WO2013125609A1

WO2013125609A1 - Reformed coal production equipment, and method for controlling same

Info

Publication number: WO2013125609A1
Application number: PCT/JP2013/054252
Authority: WO
Inventors: 慶一中川; 大本　節男; 佐藤　文昭; 佐藤　淳
Original assignee: 三菱重工業株式会社
Priority date: 2012-02-24
Filing date: 2013-02-21
Publication date: 2013-08-29
Also published as: AU2013223201A1; US20140373435A1; AU2013223201B2; DE112013001121T5; JP2013173833A; CN104066824B; IN2014DN05895A; CN104066824A; AU2013223201B9; JP5804972B2

Abstract

The purpose of the present invention is to provide reformed coal production equipment whereby it is possible to efficiently remove tar without lowering the production amount of reformed coal even when the equipment is stopped. Reformed coal production equipment provided with: a combustion furnace (124) for generating heated gas; a dry distillation gas supply pipe (101) for supplying dry distillation gas (14) that was generated at the inner cylinder (122) of a dry distillation device (121) to the combustion furnace; a vapor generator (125) to which a portion of the heated gas (11) generated at the combustion furnace is supplied and which generates waste heat gas (13) by subjecting the heated gas to heat exchange; and a discharge pipe (52), a waste heat gas delivery pipe (53), a mixed gas delivery pipe (55), a blower (126), a mixed gas supply pipe (56), a mixed gas branching pipe (102), a flow rate adjustment valve (103), and a mixed gas allocation pipe (105) which supply and allocate, to the aforementioned inner cylinder, the waste heat gas and low-temperature heated gas (12) generated by indirectly heating dried coal (2) by means of the heated gas within the outer cylinder (123) of the dry distillation device.

Description

Modified coal production facility and control method thereof

The present invention relates to a modified coal production facility and a control method thereof, and is particularly useful when applied to reforming a low-grade coal (poor coal) having a high moisture content such as lignite and subbituminous coal. Is.

Low-grade coal (poor coal) with a high moisture content such as lignite and sub-bituminous coal has a low calorific value per unit weight, so the heat value per unit weight can be reduced by heat treatment and drying. To increase.

Examples of the modified coal production equipment for reforming such low-grade coal include, for example, an indirect heating type dry distillation apparatus that indirectly heats low-grade coal with a heating gas and dry distillation generated in the dry distillation apparatus. There is a facility provided with a combustion furnace that supplies gas through a dry distillation gas supply pipe and burns the dry distillation gas or the like to generate the heated gas.

The above-mentioned dry distillation gas is composed of a low boiling point component, but is accompanied by a high boiling point component tar (dry distillation oil) in order to treat the low-grade coal at a relatively high temperature. When the dry distillation gas is cooled, the tar adheres to the wall surface of a duct or the like through which the dry distillation gas flows. As the amount of tar attached increases, problems such as blocking the duct may occur, and various techniques for removing the tar have been developed.

For example, in Patent Document 1 below, air is diluted with water vapor or an inert gas to adjust the oxygen concentration to 3% to 21% by volume, and the gas is adjusted to a temperature of 350 ° C. to 500 ° C. A decoking method for burning and removing the coke is disclosed.

In Patent Document 2 described below, by supplying an oxygen-containing gas into the inner cylinder of the external heat kiln, organic carbides and combustible gas in the processed product generated by thermal decomposition are combusted, whereby heat is generated. There has been disclosed a method for thermally decomposing a processed product using an external heat kiln in which the temperature of the cracked gas is increased to prevent liquefaction or solidification thereof.

Japanese Patent Laid-Open No. 5-188653 (see paragraphs [0013], [0017], etc.) JP 2004-3738 A (see, for example, paragraphs [0011], [0014], [0015], etc.)

However, the decoking method described in Patent Document 1 described above is applied to the above-described reformed coal production facility, and the oxygen concentration-adjusted gas whose oxygen concentration is adjusted is directly supplied to the dry distillation apparatus, so that tar generated at the time of stopping Although it is possible to suppress the tar from adhering to the carbonization apparatus, if an attempt is made to produce the oxygen concentration adjusting gas from air or an inert gas (nitrogen or water vapor), an apparatus for that purpose is required. Due to this device, the production cost of the reformed coal increases. Moreover, in order to make it react with the tar, the oxygen concentration adjusting gas must be heated in advance, and additional energy is required. That is, tar could not be removed efficiently.

In the thermal decomposition method of the processed material by the external heat kiln described in Patent Document 2, the organic carbide of the processed material generated by the thermal decomposition is burned, and therefore this method is applied to the modified coal production facility. Then, also when stopping the said equipment, coal must be supplied to a carbonization apparatus, this coal itself must be burned, and the production amount of reformed coal will fall.

From the above, the present invention has been made to solve the above-mentioned problems, and even when the facility is stopped, tar is efficiently removed without reducing the production amount of the modified coal. An object of the present invention is to provide a modified coal production facility and a control method thereof.

The reformed coal production facility according to the first invention for solving the above-mentioned problems includes a drying means for drying coal, a dry distillation means for carbonizing the dried coal, and a cooling means for cooling the dry coal. And the dry distillation means is an indirect heating type dry distillation apparatus comprising an inner cylinder to which the dried coal is transferred and an outer cylinder to which a heating gas for heating the inner cylinder is supplied. A heating gas generation means for generating the heating gas; a dry distillation gas supply means for supplying a dry distillation gas generated in the inner cylinder to the heating gas generation means; and the heating generated by the heating gas generation means. Waste gas generation means for generating a waste heat gas by exchanging heat of the heated gas when a part of the gas is supplied, the waste heat gas, and the heating gas indirectly heating the coal in the outer cylinder The low temperature heating gas Characterized in that the inner cylinder and a distributor for supplying mixed gas distribution means.

