公开(公告)号：US4333917A

公开(公告)日：1982-06-08

申请号：US119289

申请日：1980-02-07

申请人： Karl H. Dorr ,  Helmut Diekmann ,  Hugo Grimm ,  Ulrich Sander ,  Michael Tacke ,  Waldemar Weber

发明人： Karl H. Dorr ,  Helmut Diekmann ,  Hugo Grimm ,  Ulrich Sander ,  Michael Tacke ,  Waldemar Weber

IPC分类号： C01B17/56 ,  C01B17/74 ,  C01B17/76 ,  C01B17/765 ,  B01D3/00 ,  C01B17/48 ,  C01B17/98

CPC分类号： C01B17/76 ,  C01B17/56 ,  C01B17/7655

摘要： A process for the production of sulfuric acid from wet sulfur dioxide containing gases is disclosed. The sulfur dioxide containing gas is initially purified and cooled, then predried with dilute sulfuric acid, finally dried with concentrated sulfuric acid, converted to sulfur trioxide catalytically and, the sulfur trioxide is absorbed in sulfuric acid. Preliminary drying removes more water than needed to maintain the water balance in the following process steps. A portion of the dilute acid from the preliminary drying is concentrated prior to recycle to the preliminary drying step and another portion of the acid from the preliminary dryer is added to the sulfur trioxide absorber to adjust the water balance in the acid circulating between the final dryer and the sulfur trioxide absorber.

摘要翻译： 公开了一种从含有二氧化硫的气体生产硫酸的方法。 含二氧化硫的气体最初被纯化和冷却，然后用稀硫酸预干燥，最后用浓硫酸干燥，催化转化成三氧化硫，三氧化硫被吸收在硫酸中。 初步干燥除了在以下工艺步骤中维持水分平衡所需的更多的水。 将预备干燥中的一部分稀酸在再循环到预干燥步骤之前进行浓缩，并将另一部分来自预干燥器的酸加入到三氧化硫吸收器中以调节在最终干燥器之间循环的酸中的水分平衡 和三氧化硫吸收剂。

公开(公告)号：US3944401A

公开(公告)日：1976-03-16

申请号：US467387

申请日：1974-05-06

申请人： Karl-Heinz Dorr ,  Hugo Grimm ,  Ulrich Sander ,  Robert Peichl ,  Michael Tacke

发明人： Karl-Heinz Dorr ,  Hugo Grimm ,  Ulrich Sander ,  Robert Peichl ,  Michael Tacke

