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工业制硫酸的工艺流程工业制硫酸的工艺流程硫酸是一种广泛应用于工业生产的重要化学品，被广泛用于化肥生产、冶炼、制药等多个领域。
下面将介绍一种常用的工业制硫酸的工艺流程。
首先，硫矿石是制硫酸的主要原料。
硫矿石经过矿石碎磨后，与空气中的氧气反应生成二氧化硫气体。
当然，有时也可使用高纯度的硫粉作为原料。
硫矿石的磨碎是为了增加反应表面积，提高反应速率。
接下来，二氧化硫气体会进入硫磺炉中进行回收。
炉内首先操作是燃烧产生燃烧炉气，将矿石粉末送入烧结器。
在烧结器内，硫矿石首先被加热至160℃，这样可以将矿石中的硫分子升华成为岩芯硫或者岩芯粉。
然后，这些岩芯硫或岩芯粉再通过烟气中炭黑传导的方式将热量传递给炉气。
接下来，矿石中的硫分子会和炉气中的氧气反应生成二氧化硫气体。
这样，硫矿石中的硫就得以转化为硫磺。
在进一步的工艺中，二氧化硫气体会被进一步加工转化为三氧化硫气体SO3。
二氧化硫气体通过CT浓缩和HRSOX过程（冷氧化副硝酸），可以转变为60-62% SO3的SO2-O2混合气体。
这样，得到的气体混合物可以进入SO2-转变反应器，使用催化剂将混合气体中的SO2和O2反应生成SO3。
反应温度一般约为450-500℃，反应压力约为1.3-1.6兆帕。
最后，SO3气体会进入吸收塔与水反应生成硫酸。
在吸收塔中，SO3被与大量的冷却、浓硫酸发生反应，生成硫酸。
这个反应过程是放热反应，反应会产生大量的热量，需要通过冷却器来控制反应温度。
在整个制硫酸的过程中，注意控制反应条件的温度、压力和催化剂的使用，以确保反应的高效率和安全性。
此外，对于产生的废气和废水也要进行环境保护处理。
总之，工业制硫酸的工艺流程主要包括矿石粉碎、硫磺回收、SO2转变为SO3和SO3与水反应生成硫酸等步骤。
这个工艺流程的设计和操作对于提高硫酸产量和质量稳定性至关重要。
酸性气干法制硫酸工艺应用（Acid gas drying process, sulfuricacid, application）Acid gas drying process sulfuric acid application.Txt eat it, eat it is not sin, and then fat people also have the right to fatten! Slim behind, is actually haggard, love your people do not care about your waistline! Try the taste of long food, even if it is a kind of beauty! The most terrible thing about losing weight is not hunger, but the fact that you are not hungry, but you always feel that you must eat something before you are practical. This article is contributed by huogodluntanPdf documents may experience poor browsing on the WAP side. It is recommended that you first select TXT, or download the source file to the local view.54?Petrochemical environmental protection, ENVIRONMENTAL, PROTECTION, IN, PETROCHEMICAL, INDUSTRY2006 volume second, issue twenty-ninthAcid gas drying process, sulfuric acid, applicationFeng Fengquan 1, Yao Xuelong 2(1. China Petroleum Chemical Co Jingmen branch, Hubei Jingmen 448039; 2. Sinopec Nanhua Design Institute, Jiangsu Nanjing 210048)pickThe process design features, start-up and operation of sulphuric acid plant with 50 kt / A acid dry gas process in Jingmen branch are introduced:Problems and solutions. Sour gas; acid; device; characteristics of raw materials; design and operation keywords:Sinopec Corporation Jingmen branch of 50 kt / a sulfuric acid plant is to exhaust in the process of petroleum acid gas as raw material, is the first large dry hydrogen sulfide acid plant, a total investment of 39 million yuan. The device by the Design Institute of Nanhua and China Petroleum Chemical Co through the review, undertaken by Jingmen petrochemical construction company, the key equipment of acid by professional manufacturers 7, July 2004 to complete the final delivery and ready to start in the 27 month, once a day to drive the success of feeding. The car, opened up a new way for the treatment of acid gas production in petrochemical industry in the process of petroleum gas governance, to solve the Jingmen branch of the sulfur recovery unit for a long time the sulfur recovery rate is low, the environmental pollution problems. The first half of 2005 unitoperahon but because of the presence of some equipment, 141 days, 93% production of acid 12 KT, each week on a ring of time to reach the national emission monitoring, the average sulfur dioxide containing 622 mg / m3, Paul two grade discharge standard. 1 the composition and characteristics of sour gas in refinery, because hydrogen sulfide is an acid gas, so the mixed gas containing hydrogensulfide is called sour gas in refinery. Its composition and characteristics are shown in table 1:Table 1 components,% V) (normal values for acid gas composition data) (CO2, 20~30, NH3, <1, hydrocarbon, <1, H2, S, 60~70)(2) the concentration of acid gas is unstable. Because of the different concentration of different hydrogen sulfide desulfurization device, coupled with the change of operating conditions, the hydrogen sulfide concentration is usually a variation, normally containing hydrogen sulfide is 60% ~ 70%, 40% ~ 80% fluctuations in the non normal. (3) the flow of acid gas is unstable. Because the acid gas with liquid is transported through long distance pipeline, the liquid seal is formed at the low point. (4) easy to carry hydrocarbon. Under normal circumstances, the acid gas containing hydrocarbon but not more than 1% bodies) in refinery operation is not stable when containing large amounts of hydrocarbons (3%, sometimes higher) at once into the furnace burning (, produce a lot of heat in the furnace temperature and consume large amounts of oxygen and hydrogen sulfide under anoxic conditions easy to produce Claus reaction of