WO2013131451A1 - 利用含钌废催化剂制备固体亚硝酰硝酸钌的方法 - Google Patents

利用含钌废催化剂制备固体亚硝酰硝酸钌的方法 Download PDF

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WO2013131451A1
WO2013131451A1 PCT/CN2013/072105 CN2013072105W WO2013131451A1 WO 2013131451 A1 WO2013131451 A1 WO 2013131451A1 CN 2013072105 W CN2013072105 W CN 2013072105W WO 2013131451 A1 WO2013131451 A1 WO 2013131451A1
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Prior art keywords
ruthenium
nitrate
solid
spent catalyst
acid solution
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PCT/CN2013/072105
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English (en)
French (fr)
Inventor
许莉
赖波
宋德臣
刘倩倩
韩奕铭
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阳光凯迪新能源集团有限公司
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Priority to RU2014140158/13A priority Critical patent/RU2580414C1/ru
Priority to ES13758228.4T priority patent/ES2637517T3/es
Priority to EP13758228.4A priority patent/EP2823900B1/en
Priority to BR112014021848-0A priority patent/BR112014021848A2/pt
Priority to MX2014010569A priority patent/MX358426B/es
Priority to CA2866207A priority patent/CA2866207C/en
Priority to AP2014007986A priority patent/AP2014007986A0/xx
Priority to DK13758228.4T priority patent/DK2823900T3/en
Application filed by 阳光凯迪新能源集团有限公司 filed Critical 阳光凯迪新能源集团有限公司
Priority to KR1020147027911A priority patent/KR101567592B1/ko
Priority to SG11201405382UA priority patent/SG11201405382UA/en
Priority to IN1924MUN2014 priority patent/IN2014MN01924A/en
Priority to JP2014560228A priority patent/JP5902324B2/ja
Priority to AU2013230403A priority patent/AU2013230403B2/en
Priority to PL13758228T priority patent/PL2823900T3/pl
Publication of WO2013131451A1 publication Critical patent/WO2013131451A1/zh
Priority to US14/475,547 priority patent/US9005555B2/en
Priority to ZA2014/07147A priority patent/ZA201407147B/en

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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B11/00—Obtaining noble metals
    • C22B11/04—Obtaining noble metals by wet processes
    • C22B11/042—Recovery of noble metals from waste materials
    • C22B11/048—Recovery of noble metals from waste materials from spent catalysts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/80—Destroying solid waste or transforming solid waste into something useful or harmless involving an extraction step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G55/00—Compounds of ruthenium, rhodium, palladium, osmium, iridium, or platinum
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/005—Preliminary treatment of scrap
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/009—General processes for recovering metals or metallic compounds from spent catalysts
    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D3/00—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances
    • A62D3/30—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by reacting with chemical agents
    • A62D3/36—Detoxification by using acid or alkaline reagents
    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D3/00—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances
    • A62D3/40—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by heating to effect chemical change, e.g. pyrolysis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/80—Compositional purity
    • 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
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • This invention relates to the recovery and reuse of platinum group metals, and more particularly to a process for preparing solid nitrosyl nitrate nitrite using a spent catalyst. Background technique
  • Patent CN101638727A discloses a process for the recovery of ruthenium in an activated carbon supported ruthenium catalyst, which involves the preparation of nitrosyl nitrate.
  • the obtained cesium hydroxide or RuO 2H 2 0 is stirred and dissolved in a reflux apparatus with a slightly boiling nitric acid by a series of steps such as alkali fusion to obtain a nitric acid solution of Ru(NO)(N0 3 ) 3 .
  • the products obtained by the above methods are all acid solutions of nitrosyl nitrate, but because of their high acidity, they are not easy to store and transport.
  • Patent CN102167405A discloses a method for preparing solid nitrosyl nitrate nitrate, which reacts ruthenium trichloride and sodium nitrite to synthesize a nitrosylguanidinium intermediate, and an intermediate and silver nitrate to obtain a nitrosyl nitrate solution. Then, nitrosyl nitrate was extracted with diethyl ether, and finally the ether extract was evaporated to obtain a nitrosyl nitrate solid.
  • the method can produce solid nitrosyl nitrate, there are still disadvantages: First, due to the introduction of chloride during the preparation process, the product contains impurity chlorine, It is easy to cause catalyst poisoning; Secondly, the method needs to prepare the ruthenium intermediate to obtain the final product in the implementation process, resulting in low product yield; Third, the raw material RuCl 3 .xH 2 0 used in the method can be directly used. As a catalyst, the crystallization of nitrosyl nitrate is prepared by using the crystalline hydrate as a raw material, and the cost is high. Summary of the invention
  • the method is simple and efficient, and the high-purity solid nitrosyl nitrate can be directly prepared from the supported ruthenium-containing catalyst, and the obtained solid nitrosyl nitrate can be used as a raw material to prepare the ruthenium-containing catalyst again.