IPC分类号： B01D53/48 ,  B01D47/10 ,  B01D53/34 ,  B01D53/50 ,  B01D53/77 ,  C01B17/74 ,  B01D47/14

CPC分类号： B01D53/34 ,  B01D47/10 ,  C01B17/74 ,  Y02P70/34

摘要： Sulfur compounds oxidizable to form sulfuric acid and organic compounds oxidizable to CO.sub.2 and H.sub.2 O are removed from an exhaust gas of a contact-process plant for producing sulfuric acid by treating the exhaust gas with a scrubbing solution consisting of dilute sulfuric acid and peroxydisulfuric acid. The peroxydisulfuric acid is produced electrolytically from fresh dilute sulfuric acid and the resulting electrolyte is continuously introduced into the scrubbing acid cycle. The exhaust gas is treated in a vertical venturi with uniflow, i.e. codirectional flow of the gas and the scrubbing solution, and the gas is then passed through a horizontal venturi and subsequently upwardly through a packing layer.CROSS-REFERENCE TO RELATED APPLICATIONThe present Application is related to the commonly assigned copending application Ser. No. 308,849 filed Nov. 22, 1972 and entitled METHOD OF REMOVING GASEOUS IMPURITIES FROM WASTE GASES now abandoned. The latter application relates to subject matter disclosed and claimed in copending application Ser. No. 74,629 filed Sept. 23, 1970 now abandoned, commonly assigned copending application Ser. No. 188,127 filed Oct. 12, 1971, and commonly assigned copending application Ser. No. 188,128 filed Oct. 12, 1971, now U.S. Pat. Nos. 3,780,499 and 3,788,043 respectively, all dealing with absorption systems and gases containing sulfur oxides and naming one or more of the present joint inventors.FIELD OF THE INVENTIONThe present invention relates to a process for the removal of sulfur compounds oxidizable to form sulfuric acid and organic compounds oxidizable to form CO.sub.2 and H.sub.2 O from the exhaust gases produced by contact-process plants for making sulfuric acid.BACKGROUND OF THE INVENTIONAs pointed out in application Ser. No. 308,849, sulfur-containing gases and particulates are a major problem in modern societies because they are released into the atmosphere from many sources and are highly toxic to the population, to vegetation and to metal, stone and other structures.In the combustion of fuel oil and coal, for example, elemental sulfur and sulfur oxides may be released into the atmosphere.From chemical plants, organic sulfur compounds, hydrogen sulfide and sulfur oxides may be released into the atmosphere.In sulfuric acid plants, the waste gases following the final absorption may contain toxic or dangerous quantities of residual sulfur dioxide and sulfur trioxide.In the roasting of metal and other metallurgical processes, the release of elemental sulfur, and sulfur compounds, especially sulfur oxides, has long been a problem.Consequently, considerable effort has been made to obtain an efficient, low-cost system for removing sulfur compounds from waste gases and capable of minimizing the release of such gases into the atmosphere.A large number of processes have been suggested for this purpose as described, for example, in the literature references cited in application Ser. No. 308,849. These processes include washing the gas with sodium carbonate solution followed by crystallization of sodium sulfite, washing the gas with a magnesia slurry followed by crystallization and recovery of the magnesia as well as concentrated sulfur dioxide, washing the gas with gaseous potassium sulfite which is then recovered by stripping from the precipitated pyrosulfite. More complex and extensive systems may also be mentioned here, although they have been more or less fully described in the aforementioned copending applications as representing the state of the art. Suffice it to say that it has been discovered by some of the present applicants jointly with another, as decribed in application Ser. No. 308,849, that waste gases can be economically treated with a dilute sulfuric acid containing peroxydisulfuric acid in such manner that sulfur trioxide results. A critical feature of the system described in the last-mentioned application is that the peroxydisulfuric acid level in the treating solution is replenished by the electrolysis of fresh dilute sulfuric acid (electrolysis-cell acid) with the peroxydisulfuric acid solution thus produced being mixed with dilute sulfuric acid to form the gas-treating liquor. The peroxydisulfuric acid which decomposes upon treatment of the gas, the sulfuric acid formed by absorption of the sulfur trioxide in the dilute sulfur acid and the dilute sulfuric acid serving as the treatment vehicle and absorber can thus be drawn off without recycling to the electrolysis cell.Best results were obtained using this system with gas streams containing sulfur dioxide and those with the exhaust gases of combustion installations such as furnaces, metal or roasting plants and sulfuric acid plants.The system of application Ser. No. 308,849 may be used, in addition, to remove sulfur-containing impurities other than sulfur dioxide from an exhaust gas. It has been found that inorganic sulfur compounds containing sulfur in an oxidation state in which it can be oxidized to elemental sulfur and/or to sulfur dioxide can be removed with that