enters the fourth-stage preheater, and the exhaust gas discharged from the tail of the rotary kiln is preheated in the fourth-stage preheater and then decomposed and calcined.
  • the device for decomposing gypsum and producing sulfur dioxide according to the present invention wherein the fourth-stage preheater is a boiling preheater.
  • the tube of the drawings is to be explained
  • FIG. 1 is a schematic flow chart of an apparatus and a method for producing sulfur dioxide by gypsum decomposition according to the present invention
  • Figure 2 is a schematic diagram of the comprehensive system process for the gypsum decomposition and co-production of sulfur dioxide and cement.
  • FIG. 1 is a part of the device in FIG. 2. The following can be comprehensively described only through a comprehensive description of Figure 2. The present invention is explained.
  • gypsum 16 with a moisture content of 10-25%, coke 17, clay 18, bauxite 19 and the like milled by a ball mill 20 enter a batching bin 21, and the prepared raw meal 11 is preheated with a second-stage cyclone.
  • the gas 9 discharged from the heater is mixed into the first stage cyclone preheater 1 for gas-solid separation.
  • the gas 10 discharged from the top contains 11-14% sulfur dioxide (volume percentage on a dry basis), and the gas temperature is 260-400 ° C. It is sent to the sulfuric acid production section by the fan 27 through the electric precipitator 26 to prepare sulfuric acid.
  • the solid material 12 separated by the first-stage cyclone preheater is mixed with the gas 8 discharged from the third-stage cyclone preheater 3, and then enters the second-stage cyclone preheater for gas-solid separation.
  • the separated solid material 13 is also After mixing with the gas 7 discharged from the fourth-stage preheater, it enters the third-stage cyclone preheater 3 for gas-solid separation.
  • the solid material separated by the third-stage cyclone preheater enters the fourth-stage preheater 4, and the tail gas 6 flowing out of the kiln tail is boiled in the preheater for convective heat exchange and then enters the rotary kiln 5 for decomposition. Calcined to obtain cement clinker. After being cooled by the cooler 22, the cement is ground.
  • the rotary kiln uses coal 23 as fuel, which is sent to the kiln for combustion by fan 24 and coal gun 25.
  • the gypsum with a water content of 24.53% (19.12% of crystal water and 5.41% of adsorbed water) is prepared into raw meal with coke, clay, and bauxite ground by a ball mill at a ratio of 100: 8: 10: 6.
  • the prepared raw material ( 55 tons / hour) is added to the cyclone preheating system, mixed with the gas discharged from the second-stage cyclone preheater (diameter ⁇ 3370mm) at a temperature of 405 ° C, and then entered into the first-stage cyclone preheater. ( ⁇ 2500, two groups) for gas-solid separation.
  • the gas discharged from the top of the first-stage preheater contains 12.1% of S0 2 (dry basis, volume percentage), the gas temperature is 313 ° C, and it is sent to the sulfuric acid production section by the fan through an electrostatic precipitator. The process produces sulfuric acid.
  • the first stage cyclone preheater separates the solid with a temperature of 265 ° C, and then mixes with the gas discharged from the third stage cyclone preheater (0 3650) and enters the second stage cyclone preheater.
  • the solid material with the temperature of 395 ° C after the separation is mixed with the gas of temperature 659 ° C discharged from the fourth stage preheater (0 3650mm), and then enters the third stage cyclone preheater for gas-solid separation .
  • the solid material with a temperature of 515 ° C separated by the third stage cyclone preheater enters the fourth stage preheater and is discharged from the rotary kiln tail.
  • the exhaust gas at a temperature of 854 ° C is boiled in a preheater for convective heat exchange
  • the raw meal at 663 ° C enters a rotary kiln for decomposition and calcination to obtain cement clinker.
  • the rotary kiln uses coal as fuel and is sent to the kiln for combustion by fans and coal guns.
  • the gypsum with a water content of 22.19% (18.95% of crystal water and 3.24% of adsorbed water) was prepared into raw meal with coke, clay, and bauxite milled by a ball mill at a ratio of 100: 8: 10: 6.
  • a mixed gas discharged from the second stage cyclone preheater (03,370 leg) temperature of 423 ° C enters the first stage cyclone preheater (0 2500, two groups) for gas-solid separation.
  • the gas discharged from the top of the first-stage preheater contains 13.1% of S0 2 (dry basis, volume percentage), and the gas temperature is 286 ° C.
  • the separation temperature of the first stage cyclone preheater is 261 °.