A modified coal production facility according to a second invention that solves the above-described problem is the modified coal production facility according to the first invention described above, wherein the mixed gas distribution and supply means supplies the dried coal. It is connected to the receiving side of the inner cylinder to be received.

The modified coal production facility according to the third invention for solving the above-described problem is the modified coal production facility according to the second invention described above, wherein the indirect heating type carbonization device is configured to use the coal that has been carbonized. Gas temperature measuring means is provided on the discharge outlet side for measuring the gas temperature, and the mixed gas distribution supply means adjusts the flow rates of the low-temperature heating gas and the waste heat gas supplied into the inner cylinder. A gas flow rate adjusting means and a control means for controlling the gas flow rate adjusting means based on the gas temperature measured by the gas temperature measuring means are provided.

A modified coal production facility according to a fourth invention for solving the above-described problem is the modified coal production facility according to the third invention described above, wherein the drying means, the indirectly heated carbonization apparatus, and the cooling means. A plurality of equipment main bodies having the above are provided in parallel.

A control method for a modified coal production facility according to a fifth aspect of the present invention that solves the above-described problem is a method for controlling the modified coal production facility according to the third aspect of the invention, wherein the coal to the inner cylinder is controlled. The control means controls the gas flow rate adjusting means to supply the low temperature heating gas and the waste heat gas to the inner cylinder, while increasing the amount of fuel supplied to the heating gas generation means, When the gas temperature measured by the gas temperature measuring means becomes lower than a predetermined temperature, the control means controls the gas flow rate adjusting means to stop the supply of the low temperature heating gas and the waste heat gas to the inner cylinder. It is characterized by doing.

A method for controlling a reformed coal production facility according to a sixth aspect of the present invention that solves the above-described problem is a method of controlling the reformed coal production facility according to the fourth aspect of the invention, wherein the facility main body that is to be stopped is used. In addition, while stopping the supply of the coal to the inner cylinder, while increasing the amount of the coal supplied to the drying means in the equipment main body that is in steady operation, the heating gas supplied to the outer cylinder is increased, In the equipment main body to be stopped, the control means controls the gas flow rate adjusting means to start supplying the low-temperature heating gas and the waste heat gas to the inner cylinder, and in the equipment main body to be stopped, When all of the coal is discharged from the inner cylinder, the supply of the heated gas to the inner cylinder is stopped, while the heating gas supplied to the outer cylinder is set to a steady state in the equipment main body that is in steady operation. In the equipment body to stop When all of the dry distillation gas is discharged from the inner cylinder, the control means controls the gas flow rate adjusting means to stop the supply of the low-temperature heating gas and the waste heat gas to the inner cylinder. And

According to the present invention, when the equipment is stopped, the heated gas can be supplied to the indirectly heated dry distillation means until the coal (dry distilled coal) is discharged from the indirectly heated dry distillation means, It is possible to prevent new tar from being generated. Since the low temperature heating gas and the waste heat gas are supplied to the indirect heating type dry distillation means, the dry distillation gas in the indirect heating type dry distillation means and the dry distillation gas supply means can be purged. Therefore, it is possible to prevent tar from adhering to the wall surfaces in the indirectly heated dry distillation means and the dry distillation gas supply means. In addition, since the oxygen concentration of the low-temperature heating gas and waste heat gas is about 2 to 3%, even if tar adheres to the wall surface in the indirectly heated dry distillation means and the dry distillation gas supply means, the tar is burned and removed. can do. Therefore, even when the facility is stopped, tar can be efficiently removed without reducing the production amount of the modified coal. Tar removal work by indirect heating type dry distillation means and dry distillation gas supply means becomes unnecessary, and maintenance and inspection work can be performed efficiently.

1 is an overall schematic configuration diagram of a modified coal production facility according to a first embodiment of the present invention. It is a control flow figure of the reformed coal manufacturing equipment concerning the 1st example of the present invention. It is a whole schematic block diagram of the reformed coal manufacturing equipment concerning the 2nd example of the present invention. It is a control flow figure of the reformed coal manufacturing equipment concerning the 2nd example of the present invention.

Embodiments of the modified coal production facility and the control method thereof according to the present invention will be described in each example.

The modified coal production facility according to the first embodiment of the present invention will be described with reference to FIGS.

In the modified coal production facility 100 according to the present embodiment, as shown in FIG. 1, first, low-grade coal 1 such as lignite and bituminous coal is drying means for drying the low-grade coal 1 with a hopper or the like not shown. It is supplied to the drying device 111. The delivery port of the drying device 111 communicates with a receiving port 122a of the carbonization device 121 for carbonizing the dry coal 2. The outlet 122 b of the carbonization device 121 communicates with an inlet of a cooling device 131 that is a cooling means for cooling the carbonized coal 3.

The dry distillation apparatus 121 includes an inner cylinder 122 and an outer cylinder 123 that covers the inner cylinder 122. The heating gas 11 described later is supplied to the outer cylinder 123. Thereby, the dry coal 2 supplied in the inner cylinder 122 is indirectly heated and dry-distilled, and the dry-distilled coal 3 is produced | generated. That is, the dry distillation apparatus 121 is an indirect heating type apparatus in which the high-temperature gas (heating gas) serving as a heat source and the low-grade coal 1 are not in direct contact, for example, an external heating kiln or the like, and constitutes an indirect heating type dry distillation means. .