system. For example, inorganic sulfides and hydrogen sulfide can be treated with the peroxydisulfuric acid solution and oxidized to elemental sulfur and eventually sulfur trioxide.The peroxydisulfuric acid concentration was preferably between 200 and 300 grams of peroxydisulfuric acid per liter in the cell acid, most advantageously between 240 and 260 grams per liter. At these concentrations a high yield or efficiency was obtained and practically no water was introduced into the system so that local overheating and thermal degradation of the peroxydisulfuric acid was avoided.The dilute sulfuric acid had a concentration of 25 to 60% by weight, this concentration giving the efficient washing and absorption characteristics. Sulfur trioxide, present in the exhaust gas, and/or sulfuric acid mist (which is generally present when the exhaust gas is derived from a sulfuric acid plant) can be removed simultaneously in spite of the fact that these components are not oxidized. The exhaust gas may contain organic compounds which are oxidized by the peroxydisulfuric acid system to carbon dioxide and water vapor.The gas was treated with the liquid phase in uniflow by passing the gas phase and the liquid phase jointly through the constriction of a venturi absorber. As described in applications Ser. Nos. 74,629, 188,127 and 188,128 and in our earlier individual and joint efforts, for reasons which are not fully understood the intimate contact produced by forcing the liquid phase jointly through a construction and thereafter permitting the mixture of the two phases to expand past the constriction yields a far more effective interaction of the two phases than can be obtained with theoretically equivalent washing towers in which the gas and liquid have similar contact times and interflow velocity. The gas, after the treatment with and separation from dilute sulfuric acid, was conducted through a droplet separator designed to avoid entraining of acid droplets along with the gas. The droplet separator was a packed bed traversed by the gas and from an impingement, collector and interaction surfaces which not only prevent passage of the acid droplets through the layer but also bring about an intimate contact of the gas phase with the acid in the form of a liquid film of the latter or so-called after-absorption and after-reaction.Where the gas is passed upwardly through a filter bed of this type, the lowermost layer consisted of a porous packing bed with particles of a particle size of 5 to 20 millimeters, preferably 9 to 15 millimeters. In this layer precipitation and removal of entrained acid droplets occurs. The packing bodies are coated with a liquid film in which the aforementioned after-absorption takes place. When this liquid film tends to become thicker, the sulfuric acid droplets fall from the layer. The rising gas stream and the pore size maintain a thin liquid layer above the packing mass.The after-absorption is preferably effected in a layer having a height of 50 to 200 millimeters, preferably 80 to 120 millimeters, this bed height having been found to provide after-absorption with a minimum of increased flow resistance. The gas velocity furing after-absorption was 1 to 2.5 meters per second, preferably 1.3 to 1.7 meters per second.After traversing the after-absorption layer of a thickness of 50 to 200 millimeters and composed of porous packing bodies with a particle size of 5 to 20 millimeters at a gas velocity of 1 to 2.5 meters per second, the gas passed through a layer of acid-resistance nonporous packing bodies with a particle size of 20 to 50 millimeters in an after-absorption stage, the latter overlying the after-absorption bed.The after-separation bed not only loads the after-absorption bed to prevent migration of the packing bodies but also provides impingement-type liquid-separation surfaces together with narrower and random channels in which residual droplets of acid may be separated from the gas phase. The after-separation bed has a thickness of 50 to 150 millimeters, preferably 80 to 120 millimeters, a range which has been found to be effective for efficient separation of the residual liquid from the gas phase without materially increasing the flow resistance.It was found to be desirable to treat the gas (containing sulfur compounds and other compounds oxidizable by peroxydisulfuric acid to sulfur dioxide, carbon dioxide and water vapor) with a dilute sulfuric acid containing the peroxydisulfuric acid in a venturi-type apparatus in uniflow, i.e. a system in which the gas and liquid phases flow in the same direction. The venturi absorber was provided ahead of the venturi constriction and expansion chamber with a liquid-collecting chamber and means for diverting the gas stream from its axial flow direction as it emerges from the venturi chamber. The gas stream was diverted by an angle of 90.degree. or more, thereby causing droplets of high kinetic energy to pass through the bodies of liquid in the bath disposed ahead of the venturi outlet. The venturi absorber was preferably oriented vertically so that its outlet was directed downwardly into this bath and the expansion chamber was provided with lateral outlets above the bath so