초록 ▼

Disclosed is a process for reducing sulfur and olefin contents in gasoline, comprising contacting gasoline feedstock and hydrogen with a hydrorefining catalyst and an paraffin-modification catalyst. The effluent of the process is separated to obtain a hydrotreated gasoline fraction free of mercaptan

Disclosed is a process for reducing sulfur and olefin contents in gasoline, comprising contacting gasoline feedstock and hydrogen with a hydrorefining catalyst and an paraffin-modification catalyst. The effluent of the process is separated to obtain a hydrotreated gasoline fraction free of mercaptan and having a low content of sulfur, e.g. less than 200 ppm, a low content of olefins, e.g. less than 20% by volume, and little octane loss. The hydrotreated gasoline fraction can be used as blending component of a final gasoline product.

대표청구항 ▼

The invention claimed is: 1. A process for reducing sulfur and olefin contents in gasoline, comprising: a) contacting gasoline feedstock containing 35-70% by volume of olefins and hydrogen with a hydrorefining catalyst under reaction conditions including a hydrogen/gasoline ratio of 200-600 Nm3/m3,

The invention claimed is: 1. A process for reducing sulfur and olefin contents in gasoline, comprising: a) contacting gasoline feedstock containing 35-70% by volume of olefins and hydrogen with a hydrorefining catalyst under reaction conditions including a hydrogen/gasoline ratio of 200-600 Nm3/m3, a hydrogen partial pressure of 1.0 to 4.0 MPa, a temperature of 200-380�� C. and a liquid hourly space velocity of 3.0-5.0 h-1; b) contacting the hydrorefined gasoline and hydrogen with a paraffin-modification catalyst under reaction conditions including a hydrogen/gasoline ratio of 200-1000 Nm3/m3, a hydrogen partial pressure of 1.0-4.0 MPa, a temperature of 300-460�� C. and a liquid hourly space velocity of 0.5-4.0 h-1 to provide an effluent, which is separated to obtain the hydrotreated gasoline fraction, wherein the paraffin-modification catalyst comprises one or more noble or non-noble metals from Group VIII and/or Group VIB, supported over a supporter containing at least a ZSM-5 zeolite; and wherein the effluent from the hydrorefining reaction has a nitrogen content of less than 2 ppm and an olefin content of less than 5% by volume. 2. The process of claim 1, wherein said gasoline feedstock is FCC gasoline, DCC gasoline, straight-run gasoline, coker gasoline, pyrolysis gasoline, thermal cracking gasoline and a mixture thereof. 3. The process of claim 2, wherein said gasoline feedstock is the whole fractions, or a part of the whole fractions of FCC gasoline, DCC gasoline, straight-run gasoline, coker gasoline, pyrolysis gasoline, thermal cracking gasoline and a mixture thereof. 4. The process of claim 3, wherein said gasoline feedstock is a heavy fraction of FCC gasoline, deep catalytic cracking gasoline, straight-run gasoline, coker gasoline, pyrolysis gasoline, thermal cracking gasoline and a mixture thereof cut at a temperature of 70-100�� C. 5. The process of claim 1, wherein the gasoline feedstock contains 35-60% by volume of olefins. 6. The process of claim 1, wherein the hydrorefining catalyst comprises one or more non-noble metals from Group VIB and Group VIII supported over an alumina or amorphous aluminum silicate. 7. The process of claim 1 or 6, further comprising contacting the gasoline feedstock with a hydro-protecting catalyst before the hydrorefining catalyst bed. 8. The process of claim 7, wherein said hydro-protecting catalyst comprises one or more metals from Group VIII, one or more metals from Group VIB, and one or more alkali metals, supported over an alumina supporter. 9. The process of claim 8, wherein said hydro-protecting catalyst comprises an alumina supporter and, Co and/or Ni, Mo and/or W and an alkali metal, supported over the alumina supporter, all calculated as oxides and based on the total amount of the catalyst, wherein the catalyst comprises 0.5-8% by weight of Co and/or Ni, 2-25% by weight of Mo and/or W and 0.5-8% by weight of the alkali metal, the balance being the alumina supporter. 10. The process of claim 9, wherein said hydro-protecting catalyst comprises Co and/or Ni in an amount of 1-6% by weight, Mo and/or W in an amount of 4-12% by weight and the alkali metal in an amount of 2.5-6% by weight, all calculated as oxides and based on the total amount of the catalyst, the balance being the alumina supporter. 11. The process of claim 1, wherein the paraffin-modification catalyst comprises 0.5-10% by weight of one or more metals from Group VIII, and 10-75% by weight of the ZSM-5 zeolite, the balance being alumina. 12. The process of claim 11, wherein the paraffin-modification catalyst comprises 1-5% by weight of Ni and/or Co, 5-30% by weight of W or Mo and 30-40% by weight of ZSM-5 zeolite, the balance being alumina.