  • the solids are mixed with the temperature of 589 ° C discharged from the third stage cyclone preheater (0 3650), and then enter the second stage cyclone preheater for separation.
  • the separated solid materials with a temperature of 403 ° C After mixing with the temperature of 686 ° C discharged from the fourth stage preheater (0 3650mm), it enters the third stage cyclone preheater for gas-solid separation.
  • the solid material with a temperature of 537 ° C separated by the third-stage cyclone preheater enters the fourth-stage preheater, and the exhaust gas at a temperature of 884 ° C discharged from the rotary kiln tail is boiled in the preheater for convective heat exchange Then, the raw material at 685 ° C enters a rotary kiln for decomposition and calcination to obtain cement clinker. After cooling by a cooler, the cement is ground.
  • the rotary kiln uses coal as fuel and is sent to the kiln for combustion by fans and coal guns.
  • the advantages of the present invention are very obvious. Since the present invention adopts a cyclone preheater, materials and gas are in contact with each other for heat exchange, high mass and heat transfer efficiency, and no phenomena such as wall and adhesion of materials.
  • the gypsum with a water content of 10-25% can be directly prepared into raw materials without dehydration. Therefore, the drying process can be omitted, saving investment.
  • the temperature of the preheated material can reach 600-720 ° C.
  • the high temperature of the material entering the kiln can reduce the fuel consumption of the rotary kiln and save energy.
  • the gas The temperature is reduced from 800-900 ° C to 260-400 ° C, which can be directly used to produce sulfuric acid, which reduces heat loss.
  • the invention improves the 50 2 concentration in the exhaust gas to 11-14%. Therefore, sulfuric acid can be produced in a two-turn, two-absorption process, with a total conversion rate of more than 99.5% and an absorption rate of more than 99.95%. Therefore, the present invention has obvious economic and social benefits.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
  • Treating Waste Gases (AREA)
  • Curing Cements, Concrete, And Artificial Stone (AREA)
  • Furnace Details (AREA)

Description

