The Experts below are selected from a list of 168 Experts worldwide ranked by ideXlab platform
Shu Shi-tao - One of the best experts on this subject based on the ideXlab platform.
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Problems existing in operation of 600 kt/a SA plant from Sulfur Burning and its modification
Phosphate and Compound Fertilizer, 2008Co-Authors: Shu Shi-taoAbstract:The operation troubles are described,including turbine fault,failure of circulating acid pump of dry absorption,primary reforming of catalyst caking in a 600 kt/a Sulfur-based Sulfuric acid plant.The countermeasures are presented after analyzing the representation and reason.Application effect shows the operation ratio increased in the plant.
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Method for treatment of circulating cooling water from SA plant by Sulfur-Burning
Phosphate and Compound Fertilizer, 2008Co-Authors: Shu Shi-taoAbstract:With the open circulating cooling water of SA plant,the bacteria-alga and scaling corrosion appear and the cooling water and circle acid temperature are raised.The measures are used,such as adding chemical drug timingly and quantitatively in the circle water system to clean pre-film,adding in anti-scaling agent and bactericidal algicide to treat the circle water.The circle water quality is improved greatly,the circle water and acid temperature is reduced about 10 ℃ than no treatment.
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Some problems existing in the fiber demister in the production of Sulfuric acid from Sulfur-Burning
Phosphate and Compound Fertilizer, 2007Co-Authors: Shu Shi-taoAbstract:The problem of fiber demister blocked by sublimed Sulfur and oil smoke appears in the production of Sulfuric acid from Sulfur-Burning easily.Based on the illustration of Sulfuric acid production from Sulfur-Burning with'3 + 1'process,the blocking reasons in start-up stage and running stage and the corresponding anti-blocking measures are discussed
Michael S. Moats - One of the best experts on this subject based on the ideXlab platform.
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Costs of Sulfuric acid production
Sulfuric Acid Manufacture, 2013Co-Authors: Matthew J. King, William G. Davenport, Michael S. MoatsAbstract:Study estimate investment and production costs for Sulfur Burning and metallurgical Sulfuric acid plants are provided. Spent acid regeneration type acid plants are expected to have slightly higher investment costs than Sulfur Burning type acid plants. Use of stainless steels in the construction of acid plants means that their investment costs are often closely linked to the price of stainless steel. The use of fabrication facilities located in China and India has lowered acid plant investment costs. Production costs for Sulfur Burning acid plants are driven mostly by Sulfur and electricity prices. Credits for by-product electricity are significant. They appreciably lower the production costs of Sulfur Burning acid plants.
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Dehydrating air and gases with strong Sulfuric acid
Sulfuric Acid Manufacture, 2013Co-Authors: Matthew J. King, William G. Davenport, Michael S. MoatsAbstract:SO2-bearing gas must be dry before it goes to catalytic SO2 oxidation. Otherwise, the SO3 made by catalytic oxidation will react with the gas's H2O(g) to form corrosive liquid Sulfuric acid in cool flues and heat exchangers, especially during shutdowns. This problem is avoided by dehydrating (i) Sulfur Burning air and (ii) scrubbed metallurgical/spent acid furnace off-gas by contacting these gases with strong Sulfuric acid. Dehydration is represented by the reaction: H2Og+H2SO4linstrongacid→H2SO4·H2Olinslightlyweakenedacid Industrially, the process is carried out in brick-lined stainless steel towers packed with ceramic saddles. Acid descends around the saddles where it meets and reacts with ascending H2O(g)-laden gas.
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Acid temperature control and heat recovery
Sulfuric Acid Manufacture, 2013Co-Authors: Matthew J. King, William G. Davenport, Michael S. MoatsAbstract:H2SO4(l) is made by the reaction of SO3 with the H2O(l) in strong Sulfuric acid. Heat is released by the reaction, so that H2SO4 making’s output Sulfuric acid is ~ 25 K warmer than its input acid. Output acid temperature increases markedly with increasing input acid temperature and decreasing acid circulation rate. Corrosion rates increase with increasing temperature so that excessive temperatures must be avoided. They are avoided by cooling the recycled acid in water cooled “shell and tube” or “plate and frame” heat exchangers. Acid plants (especially Sulfur Burning plants) are now often built with “acid-sensible-heat-to-steam” energy recovery systems. These significantly increase acidmaking energy efficiency.
