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二段加氢催化剂
相关语句
  secondary hydrogenation catalyst
     Application of hot circulation regeneration of pyrolysis gasoline secondary,hydrogenation catalyst
     裂解汽油二段加氢催化剂热氢循环再生法的工业应用
短句来源
     The pyrolysis gasoline secondary hydrogenation catalyst was studided by hot circulation regeneration. The industrial test showed that the running period of the catalyst increased from 6 months to 16 months with good effect.
     采用热氢循环法对裂解汽油二段加氢催化剂进行再生活化 ,在小试提供的工艺参数基础上 ,经工业实验获得成功 ,催化剂运行周期由小于 6个月提高到 1 6个月以上 ,效果良好。
短句来源
  “二段加氢催化剂”译为未确定词的双语例句
     Study of Two Stage Hydrogenation Catalystfor High Space Velocity Cracking Gasoline
     高空速裂解汽油二段加氢催化剂的研究
短句来源
     PREPARATION AND COMMERCIAL APPLICATION OF DZ-1 CATALYST FOR PYROLYSIS NAPHTHA SECONDARY HYDROGENATION
     DZ-1裂解汽油二段加氢催化剂的研制与工业应用
短句来源
     Commercial trial production and application of LH-02 second-stage hydrodesulfurization catalyst for pyrolysis gasoline
     LH-02裂解汽油二段加氢催化剂的工业试生产及应用
短句来源
     The process for laboratory preparation of a Co-Mo-Ni/Al 2O 3 pyrolysis gasoline two-stage hydrogenation catalyst was described,which includes shape-forming of the carrier,preparation of co-impregnating liquor,spraying impregnation and activation.
     介绍了 Co- Mo- Ni/Al2 O3型裂解汽油二段加氢催化剂的实验室制备工艺 ,包括载体成型、共浸液配制、喷浸与活化等过程。
短句来源
     Development of DZCⅡ-1 catalyst for secondary hydrogenation of pyrolysis gasoline
     新一代裂解汽油二段加氢催化剂的开发
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  相似匹配句对
     Two.
     .
短句来源
     二.
     .
短句来源
     PROCESS PROCEDURE FOR THE BAKING OF SECONDARY REFORMER
     转化炉烘炉工艺过程
短句来源
     COMPREHENSIVE UTILIZATION OF TWO\|STAGE PURIFIED RESIDUE
     净化渣综合利用
短句来源
     It has been proved that CN 20 is a very excellent second reforming catalyst.
     是一种较为理想的转化催化剂
短句来源
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The process for laboratory preparation of a Co-Mo-Ni/Al 2O 3 pyrolysis gasoline two-stage hydrogenation catalyst was described,which includes shape-forming of the carrier,preparation of co-impregnating liquor,spraying impregnation and activation.Influnce of metal loading amount on activity of the catalyst was investigated and formulation of teh catalyst determined.Under the condition of reaction temperature 230~280℃,hydrogen pressure 4.2MPa,volumetric space...

The process for laboratory preparation of a Co-Mo-Ni/Al 2O 3 pyrolysis gasoline two-stage hydrogenation catalyst was described,which includes shape-forming of the carrier,preparation of co-impregnating liquor,spraying impregnation and activation.Influnce of metal loading amount on activity of the catalyst was investigated and formulation of teh catalyst determined.Under the condition of reaction temperature 230~280℃,hydrogen pressure 4.2MPa,volumetric space velocity 4.7h -1 ,hydrogen/oil volumetric ratio 300:1,the catalyst met the requirement of pyrolysis gasoline hydrogenation,with less than 0.5g Br/100g-oil and no diolefin in the product.