一种用于石膏分解生产二氧化硫的方法及其裝置 技术领域
本发明涉及一种生产二氧化硫的方法及其装置， 特别是涉及一种用 于石膏分解生产二氧化硫的方法及其装置。 背景技术
CN106598B专利曾公开了以 600-750 "C的烟道气预热烘干石膏至总水 量为 4-6% , 尔后配料、 分解、 煅烧， 制取二氧化硫和水泥熟料。
奥地利林茨化工厂曾提出在转窑窑尾安装了四級立筒预热器。 该装 置将洗涤后的磷石膏（掺加量 70%)脱水烘干至含水 6-8%， 与经分别烘干 粉磨的天然无水石膏及砂子、 焦炭等配制成生料， 生料经四級立筒预热 器预热， 物料温度为 650- 700 °C , 进入回转窑分解、煅烧。 窑尾进预热器 的气体温度为 800-850°C， 从预热器排出的气体温度为 425-430%。 该预 热器虽然在一定程度上降低了热能消耗， 但仍存在立筒预热器换热效率 低、 筒内易结皮堵塞等缺点， 回转窑热利用率低， 窑单位容积产量低； 而且用于制酸气体中 S02浓度偏低， 一般在 7-9% (体积浓度）左右 只能 采用一转一吸工艺， 造成制硫酸系统气体处理量大、 生产能力低等缺陷。 发明的公开
本发明的目的在于提供一种热能利用率高、 工艺流程更为简化， 并 可制得较高浓度二氧化硫的用于石膏分解生产二氧化硫的方法；
本发明的另一目的在于提供一种用于石膏分解生产二氧化硫的裝 置。
本发明涉及一种用于石膏分解生产二氧化硫的方法，
该方法包括： 新投入的石膏生料与第二級旋风预热器排出的气体直 接混合后进入第一級旋风预热器， 自顶部排出二氧化硫气体； 被分离的 固体物料靠重力下移， 再和第三級旋风预热器排出的气体混合后， 进入 第二級旋风预热器进行预热分离； 分离后的固体物料又和第四級预热器 排出的气体混合后进入第三級旋风预热器进行预热分离； 由第三級旋风 预热器分离后的固体物料进入第 級预热器， 由回转窑尾部排出的尾气 在第四級预热器中预热后进入回转窑中进行分解煅烧。
按照本发明所述的用于石膏分解生产二氧化硫的方法， 其中， 从窑 尾进入第四級预热器的气体温度为 800- 900 °C，而经四级预热器预热后生 料的进窑温度为 600- 720 °C ;其中， 从第一級旋风预热器中排出气体的温 度为 260- 400 °C， 二氧化硫干基、 体积含量为 11-14%。
本发明还涉及一种用于石膏分解生产二氧化硫的装置， 该装置包括 一組四級旋风预热器和一台分解煅烧回转窑， 所述的装置的连接方式为： 新投入的石膏生料与第二級旋风预热器排出的气体直接混合后进入 第一級旋风预热器， 自顶部排出二氧化硫气体； 被分离的固体物料靠重 力下移， 再和第三級旋风预热器排出的气体混合后， 进入第二級旋风预 热器进行预热分离； 分离后的固体物料又和第四級预热器排出的气体混 合后进入第三級旋风预热器进行预热分离； 由第三級旋风预热器分离后 的固体物料进入第四級预热器， 由回转窑尾部排出的尾气在第四級预热 器中预热后进入回转窑中进行分解煅烧。
按照本发明所述的用于石膏分解生产二氧化硫的装置 其中， 所述 的第四級预热器为一个沸腾式预热器。 附图的筒要说明
图 1 为本发明用于石膏分解生产二氧化硫的装置及其生产方法的流 程示意图；
图 2 为本发明用于石膏分解联产二氧化硫和水泥的综合系统流程示 意图。
图 1为图 2中装置的一部分。 下面仅通过对图 2的综合描述可全面 地说明本发明。
参见图 2， 含水量 10-25%的石膏 16， 与经球磨机 20粉磨的焦炭 17、 粘土 18、 铝矾土 19等进入配料仓 21， 配制好的生料 11与第二級旋风预 热器排出的气体 9混合后进入第一级旋风预热器 1进行气固分离， 从顶 部排出的气体 10中含有 11- 14%的二氧化硫（干基体积百分比），气体温度 为 260- 400 °C， 经电除尘器 26， 由风机 27送往硫酸生产工段制备硫酸。 第一級旋风预热器分离的固体物料 12再和第三級旋风预热器 3排出的气 体 8 混合后进入第二級旋风预热器进行气固分离， 同样分离后的固体物 料 13， 又和第四级预热器排出的气体 7混合后， 进入第三級旋风预热器 3进行气固分离。由第三級旋风预热器分离后的固体物料则进第四級预热 器 4 ,与窑尾流出的尾气 6在预热器中呈沸腾式作对流热交换后进入回转 窑 5中进行分解煅烧， 得到水泥熟料， 经冷却机 22冷却后， 磨制水泥。 回转窑采用煤 23作燃料， 经风机 24、 煤枪 25送入窑内燃烧。
实现本发明的最佳方式
实例 1：
含水量 24.53%的石膏 （结晶水 19.12%、吸附水 5.41%)， 与经球磨机 粉磨的焦碳、 粘土、 铝矾土按 100 :8 : 10 : 6的比例配制成生料。 配制好的 生料 （55吨 /小时） 加入到旋风预热系统， 与第二級旋风预热器 （直径 ø 3370mm) 排出的温度 405 °C的气体混合后， 进入第一級旋风预热器 （ø 2500 ,两组）进行气固分离。从第一級预热器顶部排出的气体中含有 12.1% 的 S02 (干基， 体积百分比）， 气体温度 313°C , 经电除尘器， 由风机送往 硫酸生产工段， 采用两转两吸流程生产硫酸。 第一級旋风预热器分离的 温度为 265 °C的固体， 再和第三級旋风预热器 （0 3650誦） 排出的温度 634°C的气体混合后， 进入第二級旋风预热器进行分离； 同样分离后的温 度 395 °C的固体物料， 又和第四級预热器 （0 3650mm) 排出的温度 659 °C 的气体混合后， 进入第三級旋风预热器进行气固分离。 由第三級旋风预 热器分离后的温度 515 °C的固体物料进入第四級预热器，与回转窑尾排出 的温度 854°C的尾气在预热器中呈沸腾式作对流热交换后， 663 °C的生料 进入回转窑中进行分解煅烧， 得到水泥熟料， 经冷却机冷却后， 磨制水 泥。 回转窑采用煤作燃料， 经风机、 煤枪送入窑内燃烧。