The gas discharge port of the inner cylinder 122 of the carbonization apparatus 121 communicates with the gas inlet of the combustion furnace 124 via the carbonization gas supply pipe 101. Thereby, the dry distillation gas 14 containing the gaseous tar (dry distillation oil) produced | generated by dry distillation is supplied to the gas inlet of the combustion furnace 124. FIG. A fuel (not shown) such as natural gas is also supplied to the gas receiving port of the combustion furnace 124. In the combustion furnace 124, fuel such as the dry distillation gas 14 and natural gas burns to generate the heated gas 11. That is, the combustion furnace 124 serves as a heated gas generation unit. The gas discharge port of the combustion furnace 124 communicates with the gas inlet of the outer cylinder 123 of the dry distillation apparatus 121 via the heated gas supply pipe 51.

The heated gas supply pipe 51 communicates with the gas inlet of the steam generator 125 via the heated gas branch pipe 53. The steam generator 125 constitutes a waste heat gas generating means for generating the waste heat gas 13 by generating steam by the heat gas 11 exchanging heat with water. The gas discharge port of the steam generator 125 communicates with an exhaust pipe 52 described later via a waste heat gas supply pipe 54.

The gas discharge port of the outer cylinder 123 of the dry distillation apparatus 121 is an exhaust gas purification means for purifying the low temperature heating gas 12 generated by heating the inner cylinder 122 and the waste heat gas 13 through the exhaust pipe 52. It communicates with the gas inlet of a certain exhaust gas treatment device 127. The low-temperature heating gas 12 and the waste heat gas 13 are purified by the exhaust gas treatment device 127 and discharged outside the system.

The exhaust pipe 52 communicates with the gas receiving port of the blower 126 via the mixed gas supply pipe 55. The gas outlet of the blower 126 communicates with the gas inlet of the combustion furnace 124 through the mixed gas supply pipe 56. The mixed gas supply pipe 56 communicates with the mixed gas branch pipe 102. The mixed gas branch pipe 102 communicates with the mixed gas communication pipe 104 via a flow rate adjusting valve (three-way valve) 103 and also communicates with the mixed gas distribution pipe 105 via the flow rate adjusting valve 103. The mixed gas communication pipe 104 communicates with the dry distillation gas supply pipe 101. The mixed gas distribution pipe 105 communicates with the gas inlet on the inlet 122 a side of the inner cylinder 122 of the dry distillation apparatus 121.

The dry distillation gas supply pipe 101 is provided with a gas temperature measuring device 106 which is a gas temperature measuring means for measuring the gas temperature in the pipe. The gas temperature measuring device 106 is connected to the control device 109 so that the measured gas temperature can be transmitted to the control device 109. The dry distillation gas supply pipe 101 is provided with differential

pressure measuring devices

107a and 107b for measuring a pressure difference in the pipe. The differential

pressure measuring devices

107 a and 107 b are connected to the control device 109 so that the measured pressure difference in the pipe can be transmitted to the control device 109.

At the outlet 122b of the inner cylinder 122 of the dry distillation apparatus 121, an inner cylinder gas temperature measuring device 108 which is a gas temperature measuring means for measuring the gas temperature in the inner cylinder 122 is provided. The inner cylinder gas temperature measuring device 108 is connected to the control device 109 so that the measured gas temperature in the inner cylinder can be transmitted to the control device 109.

The exhaust pipe 52, the waste heat gas supply pipe 54, the mixed gas supply pipe 55, the blower 126, the mixed gas supply pipe 56, the mixed gas branch pipe 102, the flow rate adjusting valve 103, the mixed gas distribution pipe 105, etc. are mixed and supplied with the mixed gas. It has a means. The flow rate adjusting valve 103 constitutes a gas flow rate adjusting means for adjusting the supply amounts of the low-temperature heating gas 12 and the waste heat gas 13 to the dry distillation apparatus 121.

The control device 109 controls the flow rate adjusting valve 103, the amount of fuel supplied to the combustion furnace 124, the amount of low-grade coal 1 supplied to the drying device 111, and the heating gas 11 supplied to the dry distillation device 121 based on the measurement values obtained by various measuring instruments. The supply amount is controlled. That is, the control device 109 serves as a control means for adjusting the valve opening degree of the flow rate adjusting valve 103 based on the measurement values obtained by various measuring instruments.

In the modified coal production facility 100 according to the present embodiment configured as described above, when the low-grade coal 1 is charged into the hopper, the hopper quantifies the low-grade coal 1 at room temperature into the drying device 111. Supply one by one. The low-grade coal 1 supplied to the drying device 111 is heated to about 200 ° C. by drying combustion gas (about 150 to 300 ° C.) from a drying combustor (not shown) to remove moisture. The charcoal 2 is transferred into the inner cylinder 122 of the dry distillation apparatus 121. The dry coal 2 transferred to the carbonization device 121 is indirectly heated and dry-distilled with the heated gas 11 (gas temperature: about 1050 ° C., oxygen concentration: about 2-3%) from the combustion furnace 124, Components such as the dry distillation gas 14 containing gaseous tar are removed to form the dry distillation coal 3 and fed to the cooling device 131. The dry-distilled coal 3 fed to the cooling device 131 becomes the reformed coal 4 by being cooled to about 50 ° C.

On the other hand, the heated gas 11 (gas temperature: about 1050 ° C., oxygen concentration: about 2-3%) generated in the combustion furnace 124 is fed to the outer cylinder 123 of the dry distillation apparatus 121 through the heated gas feed pipe 51. The The heating gas 11 used for heating the inner cylinder 122 in the outer cylinder 123 becomes a low-temperature heating gas 12 (gas temperature: about 350 ° C., oxygen concentration: about 2-3%). The low-temperature heating gas 12 is supplied to the exhaust pipe 52. The heated gas 11 is fed to the steam generator 125 via the heated gas feed pipe 51 and the heated gas branch pipe 53. The heated gas 11 used to generate water vapor by the steam generator 125 becomes the waste heat gas 13 (gas temperature: about 350 ° C., oxygen concentration: about 2-3%). The waste heat gas 13 is supplied to the exhaust pipe 52 through the waste heat gas supply pipe 54.

