CN112940780A - Diluent and preparation method and application thereof - Google Patents

Diluent and preparation method and application thereof Download PDF

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CN112940780A
CN112940780A CN201911254377.9A CN201911254377A CN112940780A CN 112940780 A CN112940780 A CN 112940780A CN 201911254377 A CN201911254377 A CN 201911254377A CN 112940780 A CN112940780 A CN 112940780A
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diluent
extraction
phase separation
fraction
separation time
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CN112940780B (en
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丛昱
唐南方
商庆浩
陈帅
吴春田
许国梁
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Dalian Institute of Chemical Physics of CAS
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Dalian Institute of Chemical Physics of CAS
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • 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
    • C22B60/00—Obtaining metals of atomic number 87 or higher, i.e. radioactive metals
    • C22B60/02—Obtaining thorium, uranium, or other actinides
    • C22B60/0204—Obtaining thorium, uranium, or other actinides obtaining uranium
    • C22B60/0217—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes
    • C22B60/0252—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes treatment or purification of solutions or of liquors or of slurries
    • C22B60/026—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes treatment or purification of solutions or of liquors or of slurries liquid-liquid extraction with or without dissolution in organic solvents
    • 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
    • C22B60/00—Obtaining metals of atomic number 87 or higher, i.e. radioactive metals
    • C22B60/02—Obtaining thorium, uranium, or other actinides
    • C22B60/04—Obtaining plutonium
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E30/00—Energy generation of nuclear origin
    • Y02E30/30—Nuclear fission reactors
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Geology (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Catalysts (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

The invention relates to a preparation method of a diluent. The method mainly comprises the following steps: using isoolefine and hydrogen as raw material and using M-La/Al2O3Is used as a catalyst, the reaction pressure is 0.5MPa to 3.0MPa, the reaction temperature is 100 ℃ to 300 ℃, and the space velocity is 5h‑1‑15h‑1And the hydrogen-oil ratio is 200:1-500:1, and the isoparaffin is generated by reaction. And then, rectifying the generated dodecane to separate out middle fraction, thus obtaining the target diluent. The diluent prepared by the invention is used for a spent fuel extractant, and can selectively extract and separate uranium and plutonium. The invention has mild operation condition and simple process, and the obtained diluent has excellent performance.