  • the method for preparing solid nitrosyl nitrate using the spent catalyst is designed according to the present invention, comprising the following steps:
  • cerium-containing black solid obtained in the step 1) is ground to a powder, placed in a fluidized bed reactor, replaced with nitrogen or an inert gas for 0.5 to 2 hours, then switched to hydrogen, and heated to 100 to 600 ° C. Reducing cerium oxide in the spent catalyst to metal ruthenium;
  • step 5 adding sodium nitrite solid to the acid solution of cerium nitrate obtained in step 4), stirring appropriately, heating to a slight boiling reflux of the solution to obtain a solution containing nitrosyl nitrate;
  • the nitrosyl nitrate-containing solution obtained in the step 5) is extracted with anhydrous diethyl ether, and the ethyl ether extract is collected, and the diethyl ether is evaporated to obtain a nitrosyl nitrate solid.
  • the drying condition of the spent catalyst is selected to be heated to 100 ⁇ 150 ° C in a nitrogen or inert gas atmosphere, dried for 1 ⁇ 2 h, and the spent catalyst can be placed in a muffle furnace. Calcination.
  • the flow rate of the hydrogen gas during the reduction reaction is not particularly limited, but is preferably 1200 to 400011-1, and the reduction time is 1 to 12 hours, preferably 6 to 12 hours.
  • the oxidized ruthenium in the spent catalyst is reduced by hydrogen, and the chemical equation of the reaction is as follows:
  • the flow rate of the mixed gas of ozone and air is not particularly limited, but is preferably 1200 to 4000 IT 1 , and the volume fraction of ozone in the mixed gas is 1 to 20%, preferably 15%, oxidized.
  • the time is from l to 12 h, preferably from 8 to 12 h.
  • the metal ruthenium is oxidized by the mixed gas to osmium tetroxide gas, and the chemical equation of the reaction is as follows:
  • Ru + 20 2 Ru0 4 ⁇
  • 3Ru + 40 3 3Ru0 4 ⁇
  • the temperature of the nitric acid solution is 50 to 95 ° C, and the mass concentration is 45 to 68%.
  • the theoretical amount of the nitric acid solution is calculated according to the loading amount of ruthenium in the spent catalyst, and the theoretical amount is 1.2. ⁇ 2.0 times the actual amount used as a nitric acid solution.
  • the tertiary absorption device is three brown containers in series. The osmium tetroxide gas is introduced into the nitric acid solution, and the osmium tetroxide gas is absorbed, and a cerium nitrate solution is formed under heating, and the chemical equation of the reaction is as follows:
  • the theoretical amount of the sodium nitrite solid is calculated according to the loading amount of ruthenium in the spent catalyst, and the theoretical amount of 1.5 to 2.0 times is taken as the actual amount of the sodium nitrite solid.
  • the sodium nitrite solid is suitably added slowly to the acid solution of cerium nitrate with appropriate stirring to uniformly diffuse it in the acid solution of cerium nitrate, and the solution is heated to a slight boiling for reflux, and the reflux time of the reaction is 1 to 8 h. It is preferably 4 to 8 hours.
  • the reaction vessel which is heated and refluxed is a commonly used three-necked round bottom flask, which is a common technical means in the art and will not be described herein.
  • the chemical equation for the reaction of nitric acid in nitric acid with sodium nitrite is as follows:
  • the ruthenium-containing catalyst is a supported ruthenium-containing catalyst having a wide range of supports and may be a combination of one or a mixture of alumina, silica, zirconia, titania and zeolite.
  • the carrier can be of any shape, common spherical, cylindrical, clover, four-leaf, ring, honeycomb The type or the like can be used to recover hydrazine by the method of the present invention.
  • the invention has the beneficial effects: First, the solid nitrosyl nitrate can be directly prepared from the supported ruthenium-containing spent catalyst by the method of the invention, the recovery cost is low, and the obtained solid product is convenient for storage and transportation;
  • the solid nitrosyl nitrate nitrate obtained by the invention method does not contain halogen, and avoids poisoning caused by halogen in the reaction process of the ruthenium-containing catalyst;
  • the method of the invention has simple operation steps and does not involve introduction of ruthenium intermediate, The yield of the solid product nitrosyl nitrate is effectively increased.
  • the method of the invention realizes the reuse of the cesium resources, has low recovery cost, simple operation, high product yield, high purity, and is suitable for large-scale production.
  • Figure 1 is a schematic illustration of a process for the preparation of solid nitrosyl nitrate nitrite using a spent catalyst. detailed description
  • ruthenium-containing catalyst (spherical type, Ru/Al 2 0 3 , Ru loading 5%) in a crucible, place it in a muffle furnace, pass N 2 , dry at 120 °C for 2 h, then After calcination at 450 ° C for 3 h, the organic matter remaining in the spent catalyst was removed, and cooled to room temperature to obtain 58.6 g of a solid.
