Natural gas liquid upgrading by ionic liquid catalyzed alkylation
We provide a process, comprising: a. dehydrogenating natural gas liquid to produce a mixture comprising olefins and unconverted paraffins; b. without further purification or modification other than mixing with an isoparaffin, sending the mixture to a single alkylation reactor; c. alkylating the olefins with the isoparaffin, using an ionic liquid catalyst, to produce one or more alkylate products; and d. distilling the one or more alkylate products and collecting a bottoms distillation fraction that is a middle distillate blending component having a sulfur level of 50 wppm or less and a Bromine number less than 1.
1. A process for making one or more alkylate products, comprising:
a. dehydrogenating a natural gas feedstock comprising saturated hydrocarbons in a dehydrogenation reactor to produce a mixture comprising one or more olefins and one or more unconverted paraffins, wherein the one or more olefins is at least 60 wt % of one or more isopentenes;
b. without further purification or modification other than mixing with isopentane, sending the mixture mixed with isopentane to a single alkylation reactor that is not thermally coupled with the dehydrogenation reactor; and
c. alkylating the one or more olefins with isopentane in the single alkylation reactor, using an ionic liquid catalyst, to produce the one or more alkylate products; wherein the one or more alkylate products comprises an alkylate middle distillate with a smoke point of 35 or higher, a freeze point of −40° C. or lower, a Bromine number less than 2, and a sulfur level of 10 wppm or less.
2. The process of claim 1 , wherein the natural gas feedstock comprises paraffins in the range of from C2 to C6 paraffins.
3. The process of claim 1 , wherein the mixture comprises from 30 to 80 wt % of the one or more unconverted paraffins.
4. The process of claim 1 , wherein a molar ratio of the isopentane to the one or more olefins in the single alkylation reactor is from 4:1 to 12:1.
5. The process of claim 1 , wherein a molar ratio of the isopentane to the one or more olefins in the single alkylation reactor is adjusted to change a boiling range of the one or more alkylate products.
6. The process of claim 1 , wherein dehydrogenating conditions are adjusted depending on the one or more unconverted paraffins that were originally present in the natural gas feedstock, in order to control a dehydrogenation conversion of the natural gas feedstock.
7. The process of claim 1 , wherein dehydrogenating conditions include a pressure from 0 to 100 psig, and a temperature from 400° C. to 900° C.
8. The process of claim 1 , wherein the dehydrogenating is performed with a dehydrogenation catalyst comprising Pt/Al 2 O 3 , Cr/Al 2 O 3 , Pt/C or a combination thereof.
9. The process of claim 1 , additionally comprising maintaining an overall alkylation activity of the ionic liquid catalyst by separating a used ionic liquid catalyst from an effluent of the single alkylation reactor, regenerating a portion of the used ionic liquid catalyst, and returning both a regenerated ionic liquid catalyst from the portion of the used ionic liquid catalyst and the used ionic liquid catalyst remaining after the separating to the single alkylation reactor.
10. The process of claim 1 , wherein a co-catalyst comprising a chloride is added to the ionic liquid catalyst.
11. The process of claim 1 , wherein the natural gas feedstock is produced by a hydraulic fracturing.
12. The process of claim 1 , additionally comprising isomerizing the natural gas feedstock prior to the dehydrogenating, wherein the isomerizing converts some n-pentane in the natural gas feedstock to produce the isopentane that is subsequently alkylated in the single alkylation reactor.