Description

Diluent and preparation method and application thereof
Technical Field
The invention relates to a preparation method of a diluent, in particular to a preparation method of a diluent required in a Purex process.
Background
The Purex (Prex) process is a widely applied process flow in the international post-treatment of the spent fuel at present, and is one of important technologies for guaranteeing the sustainable development of nuclear energy. The process adopts tributyl phosphate (TBP) as an extracting agent, and when the TBP is contacted with a spent fuel nitric acid aqueous solution, the process can selectively extract 3% -4% of uranium and plutonium which are used, and has extremely low extraction rate on fission products and impurities thereof, so that the uranium and the plutonium are separated from the fission products through multi-stage countercurrent extraction. And recycling the recycled uranium and plutonium in the mixed oxide fuel of the nuclear power plant. TBP has good chemical stability, high flash point, low volatility and poor water miscibility, can be easily regenerated after spent fuel treatment, is convenient to recycle, and is the most suitable extracting agent at present. However, TBP has a high density and viscosity and is not easily contacted with uranium or plutonium in the aqueous phase, and it needs to be diluted in order to obtain an optimum extraction effect. Currently, the common diluents are n-dodecane and higher kerosene. However, the two diluents have longer phase separation time and lower saturated extraction amount, and the extraction performance still has room for improvement. Therefore, there is still a need to develop a diluent with lower cost and higher performance.
Disclosure of Invention
The invention aims to provide a preparation method of a low-cost diluent with performance superior to that of n-dodecane and high-grade kerosene.
Based on the purpose, the invention adopts the technical scheme that:
A) based on the content of isoolefin (by mass percent, the content of C10-C12 isoolefin)>75%, C5-C8 fraction less than 5%, C14-C17 fraction less than 5%, and the balance of C9 and C13) and hydrogen as raw materials, and M-La/Al2O3As a catalyst, under the conditions of reaction pressure of 0.5MPa-5.0MPa, preferably 0.5-3MPa, reaction temperature of 100-400 ℃, preferably 100-300 ℃ and space velocity of 5h-1-20h-1Preferably 5h-1-15h-1The hydrogen-oil ratio is 100:1-800:1, preferably 200:1-500:1, and saturated chain hydrocarbon is generated through reaction under the condition;
B) and (4) rectifying the generated saturated chain hydrocarbon to separate out middle fraction, thus obtaining the target diluent.
The C12 isoolefin content in the step A) is more than 50%.
The catalyst in the step A)M-La/Al2O3Wherein M is one or two of Pd, Pt and other metals, the mass fraction of M in the catalyst is 0.5 wt% -2 wt%, preferably 0.5 wt% -1 wt%, and the mass fraction of La is 0.5 wt% -5 wt%, preferably 1 wt% -2 wt%; al (Al)2O3Is a mesoporous structure rich in unsaturated coordination, and has a specific surface area of 120m2/g-250m2Per g (preferably 150 m)2/g-220m2(g) an average pore diameter of 5nm to 8nm, M and La being dispersed as a single atom in Al2O3On a carrier.
During the rectification treatment in the step B), the theoretical plate number of the rectification column is 100-: 80-140 ℃ (preferably 90-120 ℃), and the kettle pressure is as follows: 0.1kPa to 1kPa (preferably 0.2kPa to 0.6kPa), and fractions with overhead vapor temperatures of 50 ℃ to 75 ℃ (preferably 55 ℃ to 70 ℃) are collected at a reflux ratio of: 10-20 (preferably 10-15).
The diluent prepared by the method is used for a spent fuel extractant, and can selectively extract and separate uranium and plutonium when being contacted with a nitric acid aqueous solution with a spent fuel molar concentration of 3.0mol/L-4.0 mol/L.
The concentration of metal ions in the spent fuel is 0.4mol/L-0.7mol/L.
The invention provides a preparation method of a diluent with high performance and low cost aiming at the problems of the existing diluent. The invention has mild operation condition and simple process, and the obtained diluent has excellent performance.
Detailed Description
To further illustrate the present invention, the following examples are set forth without limiting the scope of the invention as defined by the various appended claims.
Example 1
Preparation of the catalyst:
weighing 2.0g P123 and dissolving in 40ml of absolute ethyl alcohol, dripping 3ml of concentrated nitric acid, adding 7.5g of aluminum nitrate nonahydrate under vigorous stirring, and continuing stirring for 5 hours after the aluminum nitrate nonahydrate is completely dissolved. The resulting solution was then evaporated to dryness with ethanol at 60 ℃ and aged for 48 hours to give a pale yellow solid. And (3) putting the light yellow solid in a muffle furnace, raising the temperature rise rate to 400 ℃ at 1 ℃/min, and roasting for 4 hours to obtain alumina rich in unsaturated coordination (the coordination number of oxygen around an aluminum atom in the alumina is 4 coordination, 5 coordination and 6 coordination, wherein the unsaturated coordination is 5 coordination, the content of the unsaturated coordination can be determined by a solid nuclear magnetism characterization means, and the content of the unsaturated coordination in the alumina is 30%).
