# US 10,865,349 B2 · Two stage thermal cracking process with multistage separation system > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 10,865,349 B2 - Document ID: US10865349B2 - Status: Granted - Kind: B2 - Application number: 16/176,679 - Filed: 2018-10-31 - Published: 2019-06-20 - Granted: 2020-12-15 - Earliest claimed: 2017-12-19 - Assignees: Indian Oil Corporation Limited - Applicants: Indian Oil Corporation Limited - Inventors: Satyen Kumar Das; Terapalli Hari Venkata Devi Prasad; Ponoly Ramachandran Pradeep; Arjun Kumar Kottakuna; Debasis Bhattacharyya; Sanjiv Kumar Mazumdar; Sankara Sri Venkata Ramakumar - Web page: https://patentgrep.com/patent/US10865349B2 ## CPC - C10G 51/023: {only thermal cracking steps} - C10G 7/06: Vacuum distillation - C10G 9/005: {Coking (in order to produce liquid products mainly)} - C10G 9/14: in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means - C10G 11/18: according to the "fluidised-bed" technique - C10G 45/00: Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds - C10G 47/00: Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions (C10G15/00 takes precedence; destructive hydrogenation of non-melting solid carbonaceous or similar materials C10G1/06) - C10G 55/04: including at least one thermal cracking step - C10G 69/06: including at least one step of thermal cracking in the absence of hydrogen - C10G 2300/1044: Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C - C10G 2300/107: Atmospheric residues having a boiling point of at least about 538 °C - C10G 2300/1077: Vacuum residues - C10G 2300/708: Coking aspect, coke content and composition of deposits - C10G 2400/06: Gasoil - C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES ## Abstract The present invention relates to Delayed Coking of heavy petroleum residue producing petroleum coke and lighter hydrocarbon products. The invented process utilizes a pre-cracking reactor for mild thermal cracking of the feedstock and intermediate multistage separation system before being subjected to higher severity thermal cracking in delayed coking process, resulting in reduction in overall coke yield. ## Claims ### Claim 1 A method of reducing overall coke yield in a delayed coking process, said method comprising the steps of: a) passing a fresh hydrocarbon feed to a bottom of a main fractionator and mixing with internal recycle to make a secondary hydrocarbon feedstock; b) heating the secondary hydrocarbon feedstock in a furnace to obtain hot feed at a desired inlet temperature of a pre-cracking reactor; c) passing the hot feed at the desired inlet temperature and a pressure to the pre-cracking reactor, wherein the hot feed undergoes mild thermal cracking reactions to obtain an outlet product material stream; d) introducing the outlet product material stream to a first intermediate separator to split hydrocarbons in the outlet material stream into a first top product and bottom fractions, wherein the first top product comprises lighter products and gases and the bottom fractions is split into a first portion and a second portion; e) routing the first top product to the main fractionator; f) separating a first portion of the bottom fractions in a second intermediate separator column operating at vacuum conditions to obtain a second top product and a heavier bottom product; g) passing the second top product obtained in step (f) to the main fractionator; h) withdrawing the heavier bottom product from the second intermediate separator column of step (f) and passing to the main fractionator, wherein the heavier bottom product comprises Light Vacuum Gas Oil (LVGO) and Heavy Vacuum Gas Oil (HVGO); i) mixing the second portion from the first intermediate separator of step (d) and the heavier bottom product from the second intermediate separator column of step (f) and heating in a furnace to a desired coking temperature to obtain a hot hydrocarbon stream; j) passing the hot hydrocarbon stream from the furnace to a preheated coke drum; and k) passing product vapors exiting the coke drum to the main fractionator column to obtain product fractions. ### Claim 2 (depends on 1) The method as claimed in claim 1, wherein in step (a) the fresh hydrocarbon feedstock is heated directly in the furnace. ### Claim 3 (depends on 1) The method as claimed in claim 1, wherein a vacuum gasoil range cut is withdrawn from the second intermediate separator column and passed to secondary processing units, wherein the secondary processing units are