that the main body of gas is first directed downward toward the bath and is then diverted upwardly and laterally to shed larger droplets and high-energy particles.The acid collected in the sump was in part recirculated to the venturi. It was also advantageous to pass the gas phase into contact with the peroxydisulfuric acid/dilute sulfuric acid liquid phase by forcing the gas upwardly through a gas-permeable plate upon which the acid layer was provided. The gas-permeable plate was composed of a porous material such as sintered glass or porcelain. The gas permeability, gas-flow velocity and volume were so dimensioned that little or no sulfuric acid solution passed through the plate. Best results were obtained when the after-absorber and after-separator beds of packing were provided upon the perfoated plate or upon respective prerforated plates in cascade.The parts of the apparatus which came into contact with the acid solution were constituted from or were coated with acid resistance, preferably polyvinil chloride.OBJECTS OF THE INVENTIONIt is the principal object of the present invention to provide an improved method of removing gaseous impurities from the waste gases of a contact-process plate for producing sulfuric acid.Another object of the invention is to extend the principles originally set forth in application Ser. No. 308,849.SUMMARY OF THE INVENTIONAccording to the invention, this object is accomplished in that the exhaust gas is treated in a vertical venturi tube with cocurrent injected circulating scrubbing acid from the sump of the venturi tube, at least part of the injected scrubbing acid being separated and collected in the sump of the venturi tube.The gas is conducted into a substantially horizontal venturi tube disposed between the sump and the outlet opening of the vertical venturi tube and opening into a tower, the gas being treated in the horizontal venturi tube with cocurrent injected circulating scrubbing acid from the sump of the tower.The injected scrubbing acid is separated and is collected in the sump of the tower; the gas rising in the tower, which contains a packing layer, is treated with countercurrent circulating scrubbing acid coming from the sump of the tower and injected above the packing layer, and with the added acid electrolyte which contains peroxydisulfuric acid, and the acids fed into the tower are separated and are collected to the sump of the tower.Preferably a large part of the circulating scrubbing acid injected into the vertical venturi tube is separated and is collected in the sump of this venturi tube since even the scrubbing acid which has been entrained into the inlet of the substantially horizontal venturi tube as far as the throat thereof is recycled.The separation and recycling of the scrubbing acid which has been entrained to the narrowest part or throat of the substantially horizontal venturi tube from the vertical venturi tube may be accomplished by downwardly inclining the gas outlet conduit from the vertical venturi tube, or by the provision of baffles in the gas outlet conduit and by the provision of drain openings in the lower portion of the gas outlet conduit or in the inlet portion of the substantially horizontal venturi tube. These drain openings are connected by conduits to the sump of the vertical venturi tube.As a result of these measures, which may be used individually or in combination, a major portion of the scrubbing acid entrained from the vertical venturi tube is separated and conducted into the sump of that venturi tube so that the scrubbing acid cycles can be separated to a high degree.Advantageously, a large part of the circulating scrubbing acid injected into the vertical venturi tube is separated and is collected in the sump of the venturi tube because a packing layer is provided below the outlet opening of the venturi tube and above the inlet opening of the substantially horizontal venturi tube. This packing layer has a thickness of about 10-20 centimeter. The high turbulence produced in that layer also promotes the separation of the scrubbing acid, which is then collected in the sump of the vertical venturi tube.Scrubbing acid can be transferred from the sump of the tower via an overflow into the sump of the vertical venturi tube in a quantity which corresponds to the added electrolyte acid containing peroxydisulfuric acid and to the sulfuric acid formed as an oxidation product in the substantially horizontal venturi tube. In this simple way, a constant level is maintained in the tower sump and the entire system is operated in countercurrent of liquid and gas flow so that the active oxygen is optimally utilized. Besides, a steady-state concentration of active oxygen in the sump of the vertical venturi tube is maintained constant.The steady-state sulfuric acid concentration of the scrubbing acid in the sump of the vertical venturi tube is held constant by an addition of water. As a result, the evaporative loss of water is compensated and the heat of the resulting mixture is utilized for a hydrolysis of the residual peroxydisulfuric acid in the sump of the vertical venturi tube.The level of the sump in the vertical venturi tube is held constant by a withdrawal