China Petroleum & Chemical Corporation

Research Institute of Petroleum Processing, Sinopec

Other

China Petroleum Chemical Corporation

Chaogang Xie

Jiushun Zhang

Jun Long

Xingtian Shu

Hong Nie

Zhijian Da

Zhigang Zhang

Zheng Li

Yibin Luo

Dadong Li

Xieqing Wang

Lishun Dai

Anguo Mao

Genquan Zhu

Wei Wang

Youhao Xu

Yan Cui

Jianhong Gong

Shouye Cui

Jianguo Ma

Yongcan Gao

Qiang Fu

Qiang Liu

Xuhong Mu

Zhanzhu Zhang

Chuanfeng Niu

Wenhua Xie

Zaiting Li

Yihua Yang

Zhiguo Wu

Qiang Li

Tao Liu

Huiping Tian

Yi Luo

Nan Jiang

Zhenyu Chen

Yuxia Zhu

Zhihai Hu

Shuandi Hou

Minggang Li

Jun Fu

Kejia Xu

Yujian Liu

Yun Chen

Jingchuan Yu

Longsheng Tian

Jinbiao Guo

Fengmei Zhang

Weimin Lu

Zhiqiang Qiao

Yinan Yang

Jianwei Dong

Keyong Yang

Liuzhou Zhao

Youbao Lu

Dawei Guo

Shuandl Hou

Xiangbo Guo

Xueliang Chang

Shaobing Yu

Lisheng Li

Chenghan Yan

Wenyuan Shi

A process for producing light olefins and aromatics, which comprises reacting a feedstock by contacting with a catalytic cracking catalyst in at least two reaction zones, wherein the reaction temperature of at least one reaction zone among the reaction zones downstream of the first reaction zone is higher than that of the first reaction zone and its weight hourly space velocity is lower than that of the first reaction zone, separating the spent catalyst from the reaction product vapor, regenerating the separated spent catalyst and returning the regenerated catalyst to the reactor, and separating the reaction product vapor to obtain the desired products, light olefins and aromatics. This process produces maximum light olefins such as propylene, ethylene, etc from heavy feedstocks, wherein the yield of propylene exceeds 20% by weight, and produces aromatics such as toluene, xylene, etc at the same time.

Process for producing light olefins and aromatics

Disclosed is a combination process for improved hydrotreating and catalytic cracking of hydrocarbon oils, including: contacting residual oil, catalytic cracking cycle oil, and optional distillate oil with a hydrotreating catalyst under hydrotreating conditions in the presence of hydrogen followed by separation of the reaction products to obtain gas, hydrogenated naphtha, hydrogenated diesel oil, and hydrogenated tail oil; contacting the hydrogenated tail oil and optional normal catalytic cracking feedstock oil with a cracking catalyst under catalytic cracking conditions followed by separation of the reaction products to obtain dry gas, hydrogenated naphtha, liquefied petroleum gas, catalytic cracked gasoline, catalytic cracked diesel oil, and catalytic cracking cycle oil; wherein the hydrogenated tail oil and/or normal catalytic cracking feedstock oil are separated into at least two fractions, the light and the heavy fractions or normal catalytic cracking heavy feedstock oil and normal catalytic cracking light feedstock oil, prior to contacting the hydrogenated tail oil and/or normal catalytic cracking feedstock oil with the cracking catalyst. The process according to the present invention is especially suitable for conversion of hydrocarbon oils to produce more products of gasoline or diesel oil.

Integrated process for hydrogenation and catalytic cracking of hydrocarbon oil

The present invention discloses a method of removing sulfur oxides and/or nitrogen oxides in a regeneration flue gas emitted from a regenerator of a catalytic cracking plant and recovering the elemental sulfur and an apparatus therefor.