sulfur, blocking the cooling tower nozzle, influence of electric demister's normal operation, the process of gas purification section of temperature and water content does not meet the technological requirements. (5) easy to carry ammonia. Because the liquid hydrocarbon desulfurization agent is two ethanol ammonia sour water stripping ammonia desulfurization in raw materials, in the acid gas device operating under the condition of unbalanced is easy with ammonia, and ammonia nitrogen oxide dissolved in dilute sulfuric acid, that is increased by dilute sulfuric acidcomponent complexity and corrosion resistance the pipeline of equipment. (6) the raw material gas hydrogen sulfide contains two hydrogen atoms, which produces water vapor in the process of burning and affects the acid concentration balance. Therefore, the dry process acid is used to remove the water in the purification section. The 2 device characteristics of Jingmen branch and Nanhua Institute will design several decades after(1) toxic, flammable and explosive. Hydrogen sulfide is a colorless, smelly egg flavor, intense nerve toxic gas, when high concentrations can cause respiratory arrest and death. The maximum allowable concentration of hydrogen sulfide in air is 10 mg / m3, melting point is 82.9 DEG C, boiling point is pure H2 S, and 260 DEG C is stipulated by the state. Its explosive pole (point: 60 DEG C, limited to: 3% ~ 45.5%). FourReceived date: 2005 - 7 - 19 Author: Feng Fengquan, engineer. Engaged in environmental protection, production and management of twenty men, for many years, is the Jingmen branch of sulfuric acid plant operating procedures written and device start of the 0724 - 227049613971866187 conductor. Contact number: E - mail:ll19770605@ 163. comSecond issueFeng Feng congruent, acid air dry process, sulfuric acid, application55?The sulphuric acid plant is designed by combining the concepts of reducing investment and occupying an area, saving energy, reducing consumption, protecting environment and convenient operation, and taking into account the characteristics of hydrogen sulfide producing acid. The 2.1 device latent sulfur acid gas in Jingmen Petrochemical scale in 2001 amounted to 8 kt / a (CO production of sulfuric acid is about 2.5 T / a) with the Jingmen branch, after several years of deep processing, increase the processing capacity of crude oil and petroleum product quality index upgrade, Jingmen branch of the design scale of sulphuric acid plant 50 kt / A. 2.2 using two process "two dry 3 + 1 acid method" four transformation and efficient model S108M) (catalyst, improve the utilization rate of sulfur, the total conversion rate of more than 99.6%. Solve the sulfur recovery unit for a long time, low sulfur recovery rate of only 82%) (environmental pollution problems). The 2.3 device controlled rate device for implementing DCS control in the buffer tank and the incinerator installed at the hydrogen sulfide concentration measurement alarm, on-site monitoring of leakage of hydrogen sulfide, and hydrogen sulfide concentration in the environment in the DCS display, to ensure the safety of operator device; 2 guide analyzer distribution adjustment; absorption tower acid pipeline anode protection SO. Two level converter entrance 2.4 additional electric heating furnace for "dry" acid catalyst on the moisture content in the process gas more stringent requirements, if the individual use of heating furnace for heating the catalyst, one-time investment is relatively large, after the start of the idle equipment. (used in design, one section and four section are respectively provided with 550 kW five group (360) electric heating furnace can not only solve the construction inconverter burn kW group three) and baking catalyst temperature rising problem, but also to meet a 42 period of catalyst ignition temperature when using electric heating remedies in the raw material of low load can not to solve the acid gas conversion section, hours of reaction heat problems, improve equipment operation rate. 2.5 SO2 main fan driven by steam turbines to reduce power consumption due to corrosion of the medium pressure steam boilers and other equipment to produce 3.82 MPa waste heat boiler device, and the device around and no steam pipeline network, if a medium pressure steam pipeline and the whole plant is 5 ~ 8 per hour will be sent to the t steam pipe network, long-distance transportation steam quality will decline. For this purpose, a steam turbine is designed to drive the SO2 fan. When the acid gas load is low and the steam