of scrubbing acid, which contains the oxidation product, from the sump. In that case, the product is withdrawn from the system at a point where the content of residual active oxygen is lowest.Different concentrations of sulfuric acid are maintained in the cycles of the circulating scrubbing acid, the highest concentrations of sulfuric acid and active oxygen being provided in the acid which is sprayed into the tower, a lower concentration being provided in the acid which is injected into the substantially horizontal venturi tube, and the lowest concentration being provided in the acid which is injected into the vertical venturi tube. This results in an optimum oxidation of SO.sub.2 and/or of other oxidizable gas components and an optimum utilization of the active oxygen supplied to the system.The electrolyte acid which emerges from the electrolytic unit and contains peroxydisulfuric acid consists of sulfuric acid which has a concentration of 30 - 50% by weight H.sub.2 SO.sub.4, preferably 35 - 40% by weight H.sub.2 SO.sub.4, and contains 180 - 350 grams, preferably 200 - 300 grams, peroxydisulfuric acid per liter. These concentrations give very good results in operation.Advantageously, the acid electrolyte which contains peroxydisulfuric acid is held in intermediate storage to increase the hydrolysis of the peroxydisulfuric acid. The increased hydrolysis of H.sub.2 S.sub.2 O.sub.8 to H.sub.2 SO.sub.5 and H.sub.2 SO.sub.4 results in a higher rate of oxidation of the gas components in the succeeding scrubber. Besides, the intermediate storage provides for a supply from which acid electrolyte which contains active oxygen can be withdrawn immediately at a suitable rate in case of fluctuations of the gas rate. Besides, the high SO.sub.2 content of the exhaust gas from a sulfuric acid contact process plant when being started up, may be absorbed in that the entire system is filled from the supply tank with electrolyte acid containing a high concentration of active oxygen so that there is initially a high content of active oxygen in all absorption stages.The intermediate storage is continued until a hydrolysis of 30 - 90% has been effected. That degree of hydrolysis gives good results in operation.The stationary steady-state concentration of the scrubbing acid in the sump of the tower most desirably amounts to 30 - 50% by weight, preferably 38 - 45% by weight, sulfuric and a molar concentration of active oxygen 0.4-1.26 moles, preferably 0.6-1.0 moles per liter. High degrees of oxidation are obtained with these concentrations.The stationary steady-state concentration of the scrubbing acid in the sump of the vertical venturi tube is advantageously 25 - 40% by weight sulfuric acid, preferably 28 - 32% by weight, and the active oxygen has a concentration of 0.06-0.3 moles per liter, preferably 0.1 - 0.15 moles per liter. A relatively high water vapor partial pressure in the gas phase and high degrees of oxidation are obtained with these concentrations.The residence time of the scrubbing acid which contains the residual peroxydisulfuric acid in the sump of the tower and in the sump of the vertical venturi tube is adjusted so that 20 - 90% of the residual peroxydisulfuric acid are hydrolyzed in each sump. The further hydrolysis of H.sub.2 S.sub.2 O.sub.8 to H.sub.2 SO.sub.5 and H.sub.2 SO.sub.4 improves the degree of oxidation. Besides, the volumes of the sumps can be dimensioned such that the higher SO.sub.2 content of the exhaust gases produced during the starting period of the contact process plant can be absorbed because an adequate supply of active oxygen is available.The included angle at the outlet of the vertical venturi tube and of the substantially horizontal venturi tube is 10.degree. - 20.degree., preferably 14.degree. - 17.degree.. As a result, the total gas pressure loss in the venturi tube is minimized and, in addition to the venturi effect proper, a turbulence is created to provide for an optimum gas-liquid interface allowing an optimum degree of oxidation.The gas is passed through the entire system with an average retention time of 2 - 4 seconds. This retention time allows a high degree of oxidation while keeping the dimensions of the equipment at a minimum.The withdrawn scrubbing acid which contains the oxidation product is supplied to the final absorber of the contact process plant. In this way, the residual active oxygen withdrawn from the system is utilized for an oxidation in the final absorber of the contact process plant and the content of oxidizable compounds in the exhaust gases is reduced before they enter the system.The quantity of peracids depends on the oxidation equivalent of the exhaust gas components to be oxidized and on the desired degree of oxidation and the desired purity of the exhaust gases.The packing layer in the tower has suitably a thickness of 40-80 centimeters. This results in a high degree of oxidation and in a relatively low gas pressure loss.The outlet opening of the tower is preceded by a wire mesh filter which provides for a good separation of entrained liquid in conjunction with a low pressure loss.The entire system can be made to a large extent from plastic or synthetic-resin material