Method of removing sulfur oxides and nitrogen oxides in the flue gas

Disclosed is a combination process for improved hydrotreating and catalytic cracking of hydrocarbon oils, including: contacting residual oil, catalytic cracking cycle oil, and optional distillate oil with a hydrotreating catalyst under hydrotreating conditions in the presence of hydrogen followed by separation of the reaction products to obtain hydrogenated tail oil and other products; contacting the hydrogenated tail oil and optional normal catalytic cracking feedstock oil with a cracking catalyst under catalytic cracking conditions followed by separation of the reaction products; wherein the hydrogenated tail oil and/or normal catalytic cracking feedstock oil are separated into at least two fractions prior to contacting the hydrogenated tail oil and/or normal catalytic cracking feedstock oil with the cracking catalyst.

Combined process of hydrotreating and catalytic cracking of hydrocarbon oils

The present invention discloses catalytic cracking apparatus and process, which are useful for catalytic cracking of heavy oils with a high heavy oil conversion, a high propylene yield and low dry gas and coke yields.

Catalytic cracking apparatus and process

A process for the catalytic conversion of hydrocarbons to convert petroleum hydrocarbons in a higher yield for light olefins, particularly propylene is disclosed, the process involving a hydrocarbon-converting catalyst comprising zeolite, phosphorous and a transition metal, as defined herein.

Process for the catalytic conversion of hydrocarbons

A process for producing light olefins and aromatics, which comprises reacting a feedstock with a catalytic cracking catalyst in at least two reaction zones, wherein the reaction temperature of at least one reaction zone downstream of the first reaction zone is higher than that of the first reaction zone and its weight hourly space velocity is lower than that of the first reaction zone. The spent catalyst is separated, from the reaction product vapor, regenerated, and then returned to the reactor. The reaction product vapor is separated to obtain the desired products, light olefins and aromatics. This process efficiently produces light olefins such as propylene, ethylene, etc from heavy feedstocks, wherein the yield of propylene exceeds 20% by weight, and produces aromatics such as toluene, xylene, etc at the same time.

A hydrocarbon conversion catalyst, which comprises, based on the total weight of the catalyst, 1-60 wt % of a zeolite mixture, 5-99 wt % of a thermotolerant inorganic oxide and 0-70 wt % of clay, wherein said zeolite mixture comprises, based on the total weight of said zeolite mixture, 1-75 wt % of a zeolite beta modified with phosphorus and a transition metal M, 25-99 wt % of a zeolite having a MFI structure and 0-74 wt % of a large pore zeolite,

Hydrocarbon conversion catalyst

A catalytic conversion process which comprises catalytic cracking reaction of a hydrocarbon feedstock contacting with a medium pore size zeolite enriched catalyst in a reactor, characterized in that reaction temperature, weight hourly space velocity and catalyst/feedstock ratio by weight are sufficient to achieve a yield of fluid catalytic cracking gas oil between 12% and 60% by weight of said feedstock, wherein said weight hourly space velocity is between 25 hand 100 h, said reaction temperature is between 450&#xb0; C. and 600&#xb0; C., and said catalyst/feedstock ratio by weight is between 1 and 30. This invention relates to a catalytic conversion process, especially for heavy feedstock oil to produce higher octane gasoline and an enhanced yield of propylene. More particularly, the invention relates to a process to utilize petroleum oil resources efficiently for decreasing the yield of dry gas and coke significantly.

Catalytic conversion process

A catalytic conversion process for increasing the light olefin yields, which comprises bringing a hydrocarbon oil feedstock into contact with a catalytic conversion catalyst in a catalytic conversion reactor including one or more reaction zones to carry out the reaction, wherein the hydrocarbon oil feedstock is subjected to the catalytic conversion reaction in the presence of an inhibitor; and separating the reactant vapor optionally containing the inhibitor from the coke deposited catalyst, wherein a target product containing ethylene and propylene is obtained by separating the reactant vapor, and the coke deposited catalyst is stripped and regenerated for recycle use by being returned to the reactor. The process can weaken the further converting reaction of produced light olefins such as ethylene and propylene to 50-70% of the original level by injecting the inhibitor; thereby it can increase the yields of the target products. When vacuum gas oil is used as the feedstock, the yield of ethylene is as high as 8.73 wt % and that of propylene is as high as 29.30 wt %, increasing by 14.4% and 26.6% respectively comparing to those obtained without the inhibitor being injected.