produced is less, the SO2 fan driven by the motor can be driven when the steam turbine is not driven, and the steam produced by the device is reduced to 1 MPa by using a temperature reducing and reducing device and is fed into the pipe network. Thus, when the unit load is large, the steam drives the SO2 wind function to reduce the energy consumption, and when the device is loaded, the steam has a place to go, so that the flexibility can be seen.2.6A complementary heat exchange process is adopted, and the third and fourth sections of the outlet heat are crossed and complementaryCold gas converter first and fourth sections, the sections of converter inlet temperature and conversion rate of each segment selection and selection of gas absorption tower is independentof the temperature, optimization and transformation system to the inlet temperature of the relatively independent, transformation system in accordance with the catalyst loading quantity, the total conversion rate is maximum or the implementation of optimization the true sense of the total conversion rate of minimal impact etc., and two absorption tower gas temperature can be combined under the same conditions, in accordance with the minimum total heat transfer area, the most suitable adjustment of the heat exchange system of inlet air temperature,[1] optimal allocation can be carried out optimally.33.1The production principle and process equipment, production principle, the acid gas intake incinerator containing H2 and S and the combustion of air are producedSO2 containing gas, cooling, washing and purifying after drying, 2 and SO O2 in the catalyst three vanadium catalyst () under the action of transformation (oxidation) reaction of SO3, and SO3 in the absorption cycle by spraying 98.3% sulfuric acid and sulfuric acid generation tower. In the process gas (not layer second transformed SO2 catalyst by a vanadium catalyst) transformation to generate SO3, after second times after the absorption of SO3 into sulfuric acid and high conversion rate of SO2 and SO3 absorption rate of the process is called (3 + 1 process).The main chemical reaction for hydrogen sulfide combustion: 2H2S + 3O2 = 2SO2 + 2H2 O + 124Kcal / mol + O2 oxidation of sulfur dioxide: 2SO2 = 2SO3 + 23. 6Kcal / mol three sulfur dioxide absorbed into the acid: SO3 + H2 O = H2 SO4 + 31. 2Kcal / mol above three reactions are exothermic, which emits the first reaction heat up most of the production of steam per ton of sulfuric acid waste heat recovery boiler can produce 1.29 tons (steam). The heat of the second reaction is used to heat the gas to the reaction temperature, and the heat of the third reactions is removed by circulating cooling water due to lower circulating acid temperature. 3.2 the process flow of equipment and equipment are shown in figure 1. 4 device problems in running and the method to solve the early start of the summer of July coincides with the device of air humidity, gas drying effect is poor, one of the difficulties can be overcome by team work, make a successful start device, and the device utilization rate continues to improve.56?stoneoilturnworkringExitProtectprotect2006 volume twenty-ninthFigure 1Equipment process flow1. incineration furnace; waste heat boiler; superheater; cooling tower; circulating pump; washing tower; circulating pump; plate heat exchanger;2.3.4.5.6.7.8.9. electric demister; drying tower; 10. 11. dry cycle trough; 12. circulating pump; 13. cooler; SO2 fan; 14. 15. heat exchanger;16. a converter; a tower; 17. 18. absorption cycle trough; circulating pump; 19. 20. 21. cooler; heat exchanger; 22. two level converter; two absorption tower; circulating pump; cooler; 2324. 25. 26. chimneys4.1Incinerators for incinerator and converter are selected for use in refinery gas ovens, but in design4.3Solve the corrosion leak problem of dilute acid circulating pumpA small two gas valve are respectively DN50 and DN25, that isto use DN25 incinerator at low temperature at ambient temperature to 310 DEG C () is unable to realize the regulation, the gas with the temporary line for DN15 and manual adjustment valve, the temperature reached 350 degrees Celsius when the replacement for the fire to burn the mouth, DN25 furnace baking strictly according to the theoretical curves are. In order to ensure the catalyst drying on the newly built SO2 converter for baking, fan 3000 ~ 4500 m3 / h dry air and the number of the startup control in converter furnace temperature rise +20 degrees highest drying to 280 degrees, which respectively at 110 degrees and 280 