US20210171835A1 - Coking system and coking process - Google Patents

Coking system and coking process Download PDF

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Publication number
US20210171835A1
US20210171835A1 US16/763,913 US201816763913A US2021171835A1 US 20210171835 A1 US20210171835 A1 US 20210171835A1 US 201816763913 A US201816763913 A US 201816763913A US 2021171835 A1 US2021171835 A1 US 2021171835A1
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United States
Prior art keywords
coke
tower
feedstock
heating
heating unit
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Abandoned
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US16/763,913
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English (en)
Inventor
Renqing CHU
Xiangchen Fang
Dan Guo
Yongyi SONG
Jihua Liu
Lianzhong GOU
Dewei JIAO
Yun Wu
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China Petroleum and Chemical Corp
Sinopec Dalian Research Institute of Petroleum and Petrochemicals
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China Petroleum and Chemical Corp
Sinopec Dalian Research Institute of Petroleum and Petrochemicals
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Assigned to CHINA PETROLEUM & CHEMICAL CORPORATION, DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC CORP. reassignment CHINA PETROLEUM & CHEMICAL CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: LIU, JIHUA, FANG, XIANGCHEN, CHU, Renqing, GOU, Lianzhong, GUO, Dan, JIAO, Dewei, SONG, Yongyi, WU, YUN
Publication of US20210171835A1 publication Critical patent/US20210171835A1/en
Abandoned legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/02—Multi-step carbonising or coking processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/005—Coking (in order to produce liquid products mainly)
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
    • C10B55/02—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B1/00—Retorts
    • C10B1/02—Stationary retorts
    • C10B1/04—Vertical retorts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/08—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form in the form of briquettes, lumps and the like
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
    • C10B55/02—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials
    • C10B55/04—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials with moving solid materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
    • C10B57/045—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing mineral oils, bitumen, tar or the like or mixtures thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils

Definitions

  • the invention relates to a coking system, in particular to a coking system for producing needle coke.
  • the invention also relates to a coking process.
  • the needle coke is mainly used for producing high-power and ultrahigh-power graphite electrodes.
  • the yield of scrap steel is gradually increased, the development of electric furnace steel is promoted, the consumption of graphite electrodes, particularly high-power and ultrahigh-power electrodes, is increased inevitably, and the demand of needle coke is increased continuously.
  • CN200810017110.3 discloses a method for preparing needle coke, which comprises subjecting aromatic-rich fraction or residual oil to delayed coking treatment under a certain temperature-increasing program, and calcining the obtained green coke to obtain a needle coke with high mesophase content and developed needle structure.
  • CN201110449286.8 discloses a method for producing homogeneous petroleum needle coke, which comprises the steps of heating a feedstock for producing needle coke to a relatively low temperature of 400-480° C. by a heating furnace, and then feeding the feedstock into a coke tower, wherein the coking feedstock forms a flowable mesophase liquid crystal; after the low-temperature fresh feedstock feeding stage is completed, gradually raising the outlet temperature of the heating furnace, and simultaneously changing the feed of the coker heating furnace into a fresh feedstock and a heavy distillate oil from a fractionation tower; and when the material in the coke tower reaches the temperature for solidifying and coke-forming, changing the feed of the coker heating furnace into a coker middle distillate oil generated in the reaction process, and simultaneously increasing the feeding temperature of the coker heating furnace to ensure that the temperature in the coke tower reaches 460-510° C., and completing the high-temperature solidification of the petroleum coke to obtain a needle coke product.
  • U.S. Pat. No. 4,235,703 discloses a method for producing high-quality coke from residual oil, which comprises the steps of hydrodesulfurizing and demetallizing the feedstock, and then performing the delayed coking to produce high-power electrode petroleum coke.
  • U.S. Pat. No. 4,894,144 discloses a process for simultaneously making needle coke and high-sulfur petroleum coke by pretreating straight-run heavy oil by hydrotreating process, and the hydrogenated residual oil is divided into two parts, which are respectively coked and then calcined to obtain needle coke and high-sulfur petroleum coke.
  • CN1325938A discloses a method for producing a needle-like petroleum coke from a sulfur-containing atmospheric residue, in which the feedstock is sequentially subjected to hydrofining, hydrodemetalization and hydrodesulfurization, the hydrogenated product is separated to obtain a hydrogenated heavy distillate oil, the hydrogenated heavy distillate oil is subjected to a delayed coking to obtain the needle-like coke under the condition of producing the needle-like coke.
  • the above method adopt a conventional one-furnace and two-tower delayed coking mode to produce the needle coke, which does not solve the problems of large operation fluctuation caused by temperature and pressure change in the needle coke production process, and generally has the problem of unstable needle coke product performance. Therefore, how to produce high-quality needle coke products with uniform performance is a goal pursued by researchers.
  • the heating unit generally adopts a variable temperature control, and the heating unit circularly carries out the processes of temperature rise, constant temperature, temperature reduction and temperature rise in the production cycle of delayed coking, so that the variable temperature range is wide and the stable operation is difficult; even in some delayed coking processes, the heating unit needs to go through different heating stages to heat different feedstocks, for example, a fresh feedstock, a mixture of the a fresh feedstock and the coker gas oil and a middle distillate oil are heated in different coke-charging stages, the difference of the feeding properties of the heating unit is large, and the control of the pulling/forming ratio (the ratio of the coke-pulling feedstock to the coke-forming feedstock) in different feeding stages is different, which causes a large change in the feeding amount of the heating unit.
  • the present inventors have found, through many years of studies, that production conditions have an important influence on the performance of needle coke, that small variations in the conditions may affect the formation of streamline texture in the product and the coefficient of thermal expansion, and that the inevitable small errors in the operations such as the temperature change, the pressure change and the changed feeding amount of the heating unit during the above coke-charging process are the major causes of large differences in the quality of the product; and have completed the present invention based on this finding.
  • the present invention relates to the following aspects.
  • a coking system comprising a 1st to a m-th (total m) heating units (preferably heat exchangers or furnaces, more preferably furnaces) and a 1st to a n-th (total n) coke towers, m being any integer from 2 to n ⁇ 1, n being any integer from 3 or more (preferably any integer from 3 to 20, more preferably any integer from 3 to 5, more preferably 3), each of the m heating units being in communication with the n coke towers, respectively, each of the n coke towers (preferably the upper part and/or the overhead) being in communication with one or more (preferably one) separation towers (preferably rectifying tower, flash tower, evaporation tower or fractionation tower, more preferably fractionation tower), respectively, the one or more separation towers (preferably the lower part and/or the bottom) being in communication with the m-th heating unit and optionally being in communication with an i-th heating unit (i being any integer greater than 1 and less than m) (preferably not being in
  • the coking system of any of the preceding or subsequent aspects further comprising a control unit configured to enable to start and terminate the material transport from each of heating units to an h-th coke tower sequentially in the order from the 1st heating unit to the m-th heating unit from the time T0, and terminate the material transport from the m-th heating unit to the h-th coke tower at the time Te, assuming T0 is a coke-charging starting time and Te is a coke-charging termination time for the h-th coke tower (h being any integer from 1 to n) of the n coke towers.
  • a coking process comprises the steps of coking by using m heating units and n coke towers, wherein m is any integer of 2 to n ⁇ 1, n is any integer of 3 or more (preferably any integer of 3 to 20, more preferably any integer of 3 to 5, more preferably 3), each of the m heating units is respectively communicated with the n coke towers in a material transport manner, assuming T0 is a coke-charging starting time and Te is a coke-charging termination time for the h-th coke tower (h being any integer from 1 to n) of the n coke towers, starting at said time T0, the material transport from each of heating units to the h-th coke tower in the order from said the 1st heating unit to the m-th heating unit is sequentially started and terminated, and at the time Te, the material transport from the m-th heating unit to the h-th coke tower is terminated.
