5563results about "Catalytic cracking" patented technology

A process control system uses a data collection and distribution system and an asset utilization suite to collect data or information pertaining to the assets of a process plant from various sources or functional areas of the plant including, for example, the process control functional areas, the maintenance functional areas and the process performance monitoring functional areas. This data and information is manipulated in a coordinated manner by the data collection and distribution system and is redistributed to other applications where this it is used to perform overall better or more optimal control, maintenance and business activities. Information or data may be collected by maintenance functions pertaining to the health, variability, performance or utilization of a device, loop, unit, area, etc. and this information may then be sent to and displayed to a process operator or maintenance person to inform that person of a current or future problem. A user interface is provided that enables users to access and manipulate the expert engine to optimize plant operation or cause optimization of plant operation, to get information about the operation of the plant, etc. Furthermore, applications, such as work order generation applications may automatically generate work orders, parts or supplies orders, etc. based on events occurring within the plant.

Contacting a crude feed with one or more catalysts to produce a total product that includes the crude product is described. The crude feed has a TAN of at least 1. At least one of the catalysts includes one or more metals from Columns 6-10 of the Periodic Table and/or one or more compounds of one or more metals from Columns 6-10 of the Periodic Table. Contacting conditions are controlled contacting such that the crude product has a TAN from about 0.001 to about 0.5.

Contact of a crude feed with one or more catalysts produces a total product that includes a crude product. The crude feed may include Micro-Carbon Residue (MCR), oxygen, sulfur, or mixtures thereof. The crude product is a liquid mixture at 25° C. and 0.101 MPa. The crude product may have a MCR residue and/or oxygen content of at most 90% of the MCR residue content and/or oxygen content of the crude feed. In some instances, the crude product may have a sulfur content of about 30% to about 70% of the sulfur content of the crude feed. One or more other properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

A cracking catalyst for petroleum hydrocarbon is proportionally prepared from clay, aluminum oxide prepared from alpha-AlO(OH), Y-type molecular sieve containing RE and P and silicon oxide. Its advantages are strong power to convert heavy oil and high output rate of diesel oil.

Contact of a crude feed with one or more catalysts produces a total product that include a crude product. The crude feed may a total acid number of at least 0.3. The crude product is a liquid mixture at 25° C. and 0.101 MPa. The crude product may have a total acid number of at most 90% of the total acid number of the crude feed. At least one of the catalysts may include one or more Column 6 metals of the Periodic Table and one or more Column 10 metals of the Periodic Table. One or more other properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Systems, methods, and heaters for treating a subsurface formation are described herein. At least one method for producing hydrocarbons from a subsurface formation includes providing heat to the subsurface formation using an in situ heat treatment process. One or more formation particles may be formed during heating of the subsurface formation. Fluid that includes hydrocarbons and the formation particles may be produced from the subsurface formation. The formation particles in the produced fluid may include cenospheres and have an average particle size of at least 0.5 micrometers.

A hydrocarbon cracking catalyst contains eta-alumina and/or x- alumina or the mixture of said alumina (0.5-50 Wt %) and gamma-alumina (0-50), the mixture of Y zeolite (30-90) and MFI zeolite (10-70), clay (0-75) and P(0.1-8). Its advantage is high quality of gasoline and liquefied gas.

The invention relates to a hydrotreating method (HDT) using two plants working under different operating conditions with an intermediate stripping for co-treating a mixture made up of oils of vegetable or animal origin and petroleum cuts (gas oil cuts (GO) and middle distillates) in order to produce gas oil fuel bases meeting specifications. The first plant (HDT1) is more particularly dedicated to the reactions concerning oils of vegetable or animal origin in comixture while pretreating the hydrocarbon feed, whereas the second plant (HDS2) works under more severe conditions to obtain diesel fuel according to standards, in particular in terms of effluent sulfur content, density and cold properties. The process economy, the activity and the stability of the catalyst of the second plant are greatly improved by the intermediate stripping.

Disclosed is a process for making middle distillate and lower olefins. The process includes catalytically cracking a gas oil feedstock within a riser reactor zone by contacting under suitable catalytic cracking conditions within the riser reactor zone the gas oil feedstock with a middle distillate selective cracking catalyst that comprises amorphous silica alumina and a zeolite to yield a cracked gas oil product and a spent cracking catalyst. The spent cracking catalyst is regenerated to yield a regenerated cracking catalyst. Within an intermediate cracking reactor such as a dense bed reactor zone and under suitable high severity cracking conditions a gasoline feedstock is contacted with the regenerated cracking catalyst to yield a cracked gasoline product and a used regenerated cracking catalyst. The used regenerated cracking catalyst is utilized as the middle distillate selective catalyst.