  • the solid was triturated in a uniform black powder was transferred to a fluidized bed reactor, purged with nitrogen through for 30min switched to hydrogen gas, a space velocity 120011-1, warmed to 300 ° C, temperature reduction 12h, continue to heat up to 600 ° C , then enter the mixture 15vol%0 3 /air, keep the mixture airspeed 1200 h 1 circulation for 12h.
  • the produced Ru0 4 gas was sequentially introduced into three absorption bottles containing 40 g of a 68% by mass nitric acid solution, and the temperature of the nitric acid solution was controlled to be around 75 ° C to obtain an acid solution of Ru(N0 3 ) 3 .
  • ruthenium-containing catalyst (cylindrical type, Ru/Si0 2 , Ru loading 3%), place it in a crucible, place it in a muffle furnace, pass N 2 , dry at 120 ° C for 2 h, then at 450 ° C was calcined for 3 h, cooled to room temperature and weighed to give 48.9 g of a solid.
  • the black solid was ground into a uniform powder, transferred to a fluidized bed reactor, and replaced with hydrogen gas after being replaced by nitrogen for 30 minutes.
  • the space velocity of hydrogen was 2500 IT 1 , the temperature was raised to 350 ° C, the temperature was reduced for 10 h, and the temperature was further increased to 620 ° C.
  • ruthenium-containing catalyst (clover type, Ru/Zr0 2 , Ru loading 4%.), put it in a crucible, place it in a muffle furnace, pass N 2 , dry at 120 ° C for 2 h, then at 450 It was calcined at ° C for 3 h, cooled to room temperature and weighed to give 118.2 g of a solid.
  • the black solid was ground into a uniform powder, transferred to a fluidized bed reactor, and replaced with hydrogen gas after being replaced by nitrogen for 30 minutes.
  • the space velocity of hydrogen was 4000 IT 1 , the temperature was raised to 350 ° C, the temperature was reduced for 6 hours, and the temperature was further increased to 650 ° C.
  • ruthenium-containing catalyst (Clover type, Ru/Ti0 2 , Ru load 5%), put it in a crucible, place it in a muffle furnace, pass N 2 , dry at 120 ° C for 2 h, then After calcination at 450 ° C for 3 h, the organic matter remaining in the spent catalyst was removed, and cooled to room temperature to obtain 58.1 g of a solid.
  • the black solid was ground into a uniform powder, transferred to a fluidized bed reactor, and replaced with hydrogen gas after being replaced by nitrogen for 30 minutes.
  • the space velocity of hydrogen gas was OOO!T 1 , the temperature was raised to 350 ° C, the temperature was reduced for 8 hours, and the temperature was further increased to 620 °.
  • the produced Ru0 4 gas was sequentially introduced into three absorption bottles containing 27 g of a 68% by mass nitric acid solution, and the temperature of the nitric acid solution was controlled to be around 75 ° C to obtain an acid solution of Ru(N0 3 ) 3 .
  • the mixture gas was introduced into 15 vol% 0 3 /air, and the air-fuel mixture was kept at a space velocity of 3000 h - 1 for 8 hours.
  • the produced Ru0 4 gas was sequentially introduced into three absorption bottles containing 16 g of a 45% by mass nitric acid solution, and the temperature of the nitric acid solution was controlled to be around 75 ° C to obtain an acid solution of Ru(N0 3 ) 3 .
  • the Ru(N0 3 ) 3 acid solution obtained above was collected in a three-necked round bottom flask, and a NaN0 2 powder of 1.5 times (1.2 g) of the theoretical amount was slowly added, stirred and heated to reflux for 6 hours, and the solution gradually turned into a deep red black. .
  • the solution was cooled, extracted with EtOAc (EtOAc) EtOAc.
  • EtOAc EtOAc
  • Infrared analysis by KBr tableting showed that the characteristic peak was at 1924 cm" 1 , which was consistent with the characteristic structure parameters of RuCNO)CN0 3 ) 3 , and the calculated yield was 96.6%, and the impurity metal content was ⁇ 30 ppm.
  • ruthenium-containing catalyst honeycomb type, Ru/Al 2 0 3 -Si0 2 , Ru loading 2%.
  • put it in a crucible place it in a muffle furnace, pass N 2 , dry at 120 ° C.
  • calcination at 450 ° C for 3 h
  • the residual organic matter in the spent catalyst was removed, and cooled to room temperature to obtain 156.4 g of a solid.
  • the black solid was ground into a uniform powder, transferred to a fluidized bed reactor, and replaced with hydrogen gas after being replaced by nitrogen for 30 minutes.
  • the space velocity of hydrogen gas was SOOO!T 1 , the temperature was raised to 350 ° C, the temperature was reduced for 8 hours, and the temperature was further increased to 620 °. C, then enter the mixture of 15vol%0 3 /air, keep the mixture airspeed 2500 h- 1 for 8h.
  • the produced Ru0 4 gas was sequentially introduced into three absorption bottles containing 8.6 g of a 45% by mass nitric acid solution, and the temperature of the nitric acid solution was controlled to be around 75 ° C to obtain an acid solution of Ru(N0 3 ) 3 .