degrees at constant temperature for 4 hours, in order to reduce the use of dry acid a tower will throw off. The activation of 4.2 catalyst in the dry converter according to the design requirements of S101T and S108 in plum type catalyst, hot air drying and catalyst will slowly rise to 420 DEG C in the incinerator to introduce acid gas, in the process of switching gas and hydrogen sulfide in the gas must be closed again into the acid gas, otherwise it will generate the Claus reaction. Sulfur. Because of the online SO2 analyzer is not installed, the regulation of acid gas and air control instability, gas flow control device in the change of concentration of SO2, there has been a rapid rise in a period of up to 570 DEG C, immediately shut down a furnace entrance and increasing air flow, a bed temperature is not in when a lower rise, the highest reached 614 degrees, with a catalyst activation experience, after the process of three catalyst activation are parabolic beautiful complete.The device starts third days that dilute acid circulating pump (301 / 1.2, 302 / 1.2) of serious leakage device forced shutdown, after analysis is because the concentration of nitrate acid isrelatively high, in which the sulfuric acid concentration was 12%, concentration of acid ion is 6.8 mg / L, increased the corrosion of metal pump. After the device is shut down, the four metal circulating pumps are replaced with Yixing engineering plastics pumps, and the pump has no quality problems for months.4.4 to solve the leakage problem of dilute acid glass fiber reinforced plastic pipePurification of dilute acid glass steel pipes for non professional installation section, cause the device to start a month every day every day trap leakage, operator's personal safety is threatened. October 2004 will use FRP pipe resistance to acid, alkali, strong oxidizing agent, reducing agent PO corrosion of polyolefin and various organic solvents) (lining tube, dilute acid purification section no leakage phenomenon, found that the cooling tower 20 nozzle clogging 8, in the replacement of glass steel pipes when the reason is gas and acid gas switch and composition of raw materials is not normal to the Claus reaction. 4.5 to solve the problem of flow fluctuation caused by liquid sealing of raw material pipelineIn the design, the sour gas has two 180 m 3 raw material buffer tanks in front of the inlet device, which causes the unstable flow of acid gas and the adverse effects of the slow wave of component wave on the equipment. But in a few days after the device starts repeatedly raw materials fluctuate, but the impact of sulfuric acid is the operation of the device, but also because of the high pressure pipeline, resulting in abnormal liquid hydrocarbon desulfurization device into a vicious spiral. After investigation, the acid gas lines in front of the vulcanizing hydrogen buffer tank are heated until the back ofthe tank57?Petrochemical environmental protection, ENVIRONMENTAL, PROTECTION, IN, PETROCHEMICAL, INDUSTRY2006 volume second, issue twenty-ninthThe more than 400 meters before the incinerator is not accompanied by heat. The liquid slowly before the tank is vaporized and condensed at the bottom of the incinerator to form a liquid seal. To this end, the pipeline is also accompanied by thermal insulation, which determines the material flow rate fluctuations. 4.6 to solve the problem of high temperature washing tower outlet scrubber outlet temperature can not only ensure the polyethylene made of electric demister from harm, but also to maintain water balance device security index and the concentration of sulfuric acid, the design temperature of 37 DEG C. In actual operation, the outlet temperature of the washing tower is 41~43 degrees centigrade. Because of the high content of saturated water in the process gas, the unit can not produce 98% acids. Assistance in equipment suppliersTable 2 air flow / m3? H - 1 acid gas flow / m3? H - 1 acid gas containing 2 S% H incinerator middle temperature / outlet temperature / C / C pressure waste heat boiler steam boiler MPa cooling tower entrance temperature / outlet temperature of cooling tower outlet temperature of C / C / C washing tower the drying tower into the concentration of drying tower acid / gas temperature, absorption tower tower% acid temperature / C atower in the tower temperature / absorption tower on tower C two / C 1554453.5299623655 acid temperature data of 112449113069.081 94.277517177The exchanger is disassembled, found the entrance board for circulating water plugging by stone, welding