[go: up one dir, main page]

WO2015093845A1 - Système de traitement de haute qualité du charbon et procédé de traitement de haute qualité du charbon - Google Patents

Système de traitement de haute qualité du charbon et procédé de traitement de haute qualité du charbon Download PDF

Info

Publication number
WO2015093845A1
WO2015093845A1 PCT/KR2014/012478 KR2014012478W WO2015093845A1 WO 2015093845 A1 WO2015093845 A1 WO 2015093845A1 KR 2014012478 W KR2014012478 W KR 2014012478W WO 2015093845 A1 WO2015093845 A1 WO 2015093845A1
Authority
WO
WIPO (PCT)
Prior art keywords
coal
flue gas
dryer
carbonization reactor
quality treatment
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/KR2014/012478
Other languages
English (en)
Korean (ko)
Inventor
김태홍
윤광의
송영석
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
OCI Holdings Co Ltd
Original Assignee
OCI Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by OCI Co Ltd filed Critical OCI Co Ltd
Publication of WO2015093845A1 publication Critical patent/WO2015093845A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Images

Classifications

    • 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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • 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
    • C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
    • C10B57/10—Drying
    • 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
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C10K1/046—Reducing the tar content

Definitions

  • a high quality treatment system for coal and a high quality treatment method for coal are provided.
  • Lignite has been limited in its utilization due to its high water content, high risk of spontaneous ignition during transportation, and low calorific value.
  • interest in utilizing lignite, a low grade coal is increasing.
  • Low temperature carbonization is a technique for pyrolyzing coal and converting it into solid, liquid and gaseous products.
  • the low temperature carbonization process can be divided into direct heating, indirect heating, direct and indirect heating according to the heating method, and is divided into a method using a solid material and a gas material depending on the heat transfer method.
  • the indirect heating method has the disadvantage that the quality of the solid product produced is not uniform because the heat transfer efficiency is low and the heat is not evenly transferred.
  • the temperature in order to transfer heat to the center of the reactor, the temperature must be kept higher than the target temperature. In this case, the volatilization of coal causes a secondary reaction, which leads to a decrease in the yield of tar oil.
  • the reactor may have a uniform temperature distribution as a whole, but since the volatile matter of coal and the flue gas, which is a heat transfer material, are mixed, a separate process for separating the volatile matter and the flue gas requires a disadvantage in that the investment cost increases.
  • the heat transfer material uses a solid material such as a ceramic ball in the direct heating method, coal fine powder production is increased due to friction between the coal and the ceramic ball, thereby lowering the yield of the solid product.
  • ceramic balls must be continuously mixed to increase the area and time of contact with coal, which requires additional equipment and additional equipment to separate coal and ceramic balls. Therefore, there is a problem that the process cost increases.
  • One embodiment of the present invention can provide a high yield of tar oil from a low grade coal, and provides a high quality coal treatment system of high efficiency in terms of energy saving.
  • Another embodiment of the present invention provides a high-quality tar oil of high yield from low grade coal, and provides a high-quality treatment method of coal in terms of energy saving.
  • a dryer for supplying the heated flue gas to dry coal
  • a condenser to condense the moisture mixed with the flue gas received from the dryer
  • the apparatus may further include a combustor generating a heated flue gas supplied to the dryer, wherein the combustor may supply the heated flue gas to the carbonization reactor.
  • the flue gas supplied to the carbonization reactor may be cooled in the heat exchanger, and the flue gas supplied to the cooler in the carbonization reactor may be introduced into the combustor and recycled.
  • the high quality coal processing system may further include tar condensation means for condensing and collecting the cooled tar oil.
  • the high quality treatment system of coal may further include tar collecting means for collecting tar oil condensed in the tar condensing means.
  • Water discharged from the cooler and water discharged from the condenser may be supplied to the cooler and recycled.
  • the flue gas supplied to the dryer may be cooled in the condenser, then supplied to the heat exchanger, heated up, and then re-introduced into the dryer to be recycled.