Pd (NH) is prepared according to the mass percentage of the final contents of Pd and La of the catalysts which are both 1 percent3)4Cl2And La (NO)3)3Adding required alumina (the specific surface area is 150 m) into the precursor solution (the mass concentration of Pd and La is 16.7g/L)2G, the average pore diameter is 7nm), evenly stirring, aging for 24h at room temperature, drying the obtained solid in an oven at 120 ℃ overnight, and then roasting for 4h at 400 ℃ to obtain Pd-La/Al2O3Catalyst (electron microscope results show that Pd and La are dispersed in Al in the form of single atom2O3Above).
Hydrogenation reaction of raw materials:
taking tetrapropylene (by mass percentage, the content of C10-C12 isoolefin is 76.8%, wherein the content of C12 is 43% of the mass of the tetrapropylene, the content of C5-C8 fraction is 2.1%, the content of C14-C17 fraction is 1.5%, and the balance is C9 and C13) as raw materials, reacting at the reaction temperature: 200 ℃, reaction pressure: 2MPa, volume space velocity: 10h-1Hydrogen-oil ratio: the hydrogenation reaction is carried out under the reaction condition of 300: 1. The conversion rate of the tetrapropylene hydrogenation product measured by a fluorescence indicator adsorption method is 100%.
And (3) rectifying a hydrogenation product:
the theoretical plate number of the rectifying tower is 200, and the temperature of the kettle in the rectifying tower is as follows: 100-125 ℃ and the kettle pressure is as follows: 0.5kPa, collecting the fraction with the overhead vapor temperature of 55-68 ℃, and the reflux ratio is as follows: 15, rectifying the tetrapropylene hydrogenation product under the rectification condition, wherein the cut product is the target diluent (according to the mass percentage content, the content of C10-C12 isoparaffin is 95.6 percent, wherein the content of C12 is 54 percent of the mass of the diluent, the fraction below C8 is 0.4 percent, the fraction above C14 is 0.7 percent, and the rest is C9 and C13 fractions).
Extraction experimental testing of diluents:
1. phase separation time:preparing 30 percent TBP-diluent solution according to the volume ratio, and respectively mixing with 1mol/L HNO3Or the 1mol/L NaOH solution is oscillated in equal volume and fully mixed, then the phase separation time is recorded by standing, and the phase separation time of the two systems is the same and is 0.9 min.
Preparing a 30 percent TBP-n-dodecane solution and 1mol/L HNO respectively according to the volume ratio3Oscillating the solution in equal volume, fully mixing, standing and recording the phase separation time, wherein the phase separation time of the two systems is the same and is 1.5 min; the phase separation time of the target diluent is 0.9min better than 1.5min for n-dodecane.
2. And (3) testing the extraction performance: preparing 30 percent TBP-diluent solution according to the volume ratio, and mixing with 3.5mol/L HNO3The dissolved metal ion solutions with a molar concentration of 0.55mol/L Pu (IV) were mixed well in a volume ratio of 1:1, and the saturated extraction capacity of the metal in a 30% TBP-diluent solution was determined. The extraction saturation capacity of 30 percent TBP-target diluent is 96g/L and the extraction saturation capacity of 30 percent TBP-n-dodecane is 58 g/L.
Example 2
The target diluent obtained in the same manner as described in example 1 except that the reaction temperature in the raw material hydrogenation step was changed to 100 ℃ was subjected to the extraction test (using 1mol/L HNO) under the conditions of example 13Phase separation time) was determined, phase separation time was 0.9min better than dodecane, 30% TBP-target diluent extraction saturation capacity was 88g/L during the extraction test.
Example 3
The target diluent obtained in the same manner as described in example 1 except that the reaction temperature in the raw material hydrogenation step was changed to 150 ℃ was subjected to the extraction test (using 1mol/L HNO) under the conditions of example 13Phase separation time) was determined, phase separation time was 0.9min better than dodecane, 30% TBP-target diluent extraction saturation capacity was 90g/L during the extraction test.
Example 4
The objective diluent obtained in the same manner as described in example 1 except that the reaction temperature in the step of hydrogenation reaction of the raw material was changed to 250 ℃ was subjected to the extraction test under the conditions of example 1 (using 1)mol/L HNO3Measuring phase separation time), the phase separation time is 0.9min better than dodecane, and the extraction saturation capacity of 30% TBP-target diluent is 96g/L in the extraction test process.
Example 5
The target diluent obtained in the same manner as described in example 1 except that the reaction temperature in the raw material hydrogenation step was changed to 300 ℃ was subjected to the extraction test (using 1mol/L HNO) under the conditions of example 13Measuring phase separation time), the phase separation time is 0.9min better than dodecane, and the extraction saturation capacity of 30% TBP-target diluent is 96g/L in the extraction test process.
Example 6
The target diluent obtained in the same manner as described in example 1 except that the reaction pressure in the raw material hydrogenation step was changed to 0.5MPa, and the extraction test was carried out under the conditions of example 1 (using 1mol/L of HNO)3Phase separation time) was determined, phase separation time was 0.9min better than dodecane, 30% TBP-target diluent extraction saturation capacity was 84g/L during the extraction test.
Example 7