and other objects, will open the heat exchanger cleaning after reloading, washing tower outlet temperature control can operate in the range of design, device can produce 93% and 98% acid. 5, the main operating conditions and environmental monitoring conditions, through the trial process, the operating conditions are constantly groping and optimization, so that the normal operating conditions of the device are within the scope of process design. According to different production plans, the main operating conditions are shown in table 2.The main process equipment operation project two absorption tower in the tower entrance temperature / pressure / C sulfur dioxide fan K fan SO2 Pa sulfur dioxide concentration, a temperature conversion% upper / lower temperature conversion a / C C / C two upper temperature conversion into two lower temperature / C conversion section temperature / three C three / C lower temperature conversion into four upper temperature / C / C four lower temperature conversion% sulfuric acid concentration, gas monitoring data, m3 / Mg sulfur recovery,% 1162 2.4 6.9408578437483376 38037338198.28786 99.4 data - 2162 - 2.8 7.2429580451491414 42740140794.5 271.7 data 99.7Data 210747105671.761, 1354583.5298633451, 94.497516375Note: data 1 was collected in May 15, 2005 to produce 98%industrial sulphuric acid; data 2 was collected in May 25, 2005 to produce 93% industrial sulphuric acid.According to the data above, the temperature difference between 170 and 8 degrees when the temperature is lower than 410 degrees, and the temperature of four is lower than 380. The problem of incinerator collapse incineration furnace lining with temperature resistance can be more than 1350 DEG C corundum materials exist 66.1 start process, in November 16, 2004, the burning flames appear in front of the furnace shell, furnace lining has been found after the suspension collapsed, unit shutdown 75 days. The analysis shows that the operation platform is added outside the furnace and connected with the furnace body, which greatly constrains the expansion of the furnace body. The lining of the furnace is mostly recovered with old materials and has been running well so far. 6.2 dilute acid reaction tank lined off at the end of June 2005 found the dilute acid reaction tank lining plate off, the analysis may be over temperature to. The design temperature of the tank is 90Used of 5% dilute acid and 6% sodium hydroxide reaction. At the actual temperature, the flow rate and concentration of dilute acid and the temperature of the reaction tank are not shown, and the concentration of sodium hydroxide is 30%,Most factors may lead to over temperature of dilute acid reaction tank, and the condition of process operation has been repaired and changed. 6.3 finished acid pipeline along the tube is made from carbon steel pipeline products take acid and take along the tube, because the product acid high temperature (42 DEG C) and erosion, the pipeline investment with 4 months beganto leak, leakage has been nearly 30 times, a great security risk to other pipeline device to change, cast iron pipe and open another direction. The main problems existing in the 7 device are "the front high, the back low and the middle small"(turn to page sixtieth)60?stoneoilturnworkringExitProtectprotect2006 volume twenty-ninthGasification technology transformation of chemical fertilizer factory of Jinling pressure device in 2003 the introduction of Petrochemical Industries Co Texaco Corp coal water slurry, the coal and petroleum coke substitute naphtha to make fertilizerproduction of raw materials, and put into operation in October 2005. After transformation, the total amount of sulfur containing petroleum coke is 320 KT, which greatly reduces the production cost of chemical fertilizer and reduces the environmental pollution caused by processing sour crude oil. At the same time, 30~40 kt / a high purity hydrogen is added for refining production, and the cost of hydrogen production is only 1/3 of that of the original naphtha. The raw materials such as light oil and oil which replace the chemical fertilizer can be further utilized rationally and aggravated[4] benefit.High sulfur coke, residual oil, asphalt and other products of inferior quality, realize clean production, and to provide electricity, steam, refinery hydrogen and chemical products, to achieve a threefold benefit. With the increasingly stringent environmental protection and social requirements, the IGCC technology with inferior products as raw material will have great promise. The