  • the high quality coal processing system may further include a blower provided between the heat exchanger and the cooler to transfer the flue gas from the heat exchanger to the cooler.
  • the temperature of the volatiles including the tar oil discharged from the carbonization reactor may be 150 to 300 °C.
  • the carbonization reaction temperature of the coal in the carbonization reactor may be 500 to 700 °C.
  • the temperature of the flue gas supplied to the carbonization reactor may be 800 to 1200 °C.
  • the vertical retort device formed by integrating the dryer, the carbonization reactor, and the cooler, wherein the carbonization reactor has a tar oil in a region where the temperature is lowered from the bottom of the vertical retort device and the temperature is 150 to 300 ° C. It may be provided with a discharge port for discharging volatile matter containing.
  • the high quality treatment method of the coal may further comprise the step of supplying to the dryer after the flue gas discharged and cooled along with the water removed from the dryer is heated in contact with the tar oil discharged from the carbonization reactor, the temperature is elevated. .
  • flue gas is discharged together when the generated tar oil is discharged from the carbonization reactor, and the flue gas discharged together is discharged together with the moisture removed from the dryer to be in contact with the cooled flue gas.
  • the method may further include supplying the cooler after the heat exchange is cooled.
  • the high quality treatment method of the coal may further include the step of cooling and then discharging the coke supplied to the cooler and supplied to the dryer or the carbonization reactor.
  • the temperature of the tar oil discharged from the carbonization reactor may be 150 to 300 °C.
  • the carbonization reaction temperature of the carbonization reactor may be 500 to 700 °C.
  • the temperature of the flue gas supplied to the carbonization reactor may be 900 to 1200 °C.
  • the coke may be first cooled by the flue gas cooled in the heat exchanger after being discharged from the carbonization reactor, and secondly cooled by the water to perform a second stage cooling step.
  • FIG. 1 is a process diagram showing each step of the high-quality treatment method of coal using a high-quality treatment system of coal according to an embodiment of the present invention.
  • FIG. 1 is a process diagram showing each step of the high-quality treatment method of coal using a high-quality treatment system of coal according to an embodiment of the present invention.
  • the high quality treatment system of coal is:
  • a carbonization reactor (3) connected to the dryer (2) for carbonizing the coal dried in the dryer;
  • a cooler (4, 5) connected to the carbonization reactor (3), for cooling the coke produced from the carbonized coal;
  • a condenser (11) connected to the dryer (2) and condensing moisture mixed with the flue gas received from the dryer (2);
  • the heat exchanger 6 is connected to the condenser 11 and the dryer 2 and cools and condenses the volatile component including the tar oil discharged from the carbonization reactor.
  • the high quality coal processing system may further include connecting means for connecting the condenser 11 and the heat exchanger 6 to supply the flue gas cooled in the condenser 11 to the heat exchanger 6. .
  • the high quality treatment system of coal may further comprise a combustor 10 providing hot flue gas to the dryer 2 and the carbonization reactor 3.
  • the combustor 10 is connected to the coolers 4 and 5, the carbonization reactor 3, and the dryer 2, respectively, and receives a low temperature flue gas from the coolers 4 and 5 to raise the temperature so as to generate a high temperature flue gas. Gas may be provided to the dryer 2 and the carbonization reactor 3.
  • the high quality treatment system of coal may further comprise tar condensation means 7 for condensing and collecting the cooled tar oil.
  • the tar condensation means 7 may be connected to each of the heat exchanger 6 and the coolers 4, 5.
  • the high quality treatment system of coal may further comprise tar collecting means (not shown) for collecting the condensed tar oil 8.
  • the high quality treatment system of coal is a blower 13 provided between the heat exchanger 6 and the coolers 4, 5 for delivering flue gas from the heat exchanger 6 to the coolers 4, 5. It may further include. For example, if the tar condensation means 7 is provided between the heat exchanger 6 and the coolers 4, 5, the blower 13 is the tar condensation means 7 and the cooler 4. , 5).
  • the coal high quality treatment system may further comprise coke collecting means (not shown) for obtaining semi-coke 9 cooled in the cooler.
  • the high quality treatment system of coal is connected to the coolers (4, 5) to store the water to be provided to the coolers (4, 5), or a water storage tank for storing the water discharged from the coolers (4, 5) 12) may be further included.
