초록 ▼

A process for the recovery of gaseous products from the product mixture obtained by contacting a hydrocarbon feed with a catalyst in a fluid catalytic cracking process, wherein the liquid, obtained by separating the top product of main fractionators into gaseous and liquid fraction, when supplied to

A process for the recovery of gaseous products from the product mixture obtained by contacting a hydrocarbon feed with a catalyst in a fluid catalytic cracking process, wherein the liquid, obtained by separating the top product of main fractionators into gaseous and liquid fraction, when supplied to the absorber has a temperature of between about 8-25 DEG C. This liquid may be pre-saturated with gaseous top product from absorber; or also a high boiling fraction (cat cracker naphtha/light cycle oil) may be first separated from this liquid by distillation.

대표청구항 ▼

The invention claimed is: 1. A process for the recovery of gaseous products from a product mixture obtained by contacting a hydrocarbon feed with a catalyst in a fluid catalytic cracking process, wherein the recovery comprises; the following sequence of steps: (a) separating the product mixture in

The invention claimed is: 1. A process for the recovery of gaseous products from a product mixture obtained by contacting a hydrocarbon feed with a catalyst in a fluid catalytic cracking process, wherein the recovery comprises; the following sequence of steps: (a) separating the product mixture in a first distillation step in which a gaseous top product is obtained comprising products boiling below about 200째 C.; (b) cooling the gaseous top product of step (a) to obtain a first liquid and gaseous fractions and separating said first liquid and gaseous fractions to provide a first liquid fraction and a first gaseous fraction; (c) pressurizing the first gaseous fraction obtained in step (b) in a compressor step to obtain a pressurized product; (d) cooling the pressurized product of step (c) and to obtain a second liquid and gaseous fractions and separating said second liquid and gaseous fractions to provide a second liquid fraction and a second gaseous fraction; (e) supplying the second gaseous fraction obtained in step (d) to an absorber section of a stripper-absorber column in which the second gaseous fraction is contacted with the first liquid fraction obtained in step (b) to thereby provide for yielding from said stripper-absorber column a lower boiling fraction rich in gaseous products having a boiling point of ethane or below; (f) supplying the second liquid fraction obtained in step (d) to a stripper section of said stripper-absorber column which provides for yielding from said stripper-absorber column a liquid fraction rich in hydrocarbons having a boiling point higher than ethane; and, (g) supplying the liquid fraction rich in hydrocarbons having a boiling point higher than ethane obtained in step (f) to a debutanizer distillation step whereby a light fraction comprising butane and lower boiling compounds and a higher boiling fraction are obtained, wherein the first liquid fraction obtained in step (b) has a temperature of between from about 8째 C. to about 25째 C. when supplied to the absorber section in step (e). 2. The process according to claim 1, wherein the first liquid fraction obtained in step (b) has a temperature of between from about 12째 C. to about 20째 C. when supplied to the absorber section in step (e). 3. The process according to claim 2, wherein a heavy boiling fraction is first separated from the first liquid fraction obtained in step (b) before using this fraction in step (e). 4. The process according to claim 2, wherein the content of the absorber section in step (e) is cooled by making use of a side cooler. 5. The process according to claim 2, wherein part of the first liquid fraction obtained in step (b) is directly supplied to the debutanizer distillation step (g). 6. The process of claim 5, wherein the content of the absorber section in step (e) is cooled by making use of a side cooler. 7. The process according to claim 1, wherein a heavy boiling fraction is first separated from the first liquid fraction obtained in step (b) before using this fraction in step (e). 8. The process according to claim 7, wherein the initial boiling point of the heavy boiling fraction has an initial boiling point of between from about 100째 C. to about 160째 C. 9. The process of claim 7, wherein part of the first liquid fraction obtained in step (b) is directly supplied to the debutanizer distillation step (g). 10. The process according to claim 1, wherein the content of the absorber section in step (e) is cooled by making use of a side cooler. 11. The process according to claim 1, wherein part of the first liquid fraction obtained in step (b) is directly supplied to the debutanizer distillation step (g).