A part of the low temperature heating gas 12 and the waste heat gas 13 is supplied to the exhaust gas treatment device 127. The low temperature heating gas 12 and the waste heat gas 13 are purified by the exhaust gas treatment device 127 and discharged out of the system. The remainder of the low-temperature heating gas 12 and the waste heat gas 13 (gas temperature: about 350 ° C., oxygen concentration: about 2-3%) is fed to the blower 126 via the mixed gas feed pipe 55.

A part of the low-temperature heating gas 12 and the waste heat gas 13 fed to the blower 126 is supplied to the combustion furnace 124 through the mixed gas supply pipe 56. Further, the remaining part of the low-temperature heating gas 12 and the waste heat gas 13 (gas temperature: about 350 ° C., oxygen concentration: about 2-3%) fed to the blower 126 is supplied to the mixed gas branch pipe 102. The remainder of the low-temperature heating gas 12 and the waste heat gas 13 (gas temperature: about 350 ° C., oxygen concentration: about 2-3%) supplied to the mixed gas branch pipe 102 passes through the flow rate adjusting valve 103 and the mixed gas communication pipe 104. Is supplied to the dry distillation gas supply pipe 101, or is supplied to the inlet 122 a side of the inner cylinder 122 of the dry distillation apparatus 121 through the flow rate adjusting valve 103 and the mixed gas distribution pipe 105.

The valve opening degree of the flow rate adjusting valve 103 is controlled by the control device 109 based on the gas temperature measured by the gas temperature measuring device 106. For example, when the gas temperature measured by the gas temperature measuring device 106 is 400 ° C. or higher, the control device 109 opens the flow rate adjusting valve 103 and adjusts the opening so that the gas temperature becomes higher than 550 ° C. The flow rate adjustment valve 103 is adjusted to be throttled. As a result, a mixed gas in which the low-temperature heating gas 12 and the waste heat gas 13 (oxygen concentration: about 2 to 3%) and the dry distillation gas 14 (gas temperature: about 400 ° C., oxygen concentration: 0%) are mixed and mixed. The oxygen concentration in the gas is adjusted to about 1 to 2%. As a result, gaseous tar (dry distillation oil) is oxidatively decomposed (decoked) to lighten the tar, and adhesion of the tar to the dry distillation gas supply pipe 101 can be prevented. Further, since the tar is lightened to become a light gas, the light gas is burned, so that a decrease in gas temperature is prevented. Thereby, adhesion of the tar to the dry distillation gas supply pipe 101 can be prevented. That is, by adjusting the supply amounts of the low-temperature heating gas 12 and the waste heat gas 13 to the dry distillation gas supply pipe 101 based on the gas temperature in the dry distillation gas supply pipe 101, tar is formed on the wall surface in the dry distillation gas supply pipe 101. Decoking is performed at the timing of adhesion, and tar can be efficiently removed.

Moreover, the operation | movement when stopping the modified coal manufacturing equipment 100 which concerns on a present Example comprised as mentioned above is demonstrated below with reference to FIG.
As shown in FIG. 2, first, the reformed coal production facility 100 is in steady operation (step SA1). In order to stop the modified coal production facility 100, the transfer of the dry coal 2 to the inner cylinder 122 of the dry distillation apparatus 121 is stopped (step SA2).

Subsequently, the process proceeds to step SA3 and to step SA11. In step SA11, there is no new transfer of the dry charcoal 2 to the inner cylinder 122 of the dry distillation apparatus 121, so the amount of dry distillation gas 14 generated is reduced. As the generation amount of the dry distillation gas 14 decreases, the supply amount of the dry distillation gas 14 to the combustion furnace 124 decreases. However, the supply amount of fuel such as natural gas to the combustion furnace 124 is increased and combustion is performed. By raising the amount of additional cooking in the furnace 124, the gas temperature and the generation amount of the heated gas 11 are suppressed. That is, the amount of additional cooking to the combustion furnace is increased (step SA12). Subsequently, all the carbonized coal 3 is discharged from the carbonization apparatus 121 (step SA13). That is, the generation of the dry distillation gas 14 is stopped in the dry distillation apparatus 121.

On the other hand, in step SA3, the control device 109 adjusts the flow rate adjustment valve 103, and the low temperature heating gas 12 and waste heat gas to the inlet 122a side of the inner cylinder 122 of the dry distillation apparatus 121 via the mixed gas distribution pipe 105. 13 supply is started. That is, the low-temperature heating gas 12 and the waste heat gas 13 are forcibly sent from the receiving port 122a side of the inner cylinder 122 of the dry distillation apparatus 121 into the inside thereof. Thereby, the dry distillation gas 14 in the inner cylinder 122 of the dry distillation apparatus 121 and the dry distillation gas supply pipe 101 is purged.

Subsequently, all of the carbonized coal 3 is discharged from the inner cylinder 122 of the carbonization device 121, and generation of the carbonized gas 14 due to indirect heating of the carbonized coal 2 is eliminated, and supply of the carbonized gas 14 to the combustion furnace 124 is performed. Disappears. Therefore, the amount of additional cooking in the combustion furnace 124 is reduced (step SA4). Along with this, the gas temperature and the generation amount of the heated gas 11 generated in the combustion furnace 124 are reduced (step SA5).