The target diluent obtained in the same manner as described in example 1 except that the reaction pressure in the raw material hydrogenation step was changed to 1MPa, and the extraction experiment test (using 1mol/L HNO) was carried out under the conditions of example 13Phase separation time) was determined, phase separation time was 0.9min better than dodecane, 30% TBP-target diluent extraction saturation capacity was 88g/L during the extraction test.
Example 8
The target diluent obtained in the same manner as described in example 1 except that the reaction pressure in the raw material hydrogenation step was changed to 1.5MPa, and the extraction test was carried out under the conditions of example 1 (using 1mol/L HNO)3Phase separation time) was determined, phase separation time was 0.9min better than dodecane, 30% TBP-target diluent extraction saturation capacity was 91g/L during the extraction test.
Example 9
Except that the reaction pressure in the step of hydrogenation reaction of the raw material was changed to 2.5MPa, the same as that in example 1 was conductedThe target diluent obtained by the same method is subjected to extraction experimental test according to the conditions of example 1 (1 mol/L HNO is adopted)3Measuring phase separation time), the phase separation time is 0.9min better than dodecane, and the extraction saturation capacity of 30% TBP-target diluent is 96g/L in the extraction test process.
Example 10
The target diluent obtained in the same manner as described in example 1 except that the reaction pressure in the raw material hydrogenation step was changed to 3MPa, and the extraction experiment test (using 1mol/L HNO) was carried out under the conditions of example 13Measuring phase separation time), the phase separation time is 0.9min better than dodecane, and the extraction saturation capacity of 30% TBP-target diluent is 98g/L in the extraction test process.
Example 11
Except that the hollow speed in the step of the hydrogenation reaction of the raw material is changed into 5h-1In addition, the target diluent obtained in the same manner as described in example 1 was subjected to an extraction test (using 1mol/L of HNO) under the conditions of example 13Measuring phase separation time), the phase separation time is 0.9min better than dodecane, and the extraction saturation capacity of 30% TBP-target diluent is 98g/L in the extraction test process.
Example 12
Except that the hollow speed in the step of the hydrogenation reaction of the raw material is changed into 7.5h-1In addition, the target diluent obtained in the same manner as described in example 1 was subjected to an extraction test (using 1mol/L of HNO) under the conditions of example 13Measuring phase separation time), the phase separation time is 0.9min better than dodecane, and the extraction saturation capacity of 30% TBP-target diluent is 96g/L in the extraction test process.
Example 13
Except that the hollow speed in the raw material hydrogenation reaction step is changed into 12h-1In addition, the target diluent obtained in the same manner as described in example 1 was subjected to an extraction test (using 1mol/L of HNO) under the conditions of example 13Phase separation time) was determined, phase separation time was 0.9min better than dodecane, 30% TBP-target diluent extraction saturation capacity was 90g/L during the extraction test.
Example 14
Except that the space velocity in the step of hydrogenation reaction of raw materials is changed to 15h-1In addition, the target diluent obtained in the same manner as described in example 1 was subjected to an extraction test (using 1mol/L of HNO) under the conditions of example 13Phase separation time) was determined, phase separation time was 0.9min better than dodecane, and 30% TBP-target diluent extraction saturation capacity was 89g/L during the extraction test.
Example 15
Except that the hydrogen-to-oil ratio in the feed hydrogenation step was changed to 200:1 in addition, the target diluent obtained in the same manner as described in example 1 was subjected to the extraction test (using 1mol/L HNO) under the conditions of example 13Phase separation time) was determined, phase separation time was 0.9min better than dodecane, 30% TBP-target diluent extraction saturation capacity was 91g/L during the extraction test.
Example 16
Except that the hydrogen-to-oil ratio in the feed hydrogenation step was changed to 400: 1 in addition, the target diluent obtained in the same manner as described in example 1 was subjected to the extraction test (using 1mol/L HNO) under the conditions of example 13Phase separation time) was determined, in the course of the extraction test, the phase separation time was 0.9min better than dodecane, and the 30% TBP-target diluent extraction saturation capacity was 92 g/L.
Example 17
Except that the hydrogen-oil ratio in the step of hydrogenation reaction of the raw material was changed to 500:1 in addition, the target diluent obtained in the same manner as described in example 1 was subjected to the extraction test (using 1mol/L HNO) under the conditions of example 13Phase separation time) was determined, in the course of the extraction test, the phase separation time was 0.9min better than dodecane, and the 30% TBP-target diluent extraction saturation capacity was 92 g/L.
Example 18
The target diluent obtained in the same manner as described in example 1 except that Pd was changed to Pt during the preparation of the catalyst, and the experimental extraction test (using 1mol/L HNO) was carried out under the same conditions as in example 13To determine the phase separation time), during the extraction test,in the extraction test process, the phase separation time is 0.9min and is better than that of dodecane, and the extraction saturation capacity of 30 percent TBP-target diluent is 97 g/L.