  • the Ru(N0 3 ) 3 acid solution obtained above was collected in a three-necked round bottom flask, and a theoretical amount of 1.5 times (0.64 g) of NaN 2 2 powder was slowly added thereto, stirred and heated to reflux for 8 hours, and the solution gradually became dark reddish black.
  • the solution was cooled, extracted with EtOAc (3 mL) EtOAc.
  • EtOAc 3 mL
  • EtOAc Infrared analysis by KBr compression, the characteristic peak is located at 1924cm- 1 , which is consistent with the characteristic structure parameters of Ru(NO)(N0 3 ) 3 .
  • the calculated yield is 97.2%, and the impurity metal content is ⁇
  • the solid nitrosyl nitric acid prepared by using the spent catalyst containing ruthenium as a raw material according to the method for preparing solid nitrosyl nitrate nitrate by using a spent catalyst is prepared according to the present invention.
  • the yields are all above 90%, and under preferred conditions, the yield can be over 95%.
  • the obtained solid nitrosyl nitrate can be used as a raw material to prepare a ruthenium-containing catalyst again, thereby realizing the effective utilization of ruthenium resources.
  • the method of the invention has low recovery cost and simple operation, and the obtained product has high yield and high purity, and is suitable for large-scale production.

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Abstract

提供了一种利用含钌废催化剂制备固体亚硝酰硝酸钌的方法，其步骤为：将含钌废催化剂干燥后锻烧，获得含钌黑色固体，然后将含钌黑色固体研磨至粉末并通入氢气还原成金属钌，再利用臭氧和空气的混合气氧化金属钌，产生四氧化钌气体，收集气体通入硝酸溶液后加入固体亚硝酸钠，制得含亚硝酰硝酸钌的溶液，最后利用乙醚萃取，蒸发乙醚后获得亚硝酰硝酸钌固体。本方法可以有效地回收多种负载型含钌废催化剂中的贵金属钌，实现钌资源的有效回收再利用，操作步骤简单，不涉及钌中间体的引入，产品收率高，获得的固体亚硝酰硝酸钌不含卤素，纯度高，可直接用于催化剂的制备。

Description

利用含钌废催化剂制备固体亚硝酰硝酸钌的方法 技术领域
本发明涉及铂族金属的回收再利用， 具体地指一种利用含钌废催化剂制 备固体亚硝酰硝酸钌的方法。 背景技术
钌具有优良的催化性能， 在催化剂行业用途广泛， 多用于合成氨、 苯选 择加氢制环己烯和二氧化碳加氢制甲醇等， 然而钌资源有限、 价格昂贵、 全 球年产量仅有几十吨， 限制了钌在上述领域的应用。 从含钌废催化剂中回收 钌用于再次生产钌基催化剂， 可大幅降低该催化剂的使用成本， 有效减少废 催化剂对环境的污染， 具有广泛的应用前景。