实例 2 :
含水量 22. 19%的石膏 （结晶水 18.95%、吸附水 3.24%)， 与经球磨机 粉磨的焦碳、 粘土、 铝矾土按 100 :8 : 10 : 6的比例配制成生料。 配制好的 生料（58吨 /小时）加入到旋风预热系统，与第二級旋风预热器（0 3370腿） 排出的温度 423 °C的气体混合后，进入第一級旋风预热器（0 2500， 两组） 进行气固分离。 从第一級预热器顶部排出的气体中含有 13.1%的 S02 (干 基， 体积百分比）， 气体温度 286°C， 经电除尘器， 由风机送往硫酸生产 工段， 采用两转两吸流程生产硫酸。第一級旋风预热器分离的温度为 261 °。的固体， 再和第三級旋风预热器 （0 3650隱）排出的温度 589°C的气体 混合后， 进入第二級旋风预热器进行分离， 同样分离后的温度 403 °C的固 体物料， 又和第四級预热器 （0 3650mm) 排出的温度 686 °C气体混合后， 进入第三級旋风预热器进行气固分离。 由第三級旋风预热器分离后的温 度 537 °C的固体物料进入第四級预热器， 与回转窑尾排出的温度 884 °C的 尾气在预热器中呈沸腾式作对流热交换后， 685 °C的生料进入回转窑中进 行分解煅烧， 得到水泥熟料， 经冷却机冷却后， 磨制水泥。 回转窑采用 煤作燃料， 经风机、 煤枪送入窑内燃烧。 工业应用性
本发明的优点是很明显的， 由于本发明采用了旋风式预热器， 物料 与气体接触进行热交换、 传质传热效率高、 无物料桂壁与粘结等现象， 因此本发明对含水量 10- 25%的石膏可以直接配制生料， 不必进行烘千脱 水， 因而可省略烘千工序， 节省投资。
预热后的物料温度可以达到 600-720 °C， 物料进窑温度高， 可以減少 回转窑的燃料消耗， 节约了能源， 而窑尾尾气经四级热交换之后， 气体 溫度由 800-900 °C降至 260-400 °C， 可以直接用于制备硫酸， 減少了热量 的损失。
本发明提高了尾气中的 502浓度达到 11-14%。 因而硫酸可采取两转 两吸流程生产， 总转化率可达 99.5%以上， 吸收率可达 99.95%以上。 所 以本发明具有明显的经济效益和社会效益。

Claims

杈利要求
1、 一种用于石膏分解生产二氧化硫的方法，
其特征在于， 该方法包括： 新投入的石膏生料与第二級旋风预热器排出 的气体直接混合后进入第一級旋风预热器， 自顶部排出二氧化硫气体； 被分离的固体物料靠重力下移， 再和第三級旋风预热器排出的气体混合 后， 进入第二級旋风预热器进行预热分离； 分离后的固体物料又和第四 級预热器排出的气体混合后进入第三級旋风预热器进行预热分离； 由第 三級旋风预热器分离后的固体物料进入第四級预热器， 由回转窑尾部排 出的尾气在第四級预热器中预热后进入回转窑中进行分解煅烧。
2、 根据杈利要求 1所述的方法，
其特征在于， 从窑尾进入第四級预热器的气体温度为 800- 900°C， 而经四 級预热器预热后生料的进窑温度为 600- 720 °C 。
3、 根据杈利要求 1所述的方法，
其特征在于， 从第一级旋风预热器中排出气体的温度为 260-400°C， 二氧 化^^的干基体积含量为 11-14%。
4、 一种用于石膏分解生产二氧化硫的装置，
其特征在于， 该装置包括一組四级旋风预热器和一台分解煅烧回转窑， 所述装置的连接方式为：
新投入的石膏生料与第二級旋风预热器排出的气体直接混合后进入 第一级旋风预热器， 自顶部排出二氧化硫气体； 被分离的固体物料靠重 力下移， 再和第三级旋风预热器排出的气体混合后， 进入第二級旋风 预热器进行预热分离； 分离后的固体物料又和第四級预热器排出的气体 混合后进入第三級旋风预热器进行预热分离； 由第三級旋风预热器分离 后的固体物料进入第四級预热器， 由回转窑尾部排出的尾气在第四級预 热器中预热后进入回转窑中进行分解煅烧。
5、 根据杈利要求 4所述的装置，
其特征在于， 所述的第四級预热器为一个沸腾式预热器。
PCT/CN2001/000811 2000-09-01 2001-05-18 Procede de decomposition du gypse en dioxyde de soufre WO2002018270A1 (fr)

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AU2001273807A AU2001273807A1 (en) 2000-09-01 2001-05-18 A method of decomposing gypsum to sulfur dioxide and the apparatus thereof
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