Some variations provide a process for producing biocarbon pellets, comprising: pyrolyzing a biomass-containing feedstock in a first pyrolysis reactor to generate a first biogenic reagent and a pyrolysis vapor; introducing the pyrolysis vapor to a separation unit, to generate a pyrolysis precipitate in liquid or solid form; contacting the first biogenic reagent with the pyrolysis precipitate, thereby generating an intermediate material; pelletizing the intermediate material, to generate intermediate pellets; optionally, drying the intermediate pellets; separately pyrolyzing the intermediate pellets in a second pyrolysis reactor to generate a second biogenic reagent and a pyrolysis off-gas; and recovering the second biogenic reagent as biocarbon pellets. Some variations provide a similar process that utilizes a carbon-containing condensed-matter material, which is not necessarily a pyrolysis precipitate. The disclosure provides improved processes for producing biocarbon compositions, especially with respect to carbon yield and biocarbon properties, such as reactivity.

The present disclosure relates to the technical field of pyrolysis and improvement of caking middling coals, in particular to a low temperature pyrolysis method of a caking middling coal. The present disclosure provides a low temperature pyrolysis method of a caking middling coal, including the following steps: conveying the caking middling coal into a pyrolysis reactor through a top of the pyrolysis reactor; dividing a reaction chamber of the pyrolysis reactor into a drying section, a softening section, a melting and depolymerization section, a solidification section, and a cooling section by means of multi-channel gas distribution; and conducting zoned temperature control-based pyrolysis to obtain semi-coke at a bottom of the reactor as well as tar and coal gas at the top of the reactor. The pyrolysis method can well avoid caking and swelling of the caking middling coal during pyrolysis.

Methods and systems for coking coal blends to produce foundry coke products are disclosed herein. Methods for producing coke products can include charging a coal blend into a coke oven; and heating the charged coal blend such that a crown temperature of the coke oven is greater than a lower bound coking temperature. The pyrolysis duration begins when the crown temperature of the oven is greater than the lower bound coking temperature, and ends when the crown temperature of the oven is less than the lower bound coking temperature.

Coal blends used to produce foundry coke products are disclosed herein. Coal blends can include first coals having a first volatile matter mass fraction less than or equal to a first threshold, and second coals having a second volatile mass fraction greater than or equal to a second threshold that is less than the second threshold. The coal blend can have an ash fusion temperature less than 2600? F. and an aggregated volatile matter mass fraction between 15% and 25%.

Coal blends used to produce foundry coke products are disclosed herein. Coal blends can include first coals having a first volatile matter mass fraction less than or equal to a first threshold, and second coals having a second volatile mass fraction greater than or equal to a second threshold that is less than the second threshold. The coal blend can have an ash fusion temperature less than 2600? F. and an aggregated volatile matter mass fraction between 15% and 25%.

Embodiments of a process for producing high grade coke from crude oil residue include at least partially separating, in a solvent extraction unit, the crude oil residue into a deasphalted oil (DAO)-containing stream and an asphaltene containing-stream, producing a pressurized, heated DAO-containing stream, where the pressurized, heated DAO-containing stream, mixing a supercritical water stream with the pressurized, heated DAO-containing stream to create a combined feed stream, introducing the combined feed stream to an upgrading reactor system operating at supercritical temperature and pressure to yield one or more upgrading reactor output streams comprising upgraded product and a slurry mixture, where the slurry mixture comprises sulfur and one or more additional metals. The process also may include calcining the slurry mixture at a temperature of from 700 C. to 1900 C. to produce a product stream comprising the high grade coke.

Process embodiments for producing high grade coke and fuel grade coke from residual oil comprises: introducing the residual oil and a first paraffinic solvent having a carbon number C.sub.n to a first solvent deasphalting unit to produce a high quality deasphalted oil (HQDAO) fraction and a first asphalt fraction; passing the HQDAO fraction to a delayed coker to produce green coke; passing at least a portion of the first asphalt fraction and a second paraffinic solvent carbon number of C.sub.n+1 to a second solvent deasphalting unit to produce a low quality deasphalted oil (LQDAO) fraction and a second asphalt fraction; and passing the LQDAO fraction to the delayed coker to produce the fuel grade coke.

A method of producing low CTE graphite electrodes from needle coke formed from a coal tar distillate material having a relatively high initial boiling point.

A coal mixture is provided that maintains a high level of coke strength after carbonization, even where coal having an excessively large permeation distance is used in a large amount. The coal mixture includes large-permeation-distance coal and permeation-distance-decreasing coal. The permeation-distance-decreasing coal has a mean maximum vitrinite reflectance Ro of 1.25% or more and a total inert amount TI of 30 vol. % or less. The blending ratio of the permeation-distance-decreasing coal in the coal mixture is in a range derived by multiplying the blending ratio of the large-permeation-distance coal by 0.25 or more and 3.0 or less.

A coal mixture is provided that maintains a high level of coke strength after carbonization, even where coal having an excessively large permeation distance is used in a large amount. The coal mixture includes large-permeation-distance coal and permeation-distance-decreasing coal. The permeation-distance-decreasing coal has a mean maximum vitrinite reflectance Ro of 1.25% or more and a total inert amount TI of 30 vol. % or less. The blending ratio of the permeation-distance-decreasing coal in the coal mixture is in a range derived by multiplying the blending ratio of the large-permeation-distance coal by 0.25 or more and 3.0 or less.