| 摘要 |
The invention relates to a process for the production of middle-distillate hydrocarbon-containing bases from a butanol feedstock, with said process comprising at least the following stages:
a) isomerizing dehydration of butanol feedstock,b) separating the water from butylenic effluent,c) purifying the organic liquid effluent from stage b),d) oligomerizing of a feedstock that comprises at least a portion of the purified organic effluent from stage c), the entire effluent from stage g), and at least a portion of the light product from stage f),e) oligomerizing the first oligomerization effluent to produce a second oligomerization effluent,f) fractionating said second oligomerization effluent into at least three products: a light product that most comprises the C2 to C4 compounds, an intermediate product that mostly comprises the C5 to C9 compounds, and a middle distillate product that mostly comprises compounds having at least 10 carbon atoms,g) oligomerizing at least a portion of said intermediate product, andh) hydrogenating at least a portion of said middle distillate product. |
| 主权项 |
1. Process for the production of middle-distillate hydrocarbon-containing bases from a butanol feedstock, with said process comprising at least:
a) A stage for isomerizing dehydration of said butanol feedstock in the presence of an amorphous or zeolitic acid catalyst in at least one reactor, operating at an absolute pressure at the reactor inlet of between 0.5 and 1.2 MPa and at a temperature at the reactor inlet of between 350 and 450° C. in such a way as to produce an effluent that is for the most part butylene, b) A stage for separation of the water that is present in said butylenic effluent that operates at a pressure of between 0.5 and 1.2 MPa and at a temperature of between 35 and 60° C., c) A stage for purification of the organic liquid effluent that comes from stage b) in such a way as to produce a purified organic effluent, d) A first stage for oligomerization of a feedstock that comprises at least a portion of the purified organic effluent that comes from stage c), the entire effluent that comes from stage g), and at least a portion of the light product that comes from stage 0 in the presence of an amorphous catalyst in at least one reactor that operates at an absolute pressure of between 0.5 and 10 MPa, at a temperature of between 40 and 110° C., and at an hourly volumetric flow rate of between 0.1 and 10 h−1, in such a way as to produce a first oligomerization effluent, comprising at least 50% by weight of olefins having a number of carbon atoms that is greater than or equal to 8, with the percentage by weight being expressed relative to the total mass of olefins contained in said effluent, e) A second stage for oligomerization of said first oligomerization effluent, in the presence of an amorphous catalyst in at least one reactor that operates at an absolute pressure of between 2 and 15 MPa, at a temperature of between 100 and 200° C., and at an hourly volumetric flow rate of between 0.1 and 10 h−1, in such a way as to produce a second oligomerization effluent, f) A stage for fractionation of said second oligomerization effluent into at least three products that correspond respectively to a light product that for the most part comprises the C2 to C4 compounds, an intermediate product that for the most part comprises the C5 to C9 compounds, and a middle distillate product that for the most part comprises the compounds that have at least 10 carbon atoms, g) A third stage for oligomerization of at least a portion of said intermediate product in the presence of an amorphous catalyst in at least one reactor that operates at an absolute pressure of between 2 and 15 MPa, at a temperature of between 100 and 200° C., and at an hourly volumetric flow rate of between 0.1 and 5 h−1, and h) A stage for hydrogenation of at least a portion of said middle distillate product in the presence of a catalyst that comprises at least one metal of group VIII in at least one reactor that operates at an absolute pressure of between 2 and 4 MPa, at a temperature of between 100 and 350° C., and at an hourly volumetric flow rate of between 1 and 5 h−1 with a hydrogen to hydrocarbon H2/HC molar ratio of between 10 and 450. |