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Minimizing Sulfur emissions
Sulfuric Acid Manufacture, 2013Co-Authors: Matthew J. King, William G. Davenport, Michael S. MoatsAbstract:Equilibrium SO2 oxidation is never achieved in industrial acid plants. This results in slightly higher than minimum SO2 emissions. Methods to lower Sulfur emissions from the acid plant mainly focus on decreasing SO2 emission and include (a) switching from single to double absorption acid plants (b) installing cesium promoted catalyst and/or new LEAP™ or GEAR™ catalysts (c) scrubbing the acid plant tail gas. Steady operation and control of catalyst bed temperatures result in lower acid plant SO2 emissions. This is relatively easy for Sulfur Burning acid plants, but much more challenging for metallurgical acid plants, especially those treating intermittent Peirce-Smith converter gases. SO3 and acid mist emissions can be minimized by correct design and operation of acidmaking towers and their candle filters.
Matthew J. King - One of the best experts on this subject based on the ideXlab platform.
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3 – Sulfur Burning
Sulfuric Acid Manufacture, 2013Co-Authors: Matthew J. KingAbstract:Sixty percent of the world's Sulfuric acid is made from elemental Sulfur. Virtually, all of this Sulfur is the by-product of natural gas and petroleum refining. The first step in making Sulfuric acid from elemental Sulfur is Burning the Sulfur with dried air. It entails. (a) atomizing molten Sulfur in a hot furnace and oxidizing the resulting fine droplets with excess dried air (b) cooling the product SO2, O2, N2 gas in a heat recovery boiler. The product is ~12 volume% SO2, 9 volume% O2, and 79 volume% N2 gas (420 °C), perfect for subsequent catalytic SO2 oxidation and H2SO4(l) manufacture.
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3 Sulfur Burning
Sulfuric Acid Manufacture (Second Edition)#R##N#Analysis Control and Optimization, 2013Co-Authors: Matthew J. KingAbstract:Sixty percent of the world's Sulfuric acid is made from elemental Sulfur. Virtually, all of this Sulfur is the by-product of natural gas and petroleum refining. The first step in making Sulfuric acid from elemental Sulfur is Burning the Sulfur with dried air. It entails. (a) atomizing molten Sulfur in a hot furnace and oxidizing the resulting fine droplets with excess dried air (b) cooling the product SO2, O2, N2 gas in a heat recovery boiler. The product is ~12 volume% SO2, 9 volume% O2, and 79 volume% N2 gas (420 °C), perfect for subsequent catalytic SO2 oxidation and H2SO4(l) manufacture.
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Costs of Sulfuric acid production
Sulfuric Acid Manufacture, 2013Co-Authors: Matthew J. King, William G. Davenport, Michael S. MoatsAbstract:Study estimate investment and production costs for Sulfur Burning and metallurgical Sulfuric acid plants are provided. Spent acid regeneration type acid plants are expected to have slightly higher investment costs than Sulfur Burning type acid plants. Use of stainless steels in the construction of acid plants means that their investment costs are often closely linked to the price of stainless steel. The use of fabrication facilities located in China and India has lowered acid plant investment costs. Production costs for Sulfur Burning acid plants are driven mostly by Sulfur and electricity prices. Credits for by-product electricity are significant. They appreciably lower the production costs of Sulfur Burning acid plants.
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Dehydrating air and gases with strong Sulfuric acid
Sulfuric Acid Manufacture, 2013Co-Authors: Matthew J. King, William G. Davenport, Michael S. MoatsAbstract:SO2-bearing gas must be dry before it goes to catalytic SO2 oxidation. Otherwise, the SO3 made by catalytic oxidation will react with the gas's H2O(g) to form corrosive liquid Sulfuric acid in cool flues and heat exchangers, especially during shutdowns. This problem is avoided by dehydrating (i) Sulfur Burning air and (ii) scrubbed metallurgical/spent acid furnace off-gas by contacting these gases with strong Sulfuric acid. Dehydration is represented by the reaction: H2Og+H2SO4linstrongacid→H2SO4·H2Olinslightlyweakenedacid Industrially, the process is carried out in brick-lined stainless steel towers packed with ceramic saddles. Acid descends around the saddles where it meets and reacts with ascending H2O(g)-laden gas.
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Acid temperature control and heat recovery
Sulfuric Acid Manufacture, 2013Co-Authors: Matthew J. King, William G. Davenport, Michael S. MoatsAbstract:H2SO4(l) is made by the reaction of SO3 with the H2O(l) in strong Sulfuric acid. Heat is released by the reaction, so that H2SO4 making’s output Sulfuric acid is ~ 25 K warmer than its input acid. Output acid temperature increases markedly with increasing input acid temperature and decreasing acid circulation rate. Corrosion rates increase with increasing temperature so that excessive temperatures must be avoided. They are avoided by cooling the recycled acid in water cooled “shell and tube” or “plate and frame” heat exchangers. Acid plants (especially Sulfur Burning plants) are now often built with “acid-sensible-heat-to-steam” energy recovery systems. These significantly increase acidmaking energy efficiency.