Subsequently, since the heating gas 11 whose amount is smaller than that in the steady operation and whose temperature has decreased is supplied to the outer cylinder 123 of the dry distillation apparatus 121, the temperature of the dry distillation apparatus 121 decreases (step SA6). Along with this, the temperature of the low-temperature heating gas 12 itself also decreases, and the temperature of the waste heat gas 13 also decreases (step SA7).

Subsequently, the process proceeds to step SA8, where the control device 109 makes a determination based on the inner cylinder gas temperature measured by the inner cylinder gas temperature measuring instrument 108. If the gas temperature in the vicinity of the outlet 122b of the inner cylinder 122 of the dry distillation apparatus 121 is higher than 300 ° C., the process returns to step SA4. On the other hand, when the temperature in the vicinity of the discharge port 122b of the inner cylinder 122 of the dry distillation apparatus 121 is 300 ° C. or less, the process proceeds to step SA9, and in this step SA9, the control device 109 controls the flow rate adjusting valve 103 and The adjustment valve 103 is closed. That is, the supply of the low-temperature heating gas 12 and the waste heat gas 13 to the inner cylinder 122 of the dry distillation apparatus 121 is stopped.

Therefore, according to the modified coal production facility 100 according to the present embodiment, when the facility is stopped, the low temperature heating gas 12 and the waste heat gas 13 are supplied to the inlet 122a side of the inner cylinder 122 of the dry distillation apparatus 121. Thus, the dry distillation gas 14 in the inner cylinder 122 of the dry distillation apparatus 121 and the dry distillation gas supply pipe 101 is forcibly discharged. Further, the dry distillation gas 14 is burned in the combustion furnace 124.

Furthermore, since the oxygen concentration of the low-temperature heating gas 12 and the waste heat gas 13 is about 2-3%, tar can be lightened by oxidative decomposition. The lightened gas flows into the combustion furnace 124 and burns in the combustion furnace 124. Moreover, even if tar adheres to the wall surface in the inner cylinder 122 of the carbonization apparatus 121 or the carbonization gas supply pipe 101, the tar can be removed by combustion.

Therefore, even when the facility is stopped, tar can be efficiently removed without reducing the production amount of the reformed coal 4. Further, since tar can be prevented from adhering to the inner cylinder 122 of the carbonization apparatus 121 or the wall surface of the carbonization gas supply pipe 101, maintenance / inspection work can be performed efficiently.

A modified coal production facility according to a second embodiment of the present invention will be described with reference to FIGS. 3, 4A, and 4B.

As shown in FIG. 3, the modified coal production facility according to the present embodiment includes three modified coal

production facility bodies

100A, 100B, and 100C arranged in parallel. The reformed coal production equipment

main bodies

100A, 100B, and 100C include a drying device 111, a carbonization device 121, and a cooling device 131, respectively, as in the modified coal production facility 100 according to the first embodiment described above.

The reformed coal production facility according to this embodiment includes one combustion furnace 124, one blower 126, and one exhaust gas treatment device 127, similar to the modified coal production facility 100 according to the first embodiment described above. Prepare. The gas outlet of the blower 126 communicates with the gas inlet of the combustion furnace 124 through the mixed gas supply pipe 56. The gas discharge port of the combustion furnace 124 communicates with the outer cylinder 123 of the dry distillation apparatus 121 of each of the equipment

main bodies

100A, 100B, and 100C via the heated gas supply pipes 51a to 51c.

The heated gas feed pipes 51a to 51c communicate with the gas inlets of the respective steam generators 125 via the heated gas branch pipes 53a to 53c. The gas discharge ports of the respective steam generators 125 communicate with the waste heat gas supply pipes 54a to 54c, respectively.

The gas discharge port of the outer cylinder 123 of each carbonization apparatus 121 communicates with the exhaust pipes 52a to 52c. A part of the low-temperature heating gas 12 and the waste heat gas 13 generated by the heating gas 11 heating the inner cylinder 122 passes through the exhaust pipes 52a to 52c and the waste heat gas supply pipes 54a to 54c. The waste heat gas 13 is supplied to an exhaust gas treatment device 127 which is an exhaust gas purification means for purifying the waste heat gas 13, and is purified by the exhaust gas treatment device 127 and discharged outside the system. The remainder of the low-temperature heating gas 12 and the waste heat gas 13 are supplied to the blower 126 through the exhaust pipes 52a to 52c, the waste heat gas supply pipes 54a to 54c, and the mixed gas supply pipe 55.

The gas discharge port of the inner cylinder 122 of each carbonization device 121 communicates with the gas reception port of the combustion furnace 124 via the carbonization gas supply pipes 101a to 101c.

The mixed gas supply pipe 56 communicates with the mixed gas branch pipes 102a to 102c. The mixed gas branch pipes 102a to 102c communicate with the mixed gas communication pipes 104a to 104c via the flow rate adjusting valves (three-way valves) 103a to 103c, respectively, and the mixed gas distribution pipes 105a to 105c via the flow rate adjusting valves 103a to 103c. 105c is contacted respectively. The mixed gas communication pipes 104a to 104c communicate with the dry distillation gas supply pipes 101a to 101c, respectively. The mixed gas distribution pipes 105a to 105c are in communication with the gas inlets on the inlet 122a side of the inner cylinder 122 of each dry distillation apparatus 121, respectively.