IGCC plant, which is based on inferior petroleum products, will be an important component of the refinery. Now, foreign gasification processes include the use of residuum, bitumen, and Jiao Weiyuan[5] it is growing at a rate of 10% a year.ReferenceThe disadvantage of petroleum coke gasification process is its large investment. According to reports, due to technological advances, investment in IGCC equipment has droppedsignificantly, 5~20 years ago, 1500~2500 U. S. dollars / kW, from now dropped to 850~950 U. S. dollars / kW. 3 conclusion because the IGCC process can be used effectively in refineries, such as12345OGJ, 2004, 2212, He Yongde et al. Modern Coal Chemical Technology Handbook. Beijing: Chemical Industry Press,1273~1284 Yuhong Hu. British clean coal technology project, coal Information Research Institute of Jinling Petrochemical coal water slurry production. People's Daily News - 200510-10, Xu Chengen. New progress of residue processing technologies in China and the the development of the thought of 2003: test. Contemporary petroleum and petrochemical, (8) 1~4))))))))))))))))(up to fifty-seventh pages)The main problem is that the device is not calibrated. 7.1 "high" is the summer high temperature washing tower outlet in the summer, due to many factors of temperature, acid gas treatment capacity, circulating water temperature and flow rate, outlet temperature of the washing tower is usually around 41 degrees Celsius, the normal temperature for 38 degrees, the more water content due to the higher temperature in the process gas the resulting device can not produce 98% acid, not only unitoperahon concentration not parent acid is guaranteed, but also affect the processing capacity of the unit. 7.2 "rear low" is the first and four inlet temperature of the converter on thelow side7.3 "in the middle of a small" sulfur dioxide fan of small flow device started early due to acid gas is small, device is in low load operation, with the start of coking unit, sour gas increased sharply (currently processing sour gas 1550 m3 / h) have reached the electricity, sulfur dioxide fan driven by the rated flow rate of 18000 m3 because of / h, turbine rated flow rate of 24000 m3 / h) (there is not normal operation, so there are some problems of 400 m3 / h in sulfuric acid gas processing device.ReferenceThe insulation effect of the conversion section is not good, the heat loss of the conversion section is too large, the ignition temperature of converter, a four entrance temperature below the catalyst, the long-term need of electric heating, increase the operation cost of the unit. ,,,,,,OneApplication of Ding Hua complementary heat transfer process in the production of zinc concentrate by sulfuric acid industry, (2) 1~42003,:,,,,,,,,,,,,,,,,,,,,,,,,,,,,-Welcome to subscribe, welcome to advertise,,,,,,,,,,,,,,,,,,,,,,,—一。
简述硫酸工业工艺流程硫酸工业工艺流程可是个很有趣的事儿呢！咱先来说说原料。
制造硫酸的主要原料有硫铁矿、硫磺还有有色金属冶炼烟气等。
就拿硫铁矿来说吧，它就像是一个装满宝藏的小盒子，里面藏着制造硫酸的关键元素呢。
那怎么把这些原料变成硫酸呢？对于硫铁矿，第一步就是要把它进行焙烧。
这焙烧啊，就像是给硫铁矿来一场火热的派对。
在这个过程中，硫铁矿在沸腾炉里被加热到很高的温度，它里面的硫就会变成二氧化硫气体跑出来。
这个时候的沸腾炉可热闹啦，就像一个小火山似的，里面的硫铁矿在高温下欢快地释放着自己的硫元素。
从沸腾炉里出来的二氧化硫气体可不能直接就变成硫酸哦。
它还得经过一系列的净化。
因为这个时候的二氧化硫气体里还夹杂着很多杂质呢，什么灰尘啦，砷、硒等有害物质啦。
就像一个调皮的小孩混在一群好孩子里面，得把他挑出来。
所以要通过除尘、洗涤、干燥等步骤，把这些杂质去掉，让二氧化硫气体变得干干净净的。
接下来就是转化过程啦。
这个过程就像是一场神奇的魔法。
把净化后的二氧化硫气体和氧气混合，在催化剂的作用下，它们就会发生反应，变成三氧化硫。
这个催化剂就像是一个魔法棒，轻轻一挥，就促使了这个神奇的转变。
你能想象到那些气体分子在催化剂的表面欢快地跳舞，然后组合成新的分子吗？真的很有趣呢。
最后一步就是吸收啦。
三氧化硫可不能直接用水去吸收，不然就会像一个莽撞的家伙，弄出很多问题。
而是用浓硫酸去吸收三氧化硫，这样就能顺利地得到更高浓度的硫酸啦。
这个过程就像是把一个个小的三氧化硫分子轻轻地放进浓硫酸这个大容器里，让它们在里面乖乖地待着，最后就形成了我们需要的硫酸。
硫酸在工业上可是个大明星呢。
它在化肥生产、金属冶炼、石油精炼等好多领域都发挥着至关重要的作用。
整个硫酸工业工艺流程就像是一场精心编排的舞蹈，每个步骤都紧密相连，缺了哪一个都不行。
从原料的选择，到最后的成品硫酸，每一个环节都充满了人类的智慧和努力。
你看，这么复杂又有趣的过程，就为了制造出对我们生产生活这么有用的硫酸呢。
硫酸的制备知识点总结硫酸是一种常见且重要的化学物质，在许多工业过程和实验室中都有广泛的应用。
下面，我将为你总结硫酸的制备知识点，帮助你更好地了解这个过程。
1.硫酸的化学性质硫酸的化学式为H2SO4，是一种无色、无臭的稠密液体。
它具有强酸性，可与碱反应生成盐和水，并可与金属反应产生氢气。
2.硫酸的制备方法硫酸的制备方法有多种，常用的有浓缩法、吸收法和接触法等。
3.浓缩法浓缩法是最常见和经济的硫酸制备方法之一。
其步骤如下：•首先，将硫磺或硫化氢气体与空气反应生成二氧化硫（SO2）。
•然后，将二氧化硫与氧气反应生成三氧化硫（SO3）。
•最后，将三氧化硫与水反应生成硫酸（H2SO4）。
4.吸收法吸收法是一种利用硫酸的吸湿性制备硫酸的方法，其步骤如下：•首先，将硫磺或硫化氢气体与空气反应生成二氧化硫（SO2）。
•然后，将二氧化硫气体通入硫酸溶液中，发生吸收反应生成亚硫酸（H2SO3）。
•最后，将亚硫酸通过氧化反应转化为硫酸（H2SO4）。
5.接触法接触法是一种利用催化剂加速反应速率的硫酸制备方法，其步骤如下：•首先，将硫磺或硫化氢气体与空气反应生成二氧化硫（SO2）。
•然后，将二氧化硫气体与氧气在催化剂的作用下反应生成三氧化硫（SO3）。
•最后，将三氧化硫与水反应生成硫酸（H2SO4）。
6.硫酸的应用领域硫酸广泛应用于冶金、化工、制药、农业等众多领域。
它可用于制备肥料、染料、洗涤剂、炸药等化学品，也可用于电镀、电池制造、纺织等工业过程。
总结：硫酸的制备是一个重要的化学过程，有多种不同的方法可供选择。
浓缩法、吸收法和接触法是最常用的制备方法，每种方法都有其独特的步骤和特点。
硫酸具有强酸性和广泛的应用领域，是许多工业和实验室中不可或缺的化学物质。
SOP湿法制硫酸工艺技术及其应用前景
杨杰勇
【期刊名称】《山西化工》
【年(卷),期】2017(37)4
【摘要】介绍了SOP湿法制硫酸工艺的原理、流程、特点、正常操作条件下的控制,分析了SOP湿法制硫酸工艺的应用前景.