  • each of the 1st to the m-th heating units transports only one batch of material to the h-th coke tower, or at any time during a single material transport cycle, the h-th coke tower either (i) does not accept the transported material or (ii) only accepts the material transported from one of the 1st to the m-th heating units.
  • the 1st heating unit heats its transported material (referred to as the 1st transported material) to a feeding temperature W1 of from 400° C. to 480° C. (preferably from 420° C. to 460° C.) and the 1st transported material brings the intra-tower gas velocity G1 of the h-th coke tower to from 0.05 to 0.25 m/s (preferably from 0.05 to 0.10 m/s), the m-th heating unit heats its transported material (referred to as the m-th transported material) to a feeding temperature Wm of from 460° C. to 530° C. (preferably from 460° C.
  • the m-th transported material brings the intra-tower gas velocity Gm of the h-th coke tower to from 0.10 to 0.30 m/s (preferably from 0.15 to 0.20 m/s), the i-th heating unit (i being any integer greater than 1 and less than m) heats its transported material (referred to the i-th transported material) to a feeding temperature Wi (W1 ⁇ Wi ⁇ Wm), and the i-th transported material enables the intra-tower gas velocity Gi of the h-th coke tower to reach G1 ⁇ Gi ⁇ Gm, and/or the heating rate V1 of the transported material by the 1st heating unit is 1-30° C./h (preferably 1-10° C./h), the heating rate Vm of the transported material by the m-th heating unit is 30-150° C./h (preferably 50-100° C./h), and the heating rate Vi of the transported material by the i-th heating unit (i is any integer greater than 1 and less than m) meets the relation
  • the operating conditions of the one or more separation towers include: the pressure at the top of the tower is 0.01-0.8 MPa, the temperature at the top of the tower is 100-200° C., the temperature at the bottom of the tower is 280-400° C., and/or the operating conditions of the n coke towers are identical to or different from each other, and each independently comprises: the pressure at the top of the tower is 0.01-1.0 MPa, the temperature at the top of the tower is 300-470° C., and the temperature at the bottom of the tower is 350-510° C.
  • the 1st heating unit has (preferably only) a coke-forming feedstock as its transported material
  • the m-th heating unit has (preferably only) a coke-pulling feedstock as its transported material (preferably at least comprising the bottom material of the separation tower)
  • the i-th heating unit (i being any integer greater than 1 and less than m) has at least one selected from the group consisting of the coke-forming feedstock and the coke-pulling feedstock as its transported material.
  • coke-forming feedstock is selected from at least one of a coal-based feedstock and a petroleum-based feedstock (preferably the sulfur content ⁇ 0.6 wt %, more preferably ⁇ 0.5 wt %, and the colloid/asphaltene content ⁇ 10.0 wt %, preferably ⁇ 5.0 wt %, more preferably ⁇ 2.0 wt %), preferably from at least one of coal tar, coal tar pitch, petroleum heavy oil, ethylene tar, catalytic cracking residue or thermal cracking residue, and has a coke formation rate (referred to as coke formation rate A) of 10 to 80% (preferably 20 to 70%, more preferably 30 to 60%), and/or the bottom material of the separation tower has a 10% distillate point temperature of 300° C.
  • coke formation rate A coke formation rate
  • the coke-pulling feedstock is selected from at least one of a coal-based feedstock and a petroleum-based feedstock (preferably selected from coker gas oil, coker diesel, ethylene tar, and thermally cracked heavy oil, more preferably sulfur content ⁇ 1.0 wt %, more preferably ⁇ 0.6 wt %), and has a coke formation rate (referred to as coke formation rate B) is 1-40% (preferably 1-20%, more preferably 1-10%), provided that the coke formation rate A>the coke formation rate B.
  • coke formation rate B coke formation rate
  • the h-th coke tower has a coke-charging cycle T of from 10 to 60 hours (preferably from 24 to 48 hours), or the n coke towers have coke-charging cycles T that are identical to or different from each other (preferably identical to each other), and separately and independently from 10 to 60 hours (preferably from 24 to 48 hours).
  • a coking system which comprises three coke towers, two sets of heating furnaces, a fractionation tower and a coke-pulling feedstock storage tank, wherein the three coke towers are respectively marked as a coke tower a, a coke tower b and a coke tower c; the two sets of heating furnaces are respectively marked as a heating furnace a and a heating furnace b, any coke tower is connected with the two sets of heating furnaces, the top of any coke tower is connected with the inlet of a fractionation tower via pipeline, the bottom outlet of the fractionation tower is connected with a coke-pulling feedstock storage tank, the coke-pulling feedstock storage tank is connected with the heating furnace b and heats the material from the coke-pulling feedstock storage tank to the feeding temperature of the coke tower, and the heating furnace a is connected with the feedstock tank and heats the coking feedstock to the feeding temperature of the coke tower.
  • a coking process in which a coking device is used and comprises three coke towers, two sets of heating furnaces, a fractionation tower and a coke-pulling feedstock storage tank, wherein the three coke towers are respectively marked as a coke tower a, a coke tower b and a coke tower c; the two sets of heating furnaces are respectively marked as a heating furnace a and a heating furnace b, any coke tower is connected with the two sets of heating furnaces, the top of any coke tower is connected with the inlet of the fractionation tower via pipeline, the bottom outlet of the fractionation tower is connected with the coke-pulling feedstock storage tank, the heating furnace b is connected with the coke-pulling feedstock storage tank and is used for heating the material from the coke-pulling feedstock storage tank to the feeding temperature of the coke tower, and the heating furnace a is connected with the feedstock tank and is used for heating a fresh feedstock to the feeding temperature of the coke tower;
  • the coking feedstock is heated by the heating furnace a and enters the coke tower a, the generated oil gas enters the fractionation tower and is fractionated to obtain gas, coker gasoline, coker diesel and coker gas oil at the tower bottom, wherein the coker gas oil at the tower bottom is introduced into the coke-pulling feedstock storage tank;
  • the feeding duration of the coke tower a in the step (1) comprises 30-70% of the total coke-producing cycle
  • the coking feed of the coke tower a is switched to the coke tower b
  • the coke tower b repeats the coke-charging process of the coke tower a in the step (1)
  • the coke tower a is fed with the coke-pulling feedstock heated through a heating furnace b to continue the coke-charging;
  • the feeding duration of the coke tower b in the step (2) comprises 30-70% of the total coke-producing cycle
  • the coking feed of the coke tower b is switched to a coke tower c
  • the coke tower c repeats the coke-charging process of the coke tower a in the step (1)
  • the coke-pulling feedstock which is heated to a relatively high temperature by the heating furnace b is switched to the coke tower b
  • the coke tower a is subjected to a steam purging and decoking operation at this time, and reassembled to be on standby for the next coke-charging;
  • the feeding duration of the coke tower c in the step (3) comprises 30-70% of the total coke-producing cycle
  • the coking feed of the coke tower c is switched to the coke tower a
  • the coke tower a repeats the process in the step (1)
  • the coke-pulling feedstock which is heated to a relatively high temperature by a heating furnace b is switched to the coke tower c
  • the coke tower b is subjected to a steam purging and decoking operation at this time, and reassembled to be on standby for the next coke-charging
  • the feeding duration of the coke tower a in the step (4) comprises 30-70% of the total coke-producing cycle
  • the coking feed of the coke tower a is switched to the coke tower b
  • the coke tower b repeats the coke-charging process of the coke tower a in the step (1)
  • the coke-pulling feedstock which is heated to a relatively high temperature by a heating furnace b is switched to the coke tower a
  • the coke tower c is subjected to a steam purging and decoking operation at this time, and reassembled to be on standby for the next coke-charging;
  • outlet temperature of the furnace a is in the range 420° C. to 450° C. where the gas velocity in the coke tower is controlled to be 0.05 to 0.10 m/s; the outlet temperature of the heating furnace b ranges from 460° C. to 500° C. where the gas velocity in the coke tower is controlled to be 0.15-0.20 m/s.