  • the coolers 4 and 5 may be formed in a two-stage structure as shown in FIG. That is, the coolers 4 and 5 may include a first cooler 4 connected to the carbonization reactor 3 and a second cooler 5 connected to the first cooler 4.
  • the first cooler 4 may be connected to the combustor 10 and the tar condensation means 7, and the second cooler 5 may be connected to the water storage tank 12.
  • the coke produced in the carbonization reactor 3 is quenched in the first cooler 4 to be primarily cooled, and secondly cooled by the coolant by the second cooler 5 secondly. It can be cooled sufficiently.
  • the dryer 2, the carbonization reactor 3 and the coolers 4, 5 may be a retort device consisting of one unit, in particular a vertical retort device. It can be formed as.
  • one device is a drying unit corresponding to the dryer 2, a carbonization reaction unit corresponding to the carbonization reactor 3, and a cooling unit corresponding to the coolers 4 and 5. It may be a separate integrated reboot device.
  • the coal high quality treatment system formed by the vertical retort apparatus is an installation cost-effective, simple apparatus, and minimizes the energy required for driving.
  • the coal high quality treatment system is formed of a retort device to save energy and improve the yield of tar oil obtained by using low grade coal as a raw material.
  • the tar oil generated in the carbonization reactor (3) is discharged from the carbonization reactor (2), mixed with the water removed from the dryer (3) and discharged, and heat exchanged by contacting with the flue gas cooled together when condensing the water. Capturing tar oil; And
  • the above-mentioned high quality treatment method of coal can be divided into three steps, which is a drying step for greatly drying the coal, followed by a carbonization step for carbonizing the dried coal and a cooling step for cooling the carbonized coal such as the obtained coke.
  • the carbonization process and the cooling process proceed sequentially.
  • the high quality treatment method of coal may use a direct heating method in which hot flue gas is directly contacted with coal to dry and carbonize the coal.
  • the hot flue gas may be produced by the combustor 10 and then supplied to the dryer 2 and the carbonization reactor 3.
  • Drying of coal is carried out in the drier 2, carbonization of coal is carried out in the carbonization reactor 3, and cooling of carbonized coal such as coke obtained is carried out in the coolers 4 and 5.
  • the coal When the raw coal 1 is dried by putting the raw coal 1 into the dryer 2, the coal has a low moisture content, and at the same time, the coal is preheated before carbonization for the subsequent carbonization reaction.
  • the raw coal 1 may be a coal containing a water content of about 30 to about 50% by weight.
  • the dried coal may be dried to a moisture content of about 10% by weight or less and supplied to the carbonization reactor 3.
  • the dryer 2 may receive flue gas from the heat exchanger 6 and the combustor 10.
  • the temperature of the flue gas derived from the combustor 10 is relatively higher than the temperature of the flue gas derived from the heat exchanger 6.
  • the dryer 2 is connected to both the heat exchanger 6 and the combustor 10 so that the temperature of the flue gas supplied thereto may be maintained at about 200 ° C to about 300 ° C.
  • the moisture derived from the raw coal 1 in the dryer 2 is introduced into the condenser 11 at the top of the dryer 2 together with the flue gas, and the water is condensed in the condenser 11 to become water. Flue gas discharged from the dryer 2 is cooled in the condenser 11.
  • the water condensed in the condenser 11 may be stored in the water storage tank 12 and then quenched or rehydrated of carbonized coal such as coke obtained by being supplied to the coolers 4 and 5. have.
  • the carbonization reactor 3 is supplied with a hot flue gas and used for a carbonization reaction, and the dried coal supplied from the dryer 2 is carbonized in a carbonization reaction by the hot flue gas to generate tar oil and coke. .
  • the temperature of the carbonization reaction may be performed at about 500 to 700 °C.
  • the tar oil is obtained as a volatile component during the carbonization reaction of coal, and the volatile component is discharged from the upper portion of the carbonization reactor 3 as a mixed gas together with flue gas, and then cooled in a heat exchanger 6 to be cooled into the tar oil (8).
  • the upper temperature of the carbonization reactor 3 is maintained at a temperature above the boiling point of the volatile matter.
  • the volatile matter containing the tar oil in the heat exchanger 6 may be cooled by the flue gas cooled in the condenser 11. That is, the flue gas cooled in the condenser 11 is introduced into the heat exchanger 6 to exchange heat with the volatile component including the tar oil. As a result, the volatile matter containing the tar oil is cooled, and the flue gas cooled in the condenser 11 is heated.