摘要翻译： 通过用由稀硫酸和过氧化二硫酸组成的洗涤溶液处理废气，可氧化形成硫酸的硫化合物和可氧化成CO 2和H 2 O的有机化合物从用于生产硫酸的接触工艺装置的废气中除去。 过氧化二硫酸由新鲜的稀硫酸电解产生，所得的电解质连续引入洗涤酸循环中。 废气在垂直文丘里管中处理，具有单流，即气体和洗涤溶液的顺向流动，然后气体通过水平文丘里管，然后通过填料层向上。

公开(公告)号：US4330364A

公开(公告)日：1982-05-18

申请号：US191584

申请日：1980-09-29

申请人： Walter Blumrich ,  Karl H. Dorr ,  Hans J. Konig ,  Ulrich Sander

发明人： Walter Blumrich ,  Karl H. Dorr ,  Hans J. Konig ,  Ulrich Sander

IPC分类号： C01B17/74 ,  C01B17/765 ,  C01B25/234 ,  B01D1/00

CPC分类号： C01B25/2346 ,  C01B17/7655 ,  Y10S159/08 ,  Y10S159/16

摘要： A process for the concentration of dilute phosphoric acid in a phosphoric acid process characterized by a plurality of separate phosphoric acid cycles when the phosphoric acid is concentrated in each cycle by a vacuum evaporation is described wherein the phosphoric acid cycles is heated by indirect heat exchange by heat of formation formed in a sulfuric acid contact process.

摘要翻译： 描述了当通过真空蒸发在每个循环中浓缩磷酸时，在磷酸方法中浓缩稀磷酸的方法，其特征在于多个分开的磷酸循环，其中磷酸循环通过间接热交换加热 在硫酸接触过程中形成的形成热。

公开(公告)号：US4276116A

公开(公告)日：1981-06-30

申请号：US41468

申请日：1979-05-22

申请人： Walter Blumrich ,  Karl H. Dorr ,  Hans J. Konig ,  Ulrich Sander

发明人： Walter Blumrich ,  Karl H. Dorr ,  Hans J. Konig ,  Ulrich Sander

IPC分类号： C01B17/74 ,  C01B17/765 ,  C01B25/234 ,  B01D1/28

CPC分类号： C01B25/2346 ,  C01B17/7655 ,  Y10S159/08 ,  Y10S159/16

摘要： A process for the concentration of dilute phosphoric acid in a phosphoric acid process characterized by a plurality of separate phosphoric acid cycles when the phosphoric acid is concentrated in each cycle by a vacuum evaporation is described wherein the phosphoric acid cycles is heated by indirect heat exchange by heat of formation formed in a sulfuric acid contact process.

摘要翻译： 描述了当通过真空蒸发在每个循环中浓缩磷酸时，在磷酸方法中浓缩稀磷酸的方法，其特征在于多个分开的磷酸循环，其中磷酸循环通过间接热交换加热 在硫酸接触过程中形成的形成热。

公开(公告)号：US4368183A

公开(公告)日：1983-01-11

申请号：US203285

申请日：1980-11-03

申请人： Karl-Heinz Dorr ,  Hugo Grimm ,  Ulrich Sander ,  Robert Peichl ,  Franz Maier

发明人： Karl-Heinz Dorr ,  Hugo Grimm ,  Ulrich Sander ,  Robert Peichl ,  Franz Maier

IPC分类号： C01B17/775 ,  C01B17/82 ,  C01B17/76

CPC分类号： C01B17/775

摘要： SO.sub.2 -containing, hot gases are catalytically converted in part in a first contacting stage. The water and the SO.sub.3 formed is removed from the reaction gas. The remaining gas is heated and then supplied to the second contacting stage. The water vapor content in the reaction gas delivered by a first contacting stage corresponds to an H.sub.2 O/SO.sub.3 mole ratio below 1. The reaction gas delivered by the first contacting stage is precooled by an indirect heat exchange to such a temperature that the wall temperatures of the heat exchanger are above the dew point temperature of the reaction gas. The precooled reaction gas entering a condensing stage is contacted in a venturi with cocurrent sulfuric acid of 98.0 to 100% concentration and a temperature of at least 95.degree. C. The exit temperature of the gas from the condensing stage is maintained at least at 120.degree. C. The gas rises in a succeeding absorption stage through a packing layer, which is contacted with trickling sulfuric acid having a concentration of 98 to 100% and a temperature of 70.degree. to 120.degree. C. The dry gas which leaves the absorption stage and has been freed from SO.sub.3 is maintained at a temperature which is as high as or slightly higher than the temperature of the acid as it initially contacts the packing in the absorption stage. The sulfuric acid concentration is controlled by a supply of water into the sulfuric acid in the condensing and/or absorption stage.