  • heating furnace a has a heating rate of 1 to 10° C./h
  • the heating furnace b has a heating rate of 50 to 100° C./h.
  • coking feedstock is one or more of coal tar or coal tar pitch, petroleum heavy oil, ethylene tar, catalytic cracking residual oil or thermal cracking residual oil.
  • the petroleum or coal raw materials can be utilized to produce high-quality needle coke with stable performance.
  • the continuous operation requirement of an industrial delayed coking system can be met by the delayed coking operated by a plurality of coke towers and a plurality of heating units.
  • the manufactured needle coke has the advantages of stable streamline texture, low coefficient of thermal expansion and the like, and meets the requirements of the needle coke for a large-scale ultrahigh-power graphite electrode.
  • FIG. 1 is an exemplary schematic diagram of a coking system of the present invention, but the invention is not so limited.
  • 1 is a coke-forming feedstock (also referred to as a fresh feedstock or a coking feedstock), 2 is a heating furnace b, 3 is a heated coke-forming feedstock, 4 is a coke tower (a, b, c), 5 is an oil-gas pipeline, 6 is a fractionation tower, 7 is a coker gas, 8 is a coker naphtha, 9 is coker diesel, 10 is coker gas oil, 11 is a recycled coker gas oil, 12 is a coke-pulling feedstock storage tank, 13 is a supplemental coke-pulling feedstock pipeline, 14 is a heating furnace a, 15 is a heated coke-pulling feedstock, and 16 is a coke fine particles filtration device.
  • a coke-forming feedstock also referred to as a fresh feedstock or a coking feedstock
  • 2 is a heating furnace b
  • 3 is a heated coke-forming feedstock
  • 4 is a coke tower (a, b,
  • the coke-pulling feedstock storage tank 12 is used to store the coker gas oil from line 10 and/or other coke-pulling feedstock from line 17 , and the stored feedstock may also be vented to the environment via line 18 and/or transported as a supplemental coke-pulling feedstock via line 13 to the coke fine particles filtration device 16 after mixing with the recycled coker gas oil from line 11 in a predetermined ratio.
  • the coker gas oil from line 10 and another coke-pulling feedstock from line 17 may be mixed in the coke-pulling feedstock storage tank 12 to form a mixed coke-pulling feedstock.
  • the other coke-pulling feedstock may be an external supply (for example, from other coking system or cracking system), or may be from the coking system of the present invention, for example, may be coker gas oil or coker diesel from the fractionation tower 6 .
  • FIG. 2 is a coking system of one-furnace and two-tower switching according to the prior art.
  • 17 is a fresh feedstock
  • 18 is a heating furnace
  • 19 is a heated fresh feedstock
  • 20 is a coke tower (a, b)
  • 21 is an oil gas pipeline
  • 22 is a fractionation tower
  • 23 is a coker gas
  • 24 is coker naphtha
  • 25 is coker diesel
  • 26 is coker gas oil
  • 27 is recycled coker gas oil.
  • coker gas oil and the recycled coker gas oil are sometimes collectively referred to as coker gas oil without distinction
  • coker gas oil without distinction
  • the combined coke-pulling feedstock, the other coke-pulling feedstock, and the supplemental coke-pulling feedstock are sometimes collectively referred to as the coke-pulling feedstock without distinction.
  • the coke formation rate is measured in a 10 L tank coking reaction device at a temperature of 500° C., a pressure (gauge pressure) of 0.5 MPa and a coking duration of 10 min.
  • the coke formation rate is determined by the weight ratio of the residual solid in the coking reaction device to the reaction feedstock (such as the coke-forming feedstock or the coke-pulling feedstock) at the end of the coking reaction.
  • a coking system includes from the 1st to the m-th (a total of m) heating units and from the 1st to the n-th (a total of n) coke towers.
  • m is any integer of 2 to n ⁇ 1
  • n is any integer of 3 or more, preferably any integer of 3 to 20, more preferably any integer of 3 to 5, and still more preferably 3.
  • each of the m heating units is in communication with the n coke towers, respectively.
  • This communication may be accomplished in any manner conventionally known to those skilled in the art, such as a multi-way valve, and in particular a four-way valve (as shown in FIG. 1 ), but the invention is not limited thereto.
  • each of the n coke towers is in communication with one or more separation towers, respectively.
  • the upper part and/or the overhead of the coke tower are in communication with the separation tower.
  • the one or more separation towers are in communication with the m-th heating unit.
  • the lower part and/or the bottom of the tower (preferably the bottom of the tower) of one or more separation towers is/are in communication with the m-th heating unit.
  • the one or more separation towers may be further communicated with the i-th heating unit, as the case may be.
  • i is any integer greater than 1 and less than m.
  • the lower part of the tower and/or the bottom of the tower (preferably the bottom of the tower) of one or more separation towers is/are in communication with the i-th heating unit.
  • the one or more separation towers are not in communication with the 1st heating unit in order to further improve the performance of needle coke and to make the coking operation of the coking system smoother on the basis of the present invention.
  • the communication includes the cases of direct communication via pipeline and indirect communication with other devices such as a tank or a filter interposed therebetween.
  • the communication in a material transport manner, in particular the communication in a unidirectional material transport manner.
  • the type of the heating unit is not particularly limited, and any heating device may be used as long as it can heat the material transported through the unit to a predetermined temperature, for example heat-exchanger and heating furnace, preferably heating furnace.
  • the type of the separation tower is not particularly limited, and any separation apparatus may be used as long as it can separate the material fed to the separation tower into a plurality of components according to a predetermined requirement, and specific examples thereof include a rectification tower, a flash tower, an evaporation tower, a fractionation tower, and the like, and a fractionation tower is preferable.
  • the number of the separation towers is not particularly limited, and specifically, 1 to 10, 1 to 5, 1 to 3, or 1 tower may be mentioned.
  • the coking system is a coking unit that includes three coke towers, two sets of furnaces, a fractionation tower, and a coke-pulling feedstock storage tank. If the three coke towers are respectively marked as a coke tower a, a coke tower b and a coke tower c, and the two sets of heating furnaces are respectively marked as a heating furnace a and a heating furnace b, any one coke tower is connected with the two sets of heating furnaces, the top of any coke tower is connected with the inlet of the fractionation tower via pipeline, and the bottom outlet of the fractionation tower is connected with the coke-pulling feedstock storage tank.
  • the coke-pulling feedstock storage tank is connected with the heating furnace b to heat the materials from the coke-pulling feedstock storage tank to the feeding temperature of the coke tower.
  • the heating furnace a is connected with the feedstock tank to heat the coking feedstock to the feeding temperature of the coke tower.
  • a filtration device is provided between the raw coke-pulling feedstock tank and the heating furnace b.
  • the coking system may further comprise a control unit.