Claims (8)

1. A preparation method of a diluent mainly comprises the following steps:
A) using C10-C12 isoolefin and hydrogen as raw material, and using M-La/Al2O3The catalyst M is one or the combination of more than two of Pd and Pt, the reaction pressure is 0.5MPa to 5.0MPa, preferably 0.5MPa to 3MPa, the reaction temperature is 100 ℃ to 400 ℃, preferably 100 ℃ to 300 ℃, and the space velocity is 5h-1-20h-1Preferably 5h-1-15h-1The hydrogen-oil ratio is 100:1-800:1, preferably 200:1-500:1, and saturated chain hydrocarbon is generated through reaction under the condition;
B) and (4) rectifying the generated saturated chain hydrocarbon to separate out middle fraction, thus obtaining the target diluent.
2. The method of claim 1, wherein: the composition of the isomeric olefin containing carbon number C10-C12 comprises the following components in percentage by mass, wherein the content of the isomeric olefin containing carbon number C10-C12 is more than 75%, the content of the olefinic fraction containing C5-C8 is less than 5%, the content of the olefinic fraction containing C14-C17 is less than 5%, and the balance is the olefinic fraction containing C9 and/or C13.
3. The method of claim 2, wherein: the C12 isoolefin in the isoolefin containing C10-C12 accounts for more than 40% of the mass of the isoolefin raw material containing C10-C12.
4. The method of claim 1, wherein: the catalyst M-La/Al2O3Wherein M is one or the combination of more than two of Pd, Pt and other metals, the mass fraction of M in the catalyst is 0.5 wt% -2 wt%, preferably 0.5 wt% -1 wt%, and the mass fraction of La is 0.5 wt% -5 wt%, preferably 1 wt% -2 wt%; al (Al)2O3Is a mesoporous structure rich in unsaturated coordination (20-35 percent), and has a specific surface area of 120m2/g-250m2Per g (preferably 150 m)2/g-220m2(g) an average pore diameter of 5nm to 8nm, M and La being dispersed as a single atom in Al2O3On a carrier.
5. The method of claim 1, wherein: during the rectification treatment, the theoretical plate number of the rectification tower is 100-: 80-140 ℃ (preferably 90-120 ℃), and the kettle pressure is as follows: 0.1kPa to 1kPa (preferably 0.2kPa to 0.6kPa), and collecting a fraction (namely the target diluent) with the overhead vapor temperature of 50 ℃ to 75 ℃ (preferably 55 ℃ to 70 ℃), and the reflux ratio is as follows: 10-20 (preferably 10-15).
6. A diluent prepared by the method of any one of claims 1 to 5.
7. Use of the diluent of claim 6, wherein: the extraction agent for the spent fuel can selectively extract and separate uranium and plutonium when being contacted with a nitric acid aqueous solution with the molar concentration of the spent fuel of 3.0mol/L-4.0 mol/L.
8. Use of a diluent according to claim 7, wherein: the concentration of metal ions (uranium and plutonium) in the spent fuel is 0.4mol/L to 0.7mol/L.
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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN85100760A (en) * 1985-04-01 1986-09-24 中国科学院山西煤炭化学研究所 Hydrofining catalyst for hydrogenation of alkenes and method for making thereof
CN1072461A (en) * 1991-06-19 1993-05-26 美国能源部 The combined extraction method of transuranium element and strontium
US20020068843A1 (en) * 2000-09-29 2002-06-06 Wei Dai Selective hydrogenation catalyst for selectively hydrogenating of unsaturated olefin, process for preparing the same and its use
CN103084169A (en) * 2011-10-28 2013-05-08 中国石油化工股份有限公司 Unsaturated hydrocarbon hydrogenation catalyst, preparation method and applications thereof
CN106893878A (en) * 2017-03-02 2017-06-27 中国原子能科学研究院 A kind of method that plutonium is reclaimed in the spentnuclear fuel from radioactivity

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN85100760A (en) * 1985-04-01 1986-09-24 中国科学院山西煤炭化学研究所 Hydrofining catalyst for hydrogenation of alkenes and method for making thereof
CN1072461A (en) * 1991-06-19 1993-05-26 美国能源部 The combined extraction method of transuranium element and strontium
US20020068843A1 (en) * 2000-09-29 2002-06-06 Wei Dai Selective hydrogenation catalyst for selectively hydrogenating of unsaturated olefin, process for preparing the same and its use
CN103084169A (en) * 2011-10-28 2013-05-08 中国石油化工股份有限公司 Unsaturated hydrocarbon hydrogenation catalyst, preparation method and applications thereof
CN106893878A (en) * 2017-03-02 2017-06-27 中国原子能科学研究院 A kind of method that plutonium is reclaimed in the spentnuclear fuel from radioactivity

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