由于固体亚硝酰硝酸钌 Ru(NO)(N03 )3不含卤素、 硫、 磷等易引起催化剂 中毒的元素， 且易溶于水、 乙醚、 丙酮等有机溶剂， 因此成为众多含钌催化 剂制备过程中的理想前驱体。 如何有效地从负载型含钌废催化剂中制备高纯 固体亚硝酰硝酸钌， 具有重要的工业应用价值。
目前， 文献关于亚硝酰硝酸钌的制备方法有两种： 一种是将 Ru04直接吸 收在冷却的硝酸溶液中； 另一种是用硝酸溶解回流亚硝酰氢氧化钌。 专利 CN101638727A公开了一种活性碳负载钌催化剂中钌的回收方法， 其中涉及 到亚硝酰硝酸钌的制备。 该方法通过碱熔等一系列步骤将得到的氢氧化钌或 RuO 2H20在回流装置中用微沸的硝酸搅拌、 溶解， 得到 Ru(NO)(N03 )3的硝 酸溶液。 以上方法得到的产品均为亚硝酰硝酸钌的酸溶液， 但由于其酸度较 高， 不易于储存及运输。
专利 CN102167405A公开了一种制备固体亚硝酰硝酸钌的方法， 该方法 将三氯化钌和亚硝酸钠反应合成亚硝酰氯化钌中间体， 中间体与硝酸银作用 得到亚硝酰硝酸钌溶液， 再用乙醚萃取亚硝酰硝酸钌， 最后将乙醚萃取液蒸 发， 得到亚硝酰硝酸钌固体。 该方法虽然可以制得固体亚硝酰硝酸钌， 但仍 然存在缺点： 其一， 由于制备过程中引入氯化物， 导致产品中含有杂质氯， 容易引起催化剂中毒； 其二， 该方法在实施过程中需要通过制备钌中间体以 获得最终产品， 导致产品收率偏低； 其三， 该方法使用的原料 RuCl3.xH20本 身可以直接用作催化剂的制备， 以该结晶水合物作为原料制备亚硝酰硝酸 钌， 成本较高。 发明内容
本发明的目的就是要提供一种利用含钌废催化剂制备固体亚硝酰硝酸 钌的方法。 该方法简单、 高效， 可以从负载型含钌废催化剂中直接制备出高 纯固体亚硝酰硝酸钌， 所得的固体亚硝酰硝酸钌可以作为原料再次制备含钌 催化剂。
为实现上述目的， 本发明所设计的利用含钌废催化剂制备固体亚硝酰硝 酸钌的方法， 包括以下步骤：
1) 将含钌废催化剂干燥后， 于 300〜500°C煅烧 2〜4h， 降温至室温， 得到含钌黑色固体；
2)将步骤 1)中得到的含钌黑色固体研磨至粉末， 置于流化床反应器中， 通氮气或惰性气体置换 0.5〜2h后切换为氢气， 升温至 100〜600°C， 恒温还 原， 将废催化剂中的氧化钌还原为金属钌；
3) 将臭氧和空气的混合气通入步骤 2) 中得到的金属钌， 对金属钌进行 氧化， 温度控制在 600〜650°C， 产生四氧化钌气体；
4) 将步骤 3) 中产生的四氧化钌气体导入盛有硝酸溶液的三级吸收装置 中， 得到硝酸钌的酸溶液；
5)将亚硝酸钠固体加入步骤 4)中得到的硝酸钌的酸溶液中， 适当搅拌， 加热至溶液微沸回流， 制得含亚硝酰硝酸钌的溶液；
6) 将步骤 5) 中得到的含亚硝酰硝酸钌的溶液用无水乙醚萃取， 收集乙 醚萃取液， 再将乙醚蒸发， 得到亚硝酰硝酸钌固体。
其中， 所述步骤 1) 中， 含钌废催化剂的干燥条件可选为在氮气或惰性 气体氛围中升温至 100〜150°C， 干燥 l〜2h， 含钌废催化剂可置于马弗炉中 煅烧。 所述步骤 2 )中， 还原反应时， 氢气的流速无特别限制， 但优选为 1200〜 400011-1 , 还原时间为 l〜12h， 优选为 6〜12h。 利用氢气将含钌废催化剂中 被氧化的钌还原， 其反应的化学方程式如下：
Ru02 + 2H2 = Ru + 2H20
所述步骤 3 ) 中， 臭氧和空气的混合气的流速无特别限制， 但优选为 1200〜4000 IT1 , 臭氧在所述混合气中的体积分数为 1〜20%， 优选为 15%， 氧化时间为 l〜12h， 优选为 8〜12h。 金属钌被混合气氧化为四氧化钌气体， 其反应的化学方程式如下：
Ru + 202 = Ru04†， 3Ru + 403 = 3Ru04†
所述步骤 4 )中，所述硝酸溶液的温度为 50〜95 °C、质量浓度为 45〜68%， 根据含钌废催化剂中钌的负载量计算硝酸溶液的理论用量， 取理论用量的 1.2〜2.0 倍作为硝酸溶液的实际用量。 所述三级吸收装置为三个串联的棕色 容器。 四氧化钌气体通入硝酸溶液中， 四氧化钌气体被吸收， 在加热的条件 下生成硝酸钌溶液， 其反应的化学方程式如下：
2Ru04 + 16HN03 = 2Ru(N03 )3 + 8H20 +502† + 10NO2†