  • the flue gas cooled in the condenser 11 can sufficiently cool the volatile matter provided in the heat exchanger 6, thereby further increasing the yield of tar oil collected in the tar condensation means 7.
  • the flue gas cooled in the condenser 11 may be supplied to the dryer 2 after being heated up by heat exchange with a volatile component including tar oil in the heat exchanger 6.
  • a volatile component including tar oil in the heat exchanger 6 As a result, the flue gas supplied from the heat exchanger 6 to the dryer 2 via the condenser 11 and the heat exchanger 6 may be circulated again through the condenser 11 and the heat exchanger 6. have. That is, the flue gas is discharged from the dryer 2 to the condenser 11, cooled and then supplied to the heat exchanger 6 to be heated up, and re-injected into the dryer 2 from the heat exchanger 6. Can be recycled.
  • the flue gas cooled in the condenser 11 is recycled as a cooling gas in the heat exchanger 6, while at the same time absorbs the thermal energy of the hot volatiles discharged from the carbonization reactor 3 and again dry the coal. And since it is reused for preheating, it is possible to improve energy efficiency.
  • the hot flue gas may be replenished from the combustor 10 in addition to the flue gas circulated as described above.
  • the hot flue gas produced in the combustor 10 may be provided to the dryer 2 and the carbonization reactor 3, where the flue is provided to the dryer 2 and the carbonization reactor 3, respectively.
  • the amount of gas can be adjusted.
  • the amount of flue gas provided to the carbonization reactor 3 may be adjusted to be greater than the amount of flue gas provided to the dryer 2.
  • the tar oil 8 cooled in the heat exchanger 6 may be condensed and collected in the tar condensation means 7 connected to the heat exchanger 6.
  • the temperature of the carbonization reaction performed in the carbonization reactor 3 can be controlled by adjusting the temperature of the flue gas supplied to the carbonization reactor 3.
  • the temperature of the flue gas supplied to the carbonization reactor 3 may be about 800 to about 1200 °C.
  • the temperature of the volatiles including the tar oil discharged from the carbonization reactor 3 may be about 150 to about 300 °C. As described above, since the tar oil in the upper portion of the carbonization reactor 3 may be included in the volatile powder and discharged together with the flue gas, the temperature of the volatile matter including the tar oil discharged from the carbonization reactor 3 may be increased. It may correspond to the temperature of the top of (3).
  • the temperature of the upper portion of the carbonization reactor 3 is adjusted to the above range, it is possible to prevent condensation of the volatiles by maintaining the boiling point or more of the volatiles.
  • the yield of the tar oil 8 obtained by the tar condensation means 7 can be improved by preventing the condensation of volatile matter.
  • the flue gas discharged with the volatiles in the carbonization reactor 3 is removed from the heat exchanger 6 and optionally the tar condensation means 7 with the tar oil 8.
  • the flue gas cooled by heat exchange may be delivered to the coolers 4 and 5 by the blower 13.
  • the dryer 1, the carbonization reactor 2, and the cooler 3 may be formed as a vertical retort device formed integrally with each other. It is formed in a structure in which the temperature decreases as it goes, and in order to obtain a volatile powder containing tar oil at a temperature in the above-described range, in the carbonization reactor (3) containing the tar oil at a height of about 150 to about 300 °C A discharge port for discharging volatile matter may be provided. The temperature of the upper portion of the outlet for discharging volatile matter containing the tar oil is further lowered, the vertical retort device may have a structure in which the dryer 1 is installed above the outlet.
  • the lower end of the carbonization reactor 2 is about 800 ° C. If it has a temperature of about, when the outlet is installed at a height of about 6 to 7m from the lower end of the vertical retort device, a volatile component containing tar oil having a temperature range of 150 to 300 °C to the heat exchanger (6) It can be easily discharged. That is, the one-piece vertical retort is composed of a drying part corresponding to the dryer 1 and a carbonization reaction part corresponding to the carbonization reactor 2, and is about 3 to about 3 from the upper part between the drying part and the carbonization reaction part.
  • volatile matter can be easily discharged to the heat exchanger 6 at about 150 to about 300 °C. Accordingly, the volatile matter can be discharged to the heat exchanger 6 without being condensed by maintaining the temperature above the boiling point, thereby further increasing the yield of tar oil collected by the tar condensation means 7.
  • the coke obtained by carbonizing coal in the carbonization reactor 3 may be supplied to the coolers 4 and 5 and cooled, and then the coke 9 may be collected.