selected from fluid catalytic cracking, hydrocracker and/or hydrotreater units. ### Claim 4 (depends on 1) The method as claimed in claim 1, wherein the second top product from the second intermediate separator column is routed to at least one of product treatments units and the secondary processing unit. ### Claim 5 (depends on 1) The method as claimed in claim 1, wherein the heavier bottom product are passed to secondary processing units. ### Claim 6 (depends on 5) The method as claimed in claim 5, wherein a single stream is withdrawn from the second intermediate separator column and passed to the secondary processing units. ### Claim 7 (depends on 1) The method as claimed in claim 1, wherein the product fractions comprise off-gas with LPG and naphtha, Kerosene, Light Coker Gas Oil (LCGO), Heavy Coker Gas Oil (HCGO), and heavy bottom product. ### Claim 8 (depends on 1) The method as claimed in claim 1, wherein the heavy bottom product from the main fractionator is routed to the second intermediate separator. ### Claim 9 (depends on 1) The method as claimed in claim 1, wherein the heavier bottom product are withdrawn from the second intermediate separator and passed to secondary processing units, wherein the secondary processing units comprises at least one of fluid catalytic cracking, hydrocracker, and/or hydrotreater units. ### Claim 10 (depends on 1) The method as claimed in claim 1, wherein the pre-cracking reactor operates at the desired temperature in the range of 350 to 470° C. and the pressure in the range of 1 to 15 Kg/cm2 (g). ### Claim 11 (depends on 1) The method as claimed in claim 1, wherein feedstock within the pre-cracking reactor has a residence time in the range of 1 to 40 minutes. ### Claim 12 (depends on 1) The method as claimed in claim 1, wherein the first intermediate separator is operated at a pressure in the range of 1 to 6 Kg/cm2 (g). ### Claim 13 (depends on 1) The method as claimed in claim 1, wherein the first intermediate separator is operated at a bottom temperature in the range of 300 to 400° C. ### Claim 14 (depends on 1) The method as claimed in claim 1, wherein the second intermediate separator column is operated at a pressure in the range of pressure of 10 to 200 mmHg. ### Claim 15 (depends on 1) The method as claimed in claim 1, wherein the second intermediate separator column is operated at a bottom temperature in the range of 200 to 350° C. ### Claim 16 (depends on 1) The method as claimed in claim 1, wherein the coke drum is operated at a temperature in the range of 470 to 520° C. and a pressure in the range of 0.5 to 5 Kg/cm2 (g). ### Claim 17 (depends on 1) The method as claimed in claim 1, wherein feedstock within the coke drum is provided with a residence time of more than 10 hours for thermal cracking reactions. ### Claim 18 (depends on 7) The method as claimed in claim 7, wherein the heavy bottom product is Coker Fuel Oil (CFO). ### Claim 19 A method of reducing overall coke yield in a delayed coking process, said method comprising the steps of: a) heating a hydrocarbon feedstock in a furnace to obtain a hot feed at a desired inlet temperature of a pre-cracking reactor; b) passing the hot feed at the desired inlet temperature and a pressure to the pre-cracking reactor, wherein the hot feed undergoes mild thermal cracking reactions to obtain an outlet product material stream; c) introducing the outlet product material stream to a first intermediate separator to split hydrocarbons in the outlet material stream into a first top product and bottom fractions; d) routing the first top product to a main fractionator; e) separating the bottom fractions in a second intermediate separator column operating at vacuum conditions to obtain a second top product, a heavier bottom product and a heavy bottom material, wherein the heavy bottom product comprises of Coker Fuel Oil (CFO); f) passing the second top product obtained in step (e) to the main fractionator; g) withdrawing the heavier bottom product from the second intermediate separator of step (e) and passing to the main fractionator, wherein the heavier bottom product comprises Light Vacuum Gas Oil (LVGO) and Heavy Vacuum Gas Oil (HVGO); h) heating the heavy bottom material in a furnace to a desired coking temperature to obtain a hot hydrocarbon stream; i) passing the hot hydrocarbon stream from the furnace to a preheated coke drum; and j) passing product vapors exiting the coke drum to the main fractionator column to obtain product fractions.