Nilay Kumar Sarker - One of the best experts on this subject based on the ideXlab platform.
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Simulation of the Production of Sulfuric Acid from a Sulfur-Burning Single-absorption Contact Sulfuric Acid Plant
The Journal of Engineering, 2015Co-Authors: Nilay Kumar SarkerAbstract:The purpose of this work is to develop and implement an effective knowledge on simulation of process plant in HYSYS. A theoretical examination of the simulation of Sulfuric acid process plant has been demonstrated in our work. Relationship among changes on several parameters has also been studied. The burner outlet temperature shows linearly increasing relationship with the liquid Sulfur temperature. Waste energy flow shows linearly decreasing relationship with the boiler outlet temperature. Flue gas temperature initially had no regular relationship with Absorber inlet temperature, but with temperature increased more than 60 0 Celsius it seems to decrease linearly. Flu gas pressure has no effect on Absorber inlet temperature. The mass flow of Sulfuric Acid for storage decreases linearly with the increasing temperature of moist air. The molar enthalpy of Sulfuric Acid for storage increases linearly up to 50 0 Celsius, and after this temperature the increase is associated linearly with higher slope. In this design HYSYS has been successfully used to design every sub-process of the Sulfuric acid plant in one integrated environment. Peng-Robinson was used for liquid and vapor phase respectively as fluid package and HYSYS properties were used for simulation.
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Simulation of the Production of Sulfuric Acid from a Sulfur-Burning Single-absorption Contact Sulfuric Acid Plant
Journal of emerging technologies and innovative research, 2015Co-Authors: Nilay Kumar Sarker, Tanveer Ahmed KhanAbstract:Sulfuric acid is one of the most important chemical that is used in different chemical industries throughout the world. The purpose of this work is to develop and implement an effective knowledge on simulation of process plant in HYSYS. A theoretical examination of the simulation of Sulfuric acid process plant has been demonstrated in our work. In contact process, in the production of the Sulfuric acid, liquid Sulfur is oxidized to SO2 via an exothermic reaction. The SO2 gas that has been partially converted to SO3 by catalysis is cooled, passed through Sulfuric acid to remove SO3, reheated and then passed through another one or two catalysts bed. By this means the overall conversions can be increased from 98 up to 99.5-99.8% thereby reduced emissions of unconverted SO2 to the atmosphere. Relationship among changes on several parameters has also been studied. The burner outlet temperature shows linearly increasing relationship with the liquid Sulfur temperature. Waste energy flow shows linearly decreasing relationship with the boiler outlet temperature. Flue gas temperature initially had no regular relationship with Absorber inlet temperature, but with temperature increased more than 600 Celsius it seems to decrease linearly. Flu gas pressure has no effect on Absorber inlet temperature. The mass flow of Sulfuric Acid for storage decreases linearly with the increasing temperature of moist air. The molar enthalpy of Sulfuric Acid for storage increases linearly up to 500 Celsius, and after this temperature the increase is associated linearly with higher slope. In this design HYSYS has been successfully used to design every sub- process of the Sulfuric acid plant in one integrated environment. Peng-Robinson was used for liquid and vapor phase respectively as fluid package and HYSYS properties were used for simulation.
Wang Geng-ya - One of the best experts on this subject based on the ideXlab platform.
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The selection of start-up process for Sulfuric acid plant by Sulfur-Burning
Phosphate and Compound Fertilizer, 2010Co-Authors: Wang Geng-yaAbstract:The selection of start-up process for Sulfuric acid plant by Sulfur-Burning,and their respective advantages and disadvantages are discussed.Some auxiliary clever operations are adopted to shorten startup time and thus to obtain a better efficiency.Some concerned technical links for the start-up of related process equipment are introduced.
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Technical Analysis of Start-up Process of a Sulfur-Burning Sulfuric Acid Production Plant
Sulphur Phosphorus & Bulk Materials Handling Related Engineering, 2009Co-Authors: Wang Geng-yaAbstract:The key of the start-up technology for Sulfur-Burning Sulfuric acid production plant is the temperature rise of the conversion system,which also includes boiler dry-out boiling out,Sulfur spray,pre-saturation of vanadium catalyst and operation,etc.The methods for producing the hot air required by the temperature rise of the conversion system,and their advantages and disadvantages are introduced.With consideration of the time required for the plant start-up,cost,and stable operation,auxiliary temperature rise method is recommended.Operating experiences are also introduced,such as the operation of dry-out and boiling out,determination of Sulfur spray time,control of Sulfur spray quantity,pre-saturation of new catalyst and operation,as well as secondary cleaning of the dry absorber.It is considered that such operating experiences offer strong applicability.