  • the control unit is configured to enable to start and terminate the material transport of each heating unit to the h-th coke tower sequentially in the order from the 1st heating unit to the m-th heating unit from the time T0, and terminate the material transport of the m-th heating unit to the h-th coke tower at the time Te.
  • h is any integer from 1 to n.
  • the sum of the material transport amounts of the 1st to the m-th heating units to the h-th coke tower is equal to the target coke-charging capacity of the h-th coke tower.
  • target coke-charging capacity is meant the maximum safe coke-charging capacity allowed for the coke tower.
  • the material transport from the 1st heating unit to the m-th heating unit to the h-th coke tower is completed from the time T0 to the time Te, which is referred to as a material transport cycle.
  • each of the 1st to the m-th heating units transports only one batch of material to the h-th coke tower during one material transport cycle.
  • the transport can be carried out here in a continuous, semi-continuous or batch manner.
  • the h-th coke tower does not accept the material transport at any time during a material transport cycle.
  • the h-th coke tower accepts only the material transport from only one of the 1st to the m-th heating units at any time during a single material transport cycle.
  • the h-th coke tower is purged and decoked, and then the h-th coke tower is on standby.
  • the h-th coke tower is purged and decoked, and then the next material transport cycle is started for the h-th coke tower.
  • each of the 1st to the m-th heating units is configured to heat its transport material to the feeding temperature required by the h-th coke tower for that transport material.
  • the 1st heating unit heats its transport material (referred to as the 1st transport material) to a feeding temperature W1 of 400° C. to 480° C. (preferably 420° C. to 460° C.).
  • the 1st transport material brings the intra-tower gas velocity G1 in the h-th coke tower to 0.05-0.25 m/s, preferably 0.05-0.10 m/s.
  • the m-th heating unit heats its transport material (referred to as the m-th transport material) to a feeding temperature Wm in the range of 460° C. to 530° C., preferably 460° C. to 500° C.
  • the m-th transport material brings the intra-tower gas velocity Gm in the h-th coke tower to 0.10-0.30 m/s, preferably 0.15-0.20 m/s.
  • the i-th heating unit heats its transport material (referred to as the i-th transport material) to a feeding temperature Wi, where W1 ⁇ Wi ⁇ Wm.
  • i is any integer greater than 1 and less than m.
  • the i-th transport material allows the intra-tower gas velocity in the h-th coke tower Gi to reach G1 ⁇ Gi ⁇ Gm.
  • the heating rate V1 of the 1st heating unit for its transport material is 1-30° C./h, preferably 1-10° C./h. After reaching the corresponding feeding temperature, the temperature is maintained constant.
  • the heating rate Vm of the m-th heating unit for its transport material is 30-150° C./h, preferably 50-100° C./h. After reaching the corresponding feeding temperature, the temperature is maintained constant.
  • the heating rate Vi of the i-th heating unit for its transport materials meets the relation V1 ⁇ Vi ⁇ Vm.
  • i is any integer greater than 1 and less than m. After reaching the corresponding feeding temperature, the temperature is maintained constant.
  • the upper part and/or the overhead (e.g., the top) of each of the n coke towers is communicated in a material transport manner with the one or more separation towers.
  • the upper material and/or overhead material (such as overhead material) of each of the n coke towers are transported to the one or more separation towers.
  • the overhead material of each coke tower is split into at least the overhead material of the separation tower and the bottom material of the separation tower, e.g. the overhead material may be split into an overhead material (commonly referred to as coker gas), a plurality of tower side materials (e.g. including naphtha and coker gas oil) and the bottom material.
  • the bottom material of the separation tower is sometimes also referred to as coker gas oil.
  • the coker gas oil has a 10% distillate point temperature of from 300° C. to 400° C., preferably from 350° C. to 380° C., and a 90% distillate point temperature of from 450° C. to 500° C., preferably from 460° C. to 480° C.
  • the operating conditions of the one or more separation towers comprise: the pressure at the top of the tower is 0.01-0.8 MPa, the temperature at the top of the tower is 100-200° C., and the temperature at the bottom of the tower is 280-400° C.
  • the operating conditions of the n coke towers which are identical to or different from each other, each independently comprise: the pressure at the top of the tower is 0.01-1.0 MPa, the temperature at the top of the tower is 300-470° C., and the temperature at the bottom of the tower is 350-510° C.
  • the 1st heating unit uses the coke-forming feedstock as the transport material.
  • the coking system may also generally include at least one coke-forming feedstock storage tank (sometimes also referred to as the feedstock tank) for the smooth operation.
  • the at least one coke-forming feedstock tank is in communication with the 1st heating unit for transporting coke-forming feedstock in the at least one coke-forming feedstock tank to the 1st heating unit.
  • the 1st heating unit only uses a coke-forming feedstock as the transportation material, and does not use a coke-pulling feedstock, especially does not use the bottom material of the separation tower or coker gas oil as the transportation material, even if it is a part of the transportation material.
  • the at least one coke-forming feedstock storage tank is not in communication with the m-th heating unit.
  • the communication includes the case of direct communication via pipeline and indirect communication with other devices such as a tank or a filter interposed therebetween.
  • the m-th heating unit uses a coke-pulling feedstock as the transport material.
  • the coke-pulling feedstock comprises at least the bottom material of the one or more separation towers.
  • the ratio of the bottom material in the coke-pulling feedstock (generally referred to as make-up ratio) is not particularly limited, but may be generally 0 to 80%, preferably 30 to 70%, more preferably 50 to 70%.
  • the at least one coke-forming feedstock storage tank is not in communication with the m-th heating unit in order to further improve the performance of needle coke and to make the coking operation of the coking system smoother on the basis of the present invention.
  • the communication includes the case of direct communication via pipeline and indirect communication with other devices such as a tank or a filter interposed therebetween.
  • the m-th heating unit uses only the coke-pulling feedstock as its transported material, and does not use the coke-forming feedstock as its transported material.
  • the i-th heating unit has at least one selected from the coke-forming feedstock and the coke-pulling feedstock as the transport material.
  • the at least one coke-forming feedstock storage tank may be in communication with the i-th heating unit (when the coke-forming feedstock is used as the transport material) or may be not in communication with the i-th heating unit (when the other materials are used as the transport material).
  • i is any integer greater than 1 and less than m.
  • the coke-forming feedstock is selected from at least one of a coal-based feedstock and a petroleum-based feedstock, preferably at least one of coal tar, coal tar pitch, heavy petroleum oil, ethylene tar, catalytic cracking residue, or thermal cracking residue.
  • the coke formation rate of the coke-forming feedstock (referred to as coke formation rate A) is generally 10 to 80%, preferably 20 to 70%, more preferably 30 to 60%.
  • the sulfur content of the coke-forming feedstock is generally ⁇ 0.6 wt %, preferably ⁇ 0.5 wt %. For this reason, the coke-forming feedstock is usually refined.
  • the colloid and asphaltene content of the coke-forming feedstock is generally ⁇ 10.0 wt %, preferably ⁇ 5.0 wt %, more preferably ⁇ 2.0 wt %.
  • the colloid and asphaltene contents are measured according to the standard SH/T05094-2010.
  • the 10% distillate point temperature of the bottom material of the one or more separation towers is from 300° C. to 400° C., preferably from 350° C. to 380° C.
  • the 90% distillate point temperature is from 450° C. to 500° C., preferably from 460° C. to 480° C.
  • the coke-pulling feedstock is selected from at least one of coal-based raw material and petroleum-based raw material, preferably at least one of coker gas oil, coker diesel, ethylene tar and thermally cracked heavy oil.