所述步骤 5 ) 中， 根据含钌废催化剂中钌的负载量计算亚硝酸钠固体的 理论用量， 取理论用量的 1 .5〜2.0倍作为亚硝酸钠固体的实际用量。 亚硝酸 钠固体适宜缓慢地加入硝酸钌的酸溶液中且伴随适当搅拌， 以使其均匀扩散 在硝酸钌的酸溶液中， 加热该溶液至微沸进行回流， 该反应回流时间为 1〜 8h， 优选为 4〜8h。 加热回流的反应容器为常用的三颈圆底烧瓶， 为本领域 常用技术手段， 此处不做赘述。 硝酸钌的硝酸溶液与亚硝酸钠发生反应的化 学方程式如下：
Ru(N03 )3 +2NaN02 + 2HN03 = Ru(NO)(N03 )3 + 2NaN03 + N02† + H20 所述步骤 6 ) 中， 可进行多次无水乙醚萃取， 提高亚硝酰硝酸钌固体的 收率。
所述含钌废催化剂为负载型含钌废催化剂， 其载体范围广， 可为氧化铝、 二氧化硅、 二氧化锆、 二氧化钛和沸石中的一种或几种混合物的组合。 载体 可以为任何形状， 常见的球型、 圆柱型、 三叶草型、 四叶草型、 环型、 蜂窝 型等均可利用本发明所述的方法回收钌。
本发明的有益效果： 其一， 利用本发明所述的方法可以由负载型含钌的 废催化剂直接制备固体亚硝酰硝酸钌， 回收成本低， 所得固体产品便于储存 及运输； 其二， 本发明方法制得的固体亚硝酰硝酸钌不含卤素， 避免了含钌 催化剂在反应过程中由于卤素而引起的中毒现象； 其三， 本发明方法操作步 骤简单， 不涉及钌中间体的引入， 有效地提高了固体产品亚硝酰硝酸钌的收 率。 综上所述， 本发明方法实现了钌资源的再利用， 回收成本低， 操作简单， 产品收率高、 纯度高， 适于规模化生产。 附图说明
图 1为本发明利用含钌废催化剂制备固体亚硝酰硝酸钌的方法的流程示 意图。 具体实施方式
以下结合附图和具体实施例对本发明作进一步的详细描述， 本发明的保 护范围并不受这些实施例的限制。
实施例 1
称取 60g含钌催化剂 （球型， Ru/Al203， Ru负载量 5% ) 装在坩埚中， 将其置于马弗炉中， 通入 N2， 120 °C干燥 2h， 随后在 450 °C煅烧 3h， 除去废 催化剂中残留的有机物质， 冷却至室温称重得到 58.6g固体。 将黑色固体研 磨呈均匀粉末， 转移至流化床反应器中， 通氮气置换 30min后切换为氢气， 氢气空速为 120011-1， 升温至 300 °C， 恒温还原 12h， 继续升温至 600 °C， 再 通入混合气 15vol%03/空气， 保持混合气空速 1200 h 1流通 12h。 将产生的 Ru04气体依次导入 3个装有 40g质量浓度为 68%的硝酸溶液的吸收瓶中， 并 控制硝酸溶液温度为 75 °C附近， 得到 Ru(N03 )3的酸溶液。
收集上述得到的 Ru(N03 )3酸溶液于三颈圆底烧瓶中， 缓慢加入理论用量 1.5 倍 （6g ) 的 NaN02粉末， 搅拌并加热回流 8h， 溶液逐渐变为深红黑色。 冷却该溶液， 用 130ml无水乙醚萃取 3次， 收集乙醚萃取液， 并将乙醚蒸发， 得到棕黄色固体 8.84g。 经 KBr压片红外分析， 其特征峰位于 1924cm-1, 与 Ru(NO)(N03)3特征结构参数吻合， 计算收率为 96.2%， 杂质金属含量 < 30ppm。 实施例 2
称取 50g含钌催化剂 （圆柱型， Ru/Si02， Ru负载量 3%) 装在坩埚中， 将其置于马弗炉中， 通入 N2， 120°C干燥 2h， 随后在 450°C煅烧 3h， 冷却至 室温称重得到 48.9g固体。 将黑色固体研磨呈均匀粉末， 转移至流化床反应 器中， 通氮气置换 30min后切换为氢气， 氢气空速为 2500 IT1, 升温至 350°C， 恒温还原 10h， 继续升温至 620°C， 再通入混合气 15vol%03/空气， 保持混合 气空速 2500 h-1流通 10h， 将产生的 Ru04气体依次导入 3个装有 24g质量浓 度为 60%的硝酸溶液的吸收瓶中， 控制硝酸溶液温度为 75°C附近， 得到 RuCN03)3的酸溶液。
将得到的 Ru(N03)3的酸溶液转移至三颈圆底烧瓶中， 缓慢加入理论用量 1.8倍 （3.6g) 的 NaN02粉末， 搅拌并加热回流 4h， 溶液逐渐变为深红黑色。 冷却该溶液， 用 80ml无水乙醚萃取 3次， 收集乙醚萃取液， 并将乙醚蒸发， 得到棕黄色固体 4.41g。 经 KBr压片红外分析， 其特征峰位于 1924cm-1, 与 Ru(NO)(N03)3特征结构参数吻合， 计算收率为 95.8%， 杂质金属含量 < 30ppm。 实施例 3