A wide-cut lubricant base stock is made by hydroisomerizing and then catalytically dewaxing a waxy Fischer-Tropsch synthesized hydrocarbon fraction feed and comprises the entire dewaxate having an initial boiling point in the 650-75O° F.+ range. Formulated lubricating oils made by admixing the base stock with a commercial automotive additive package meet all specifications, including low temperature properties, for multigrade internal combustion engine crankcase oils. The waxy feed has an initial boiling point in the 650-750° F. range and continuously boils to an end point of at least 1050° F.+. Lower boiling hydrocarbons produced by the process are separated from the base stock by simple flash distillation. The base stock comprises the entire dewaxate having an initial boiling point in the 650-750° F. range.

A method for upgrading a naphtha feed to a naphtha product containing less than about 10 wppm of nitrogen and less than about 15 wppm sulfur, the method comprising contacting said naphtha feed with hydrogen in the presence of a bulk multimetallic catalyst under effective reactor conditions to hydrodesulfurize and hydrodenitrogenize said naphtha feed to produce said naphtha product, wherein said bulk multimetallic catalyst comprises at least one Group VIII non-noble metal and at least two Group VIB metals.

Thousands of process and equipment measurements are gathered by the modern digital process control systems that are deployed in refineries and chemical plants. Several years of these data are historized in databases for analysis and reporting. These databases can be mined for the data patterns that occur during normal operation and those patterns used to determine when the process is behaving abnormally. These normal operating patterns are represented by sets of models. These models include simple engineering equations, which express known relationships that should be true during normal operations and multivariate statistical models based on a variation of principle component analysis. Equipment and process problems can be detected by comparing the data gathered on a minute by minute basis to predictions from these models of normal operation. The deviation between the expected pattern in the process operating data and the actual data pattern are interpreted by fuzzy Petri nets to determine the normality of the process operations. This is then used to help the operator localize and diagnose the root cause of the problem.

The propylene production of a fluid catalytic cracking unit employing a large pore zeolite cracking catalyst, produces more propylene by adding a naphtha cracking riser and a medium pore zeolite catalytic component to the unit, and recycling at least a portion of the naphtha crackate to the naphtha riser. The large pore size zeolite preferably comprises a USY zeolite and the medium pore size is preferably ZSM-5. Propylene production per unit of naphtha feed to the naphtha riser is maximized, by using the 60-300.degree. F. naphtha crackate as the feed.

A hydrotreating method uses two catalyst beds with the introduction, on the last catalyst bed, of oils of animal or vegetable origin for co-treating a mixture made up of oils of vegetable or animal origin and of petroleum cuts (gas oil cuts (GO) and middle distillates) in order to produce gas oil effluents meeting specifications with an improved cetane number. The first catalyst bed is dedicated to only the deep desulfurization reactions (HDS1) of a petroleum type feed. The effluents of the first catalyst bed having an effluent sulfur content below or equal to 50 mg/kg are separated into two streams. The first stream, which is predominant, is sent to the gas oil pool. The second stream is mixed with oils of vegetable or animal origin. The resultant oil-petroleum cut mixture is then subjected to a milder hydrotreatment (HDT2). The effluents obtained at the outlet of the second catalyst bed can optionally be mixed with the predominant stream from the first bed. The process economy, the tolerance to the specifications relative to oils of animal or vegetable origin and the quality of the products obtained are thus greatly improved.

A fluid catalytic cracking process includes feeding hydrocarbon into a riser in the presence of a catalyst, cracking the hydrocarbon in the riser in the presence of the catalyst to form a cracked stream, and separating the catalyst from the cracked stream. When in a gasoline mode, the hydrocarbon is fed through a first distributor into the riser, and when in a light olefin mode, the hydrocarbon is fed through a second distributor into the riser. The second distributor is positioned at a higher elevation than the first distributor.

Atomization of a high boiling point, hot liquid, such as a hydrocarbon feed oil for a fluid cat cracker, is enhanced by injecting subcooled water into the hot liquid, to form a two-phase fluid of the liquid and steam, upstream of the atomization. The hot liquid is at conditions of temperature and pressure effective for the injected, subcooled water to vaporize into steam, when the water contacts it. Typically this means that the hot liquid is hotter and at a lower pressure than the water. In an FCC process, the subcooled water is sparged into the flowing hot oil in a conduit in a riser feed injector. This produces a spray of hot oil in the riser reaction zone in which the oil drops are smaller and more uniformly distributed in the spray.