Catalytic conversion method of increasing the yield of lower olefin

A catalytic conversion process to convert inferior feedstock to high quality fuel oil and propylene is disclosed. Inferior feedstock is introduced into first and second reactor zone, wherein first step and second step reactions occur by contacting with catalytic conversion catalyst. Product vapors include fluid catalytic cracking gas oil (FGO) which is introduced into a hydrotreating unit and/or extraction unit to obtain hydrotreated FGO and/or extracted FGO. Hydrotreated FGO and/or extracted FGO returns to the first reactor zone and/or another catalytic cracking unit to obtain propylene and gasoline. The extracted oil of said FGO is rich in double ring aromatics and the raffinate of said FGO is rich in chain alkane and cycloalkane. More particularly, the invention utilizes petroleum oil resources efficiently for decreasing the yield of dry gas and coke significantly.

Process for converting inferior feedstock to high quality fuel oil

Disclosed is a process for producing dimethyl ether from methanol, which is characterized in that the absorbing liquid used in said absorbing column is the bottom liquid of DME-fractionating column and/or bottom waste water of the methanol-recovering column. Said process can significantly reduce energy consumption of the apparatus.

Process for producing dimethyl ether from methanol

The present invention relates to a catalytic conversion process for producing more diesel and propylene, comprising contacting the feedstock oil with a catalyst having a relatively homogeneous activity in a reactor, wherein the reaction temperature, weight hourly space velocity and weight ratio of the catalyst/feedstock oil are sufficient to obtain a reaction product containing from 12 to 60% by weight of a fluid catalytic cracking gas oil relative to the weight of the feedstock oil; the fluid catalytic cracking gas oil is fed into the fluid catalytic cracking gas oil treatment device for further processing. Catalytic cracking, hydrogenation, solvent extraction, hydrocracking and process for producing more diesel are organically combined together, and hydrocarbons such as alkanes, alkyl side chains in the feedstock for catalysis are selectively cracked and isomerized.

Catalytic conversion process for producing more diesel and propylene

A process for combining the catalytic conversion of organic oxygenates and the catalytic conversion of hydrocarbons: an organic oxygenate feedstock is contacted with a Y-zeolite containing catalyst to produce a reaction stream, and a coked catalyst and a product stream are obtained after separating the reaction stream; a hydrocarbon feedstock is contacted with a Y-zeolite containing catalyst to produce a reaction stream, a spent catalyst and a reaction oil vapor are obtained after separating the reaction stream, and the reaction oil vapor is further separated to give the products such as gas, gasoline and the like; a part or all of the coked catalyst and a part or all of the spent catalyst enter the regenerator for the coke-burning regeneration, and the regenerated catalyst is divided into two portions, wherein one portion returns to be contacted with the hydrocarbon feedstock, and the other portion, after cooling, returns to be contacted with the organic oxygenate feedstock. This process not only reasonably utilizes the excessive thermal energy of the hydrocarbon conversion, but also solves the problem of heat supply for the conversion of the organic oxygenate, thus ensuring the continuous catalytic conversion of the organic oxygenate.

Process for combining the catalytic conversion of organic oxygenates and the catalytic conversion of hydrocarbons

The present invention provides a fluidized catalytic process for production of dimethyl ether from methanol, wherein said process is carried out in a reactor in which the catalyst is in a fluidized state. Said process comprises the following steps of (1) feeding the methanol feedstock via two or more locations selected from the bottom, lower part, middle part and upper part of the reactor, contacting with the catalyst for preparation of dimethyl ether by methanol dehydration, carrying out the reaction of preparing dimethyl ether by methanol dehydration to obtain the reaction stream, separating said reaction stream to obtain a coked catalyst and a crude product primarily containing the target product, i.e. dimethyl ether; (2) totally or partially feeding the coked catalyst obtained in step (1) into a regenerator in a continuous or batch manner for regeneration via coke-burning, the regenerated catalyst being directly recycled to step (1) after being totally or partially cooled.

Fluidized catalytic process for production of dimethyl ether from methanol

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Beijing, China

Chaogang Xie