  • the coke-pulling feedstock (especially coker gas oil) may be obtained from the aforementioned separation tower (e.g., as the bottom material of the separation tower), or may be obtained from another source, such as commercially available or produced by any method known in the art, and is not particularly limited.
  • the coke-pulling feedstock comprises at least the bottom material of the one or more separation towers.
  • the ratio of the bottom material in the coke-pulling feedstock (generally referred to as make-up ratio) is not particularly limited, but may be generally 0 to 80%, preferably 30 to 70%, more preferably 50 to 70%.
  • the coke formation rate of the coke raw material (referred to as coke formation rate B) is generally 1 to 40%, preferably 1 to 20%, more preferably 1 to 10%.
  • the coke formation rate A >the coke formation rate B.
  • the sulfur content of the coke-pulling feedstock is generally ⁇ 1.0 wt %, preferably ⁇ 0.6 wt %.
  • the weight ratio of the total amount of the coke-pulling feedstock to the total amount of the coke-forming feedstock transported to the h-th coke tower during a single material transport cycle is generally in the range of from 0.5 to 4.0, preferably in the range of from 1.0 to 2.0.
  • h is any integer from 1 to n.
  • the coke-charging cycles T of the n coke towers which are identical to or different from each other (preferably identical to each other), are each independently from 10 to 60 hours, preferably from 24 to 48 hours.
  • the control unit is configured to start and stop the material transport of the j-th heating unit to the a-th coke tower, and then start and stop the material transport of the j-th heating unit to the b-th coke tower.
  • j is any integer of 1 to m.
  • a is any integer from 1 to n, and b is any integer from 1 to n, but a ⁇ b.
  • any two of the n coke towers that are numbered adjacent are the a-th coke tower and the b-th coke tower, respectively.
  • the material transport from the j-th heating unit to the b-th coke tower is started (after a necessary delay time has elapsed, as the case may be) at the time when the material transport from the j-th heating unit to the a-th coke tower is completed.
  • a coking process comprising the step of coking with m heating units and n coke towers.
  • the process comprises the step of coking using the coking system of the present invention as described hereinbefore. Except for what is specifically described below, all the matters or contents of the coking process which are not specified can be directly applied to the corresponding description of the coking system, and are not described in detail herein.
  • At least a portion of the upper material and/or the overhead material (such as the overhead material) of each of the n coke towers is transported to the one or more separation towers, and at least a portion of the lower material and/or the bottom material of the one or more separation towers is transported to the m-th heating unit, and optionally to the i-th heating unit.
  • i is any integer greater than 1 and less than m.
  • the term “at least a portion of” means, for example, 10 wt % or more, 20 wt % or more, 30 wt % or more, 40 wt % or more, 50 wt % or more, 60 wt % or more, 70 wt % or more, 80 wt % or more, 90 wt % or more, or 100 wt %.
  • the lower material and/or the bottom material of the one or more separation towers is not fed to the 1st heating unit in order to further improve the performance of the needle coke and to make the coking operation of the coking system smoother on the basis of the invention.
  • the coking device used in the coking process comprises three coke towers, two sets of heating furnaces, a fractionation tower and a coke-pulling feedstock storage tank, wherein the three coke towers are respectively marked as a coke tower a, a coke tower b and a coke tower c; the two sets of heating furnaces are respectively marked as a heating furnace a and a heating furnace b, any coke tower is connected with the two sets of heating furnaces, the top of any coke tower is connected with the inlet of the fractionation tower via pipeline, the bottom outlet of the fractionation tower is connected with the coke-pulling feedstock storage tank, the heating furnace b is connected with the coke-pulling feedstock storage tank and is used for heating the material from the coke-pulling feedstock storage tank to the feeding temperature of the coke tower, and the heating furnace a is connected with the feedstock tank and is used for heating a fresh feedstock to the feeding temperature of the coke tower;
  • the coking feedstock is heated by the heating furnace a and enters the coke tower a, the generated oil gas enters the fractionation tower and is fractionated to obtain gas, coker gasoline, coker diesel and coker gas oil at the tower bottom, wherein the coker gas oil at the tower bottom is introduced into the coke-pulling feedstock storage tank;
  • the feeding duration of the coke tower a in the step (1) comprises 30-70% of the total coke-producing cycle
  • the coking feed of the coke tower a is switched to the coke tower b
  • the coke tower b repeats the coke-charging process of the coke tower a in the step (1)
  • the coke tower a is fed with the coke-pulling feedstock heated through a heating furnace b to continue the coke-charging;
  • the feeding duration of the coke tower b in the step (2) comprises 30-70% of the total coke-producing cycle
  • the coking feed of the coke tower b is switched to a coke tower c
  • the coke tower c repeats the coke-charging process of the coke tower a in the step (1)
  • the coke-pulling feedstock which is heated to a relatively high temperature by the heating furnace b is switched to the coke tower b
  • the coke tower a is subjected to a steam purging and decoking operation at this time, and reassembled to be on standby for the next coke-charging;
  • the feeding duration of the coke tower c in the step (3) comprises 30-70% of the total coke-producing cycle
  • the coking feed of the coke tower c is switched to the coke tower a
  • the coke tower a repeats the process in the step (1)
  • the coke-pulling feedstock which is heated to a relatively high temperature by a heating furnace b is switched to the coke tower c
  • the coke tower b is subjected to a steam purging and decoking operation at this time, and reassembled to be on standby for the next coke-charging
  • the feeding duration of the coke tower a in the step (4) comprises 30-70% of the total coke-producing cycle
  • the coking feed of the coke tower a is switched to the coke tower b
  • the coke tower b repeats the coke-charging process of the coke tower a in the step (1)
  • the coke-pulling feedstock which is heated to a relatively high temperature by a heating furnace b is switched to the coke tower a
  • the coke tower c is subjected to a steam purging and decoking operation at this time, and reassembled to be on standby for the next coke-charging;
  • the coking process comprises at least the steps of:
  • At least one material selected from the group consisting of the coke-forming feedstock and the coke-pulling feedstock is filtered before entering the respective heating unit and/or entering the respective coke tower.
  • the coke fine particle concentration of the material is generally controlled to 0 to 200 mg/L, preferably 0 to 100 mg/L, more preferably 0 to 50 mg/L.
  • the filtration method for example, fine filtration, centrifugal separation, flocculation separation and the like can be mentioned, and fine filtration is preferable. These filtration methods may be used singly or in combination of two or more at an arbitrary ratio.
  • said material it is preferably said coke-pulling feedstock, more preferably the bottom material of said one or more separation towers or coker gas oil.
  • said material is subjected to said filtration before entering the respective heating unit, more preferably said material (in particular said coker gas oil) is subjected to said filtration before entering the m-th heating unit, and/or said material (in particular said coker gas oil) is subjected to said filtration before entering the i-th heating unit.
  • i is any integer greater than 1 and less than m.
  • the coking system further optionally comprises at least one filtration device provided at the inlet and/or outlet of at least one of the heating units.
  • the at least one filtration device is provided at the inlet and/or outlet of the m-th heating unit.
  • the at least one filtration device is provided at the inlet and/or outlet of the i-th heating unit.
  • i is any integer greater than 1 and less than m.
  • the filtration device of the present invention is not particularly limited, and any filtration device conventionally used in the art may be used as long as the desired filtration object can be achieved, and specific examples thereof include a fine filtration device, a centrifugal separation device, and a flocculation separation device.
  • the inlet is referred to as the transport material inlet and the outlet is referred to as the transport material outlet.