介绍了 Co- Mo- Ni/Al2 O3型裂解汽油二段加氢催化剂的实验室制备工艺 ,包括载体成型、共浸液配制、喷浸与活化等过程。重点考察了金属负载量对催化剂活性的影响 ,确定出催化剂的组成范围。该催化剂在反应温度 2 30~ 2 80℃ ,氢分压 4 .2 MPa,体积空速 4 .7h- 1 ,氢油体积比 30 0∶ 1的条件下 ,满足裂解汽油加氢的工艺要求 ,产品油溴价≤ 0 .5g- Br/1 0 0 g-油 ,二烯价为 0

Pseudo bochmite was extruded to shaping three leaves and used as matrix. The catalyst for pyrolysis naphtha secondary hydrogenation was prepared by immersing transition metals on the matrix. Catalyst evaluation was conducted on a 100 ml unit. The bromine number and diolefin number of the hydrogenation products were less than 0.5 gBr/(100 g) and 0 respectively at a hydrogen partial pressure of 4.2 MPa, a volume space velocity of 3.0 h -1 , a hydrogen/oil volume ratio of 200-300∶1 and a reaction temperature...

Pseudo bochmite was extruded to shaping three leaves and used as matrix. The catalyst for pyrolysis naphtha secondary hydrogenation was prepared by immersing transition metals on the matrix. Catalyst evaluation was conducted on a 100 ml unit. The bromine number and diolefin number of the hydrogenation products were less than 0.5 gBr/(100 g) and 0 respectively at a hydrogen partial pressure of 4.2 MPa, a volume space velocity of 3.0 h -1 , a hydrogen/oil volume ratio of 200-300∶1 and a reaction temperature range of 210-280 ℃. The catalyst stood up to 1 500 h activity stability test. The commercial made catalyst reached the laboratory level. It can be used at a volume space velocity of 3.0 h -1 as well as high space velocity such as 4.7 h -1 .

采用拟薄水铝石粉进行挤条成型制得了三叶草载体 ,用过渡金属浸渍制备出了DZ 1裂解汽油二段加氢催化剂。在 10 0mL小型加氢装置上 ,在氢分压 4.2MPa ,体积空速 3 .0h-1,氢油体积比 2 0 0~ 30 0∶1,反应温度 2 10~ 2 80℃的条件下 ,生成油的溴值小于等于 0 .5gBr/ 10 0g油 ,二烯值为 0。同时通过了 15 0 0h的活性稳定性试验。工业生产的催化剂达到了实验室的水平 ,不但可在体积空速 3.0h-1下使用 ,而且也可以在 4.7h-1空高速下使用。

a new type of pyrolysis gasoline two-stage hydrogenation catalyst is developed. By way of bearer modifying and bore expanding and multiple metallic elements impregnated in special co-impregnation liquid to prepare catalyst which has good activity. When oil stock bromine valency is greater or equal to 17.2 gBr2/100g, diene valency is less than or equal to 3.0 gI2/100g, process conditions are: hydrogen partial pressure is 4.2 MPa, volumetric space velocity is 3.0 h-1, hydrogen-to-oil ration is 200:1~300:1, reaciton...

a new type of pyrolysis gasoline two-stage hydrogenation catalyst is developed. By way of bearer modifying and bore expanding and multiple metallic elements impregnated in special co-impregnation liquid to prepare catalyst which has good activity. When oil stock bromine valency is greater or equal to 17.2 gBr2/100g, diene valency is less than or equal to 3.0 gI2/100g, process conditions are: hydrogen partial pressure is 4.2 MPa, volumetric space velocity is 3.0 h-1, hydrogen-to-oil ration is 200:1~300:1, reaciton temperature is 220~280 ℃, the bromine valency of formation oil is less than or equal to 0.5 gBr2/100g, diene valency is zero , which is successfully applied in industrial units.

研制开发了新型裂解汽油二段加氢催化剂 ,经过载体改性和扩孔,采用特制共浸液浸渍多种金属元素,所制备的催化剂活性较好。在原料油溴价≥17.2 gBr2/100g,二烯价≤ 3.0 gI2/100g,工艺条件为:氢分压4.2 MPa,体积空速3.0 h-1,氢油体积比200:1~300:1 ,反应温度220~280 ℃,使生成油的溴价≤0.5 gBr2/100g,二烯价为0。并在工业装置得到成功应用。

 
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