A method and a system for the real-time optimization of a molecular-level device, and a storage medium are described. The method includes: inputting molecular composition of petroleum processing feedstocks into a pre-trained product prediction model to obtain a predicted molecular composition of corresponding predicted products and a predicted molecular content of each single molecule; determining whether the predicted product meets a preset standard for a target product; if the predicted product does not meet any preset standard for a target product, adjusting an operation parameter in the product prediction model, to re-obtain the predicted molecular composition and the predicted molecular content, until the preset standard is met. By means of the present disclosure, molecular-level integral simulation and real-time optimization of the molecular-level device from the feedstocks to the product processing process are achieved, and the precision and production efficiency are improved.

An optimization method and system for a whole process of molecular-level oil refinery processing and a storage medium are described. According to an embodiment, for mixed products obtained by prediction from simulation of a molecular-level crude oil processing process, when physical properties of any mixed product do not meet any preset standard, or when a target parameter of the mixed products does not meet a preset condition, the proportion of different fractions entering respective petroleum processing device, an operating parameter in a product prediction model, and a mixing rule for mixing predicted products are adjusted, and the mixed products are re-obtained, until the product properties meet any preset standard and the target parameter meets the preset condition. Final predicted products are predicted by adjusting the proportion of fractions for secondary processing, and the production efficiency is improved by means of the simulation optimization of a production process.

Systems and methods are provided for integrated pyrolysis and gasification of a biomass feed, either as a separate feed or under co-processing conditions. The integrated pyrolysis and gasification can be performed using any convenient reactor configuration, such as fluidized coking reactor configuration or a fluid catalytic cracking reactor configuration. The biomass feed can initially by pyrolyzed to form liquid products, gas phase products, and char. The char can then be used as the input feed to gasification. In aspects where the biomass feed is co-processed, the biomass can be co-processed with a co-feed that is suitable for processing under fluidized coking conditions or other pyrolysis conditions, such as a conventional fluidized coking feedstock.

The present invention relates to a coke reducing additive composition capable of simultaneously (a) reducing coke formation and (b) increasing distillate yield during pyrolysis of a feedstock in the presence of a plastic material, wherein the feedstock is a vacuum residue (VR), plastic material is a waste plastic material or an olefin polymer (OP) material, or a mixture thereof, and the coke reducing additive composition comprises a naphthenate, preferably a calcium naphthenate, or sodium naphthenate, or a mixture thereof, and to a method of employing the coke reducing additive composition, and to a method of use of the coke reducing additive composition of the present invention.

Particularly, in another embodiment, the present invention relates to a coke reducing additive composition capable of simultaneously (a) reducing formation of coke deposits on walls of the processing unit; and (b) reducing fouling caused due to deposits of coke products on walls of the processing unit during pyrolysis of a feedstock in the presence of a plastic material, wherein the feedstock is a vacuum residue (VR), plastic material is a waste plastic material or an olefin polymer (OP) material, or a mixture thereof, and the coke reducing additive composition comprises a naphthenate, preferably a calcium naphthenate, or sodium naphthenate, or a mixture thereof, and to a method of employing the coke reducing additive composition, and to a method of use of the coke reducing additive composition of the present invention.

Particularly, in yet another embodiment, the present invention relates to a method to convert a waste plastic into useful chemical commodity.

The present invention provides a process for production of graphite coke from an admixture of coal and petroleum-based hydrocarbons. This particularly describes a process wherein a mixture of coal tar pitch and hydrocarbon feedstock such as CLO is purified in a solvent treatment step and the purified mixed feedstock is subjected to thermal cracking to produce high quality graphite/needle coke. This process also provides a synergy in improved coke quality coke formation while using an admixture of coal tar pitch and CLO while subjected to common purification and coking steps.

In one aspect, the present invention relates to a furnace having a heated portion arranged adjacent to an unheated portion. A plurality of straight tubes are formed of a first material and are at least partially disposed in the heated portion. A plurality of return bends are operatively coupled to the plurality of straight tubes. The plurality of return bends are formed of a second material and are at least partially disposed in the unheated portion. The first material exhibits a maximum temperature greater than the second material thereby facilitating increased run time of the furnace. The second material exhibits wear-resistance properties greater than the first material thereby facilitating wear-resistance of the furnace.

An improved fired heater with air preheating provided by one or more heat pipes. The fired heater may include at least one burner for combusting a fuel stream and an air stream and producing heated exhaust gases; a hot gas flow path and at least one conduit containing a process fluid to be heated by heat transfer from the heated exhaust gases; and an air preheater comprising at least one heat pipe having a first section exposed to the heated exhaust gases and a second section exposed to the air stream, wherein the heat pipe is positioned and arranged to transfer heat from the heated exhaust gases to the air stream, wherein the at least one heat pipe contains a working fluid sealed within the heat pipe, wherein said working fluid transfers heat from the heated exhaust gas to the air stream to be preheated.

The present invention provides a delayed coking process comprising a step of subjecting a mixed feed comprises residual heavy hydrocarbon feedstock and bio oil obtained from fast pyrolysis of lignocellulosic biomass of one or more of Jatropha, Cashew nut, Karanjia and Neem to a delayed coking process and a system for the delayed coking process.

A processing facility is provided. The processing facility includes an asphaltenes and metals (AM) removal system configured to process a feed stream to produce a power generation stream, a hydroprocessing feed stream, and an asphaltenes stream. A power generation system is fed by the power generation feed stream. A hydroprocessing system is configured to process the hydroprocessing feed stream to form a gas stream and a liquid stream. A hydrogen production system is configured to produce hydrogen, carbon monoxide and carbon dioxide from the gas feed stream. A carbon dioxide conversion system is configured to produce synthetic hydrocarbons from the carbon dioxide, and a cracking system is configured to process the liquid feed stream.

Methods and systems for using temperature measurements taken from a compact insulated skin thermowell to optimize a pyrolysis reaction are provided. In the present systems and methods, the upstream temperature and the upstream pressure of a pyrolysis reactor is measured through an adiabatic restriction in the inlet manifold of a parallel tube assembly to provide an absolute upstream temperature and an upstream pressure. The downstream temperature of the pyrolysis reactor is also measured following an adiabatic restriction to provide an absolute downstream temperature. The downstream pressure is then determined by multiplying the absolute upstream pressure with the quotient of the downstream temperature divided by the upstream temperature as taken to the power of k/k−1, where k is the ratio of fluid specific heat at constant pressure (Cp) to fluid specific heat at constant volume (Cv).