  • the collection of coke 9 may be by coke collecting means (not shown).
  • the water stored in the water storage tank 12 may be transferred to the coolers 4 and 5 to quench or rehydrate the coke supplied to the coolers 4 and 5.
  • the coolers 4 and 5 may be formed in a two-stage structure of the first cooler 4 and the second cooler 5 to perform a two-stage cooling step.
  • the coke delivered from the carbonization reactor 3 in the first cooler 4 is first cooled by the flue gas cooled in the heat exchanger 6 after being discharged from the carbonization reactor 3. Then, after being transferred to the second cooler (5), it can be secondarily cooled by the water supplied to the second cooler.
  • the flue gas recovers heat from the coke and enters the combustor (10), thereby absorbing the thermal energy of the high temperature coke after the carbonization process and reusing the coal for drying and carbonizing. can do.
  • the coke produced at the carbonization reaction temperature of about 500 to about 700 ° C. may be a high temperature of about 400 ° C. or more upon exiting the carbonization reactor 3, and when such high temperature coke comes into contact with oxygen, volatile matter and carbon in the coke may Reaction with oxygen causes an additional reaction, thereby adversely affecting the physical properties of the coke, which may result in a lower coke yield. In order to prevent this, it is necessary to quickly quench the coke obtained by the carbonization reaction to suppress further reactions, and it is advantageous to carry out the above two cooling steps to suppress such additional reactions.
  • the water discharged from the coolers 4 and 5 may be sent to the water storage tank 12, cooled again, and then introduced into the coolers 4 and 5 to be circulated. As such, it is possible to circulate the water so as not to use additional process water, and on the other hand, it does not generate waste water.
  • water condensed with moisture removed from the dryer 2 may be supplied to the coolers 4 and 5 and recycled.
  • the raw material coal 1 of the high quality treatment method of coal may use not only high grade coal such as bituminous coal and sub-bituminous coal but also low grade coal such as lignite.
  • the high quality treatment method of coal is a low temperature carbonization process of coal by a direct heating method for low grade coal, such as lignite, by using a vertical retort device, by collecting the tar oil in high yield and recycling the thermal energy Energy-saving operation is possible.
  • the volatiles are condensed again when the volatiles generated from the flue gas and coal exit the top of the retort.
  • the theoretical yield of tar oil obtained when using bituminous coal is only about 15 to about 20% by weight compared to dry coal, and even when used commercially, the yield of tar oil is only about 4 to about 5% by weight, and is known in the art. Even in low-grade coal such as lignite, it is very difficult to capture tar oil by more than about 5% by weight.
  • the high quality treatment apparatus of the coal and the high quality treatment method of the coal according to the present invention at least about 5% by weight or more for low grade coal such as lignite, and about 10 for high grade coal such as bituminous coal. More than one percent by weight tar oil can be collected.
  • the yield of the tar oil may be improved by sufficiently cooling the tar oil included in the volatile matter discharged from the carbonization reactor by heat exchange with the cooled flue gas discharged from the dryer.
  • the high quality treatment apparatus of the coal and the high quality treatment method of the coal also achieve the effect of energy saving by recycling the flue gas to utilize the energy as described above with reference to Figs.
  • the solid product produced after the carbonization reaction must be cooled to suppress the secondary reaction, water can be used for quenching.
  • water can be used for quenching.
  • the water used for quenching may contain environmental pollutants, which may not be environmentally friendly. There may be a problem that energy utilization is not efficient.
  • the high quality treatment apparatus of the coal and the high quality treatment method of the coal as described above with reference to Figure 1 and described above by recycling the water, transfer the heat energy from the hot coke to the flue gas to recycle the energy efficiently by utilizing energy efficiently Get the effect.
  • lignite was used as raw coal to obtain tar oil and coke.
  • An outlet for discharging volatile matter containing tar oil at the top of the carbonization reactor 3 was installed, but was installed at a lower position than the outlet of Example 1, and the temperature of the volatile discharged from the outlet was about 150 ° C.
  • the components of the resultant obtained in the tar condensation means 7 were analyzed and described in Table 1 below.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Coke Industry (AREA)