The dry distillation gas supply pipe 101a is provided with a gas temperature measuring device 106 which is a gas temperature measuring means for measuring the gas temperature in the pipe. The gas temperature measuring device 106 is connected to the control device 109 so that the measured gas temperature can be transmitted to the control device 109. Similarly to the dry distillation gas supply pipe 101a, gas temperature measuring instruments (not shown) are also provided in the dry distillation

gas supply pipes

101b and 101c. These gas temperature measuring devices are also connected to the control device 109 so that the gas temperature measured by the gas temperature measuring device can be transmitted to the control device 109.

The dry distillation gas supply pipe 101a is provided with differential

pressure measuring devices

107a and 107b for measuring the pressure difference in the pipe. The differential

pressure measuring devices

107 a and 107 b are connected to the control device 109 so that the measured pressure difference in the pipe can be transmitted to the control device 109. Similarly to the dry distillation gas supply pipe 101a, a differential pressure measuring instrument (not shown) is provided in each of the dry distillation

gas supply pipes

101b and 101c. These differential pressure measuring devices are also connected to the control device 109 so that the pressure difference in the pipe measured by the differential pressure measuring device can be transmitted to the control device 109.

The inner cylinder internal gas temperature measuring device 108 which measures the gas temperature in the inner cylinder 122 is provided in the delivery port 122b of the inner cylinder 122 of the carbonization apparatus 121 of the equipment main body 100A. The inner cylinder gas temperature measuring device 108 is connected to the control device 109 so that the measured gas temperature in the inner cylinder can be transmitted to the control device 109. Similarly to the equipment main body 100A, an inner cylinder internal gas temperature measuring device (not shown) that measures the gas temperature in the inner cylinder 122 is also provided at the outlet 122b of the inner cylinder 122 of the dry distillation apparatus 121 of the equipment

main bodies

100B and 100C. Each is provided. These in-cylinder gas temperature measuring devices are also connected to the control device 109 so that the measured gas temperature in the inner cylinder can be transmitted to the control device 109.

Exhaust pipes 52a to 52c, waste heat gas supply pipes 54a to 54c, mixed gas supply pipe 55, blower 126, mixed gas supply pipe 56, mixed gas branch pipes 102a to 102c, flow rate adjusting valves 103a to 103c, mixed gas components The pipes 105a to 105c and the like constitute mixed gas distribution supply means. The flow rate adjusting valves 103a to 103c constitute gas flow rate adjusting means for adjusting the supply amounts of the low-temperature heating gas 12 and the waste heat gas 13 to the dry distillation apparatuses 121 of the equipment

main bodies

100A, 100B, and 100C.

The control device 109 supplies the low-grade coal 1 to the drying devices 111 of the equipment

main bodies

100A, 100B, and 100C based on the flow rate adjusting valves 103a to 103c and the amount of fuel supplied to the combustion furnace 124 based on the measurement values obtained by various measuring instruments. The amount, the supply amount of the heated gas 11 to the dry distillation apparatus 121 of each equipment

main body

100A, 100B, 100C, etc. are controlled. That is, the control device 109 constitutes a control means for adjusting the valve opening degree of the flow rate adjusting valves 103a to 103c based on the measurement values obtained by various measuring instruments.

In the reformed coal production facility according to the present embodiment configured as described above, the operation for controlling to prevent the tar from adhering to the dry distillation

gas supply pipes

101a, 101b, 101c during the steady operation is the above-described first operation. This is the same as the modified coal production facility 100 according to the embodiment, and the description thereof is omitted.

The operation when the reformed coal production facility main body included in the modified coal production facility according to the present embodiment is stopped and returned to the steady operation state will be described below with reference to FIGS. 4A and 4B.
The case where the reformed coal production equipment

main body

100B, 100C is in the steady operation state, while the reformed coal production equipment main body 100A is stopped and returned to the steady operation state will be described.

As shown in FIG. 4A and FIG. 4B, first, the reformed coal production facility main body 100A is in steady operation (step SB1). The reformed coal production equipment

main bodies

100B and 100C are also in steady operation (step SC1).

In order to stop the reformed coal production facility main body 100A, the transfer of the dry coal 2 to the inner cylinder 122 of the carbonization device 121 is stopped (step SB2). As a result, the amount of dry coal 2 in the inner cylinder 122 of the dry distillation apparatus 121 of the equipment main body 100A decreases, so the supply amount of the heated gas 11 from the combustion furnace 124 to the outer cylinder 123 of the dry distillation apparatus 121 is reduced. The amount is reduced (step SB3). That is, in the carbonization apparatus 121 of the equipment main body 100A, the heat load is reduced. On the other hand, the equipment

main bodies

100B and 100C increase the transfer of the dry charcoal 2 to the inner cylinder 122 of each dry distillation apparatus 121 of the equipment

main bodies

100B and 100C (step SC2). As a result, the amount of dry coal 2 in the inner cylinder 122 of each of the carbonization devices 121 of the equipment

main bodies

100B and 100C increases, so the heated gas 11 from the combustion furnace 124 to the outer cylinder 123 of each of the carbonization devices 121 is increased. Is increased (step SC3). That is, in each of the carbonization devices 121 of the equipment

main bodies

100B and 100C, the heat load increases.

Subsequently, the control device 109 adjusts the flow rate adjusting valve 103a, and supplies the low-temperature heating gas 12 and the waste heat gas 13 to the inlet 122a side of the inner cylinder 122 of the dry distillation apparatus 121 via the mixed gas distribution pipe 105a ( Step SB4). As a result, the dry distillation gas 14 in the inner cylinder 122 and the dry distillation gas supply pipe 101a of the dry distillation apparatus 121 of the equipment main body 100A is purged by the low temperature heating gas 12 and the waste heat gas 13. Further, the oxygen concentration of the gas inside the inner cylinder 122 and the dry distillation gas supply pipe 101a becomes about 1 to 2%, and tar is oxidatively decomposed and lightened. Also, the lightened light gas is burned. Therefore, the adhesion of tar to the inner cylinder 122 and the wall surface of the dry distillation gas supply pipe 101a is prevented.