  • the coking system comprises at least three coke towers and two heating units; any coke tower is communicated with the at least two heating units, said two heating units are used for heating feedstock 1 and feedstock 2 , respectively, to a feeding temperature, and said any coke tower is in communication with a fractionation tower.
  • the feedstock 1 is typically a fresh coker feedstock
  • the feedstock 2 is typically a coke-pulling feedstock (especially coker gas oil).
  • the coking system comprises three coke towers, two sets of heating furnaces, a fractionation tower and a coke-pulling feedstock storage tank, wherein the three coke towers are respectively marked as a coke tower a, a coke tower b and a coke tower c; the two sets of heating furnaces are respectively marked as a heating furnace a and a heating furnace b, any coke tower is communicated with the two sets of heating furnaces, the top of any coke tower is communicated with the inlet of a fractionation tower via pipeline, the bottom outlet of the fractionation tower is communicated with the coke-pulling feedstock storage tank, the coke-pulling feedstock storage tank is communicated with the heating furnace b to heat the material in the coke-pulling feedstock storage tank to the feeding temperature of the coke tower, and the heating furnace a is communicated with the feedstock tank to heat the coking feedstock to the feeding temperature of the coke tower.
  • the coking system includes three coke towers and two heating furnaces, the three coke towers are respectively denoted as a coke tower a, a coke tower b, and a coke tower c, the two heating furnaces are respectively denoted as a heating furnace 1 and a heating furnace 2 , any one coke tower is communicated with at least two heating furnaces, the two heating furnaces are respectively used for heating the raw material 1 and the raw material 2 to the feeding temperature, and any one coke tower is communicated with a fractionation tower.
  • the feedstock 1 is generally a fresh feedstock
  • the feedstock 2 is generally a coke-pulling feedstock (in particular coker gas oil).
  • the specific operation of the coking system is as follows:
  • the feeding duration of the coke tower a in the step (1) comprises 30-70% of the coke-charging cycle, switching the raw material 1 heated by the heating furnace 1 to a coke tower b, repeating the coke-charging process of the coke tower a in the step (1) on the coke tower b, and feeding the coke tower a with the coke-pulling feedstock heated through a heating furnace b to continue the coke-charging;
  • the feeding duration of the coke tower b in the step (2) comprises 30-70% of the coke-charging cycle, switching the raw material 1 heated by the heating furnace 1 to a coke tower c, repeating the coke-charging process of the coke tower a in the step (1) on the coke tower c, switching the raw material 2 heated by the heating furnace b to the coke tower b, and subjecting the coke tower a to a steam purging and decoking operation at this time, and reassembling to be on standby for the next coke-charging;
  • the feeding duration of the coke tower c in the step (3) comprises 30-70% of the coke-charging cycle, switching the raw material 1 heated by the heating furnace 1 to a coke tower a, repeating the coke-charging process of the coke tower a in the step (1), switching the raw material 2 heated by the heating furnace b to the coke tower c, and subjecting the coke tower b to a steam purging and decoking operation at this time, and reassembling to be on standby for the next coke-charging;
  • the feeding duration of the coke tower a in the step (4) comprises 30-70% of the coke-charging cycle, switching the raw material 1 heated by the heating furnace 1 to a coke tower b, repeating the coke-charging process of the coke tower a in the step (1) on the coke tower b, switching the raw material 2 heated by the heating furnace b to the coke tower a, and subjecting the coke tower c to a steam purging and decoking operation at this time, and reassembling to be on standby for the next coke-charging;
  • the coke tower has a coke-charging cycle of 24-48 h, wherein the coke-charging cycle is the total coke-charging time of the coke-forming feedstock and the coke-pulling feedstock (such as coker gas oil) in a single coke tower.
  • the coke-charging cycle is the total coke-charging time of the coke-forming feedstock and the coke-pulling feedstock (such as coker gas oil) in a single coke tower.
  • the coking feed to a coke tower is switched to another coke tower.
  • the outlet temperature of the heating furnace a ranges from 400° C. to 460° C., preferably from 420° C. to 450° C., while the intra-tower gas velocity in the coke tower is controlled to be 0.05 to 0.25 m/s, preferably 0.05 to 0.10 m/s.
  • the heating rate of the heating furnace a is 1 to 30° C./h, preferably 1 to 10° C./h.
  • the outlet temperature of the heating furnace b is in the range of 460° C. to 530° C., preferably 460° C. to 500° C.
  • the intra-tower gas velocity in the coke tower is controlled to be 0.10 to 0.30 m/s, preferably 0.15 to 0.20 m/s.
  • the heating rate of the heating furnace b is 30 to 150° C./h, preferably 50 to 100° C./h.
  • a coking system used by the coking process comprises three coke towers, two sets of heating furnaces, a fractionation tower and a coke-pulling feedstock storage tank, wherein the three coke towers are respectively marked as a coke tower a, a coke tower b and a coke tower c; the two sets of heating furnaces are respectively marked as a heating furnace a and a heating furnace b, any coke tower is communicated with the two sets of heating furnaces, the top of any coke tower is communicated with the inlet of a fractionation tower via pipeline, the bottom outlet of the fractionation tower is communicated with a coke-pulling feedstock storage tank, the heating furnace b is communicated with the coke-pulling feedstock storage tank to heat the material in the coke-pulling feedstock storage tank to the feeding temperature of the coke tower, and the heating furnace a is communicated with the feedstock tank to heat a fresh feedstock to the feeding temperature of the coke tower.
  • the specific operating procedure of the coking process is as follows:
  • a coke-forming feedstock is heated by a heating furnace a and enter a coke tower a, the generated oil gas enters a fractionation tower, and the generated oil gas enters the fractionation tower and is fractionated to obtain gas, coker gasoline, coker diesel and coker gas oil at the tower bottom, wherein the coker gas oil at the tower bottom is introduced into the coke-pulling feedstock storage tank;
  • the feeding duration of the coke tower a in the step (1) comprises 30-70% of the total coke-charging cycle
  • the coking feed of the coke tower a is switched to the coke tower b
  • the coke tower b repeats the coke-charging process of the coke tower a in the step (1)
  • the coke tower a is fed with the coke-pulling feedstock heated through a heating furnace b to continue the coke-charging
  • the feeding duration of the coke tower b in the step (2) comprises 30-70% of the total coke-charging cycle
  • the coking feed of the coke tower b is switched to a coke tower c
  • the coke tower c repeats the coke-charging process of the coke tower a in the step (1)
  • the coke-pulling feedstock which is heated to a relatively high temperature by the heating furnace b is switched to the coke tower b
  • the coke tower a is subjected to a steam purging and decoking operation at this time, and reassembled to be on standby for the next coke-charging;
  • the feeding duration of the coke tower c in the step (3) comprises 30-70% of the total coke-charging cycle
  • the coking feed of the coke tower c is switched to the coke tower a
  • the coke tower a repeats the process in the step (1)
  • the coke-pulling feedstock which is heated to a relatively high temperature by a heating furnace b is switched to the coke tower c
  • the coke tower b is subjected to a steam purging and decoking operation at this time, and reassembled to be on standby for the next coke-charging
  • the feeding duration of the coke tower a in the step (4) comprises 30-70% of the total coke-charging cycle
  • the coking feed of the coke tower a is switched to the coke tower b
  • the coke tower b repeats the coke-charging process of the coke tower a in the step (1)
  • the coke-pulling feedstock which is heated to a relatively high temperature by a heating furnace b is switched to the coke tower a
  • the coke tower c is subjected to a steam purging and decoking operation at this time, and reassembled to be on standby for the next coke-charging
  • the coke tower has a coke-charging cycle of 24-48 h, and said coke-charging cycle is the total charging time of the coke-forming feedstock and the coke-pulling feed (such as coker gas oil) in a single coke tower.