称取 120g含钌催化剂 （三叶草型， Ru/Zr02， Ru负载量 4%。） 装在坩埚 中， 将其置于马弗炉中， 通入 N2， 120°C干燥 2h， 随后在 450°C煅烧 3h， 冷 却至室温称重得到 118.2g固体。 将黑色固体研磨呈均匀粉末， 转移至流化床 反应器中， 通氮气置换 30min后切换为氢气， 氢气空速为 4000 IT1, 升温至 350°C， 恒温还原 6h， 继续升温至 650°C， 再通入混合气 15vol%03/空气， 保 持混合气空速 4000 h-1流通 8h， 将产生的 Ru04气体依次导入 3个装有 13g质 量浓度为 45%的硝酸溶液的吸收瓶中， 控制硝酸溶液温度为 75°C附近， 得到 RuCN03)3的酸溶液。
将得到的 Ru(N03)3的酸溶液转移至三颈圆底烧瓶中， 缓慢加入理论用量 2.0 倍 （1.29g) 的 NaN02粉末， 搅拌并加热回流 6h， 溶液逐渐变为深红黑 色。 冷却该溶液， 用 60ml无水乙醚萃取 3次， 收集乙醚萃取液， 并将乙醚蒸 发， 得到棕黄色固体 1.44g。 经 KBr压片红外分析， 其特征峰位于 1924cm- 与 Ru(NO)(N03)3特征结构参数吻合， 计算收率为 97.3%， 杂质金属含量 < 30ppm。 实施例 4
称取 60g含钌催化剂 （四叶草型， Ru/Ti02， Ru负载量 5%) 装在坩埚中， 将其置于马弗炉中， 通入 N2， 120°C干燥 2h， 随后在 450°C煅烧 3h， 除去废 催化剂中残留的有机物质， 冷却至室温称重得到 58.1g固体。 将黑色固体研 磨呈均匀粉末， 转移至流化床反应器中， 通氮气置换 30min后切换为氢气， 氢气空速为 OOO!T1, 升温至 350°C， 恒温还原 8h， 继续升温至 620°C， 再通 入混合气 10vol%O3/空气， 保持混合气空速 15001T1流通 5h。 将产生的 Ru04 气体依次导入 3个装有 27g质量浓度为 68%的硝酸溶液的吸收瓶中， 并控制 硝酸溶液温度为 75°C附近， 得到 Ru(N03)3的酸溶液。
收集上述得到的 Ru(N03)3酸溶液于三颈圆底烧瓶中， 缓慢加入理论用量 0.9倍的 （3.56g) NaN02粉末， 搅拌并加热回流 6h， 溶液逐渐变为深红黑色。 冷却该溶液， 用 100ml无水乙醚萃取 3次， 收集乙醚萃取液， 并将乙醚蒸发， 得到棕黄色固体 8.21g。 经 KBr压片红外分析， 其特征峰位于 1924cm-1, 与 Ru(NO)(N03)3特征结构参数吻合， 计算收率为 90.3%， 杂质金属含量 < 30ppm。 实施例 5
称取 60g含钌催化剂 （环型， Ru/Al203-ZSM-5， Ru负载量 1%) 装在坩 埚中， 将其置于马弗炉中， 通入 N2， 120°C干燥 2h， 随后在 450°C煅烧 3h， 除去废催化剂中残留的有机物质， 冷却至室温称重得到 59.0g固体。 将黑色 固体研磨呈均匀粉末， 转移至流化床反应器中， 通氮气置换 30min后切换为 氢气， 氢气空速为 SOOO!T1, 升温至 350°C， 恒温还原 8h， 继续升温至 620°C， 再通入混合气 15vol%03/空气， 保持混合气空速 3000 h-1流通 8h。 将产生的 Ru04气体依次导入 3个装有 16g质量浓度为 45%的硝酸溶液的吸收瓶中， 并 控制硝酸溶液温度为 75°C附近， 得到 Ru(N03)3的酸溶液。
收集上述得到的 Ru(N03)3酸溶液于三颈圆底烧瓶中， 缓慢加入用量为理 论用量 1.5倍 （1.2g) 的 NaN02粉末， 搅拌并加热回流 6h， 溶液逐渐变为深 红黑色。 冷却该溶液， 用 50ml无水乙醚萃取 3次， 收集乙醚萃取液， 并将乙 醚蒸发， 得到棕黄色固体 1.78g。 经 KBr压片红外分析， 其特征峰位于 1924cm"1, 与 RuCNO)CN03)3特征结构参数吻合， 计算收率为 96.6%， 杂质金 属含量〈 30ppm。 实施例 6
称取 160g含钌催化剂 （蜂窝型， Ru/Al203-Si02， Ru负载量 2%。） 装在 坩埚中， 将其置于马弗炉中， 通入 N2， 120°C干燥 2h， 随后在 450°C煅烧 3h， 除去废催化剂中残留的有机物质， 冷却至室温称重得到 156.4g固体。 将黑色 固体研磨呈均匀粉末， 转移至流化床反应器中， 通氮气置换 30min后切换为 氢气， 氢气空速为 SOOO!T1, 升温至 350°C， 恒温还原 8h， 继续升温至 620°C， 再通入混合气 15vol%03/空气， 保持混合气空速 2500 h-1流通 8h。 将产生的 Ru04气体依次导入 3个装有 8.6g质量浓度为 45%的硝酸溶液的吸收瓶中，并 控制硝酸溶液温度为 75°C附近， 得到 Ru(N03)3的酸溶液。