Abstract

La présente invention concerne un système de traitement de haute qualité du charbon comportant : un séchoir pour alimenter un gaz de combustion, dont la température a été élevée, et séchant ainsi le charbon ; un réacteur de carbonisation pour carboniser le charbon, qui a été séché par le séchoir, dans une réaction de carbonisation ; un appareil de refroidissement pour refroidir les cokes, qui ont été générés à partir du charbon ayant subi une réaction de carbonisation ; un condenseur pour condenser l'humidité mêlée au gaz de combustion alimenté depuis le séchoir ; et un échangeur de chaleur pour refroidir une fraction volatile contenant une huile de goudron déchargée depuis le réacteur de carbonisation à l'aide du gaz de combustion refroidi par le condenseur. Le système de traitement de haute qualité du charbon permet d'obtenir une huile de goudron de manière économique et très efficace au moyen d'un procédé de carbonisation à basse température concernant un charbon de basse qualité.
PCT/KR2014/012478 2013-12-18 2014-12-17 Système de traitement de haute qualité du charbon et procédé de traitement de haute qualité du charbon Ceased WO2015093845A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
KR1020130158039A KR101549312B1 (ko) 2013-12-18 2013-12-18 석탄의 고품위 처리 시스템 및 석탄의 고품위 처리 방법
KR10-2013-0158039 2013-12-18

Publications (1)

Publication Number Publication Date
WO2015093845A1 true WO2015093845A1 (fr) 2015-06-25

Family

ID=53403106

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/KR2014/012478 Ceased WO2015093845A1 (fr) 2013-12-18 2014-12-17 Système de traitement de haute qualité du charbon et procédé de traitement de haute qualité du charbon

Country Status (2)

Country Link
KR (1) KR101549312B1 (fr)
WO (1) WO2015093845A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108641753A (zh) * 2018-04-08 2018-10-12 王树宽 立式炉低阶煤热解制取煤焦油煤气的系统及方法
CN108977216A (zh) * 2018-09-20 2018-12-11 浙江布莱蒙农业科技股份有限公司 一种炭化炉余热再利用结构及控制方法
CN114907870A (zh) * 2022-05-16 2022-08-16 延安大学 一种粘结性洗中煤的提质方法及热解反应器

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR102489352B1 (ko) * 2022-06-09 2023-01-18 손영호 친환경 무연탄의 제조방법 및 이에 의해 제조된 친환경 무연탄

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR810001673B1 (ko) * 1978-08-25 1981-10-27 요한스 벌프마이어 하트무스지. 태그랭 연도 가스를 이용한 코오크스 제조용 석탄의 건조 및 예열방법
KR20010067082A (ko) * 1999-08-18 2001-07-12 아사무라 타카싯 석탄의 건조방법 및 건조장치
WO2010090230A1 (fr) * 2009-02-03 2010-08-12 新日本石油株式会社 Procédé de valorisation pour charbon de qualité inférieure et procédé pour la production de coke
KR20120056091A (ko) * 2010-11-24 2012-06-01 에스케이이노베이션 주식회사 탄소연료의 가스화 복합설비

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100698764B1 (ko) 2005-10-17 2007-03-26 세계화학공업(주) 휘발성 유기화합물의 흡착 응축식 회수 방법 및 회수 장치
JP5461100B2 (ja) 2009-02-27 2014-04-02 三菱重工業株式会社 低品位炭を燃料とする火力発電プラント