Subsequently, all the carbonized carbon 3 is discharged from the inner cylinder 122 of the carbonization device 121 of the equipment main body 100A (step SB5), and the supply of the heating gas 11 to the outer cylinder 123 of the carbonization device 121 of the equipment main body 100A is stopped. (Step SB6). Thereby, the thermal load of the dry distillation apparatus 121 of the equipment main body 100A is reduced. On the other hand, in the equipment

main bodies

100B and 100C, the supply of the heating gas 11 to the outer cylinder 123 of each dry distillation apparatus 121 of the equipment

main bodies

100B and 100C is in a steady state (step SC4). Thereby, it maintains with the state in which the thermal load of each dry distillation apparatus 121 of each equipment

main body

100B and 100C increased.

Subsequently, in the equipment main body 100A, when the supply of the heated gas 11 to the outer cylinder 123 of the dry distillation apparatus 121 of the equipment main body 100A is stopped for a predetermined time (step SB7), the inside of the carbonization apparatus 121 of the equipment main body 100A. Since the dry distillation gas 14 is eliminated in the cylinder 122 and the dry distillation gas supply pipe 101a, the supply of the low temperature heating gas 12 and the waste heat gas 13 is not required, and therefore the inlet 122a of the inner cylinder 122 of the dry distillation apparatus 121 of the equipment body 100A. The supply of the low-temperature heating gas 12 and the waste heat gas 13 to the side is stopped (step SB8). In step SB8, operations such as maintenance and inspection for the equipment main body 100A are performed as necessary.

Subsequently, when the operations such as maintenance and inspection described above are completed, first, the dry coal from the drying device 111 of the equipment main body 100A to the inner cylinder 122 of the carbonization device 121 is returned to return to the steady operation state. 2 is started (step SB9). Thereby, since the amount of dry coal 2 in the inner cylinder 122 of the dry distillation apparatus 121 of the equipment main body 100A increases, the supply amount of the heating gas 11 from the combustion furnace 124 to the outer cylinder 123 of the dry distillation apparatus 121 is reduced. The amount is increased (step SB10). Thereby, in the dry distillation apparatus 121 of the equipment main body 100A, the heat load increases. On the other hand, in the equipment

main bodies

100B and 100C, the transfer of the dry coal 2 to the inner cylinder 122 of each of the carbonization devices 121 of the equipment

main bodies

100B and 100C is reduced (step SC5). As a result, the amount of dry charcoal 2 in the inner cylinder 122 of each of the carbonization devices 121 of the equipment

main bodies

100B and 100C decreases, so the heated gas 11 from the combustion furnace 124 to the outer cylinder 123 of each of the carbonization devices 121 is reduced. Is reduced (step SC6). Thereby, in each dry distillation apparatus 121 of the equipment

main bodies

100B and 100C, the heat load is reduced.

Subsequently, the supply amount of the dry coal 2 to the inner cylinder 122 of the dry distillation apparatus 121 of the equipment main body 100A reaches a predetermined amount, and the supply amount of the heated gas 11 to the outer cylinder 123 of the dry distillation apparatus 121 reaches a predetermined amount. Then, the equipment main body 100A returns to the steady operation state (step SB11). On the other hand, the supply amount of the dry coal 2 to the inner cylinder 122 of each of the carbonization devices 121 of the equipment

main bodies

100B and 100C reaches a predetermined amount, and the supply amount of the heating gas 11 to the outer tube 123 of each of the carbonization devices 121. When the amount reaches a predetermined amount, the equipment

main bodies

100B and 100C also return to the steady operation state (step SC7).

Even when the equipment main body 100B or the equipment main body 100C is stopped, by operating in the same procedure as the equipment main body 100A described above, the inside of the inner cylinder 122 of each dry distillation apparatus 121 included in the equipment

main bodies

100B and 100C or the dry distillation gas supply pipe It is possible to prevent tar from adhering to the wall surfaces in 101b and 101c. In other words, by performing the above-described operations sequentially on the equipment main body to be stopped, the efficiency of the main body of the reformed coal manufacturing equipment that is the target of the stoppage is suppressed while suppressing a decrease in the operating rate of the entire reformed coal manufacturing equipment. Tar can be removed well.

Therefore, according to the modified coal production facility according to the present embodiment, as with the modified coal production facility 100 according to the first embodiment described above, when the facility main body is stopped, dry distillation of the facility main body to be stopped is performed. By supplying the low-temperature heating gas 12 and the waste heat gas 13 to the inlet 122a side of the inner cylinder 122 of the apparatus 121, the dry distillation gas 14 in the inner cylinder 122 and the dry distillation gas supply pipe of the dry distillation apparatus 121 is forcibly discharged. Will be. Further, the dry distillation gas 14 is burned in the combustion furnace 124.

Furthermore, since the oxygen concentration of the low-temperature heating gas 12 and the waste heat gas 13 is about 2-3%, tar can be lightened by oxidative decomposition. The lightened gas flows into the combustion furnace 124 and burns in the combustion furnace 124. Further, even if tar adheres to the wall surface of the inner cylinder 122 of the carbonization apparatus 121 or the carbonization gas supply pipe, the tar can be removed by combustion.

Therefore, even when the equipment main body is stopped, tar can be efficiently removed without reducing the production amount of the reformed coal 4. Further, since tar can be prevented from adhering to the inner cylinder 122 of the carbonization apparatus 121 or the wall surface of the carbonization gas supply pipe, maintenance and inspection work can be performed efficiently.