  • the coking feed to a coke tower is switched to another coke tower.
  • the outlet temperature of the heating furnace a ranges from 400° C. to 460° C., preferably from 420° C. to 450° C., while the intra-tower gas velocity in the coke tower is controlled to be 0.05 to 0.25 m/s, preferably 0.05 to 0.10 m/s.
  • the heating rate of the heating furnace a is 1 to 30° C./h, preferably 1 to 10° C./h.
  • the outlet temperature of the heating furnace b is in the range of 460° C. to 530° C., preferably 460° C. to 500° C.
  • the intra-tower gas velocity in the coke tower is controlled to be 0.10 to 0.30 m/s, preferably 0.15 to 0.20 m/s.
  • the heating rate of the heating furnace b is 30 to 150° C./h, preferably 50 to 100° C./h.
  • Feedstock 1 is firstly fed as a coke-forming feedstock through a heating furnace 2 to a coke tower 4 a .
  • the oil gas generated by the coke tower 4 a is fed to a separation tower 6 via pipeline 5 , and separated to produce a gas 7 , a gasoline 8 and a diesel 9 , which leave the separation tower for the further treatment, and a coker gas oil, which leaves the separation tower from the bottom of the tower.
  • the oil gas generated by the coke towers 4 a and 4 b is fed to the separation tower 6 , and separated to produce a gas 7 , a gasoline 8 and a diesel 9 that leave the separation tower for the further treatment, and a coker gas oil at the bottom of the tower, a part of which is fed to the coke-pulling feedstock storage tank 12 via pipeline 10 , and another part of which is recycled via pipeline 11 and mixed with the supplementary coke-pulling feedstock from the pipeline 13 to return to the coke tower 4 a.
  • the oil gas generated by the coke towers 4 b and 4 c is fed to the separation tower 6 , and separated to produce a gas 7 , a gasoline 8 and a diesel 9 that leave the separation tower for the further treatment, and a coker gas oil at the bottom of the tower, a part of which is fed to the coke-pulling feedstock storage tank 12 via pipeline 10 , and another part of which is recycled via pipeline 11 and mixed with the supplementary coke-pulling feedstock from the pipeline 13 to return to the coke tower 4 b.
  • the oil gas generated by the coke towers 4 a and 4 c is fed to the separation tower 6 , and separated to produce a gas 7 , a gasoline 8 and a diesel 9 that leave the separation tower for the further treatment, and a coker gas oil at the bottom of the tower, a part of which is fed to the coke-pulling feedstock storage tank 12 via pipeline 10 , and another part of which is recycled via pipeline 11 and mixed with the supplementary coke-pulling feedstock from the pipeline 13 to return to the coke tower 4 c.
  • the oil gas generated by the coke towers 4 a and 4 b is fed to the separation tower 6 , and separated to produce a gas 7 , a gasoline 8 and a diesel 9 that leave the separation tower for the further treatment, and a coker gas oil at the bottom of the tower, a part of which is fed to the coke-pulling feedstock storage tank 12 via pipeline 10 , and another part of which is recycled via pipeline 11 and mixed with the supplementary coke-pulling feedstock from the pipeline 13 to return to the coke tower 4 a;
  • a fresh feedstock for needle coke 17 is heated by a heating furnace 18 and then enters a coke tower 20 via pipeline 19 , the generated oil gas enters a fractionation tower 22 via pipeline 21 , and is separated to produce coker gas, naphtha, coker diesel and coker gas oil respectively, which leave the fractionation tower for further treatment via pipelines 23 , 24 , 25 and 26 .
  • the recycled coker gas oil enters the coke tower 20 via pipeline 27 , and the needle coke product leave the coke tower from the bottom of the tower for the further treatment.
  • the coke towers 20 a and 20 b are operated in an intermittent switching manner, namely when the feeding amount of a coke tower reaches the maximum safe coke-charging amount, the feeding is switched to another coke tower to continue the feeding, and the first coke tower is subjected to steam purging and decoking to be on standby.
  • the coefficient of thermal expansion was determined according to International Standard GB/T3074.4 “Determination of Coefficient of Thermal Expansion (CTE) for Graphite Electrodes”, the volatile was determined according to Petrochemical Standard SH/T0313 “Petroleum Coke Test Method”, the true density was determined according to International Standard GB/T6155 “Determination of True Density of Carbon Material”, the resistivity was determined according to GB24525-2009 “Determination of Resistivity of Carbon Material”, and the streamlined texture in the appearance of the needle coke was directly evaluated by naked eyes.
  • CTE Coefficient of Thermal Expansion
  • Catalytic slurry oil from a refinery was used as the coking feedstock.
  • the specific analysis properties of the slurry oil were shown in Table 1.
  • the top pressure of the coke tower was 0.5 MPa, and the coke-producing cycle of the coking procedure was 32 h.
  • the three-tower switching process provided by the invention was performed.
  • the outlet temperature of the heating furnace 1 was 420-440° C., where a procedure of rising the temperature and maintaining the temperature was performed, the heating rate was 5° C./h, and the temperature-maintaining time was 12 h, and the gas velocity in the coke tower was controlled to 0.05-0.08 m/s.
  • step (2) the outlet temperature of the heating furnace 2 was 460-490° C., where a procedure of rising the temperature and maintaining the temperature was performed, the heating rate was 10° C./h, and the temperature-maintaining time was 13 h, and the gas velocity in the coke tower was controlled to 0.13-0.18 m/s.
  • steps (1) to (5) the coker gas oil had a 10% distillate point temperature of 350° C. and a 90% distillate point temperature of 460° C.
  • the pulling/forming ratio (the ratio of the coke-pulling feedstock to the coke-forming feedstock) was controlled to 1.0.
  • the concentration of the coke fine particles in the coke-pulling feedstock was controlled to 20 mg/L.
  • Table 2 The properties of different batches of needle cokes obtained with the three-tower process were shown in Table 2.
  • catalytic slurry oil from a refinery was used as the coke-forming material for producing the needle coke
  • the specific analysis properties of the slurry oil were shown in table 1, and its coke formation rate A was 40%.
  • the supplementary coke-pulling feedstock was a coker gas oil (temporarily stored in a coke-pulling feedstock storage tank 12 ) from a separation tower 6 , which had a 10% distillate point temperature of 350° C. and a 90% distillate point temperature of 460° C., and its coke formation rate B was 10%.
  • the coke-charging cycle T of the coke tower was 32 h.
  • the specific operations were as follows:
  • the feedstock 1 was heated by a heating furnace 2 and fed to the coke tower 4 a as the coke-forming feedstock.
  • the outlet of the heating furnace 2 was controlled in a mode of variable temperature and constant temperature.
  • the variable temperature range was 420-440° C. with a heating rate of 5° C./h.
  • the top pressure of the coke tower 4 a was 0.5 MPa.
  • the oil gas generated by the coke tower 4 a was fed to a separation tower 6 via pipeline 5 .
  • the top pressure of the separation tower 6 was 0.5 MPa, and the top temperature of the tower was 150° C., the bottom temperature of the tower was 350° C.
  • the oil gas was separated to produce a gas 7 , a gasoline 8 and a diesel 9 that left the separation tower for the further treatment, and a coker gas oil that left the separation tower from the bottom of the tower.