【总页数】3页(P67-69)
【作者】杨杰勇
【作者单位】阳煤集团太原化工新材料有限公司,山西太原 030400
【正文语种】中文
【中图分类】O611.63;TQ125.1
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1.湿法制造热塑性片材的工艺技术研究Ⅳ湿片的干燥及压轧工艺研究 [J], 张淑萍;周放;刘永纯;赵迎春;王朝辉
2.湿法制造热塑性片材的工艺技术研究Ⅲ.湿片成型工艺研究 [J], 张淑萍;赵迎春;刘其贤;王朝辉;陈二龙
3.兰精30 kt/a湿式催化法制硫酸装置设计简介 [J], 程广春
4.硫化氢湿式催化法制硫酸工艺在焦炉煤气精制系统中的应用 [J], 廖抗祥;张之达
5.克劳斯+SSR制硫黄与SULFOX湿法制硫酸工艺技术比较 [J], 刘辉;农程心;傅超因版权原因，仅展示原文概要，查看原文内容请购买。
硫酸生产工艺及过程控制一、硫酸生产工艺介绍：硫酸是一种广泛应用于工业生产的化学品，主要用于电池制造、矿山开采、纺织、塑料制造等领域。
硫酸的生产主要通过硫磺氧化得到，硫磺氧化生成的二氧化硫进一步与空气中的氧气反应，产生硫酸。
硫酸生产的工艺一般包括以下几个步骤：1.硫磺燃烧：硫磺燃烧是硫酸生产的第一步，通过将硫磺与氧气进行反应，产生二氧化硫。
硫磺燃烧需要保证充分的供氧，一般会采用氧气进行辅助供氧，以提高反应速率和转化率。
2.二氧化硫氧化：硫磺燃烧产生的二氧化硫通过氧化反应转化为三氧化硫，利用空气中的氧气在催化剂的作用下，使二氧化硫氧化。
常用的催化剂有铂、二氧化钛等。
3.清洗：氧化后的三氧化硫中可能带有一些杂质，需要进行清洗，以提高硫酸的纯度。
清洗的主要方法包括冷却、洗涤和过滤。
4.硫酸生成：经过清洗后的气体进入吸收塔，在塔内与浓硫酸进行吸收反应，生成浓硫酸。
吸收塔内通常还配有冷凝器和排出装置，用于收集产生的硫酸蒸气。
5.硫酸的浓缩和脱水：从吸收塔中得到的浓硫酸需要进行进一步的浓缩和脱水处理，以得到工业所需的硫酸产品。
浓缩和脱水主要通过蒸发和冷凝的方式进行，将硫酸中的水分蒸发出来，使其浓度达到要求。
二、硫酸生产过程控制：硫酸的生产过程需要进行一系列的控制，以保证生产的安全、稳定和高效。
1.进料控制：对于硫磺和氧气的进料需要进行控制，确保其进入反应炉的比例和流量符合工艺要求。
可以通过流量计、仪表和自动控制系统实现。
2.反应温度控制：硫磺燃烧和二氧化硫氧化反应都需要控制在一定的温度条件下进行，以保证反应的进行和产物的质量。
可以通过温度探头和温度控制器进行实时监测和调节。
3.催化剂控制：催化剂的使用对反应的速率和转化率有重要影响，需要根据实际情况进行催化剂的投加和更换。
可以通过自动控制系统对催化剂的供给进行控制。
4.流程控制：硫酸生产的各个步骤需要协调配合，确保流程的畅通和稳定。
可以通过流量控制阀、液位探头和自动控制系统进行流程的监测和调节。
工艺流程说明本生产装置为50kt/ a硫铁矿制酸，封闭酸洗净化，（3+2）二次转化二次吸收。
硫铁矿经原料工段、焙烧工段、净化工段、转化工段、干吸工段等工序，其工艺流程详尽介绍如下：（一）原料岗位在原料厂房内，经料斗至1#皮带入破碎机后经2#皮带至筛分，筛分后经3#皮带至大倾角皮带再至供料皮带进入沸腾炉料斗，料再由沸腾大炉料斗喂入沸腾炉。