摘要翻译： 含SO 2的热气体部分地在第一接触阶段被催化转化。 所形成的水和SO 3从反应气体中除去。 将剩余气体加热，然后供给到第二接触级。 由第一接触阶段输送的反应气体中的水蒸汽含量对应于低于1的H 2 O / SO 3摩尔比。由第一接触阶段输送的反应气体通过间接热交换预冷至如此温度 热交换器高于反应气体的露点温度。 进入冷凝阶段的预冷反应气体在文氏管中与98.0至100％浓度的并流硫酸和至少95℃的温度接触。来自冷凝级的气体的出口温度保持在至少120℃ C.气体在接下来的吸收阶段通过填充层升高，该填充层与浓度为98-100％，温度为70-120℃的滴流硫酸接触。离开吸收阶段的干燥气体 已被除去的SO3保持在与吸收阶段最初接触填料时酸的温度高或略高的温度。 通过在冷凝和/或吸收阶段向硫酸中供应水来控制硫酸浓度。

公开(公告)号：US09066474B2

公开(公告)日：2015-06-30

申请号：US13428093

申请日：2012-03-23

申请人： Nils Klemm ,  Ulrich Sander ,  Antonius De Bresser ,  Dirk Schimmelpfeng ,  Andreas Rinnergschwentner

发明人： Nils Klemm ,  Ulrich Sander ,  Antonius De Bresser ,  Dirk Schimmelpfeng ,  Andreas Rinnergschwentner

IPC分类号： A01G9/02 ,  A01G9/04

CPC分类号： A01G9/028 ,  A01G9/045

摘要： A method for cultivating a plurality of young plants of different species or variety to form a group of young plants which can be handled as a unit. The method includes providing a plurality of propagation pots, each containing a substrate, which allow roots that form in a propagation pot to grow out at the sides, loading at least one growing container with the plurality of propagation pots such that the propagation pots arranged in each growing container contact one another along a portion of their lateral peripheral surface, introducing at least one cutting or seed into each propagation pot, and allowing roots to form in the propagation pots of each growing container until roots emerging from the sides of the propagation pots have formed a network of roots binding the propagation pots together as a cluster of propagation pots.

摘要翻译： 一种用于培育多种不同种类或品种的幼苗的方法，以形成可作为一个单元处理的一组幼苗。 该方法包括提供多个传播盆，每个传播盆各自含有基底，其允许在传播罐中形成的根在侧面生长，将至少一个生长容器装载到多个传播罐中，使得传播罐布置在 每个生长的容器沿其侧面周边表面的一部分彼此接触，将至少一个切割或种子引入每个传播罐中，并且允许根在每个生长容器的传播罐中形成，直到从传播罐的侧面出来的根 已经形成了将传播罐捆绑在一起作为一群传播盆的根网络。

公开(公告)号：US08508230B2

公开(公告)日：2013-08-13

申请号：US13084096

申请日：2011-04-11

申请人： Ulrich Sander

发明人： Ulrich Sander

IPC分类号： G01V3/00

CPC分类号： G02B21/0012 ,  A61B5/055 ,  A61B34/20 ,  A61B90/20 ,  A61B2090/364 ,  A61B2090/374 ,  G02B21/24 ,  G02B21/364

摘要： The present invention relates to a microscope apparatus (100) comprising an operating microscope (20), a magnetic resonance or MR apparatus (30), a stand (10) that carries the operating microscope (20) and the MR apparatus (30), at least one detector (14) for determining the spatial position of the MR apparatus (30) relative to the operating microscope (20), a reflecting device (23) for reflecting an image obtained using the MR apparatus (30) into at least one observation beam path of the operating microscope (20), a computer unit (40) which is connected to the at least one detector (14) and is arranged so as to determine the spatial position of the MR apparatus (20) relative to the operating microscope (30), the computer unit (40) being connected to the reflecting device (23) and to the MR apparatus (30) and being arranged so as to provide the image that is to be reflected in for the reflecting device (23) on the basis of the spatial position determined for the MR apparatus (30) relative to the operating microscope (20).