  • the outlet temperature of the heating furnace 14 was 460-490° C., where a procedure of rising the temperature and maintaining the temperature was performed and the heating rate was 10° C./h.
  • the top pressure of the coke towers 4 a and 4 b was controlled to 0.5 MPa.
  • the oil gas generated by the coke towers 4 a and 4 b was fed to the separation tower 6 , where the top pressure of the separation tower 6 was 0.5 MPa, the top temperature of the tower was 150° C., and the bottom temperature of the tower was 350° C., and separated to produce a gas 7 , a gasoline 8 and a diesel 9 that left the separation tower for the further treatment, and a coker gas oil at the bottom of the tower.
  • a part of the coker gas oil was fed to the coke-pulling feedstock storage tank 12 via pipeline 10 , and another part was recycled via pipeline 11 and mixed with the supplementary coke-pulling feedstock from the pipeline 13 to return to the coke tower 4 a .
  • the pulling/forming ratio (the ratio of the coke-pulling feedstock to the coke-forming feedstock) was controlled to 1.0.
  • the outlet temperature of the heating furnace 14 was 460-490° C., where a procedure of rising the temperature and maintaining the temperature was performed and the heating rate was 10° C./h.
  • the top pressure of the coke towers 4 b and 4 c was controlled to 0.5 MPa.
  • the oil gas generated by the coke towers 4 b and 4 c was fed to the separation tower 6 , where the top pressure of the separation tower 6 was 0.5 MPa, the top temperature of the tower was 150° C., and the bottom temperature of the tower was 350° C., and separated to produce a gas 7 , a gasoline 8 and a diesel 9 that left the separation tower for the further treatment, and a coker gas oil at the bottom of the tower.
  • a part of the coker gas oil was fed to the coke-pulling feedstock storage tank 12 via pipeline 10 , and another part was recycled via pipeline 11 and mixed with the supplementary coke-pulling feedstock from the pipeline 13 to return to the coke tower 4 b .
  • the pulling/forming ratio (the ratio of the coke-pulling feedstock to the coke-forming feedstock) was controlled to 1.0.
  • the outlet temperature of the heating furnace 14 was 460-490° C., where a procedure of rising the temperature and maintaining the temperature was performed and the heating rate was 10° C./h.
  • the top pressure of the coke towers 4 a and 4 c was controlled to 0.5 MPa.
  • the oil gas generated by the coke towers 4 a and 4 c was fed to the separation tower 6 , where the top pressure of the separation tower 6 was 0.5 MPa, the top temperature of the tower was 150° C., and the bottom temperature of the tower was 350° C., and separated to produce a gas 7 , a gasoline 8 and a diesel 9 that left the separation tower for the further treatment, and a coker gas oil at the bottom of the tower.
  • a part of the coker gas oil was fed to the coke-pulling feedstock storage tank 12 via pipeline 10 , and another part was recycled via pipeline 11 and mixed with the supplementary coke-pulling feedstock from the pipeline 13 to return to the coke tower 4 c .
  • the pulling/forming ratio (the ratio of the coke-pulling feedstock to the coke-forming feedstock) was controlled to 1.0.
  • the outlet temperature of the heating furnace 14 was 460-490° C., where a procedure of rising the temperature and maintaining the temperature was performed and the heating rate was 10° C./h.
  • the top pressure of the coke towers 4 a and 4 b was controlled to 0.5 MPa.
  • the oil gas generated by the coke towers 4 a and 4 b was fed to the separation tower 6 , where the top pressure of the separation tower 6 was 0.5 MPa, the top temperature of the tower was 150° C., and the bottom temperature of the tower was 350° C., and separated to produce a gas 7 , a gasoline 8 and a diesel 9 that left the separation tower for the further treatment, and a coker gas oil at the bottom of the tower.
  • the same coke-forming feedstock as in example 1 was used.
  • the coke-charging cycle T was 32 hours.
  • the conventional two-tower switching operation shown in FIG. 2 was performed.
  • a fresh feedstock for needle coke 17 was heated by a heating furnace 18 and then enters a coke tower 20 via pipeline 19 .
  • the outlet of the heating furnace 18 was controlled in a mode of variable temperature and constant temperature.
  • the variable temperature range was 420-440° C. with a heating rate of 5° C./h.
  • the top pressure of the coke tower 20 was 0.5 MPa.
  • the generated oil gas was fed via pipeline 21 to a fractionation tower 22 , where the top pressure of the fractionation tower 22 was 0.5 MPa, the top temperature of the tower was 150° C., and the bottom temperature of the tower was 350° C., and separated to produce coker gas, naphtha, coker diesel and coker gas oil respectively, which left the fractionation tower for further treatment via pipelines 23 , 24 , 25 and 26 .
  • the recycled coker gas oil was fed via pipeline 27 to the coke tower 20 .
  • the pulling/forming ratio (the ratio of the coke-pulling feedstock to the coke-forming feedstock) was 1.0.
  • Example 1 Comparative Example 1 Analysis Item Batch 1 Batch 2 Batch 3 Batch 1 Batch 2 Batch 3 Coefficient of thermal 1.0 1.1 1.0 1.2 1.6 1.9 expansion, 10 ⁇ 6 /° C. Volatile, w % 8.5 8.2 8.5 9.8 9.5 8.8 Resistivity, ⁇ ⁇ m 7.8 7.0 7.6 8.0 10.5 14.5 True density, g/cm 3 2.12 2.12 2.12 2.10 2.12 2.09 Streamlined texture in the Obvious Obvious Obvious Obvious Not obvious Not obvious appearance
  • the same apparatus and coke-forming feedstock for producing needle coke as in example 1 were used.
  • the supplementary coke-pulling feedstock was a coker gas oil (temporarily stored in a coke-pulling feedstock storage tank 12 ) from a separation tower 6 having a 10% distillate point temperature of 330° C. and a 90% distillate point temperature of 480° C., and its coke formation rate B is 20%.
  • the coke-charging cycle T of the coke tower was 40 h.
  • the top pressure of the coke tower was 0.8 MPa.
  • the outlet temperature of the heating furnace 2 was 400-460° C., where a procedure of rising the temperature and maintaining the temperature was performed, the heating rate was 4° C./h.
  • the gas velocity in the coke tower was controlled to 0.07-0.10 m/s.
  • the outlet temperature of the heating furnace 14 was 470-510° C., and the heating rate was 10° C./h.
  • the gas velocity in the coke tower was controlled to 0.18-0.25 m/s.
  • the pulling/forming ratio (the ratio of the coke-pulling feedstock to the coke-forming feedstock) was controlled to 2.0.
  • the concentration of the coke fine particles in the coke-pulling feedstock was controlled to ⁇ 10 mg/L.
  • the top pressure of the fractionation tower was 0.2 MPa, the top temperature of the tower was 100° C., and the bottom temperature of the tower is 330° C.
  • Other conditions were the same as in Example 1.
  • the properties of different batches of needle cokes obtained with the three-tower process were shown in Table 3.
  • the same coke-forming feedstock as that in the Example 2 was used.
  • the coke-charging cycle T was 40 h.
  • the outlet of the heating furnace 18 was controlled in a mode of variable temperature and constant temperature, and the variable temperature range was 420-460° C. with a heating rate of 4° C./h.
  • the top pressure of the coke tower 20 was 0.8 MPa.
  • the top pressure of the fractionation tower was 0.2 MPa, and the top temperature of the tower was 100° C., the bottom temperature of the tower was 330° C.
  • the pulling/forming ratio (the ratio of the coke-pulling feedstock to the coke-forming feedstock) was 0.5.

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