[Other embodiments]
In the above description, the reformed coal manufacturing facility in which three reformed coal

manufacturing facility bodies

100A, 100B, and 100C are arranged in parallel has been described. It is also possible to use two or more coal production equipment main bodies as modified coal production equipment arranged in parallel.

In the above, based on the elapsed time since the supply of the heating gas 11 to the outer cylinder 123 of the carbonization device 121 of the equipment main body 100A is stopped, the low temperature heating gas 12 to the inner cylinder 122 of the carbonization device 121 of the equipment main body 100A. The reformed coal production facility for stopping the supply of the waste heat gas 13 has been described, but the facility main body to be stopped based on the measured values of the measuring devices such as the differential

pressure measuring devices

107a and 107b of the facility main body to be stopped It is also possible to provide a modified coal production facility that stops the supply of the low-temperature heating gas and the waste heat gas to the inner cylinder of the dry distillation apparatus.

The reformed coal production facility and the control method thereof according to the present invention can remove tar efficiently without reducing the production amount of the reformed coal even when the facility is stopped. It can be used beneficially.

DESCRIPTION OF SYMBOLS 1 Low grade coal 2 Dry coal 3 Dry distillation coal 4 Modified coal 11 Heated gas 12 Low temperature heating gas 13 Waste heat gas 14

Dry distillation gas

51, 51a-51c Heated

gas supply pipe

52, 52a-

52c Exhaust pipe

53, 53a-53c Heated

gas branch pipes

54, 54a to 54c Waste heat gas supply pipe 55 Mixed gas supply pipe 56 Mixed gas supply pipe 100 Modified

coal production equipment

100A, 100B, 100C Modified coal production equipment main body 101, 101a to 101c Dry distillation

gas Supply pipe

102, 102a to 102c Mixed

gas branch pipe

103, 103a to 103c Flow rate adjusting valve (three-way valve)
104, 104a to 104c Mixed gas communication pipe 105, 105a to 105c Mixed gas distribution pipe 106 Gas

temperature measuring instrument

107a, 107b Differential pressure measuring instrument 108 Inner cylinder gas temperature measuring instrument 109 Controller 111 Drying apparatus 121 Dry distillation apparatus 122 Inner cylinder 123 Outer cylinder 124 Combustion furnace 125 Steam generator 126 Blower 127 Exhaust gas treatment device 131 Cooling device

Claims

A drying means for drying the coal;
A carbonization means for carbonizing the dried coal;
Cooling means for cooling the coal that has been carbonized,
The dry distillation means is a modified coal production facility that is an indirect heating type dry distillation apparatus including an inner cylinder to which the dried coal is transferred and an outer cylinder to which a heating gas for heating the inner cylinder is supplied. ,
Heated gas generating means for generating the heated gas;
Dry distillation gas supply means for supplying dry distillation gas generated in the inner cylinder to the heated gas generation means;
A part of the heating gas generated by the heating gas generation means is supplied, and waste heat gas generation means for generating waste heat gas by exchanging heat of the heating gas;
And a mixed gas distribution supply means for distributing and supplying the waste heat gas and the low-temperature heating gas generated by indirectly heating the coal in the outer cylinder to the inner cylinder. Quality coal production equipment.
The modified coal production facility according to claim 1,
The reformed coal production facility, wherein the mixed gas distribution and supply means is connected to a receiving port side of the inner cylinder that receives the dried coal.
The modified coal production facility according to claim 2,
The indirect heating type carbonization apparatus is provided on a discharge port side for discharging the coal that has been carbonized, and includes a gas temperature measuring unit that measures a gas temperature,
The mixed gas distribution supply means measures the gas flow rate adjusting means for adjusting the flow rates of the low-temperature heating gas and the waste heat gas supplied into the inner cylinder, and the gas flow rate adjusting means is measured by the gas temperature measuring means. A reformed coal production facility comprising a control means for controlling based on the gas temperature.
A modified coal production facility according to claim 3,
A reformed coal production facility comprising a plurality of facility bodies having the drying means, the indirectly heated carbonization apparatus, and the cooling means in parallel.
A method for controlling a modified coal production facility according to claim 3, comprising:
Stopping the supply of the coal to the inner cylinder,
The control means controls the gas flow rate adjusting means to supply the low temperature heating gas and the waste heat gas to the inner cylinder, while increasing the amount of fuel supplied to the heating gas generation means,
When the gas temperature measured by the gas temperature measuring means becomes lower than a predetermined temperature, the control means controls the gas flow rate adjusting means to stop the supply of the low temperature heating gas and the waste heat gas to the inner cylinder. A method for controlling a reformed coal production facility.
A method for controlling a modified coal production facility according to claim 4, comprising:
While stopping the supply of the coal to the inner cylinder in the equipment main body to be stopped, the equipment main body in steady operation increases the amount of the coal supplied to the drying means and supplies the coal to the outer cylinder. Increase the heating gas,
In the equipment main body to be stopped, the control means controls the gas flow rate adjusting means to start supplying the low-temperature heating gas and the waste heat gas to the inner cylinder,
When all the coal is discharged from the inner cylinder in the equipment main body to be stopped, the supply of the heated gas to the inner cylinder is stopped, while the equipment main body in steady operation is supplied to the outer cylinder. The heated gas to a steady state,
When all of the dry distillation gas is discharged from the inner cylinder in the facility main body to be stopped, the control means controls the gas flow rate adjusting means, and the low-temperature heating gas and the waste heat gas to the inner cylinder The control method of the reformed coal manufacturing facility characterized by stopping supply of coal.