摘要翻译： 本发明涉及包括操作显微镜（20），磁共振或MR装置（30），承载操作显微镜（20）和MR装置（30）的支架（10）的显微镜装置（100） 用于确定MR装置（30）相对于操作显微镜（20）的空间位置的至少一个检测器（14），用于将使用该MR装置（30）获得的图像反射到至少一个 操作显微镜（20）的观察光束路径，连接到所述至少一个检测器（14）的计算机单元（40），并被布置成确定MR装置（20）相对于操作的空间位置 显微镜（30），所述计算机单元（40）连接到所述反射装置（23）和所述MR装置（30），并且被布置成提供要被反射用于所述反射装置（23）的图像， 基于为MR装置（30）确定的空间位置 操作显微镜（20）。

公开(公告)号：US08487989B2

公开(公告)日：2013-07-16

申请号：US13187579

申请日：2011-07-21

申请人： Ulrich Sander

发明人： Ulrich Sander

IPC分类号： H04N7/18

CPC分类号： G02B21/0012 ,  G02B27/646 ,  H04N5/23258 ,  H04N5/2328

摘要： The present invention relates to an image stabilization device which is particularly space-efficient and has a quick response time, and which is integrated into an image capture device for an image capture system of a surgical microscope, including a carrier substrate (101, 102) defining a sensor plane, a plurality of optoelectronic image capturing cells (110) arranged, in particular, in a matrix array; and at least one moving means (120) for moving the optoelectronic image capturing cells (110) relative to the carrier substrate (101, 102).

摘要翻译： 本发明涉及一种特别节省空间并且具有快速响应时间的图像稳定装置，并且其集成到用于外科显微镜的图像捕获系统的图像捕获装置中，该图像捕获装置包括载体基板（101,102） 限定传感器平面，特别地以矩阵阵列布置的多个光电子图像捕获单元（110）; 以及用于相对于载体衬底（101,102）移动光电图像捕获单元（110）的至少一个移动装置（120）。

公开(公告)号：US20110194073A1

公开(公告)日：2011-08-11

申请号：US13021864

申请日：2011-02-07

申请人： Ulrich Sander ,  Lothar Knuenz

发明人： Ulrich Sander ,  Lothar Knuenz

IPC分类号： A61B3/13

CPC分类号： A61B3/13 ,  G02B21/0012 ,  G02B21/025 ,  G02B21/22

摘要： Attachment module for a microscope, having an ophthalmoscopic lens (142; 242; 342) and an inverting device (140; 240; 340) for inverting an image of an object (143; 243; 343) that is to be observed generated by means of the ophthalmoscopic lens, wherein the inverter device comprises at least four deflection surfaces (146a, 146b, 146c; 246a, 246b, 246c; 346a, 346b, 346c, 346d) by means of which observation beam paths (102) which emanate from the object to be observed can be introduced into a main objective (110) of the microscope, at least two deflection surfaces being planar and at least two further deflection surfaces being non-planar, particularly spherical or in the shape of free-form surfaces.

摘要翻译： 具有眼镜镜片（142; 242; 342）和反转装置（140; 240; 340）的显微镜的附件模块，用于使待观察的物体（143; 243; 343）的图像反转， ，其中所述逆变器装置包括至少四个偏转表面（146a，146b，146c; 246a，246b，246c; 346a，346b，346c，346d），通过所述至少四个偏转表面发出观察光束路径（102） 可观察到的物体可以被引入到显微镜的主要目标（110）中，至少两个偏转表面是平面的，并且至少两个另外的偏转表面是非平面的，特别是球形的或具有自由曲面的形状。

公开(公告)号：US07593156B2

公开(公告)日：2009-09-22

申请号：US12247519

申请日：2008-10-08

申请人： Ulrich Sander

发明人： Ulrich Sander

IPC分类号： A61B3/13 ,  G02B21/22

CPC分类号： G02B21/18 ,  G02B21/082 ,  G02B21/22 ,  G02B26/0833

摘要： The present invention concerns a microscope with at least one optical element (21a, 21b) for optional deflection and/or splitting of a beam path passing through the microscope, wherein the at least one optical element (21a, 21b) is fashioned as a micro-mirror array (80) having a number of individually controllable and adjustable micro-mirrors (82).

摘要翻译： 本发明涉及具有至少一个光学元件（21a，21b）的显微镜，用于可选地偏转和/或分裂通过显微镜的光束路径，其中至少一个光学元件（21a，21b）被形成为微型 - 镜阵列（80）具有多个可独立控制和可调节的微镜（82）。