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR810001673B1 (ko) * 1978-08-25 1981-10-27 요한스 벌프마이어 하트무스지. 태그랭 연도 가스를 이용한 코오크스 제조용 석탄의 건조 및 예열방법
KR20010067082A (ko) * 1999-08-18 2001-07-12 아사무라 타카싯 석탄의 건조방법 및 건조장치
WO2010090230A1 (fr) * 2009-02-03 2010-08-12 新日本石油株式会社 Procédé de valorisation pour charbon de qualité inférieure et procédé pour la production de coke
KR20120056091A (ko) * 2010-11-24 2012-06-01 에스케이이노베이션 주식회사 탄소연료의 가스화 복합설비

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108641753A (zh) * 2018-04-08 2018-10-12 王树宽 立式炉低阶煤热解制取煤焦油煤气的系统及方法
CN108641753B (zh) * 2018-04-08 2020-09-11 王树宽 立式炉低阶煤热解制取煤焦油煤气的系统及方法
CN108977216A (zh) * 2018-09-20 2018-12-11 浙江布莱蒙农业科技股份有限公司 一种炭化炉余热再利用结构及控制方法
CN108977216B (zh) * 2018-09-20 2024-05-03 浙江钱江伟岸干燥设备有限公司 一种炭化炉余热再利用结构及控制方法
CN114907870A (zh) * 2022-05-16 2022-08-16 延安大学 一种粘结性洗中煤的提质方法及热解反应器

Also Published As

Publication number Publication date
KR101549312B1 (ko) 2015-09-01
KR20150071246A (ko) 2015-06-26

Similar Documents

Publication Publication Date Title
WO2015093845A1 (fr) Système de traitement de haute qualité du charbon et procédé de traitement de haute qualité du charbon
WO2015122688A1 (fr) Système de production de biocharbon, et procédé de production de biocharbon
WO2012144700A1 (fr) Système de fabrication et procédé de fabrication d'une biomasse solide
WO2013094879A1 (fr) Appareil de pyrolyse utilisant du métal fondu
WO2017078225A1 (fr) Appareil de récupération de bio-huile faisant appel à un vent de plasma
US4308102A (en) Process and apparatus for drying and preheating coking coal by means of flue gas
WO2017099495A1 (fr) Procédé de production de bio-huile à l'aide d'un procédé de torréfaction et de pyrolyse rapide
US4284476A (en) Process and apparatus for utilization of the sensible heat of hot coke for drying and preheating coking coal
WO2010137858A2 (fr) Dispositif et système de préparation d'huile biologique et procédé de préparation d'huile biologique qu'ils permettent de mettre en oeuvre
CA1135211A (fr) Methode et installation de cokefaction
CN103409152A (zh) 高热值气体热载体低阶煤提质工艺及系统
WO2012086961A2 (fr) Procédé pour fabriquer des briquettes de charbon partiellement carbonisées, appareil pour fabriquer des briquettes de charbon partiellement carbonisées, et appareil pour fabriquer du fer fondu
WO2024034745A1 (fr) Système et procédé de transformation de déchet organique en combustible solide par carbonisation hydrothermale et production d'énergie
WO2022255640A1 (fr) Système de conversion d'énergie utilisant le bioséchage et la torréfaction
CA1245595A (fr) Refroidissement a sec du coke par intervention de la chaleur latente derivee dudit refroidissement
US8821695B2 (en) Coal reforming system
WO2023176999A1 (fr) Système de traitement à la vapeur d'eau pour le réchauffage de combustible solide
WO2024128715A1 (fr) Système de production de biocharbon à économie d'énergie utilisant une matière organique
WO2012138191A2 (fr) Appareil et procédé de traitement d'un gaz de four à coke
JP4074521B2 (ja) Ｃｄｑにおけるバイオマス処理時の可燃ガス回収方法
WO2023277565A1 (fr) Dispositif et procédé de pyrolyse en continu à basse température
JPH11310782A (ja) 汚泥の炭化方法
WO2013094864A1 (fr) Appareil de fabrication de fer fondu et procédé de fabrication de fer fondu
CN203451475U (zh) 高热值气体热载体低阶煤提质系统
CN201756532U (zh) 用于褐煤或高挥发分煤干馏的系统

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 14871781

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 14871781

Country of ref document: EP

Kind code of ref document: A1