（二）焙烧岗位硫铁矿在沸腾炉内与空气鼓风机鼓入的空气在进行沸腾焙烧，焙烧出的高温炉气含SO2在12-13%，由炉顶侧向引出，沸腾层温度控制在800-850℃，经炉气冷却器冷却，沉降部分粉尘后再进入旋风除尘器进行除尘，同时SO2炉气降温至350℃左右再进入电除尘器进行除尘。
（三）电除尘器来自焙烧工段的炉气，炉气温度约在350℃左右，含尘量约在30g/NM3，进入电除尘器，炉气中的微小尘粒受电场力的作用，经电离、荷电分别向阴极，阳极移动，并沉积于放电极线上和集尘极板上，通过振打，掉落至集灰斗，由溢流螺旋排灰机排出，炉气净化到含尘0.2g/NM3。
进入净化工段。
（四）净化工段净化采用内喷文氏管——泡沫塔——间冷器——电除雾器封闭稀酸洗净化流程。
来自电除尘器的炉气，炉气温度约在300℃左右，含尘量约在0.2g/NM3，首先进入内喷文氏管，炉气在喉管内以50米/秒气速冲击送入稀酸，使稀酸雾化，气体与液体充分接触，炉气温度降到65℃左右，炉气中大部分灰尘、砷、氟等杂质被除去。
经增湿后的炉气进入泡沫塔进一步洗涤、冷却，炉气温度降至50℃左右，进入间冷器。
炉气在间冷器内与水间接冷却，换热使炉气温度降至35℃以下，炉气中的热量绝大部分在此设备移出系统。
进入电除雾器进一步除去残余的灰尘和酸雾，使炉气中酸雾<0.03g/NM3，砷<1.0mg/NM3，氟<3.0mg/NM3，净化后的炉气进入干燥塔。
由内喷文氏管流出的洗涤稀酸，温度60-65℃进入斜管沉降器，进行固液分离，清液回循环槽，斜管沉降器底部定期排出的酸泥及少量稀酸流至中和槽用石灰中和处理。
硫酸的制作方法硫酸（H2SO4）是一种无色、无臭的强酸，常用于工业和实验室中。
它是许多重要化学物质的重要原料，也是许多工业过程的关键步骤之一。
本文将介绍两种常用的硫酸制作方法。
请注意，硫酸的制作必须在安全操作下进行，并遵循相关的安全规定和指南。
方法一：铁—硫氧化法铁—硫氧化法是制备硫酸的一种常用方法。
该方法利用铁粉（Fe）与硫磺（S）反应生成硫酸。
材料准备•纯净的铁粉•纯净的硫磺•蒸馏水•集气瓶或蒸馏器•酸性环境下使用的玻璃容器（如耐酸瓶）实验步骤1.将铁粉和硫磺按1：1的比例混合均匀，放入酸性环境下的玻璃容器中。
2.在容器中加入适量的蒸馏水，使铁粉和硫磺湿润。
3.将容器加热至适当温度（通常为200-250摄氏度），可使用燃气灯或电炉加热。
加热后，反应会迅速发生。
4.将生成的气体通过集气瓶或蒸馏器收集起来。
生成的气体为二氧化硫（SO2）。
5.将二氧化硫通入蒸馏水中，进行吸收反应。
生成的溶液中包含亚硫酸（H2SO3）。
6.将亚硫酸溶液加热至沸腾，并通过加入过量氧气使其氧化。
反应为：2H2SO3 + O2 -> 2H2SO47.继续加热溶液，使溶液中的水分得到蒸发，从而得到浓硫酸。
注意事项•在进行反应时，需要控制加热温度和反应时间，以避免过热和过长的反应时间。
•硫磺和铁粉的等量反应能够产生足够的二氧化硫，但是反应速度较慢。
若需要提高反应速度，可以使用过量的硫磺。
•铁—硫氧化法制备的硫酸含有较高的杂质，需要进行后续的蒸馏和纯化过程。
方法二：接触过程法接触过程法是工业上制备硫酸的常用方法，该方法通过催化剂催化二氧化硫与氧气反应生成二氧化硫。
材料准备•纯净的二氧化硫气体（SO2）•空气或纯净的氧气•催化剂（通常为硅铝酸复合催化剂）实验步骤1.在反应器中放入催化剂，通常使用硅铝酸复合催化剂。
2.将二氧化硫与氧气按特定摩尔比例（如2:1）通入反应器中。
3.控制反应温度（通常为400-500摄氏度）和压力，使反应发生。