收集上述得到的 Ru(N03)3酸溶液于三颈圆底烧瓶中， 缓慢加入理论用量 1.5倍 （0.64g) 的 NaN02粉末， 搅拌并加热回流 8h， 溶液逐渐变为深红黑色。 冷却该溶液， 用 30ml无水乙醚萃取 3次， 收集乙醚萃取液， 并将乙醚蒸发， 得到棕黄色固体 0.95g。 经 KBr压片红外分析， 其特征峰位于 1924cm-1, 与 Ru(NO)(N03)3特征结构参数吻合， 计算收率为 97.2%， 杂质金属含量 <
30ppm。 结果分析：
根据实施例 1〜6 的实验结果， 可以得出， 根据本发明所述的利用含钌 废催化剂制备固体亚硝酰硝酸钌的方法， 以含钌的废催化剂作为原料制备的 固体亚硝酰硝酸钌收率均在 90%以上， 并且在优选条件下， 其收率可达 95 % 以上。 所得的固体亚硝酰硝酸钌可以作为原料再次制备含钌催化剂， 实现了 钌资源的有效利用。 本发明方法回收成本低， 操作简单， 制得的产品收率高、 纯度高， 适于规模化生产。

Claims

权 利 要 求 书
1、 一种利用含钌废催化剂制备固体亚硝酰硝酸钌的方法， 包括以下步 骤：
1) 将含钌废催化剂干燥后， 于 300〜500°C煅烧 2〜4h， 降温至室温， 得到含钌黑色固体；
2)将步骤 1)中得到的含钌黑色固体研磨至粉末， 置于流化床反应器中， 通氮气或惰性气体置换 0.5〜2h后切换为氢气， 升温至 100〜600°C， 恒温还 原， 将废催化剂中的氧化钌还原为金属钌；
3) 将臭氧和空气的混合气通入步骤 2) 中得到的金属钌， 对金属钌进行 氧化， 温度控制在 600〜650°C， 产生四氧化钌气体；
4) 将步骤 3) 中产生的四氧化钌气体导入盛有硝酸溶液的三级吸收装置 中， 得到硝酸钌的酸溶液；
5)将亚硝酸钠固体加入步骤 4)中得到的硝酸钌的酸溶液中， 适当搅拌， 加热至溶液微沸回流， 制得含亚硝酰硝酸钌的溶液；
6) 将步骤 5) 中得到的含亚硝酰硝酸钌的溶液用无水乙醚萃取， 收集乙 醚萃取液， 再将乙醚蒸发， 得到亚硝酰硝酸钌固体。
2、 根据权利要求 1 所述的利用含钌废催化剂制备固体亚硝酰硝酸钌的 方法， 其特征在于： 所述步骤 1) 中， 含钌废催化剂的干燥条件为在氮气或 惰性气体氛围中升温至 100〜150°C， 干燥 l〜2h。
3、 根据权利要求 1 所述的利用含钌废催化剂制备固体亚硝酰硝酸钌的 方法， 其特征在于： 所述步骤 2) 中， 氢气的流速为 1200〜4000h- 还原时 间为 l〜12h。
4、 根据权利要求 3 所述的利用含钌废催化剂制备固体亚硝酰硝酸钌的 方法， 其特征在于： 所述步骤 2) 中， 还原时间为 6〜12h。
5、 根据权利要求 1 所述的利用含钌废催化剂制备固体亚硝酰硝酸钌的 方法， 其特征在于： 所述步骤 3 ) 中， 臭氧和空气的混合气的流速为 1200〜 400011 1 , 臭氧在所述混合气中的体积分数为 1〜20%， 氧化时间为 l〜12h。
6、 根据权利要求 5 所述的利用含钌废催化剂制备固体亚硝酰硝酸钌的 方法， 其特征在于： 所述步骤 3 ) 中， 臭氧的体积分数为 15%， 氧化时间为 8〜12h。
7、 根据权利要求 1 所述的利用含钌废催化剂制备固体亚硝酰硝酸钌的 方法， 其特征在于： 所述步骤 4 ) 中， 硝酸溶液的温度为 50〜95 °C、 质量浓 度为 45〜68%， 根据含钌废催化剂中钌的负载量计算硝酸溶液的理论用量， 取理论用量的 1.2〜2.0倍作为硝酸溶液的实际用量， 且硝酸溶液的盛放容器 为三个串联的棕色容器。
8、 根据权利要求 1 所述的利用含钌废催化剂制备固体亚硝酰硝酸钌的 方法， 其特征在于： 所述步骤 5 ) 中， 根据含钌废催化剂中钌的负载量计算 亚硝酸钠固体的理论用量， 取理论用量的 1.5〜2.0倍作为亚硝酸钠固体的实 际用量， 加热回流的时间为 l〜8h。
9、 根据权利要求 8 所述的利用含钌废催化剂制备固体亚硝酰硝酸钌的 方法， 其特征在于： 所述步骤 5 ) 中， 加热回流的时间为 4〜8h。
10、 根据权利要求 1〜9 中任一项所述的利用含钌废催化剂制备固体亚 硝酰硝酸钌的方法， 其特征在于： 所述含钌废催化剂为负载型含钌废催化剂， 其载体为氧化铝、 二氧化硅、 二氧化锆、 二氧化钛和沸石中的一种或几种混 合物的组合。
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