ES2573407T3 - Compuestos catalizadores de oxidación diésel en capas - Google Patents

Compuestos catalizadores de oxidación diésel en capas Download PDF

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ES2573407T3
ES2573407T3 ES10732120.0T ES10732120T ES2573407T3 ES 2573407 T3 ES2573407 T3 ES 2573407T3 ES 10732120 T ES10732120 T ES 10732120T ES 2573407 T3 ES2573407 T3 ES 2573407T3
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palladium
oxidation catalyst
diesel oxidation
catalyst compounds
surface area
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Shahjahan M. Kazi
Michel Deeba
Torsten Neubauer
Helmut Alfred Punke
Wolfgang Torsten Mueller-Stach
Gerd Grubert
A. Stanley Roth
Barmont Jeffrey Hoke
Shiang Sung
Yuejin Li
Xinyi Wei
Chung-Zong Wan
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BASF Corp
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    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
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    • B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
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Abstract

Un compuesto catalizador de oxidación diésel en capas, que comprende: un material catalítico de oxidación diésel sobre un vehículo, donde el material catalítico comprende un componente de paladio en una cantidad en el intervalo de 5 a 75 g/pie3 (0.18 a 2.65 kg/m3) y por lo menos dos capas: una capa trampa de hidrocarburo que comprende por lo menos un tamiz molecular, donde la capa trampa de hidrocarburo es sustancialmente libre de paladio; y una capa que contiene paladio que comprende el componente de paladio, y está sustancialmente libre de un tamiz molecular, en la que el componente de paladio está localizado sobre un soporte de óxido metálico refractario poroso, de elevada área superficial; en la que el soporte de óxido metálico refractario poroso de elevada área superficial comprende alúmina que tiene un volumen de poro en el intervalo de 0.5 a 1.5 cm3/g y un promedio de diámetro de poro de por lo menos 75 Å.

Description

imagen1
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tamaño 1.5" x 3.0" (3.8 cm x 7.6 cm) con envejecimiento de laboratorio a aproximadamente 750°C por 5 horas en corriente de aire al 10 %. Después del envejecimiento, se evaluó en los compuestos el inicio de la reacción catalítica, usando un sistema reactor de laboratorio. El protocolo de prueba de inicio de la reacción catalítica incluyó una composición de gas de prueba de 1500 ppm de CO, 400 ppm de C1 (134 ppm de C3H6, 133 ppm de C7H8, n
5 C10H22), 10 % de O2, 100 ppm de NO, 5 % de CO2, y 7 % de H2O. La rata de la rampa fue de 15°C/min. La velocidad espacial era 50,000 h-1. No hubo saturación inicial en la alimentación de gas de reacción.
Se midieron las conversiones de HC/CO mientras se aumentó rápidamente la temperatura de 80°C a 325°C. Se midió la concentración de CO usando un equipo de Análisis Infrarrojo de Transformada de Fourier (FTIR). Se midieron los hidrocarburos totales (THC) usando un FID. En la tabla 1 se reporta la temperatura a la cual ocurrió 50
10 % de la conversión de CO y THC.
Tabla 1:
HC, °C
CO,°C
Ejemplo 1
157 156
Ejemplo 2
153 154
Ejemplo 3 de comparación
170 177
Los resultados de la prueba de inicio de la reacción catalítica indicaron claramente los beneficios del uso de catalizador que tiene paladio separado de la capa de zeolita, y que tiene una alúmina porosa en la capa interior, que
15 soporta los componentes de metal precioso.
Ejemplo 5
Se evaluó el efecto de la porosidad sobre el soporte del catalizador. La prueba de inicio de la reacción catalítica fue hecha sobre soportes recubiertos individuales formados de acuerdo con los métodos establecidos aquí en "Preparation of Catalyst Composites" de revestimientos delgados que contienen polvos de alúmina de alta
20 porosidad, en niveles de carga de 0.06 g/cm3 (1 g/pulgada3) y metales preciosos de platino y paladio, que tienen una relación Pt:Pd de 2:1 para cargas de 2.1 g/L (60 g/pie3). La alúmina de alta porosidad de la muestra 5A muestra una ventaja de inicio de la reacción catalítica de 25°C, comparada con una alúmina de baja porosidad de la muestra 5B (de comparación) como se muestra en la Tabla 2.
Tabla 2:
Muestra
Área superficial de alúmina (m2/g) Volumen total de poro de alúmina (cm3/g) Tamaño promedio de poro de alúmina (diámetro) Inicio de reacción catalítica de CO (T50, °C)
5A
148 0.85 99 179
5B de comparación
143 0.47 50 204
25
Ejemplo 6
Se evaluó el efecto de la segregación de paladio y la mayoría del platino de la zeolita. Se evaluó la conversión de monóxido de carbono para 3 catalizadores usando un vehículo de prueba EURO 4, de 2.0 L durante la prueba NEDC después de un envejecimiento del motor a 750 °C/24 horas. Los catalizadores tenían las siguientes 30 composiciones y estructuras y suministraron la citada eficiencia de conversión de CO, como se muestra en la Tabla
3:
10
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Claims (1)

  1. imagen1
    imagen2
ES10732120.0T 2009-01-16 2010-01-15 Compuestos catalizadores de oxidación diésel en capas Active ES2573407T3 (es)

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US14541209P 2009-01-16 2009-01-16
US145412P 2009-01-16
US12/687,597 US8329607B2 (en) 2009-01-16 2010-01-14 Layered diesel oxidation catalyst composites
US687597 2010-01-14
PCT/US2010/021107 WO2010083357A2 (en) 2009-01-16 2010-01-15 Layered diesel oxidation catalyst composites

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EP (1) EP2387463B2 (es)
JP (1) JP5787768B2 (es)
KR (1) KR101598647B1 (es)
CN (1) CN102355951B (es)
BR (1) BRPI1007322B1 (es)
ES (1) ES2573407T3 (es)
PL (1) PL2387463T3 (es)
WO (1) WO2010083357A2 (es)

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US8211392B2 (en) * 2009-01-16 2012-07-03 Basf Corporation Diesel oxidation catalyst composite with layer structure for carbon monoxide and hydrocarbon conversion
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