SU1458374A1 - Method of producing coke and reducing gas - Google Patents

Abstract

The invention relates to the field of thermal processing of coal and contributes to increasing the yield of reducing gas and simplifying the process. Coal or briquettes with a moisture content of 7-10% are heated in the preheating zone (ZPN) of a vertical furnace with the formation of direct coke oven gas, water vapor and coke, which are sent to the coke's electric broker (EPB) zone, where coke is heated to 1200-1300 C. This creates a pressure drop from the ZPN to the ZZP of 30-55 Pa / m, which ensures the movement of gaseous products in the stream with heated coal. In the process of direct coke oven gas conversion on hot coke, in the process of production process in the presence of leached water vapor, a reducing gas is formed, containing 98.8% of CO and N. 2 ill., 4 abl. S (/)

Description

The invention relates to the technique of thermal processing of coal and can be used in the coke industry, metallurgical production and industry of organic synthesis.

The purpose of the invention is to increase the yield of the reducing gas. And simplify the process.

FIG. 1 shows an installation diagram for carrying out the method; in fig. 2 - dependence of coke yield on coal moisture

Example. Processing refines coal grade G with a grain size of 6-13 mm; characterized by humidity (Wt / i 8.2%, volatile matter yield (V)

38.4% and plastometric index (y) 6 mmo

Coal is loaded into the mine of the test furnace in the amount of 8 kg / h. Preheating of the coal in the zone is carried out up to 650 ° C due to the heat of the reducing gas flowing with the temperature from the gas collecting channel 1 into the heating room

ovens.

The coke obtained in this mode is then subjected to electric puller up to 1300 ° C in the presence of water vapor and raw coke oven gas entering the calcination zone 2 from the coal preheating zone 3 by creating a pressure differential between 4 SP

ac 00 vj

1458374

do the preheating zones of coal and electric coke coke, equal to 50 Ia / m, from 105 to 17.5 Pa with the total height of the preheating zones of the coal and coke irokalki equal to 1.75 m (ie. (105-17.5); 1.75 50 Pa / m),

In the process of conversion of direct coke oven gas, on a hot coke in the electric incinerator zone, in the presence of carbon vapor emitted from the vapor, a reducing gas is obtained, which is sent to the gas collecting channel 1 and then used for preheating coal. Reducing gas cooled to 150 ° C due to heat transfer to the heated coal from the heating walls of zone 3 is fed to the piers of the coke cooling zone 5 using gas-tube 4, where it is heated to 850-900 ° C and used as a target product, and cooled to 200 With a coke, a discharge device (pusher) b is unloaded into a receiving lined bunker,

You get a reducing gas of the following composition, vol.%:

,

g

98.5

From

0.3

Ots.

0.3

0.4

0.17

Ots about

The recovery gas bicode is 1485 im / t.

The resulting coke is characterized by the following indications;

Hardness mg 60.1

With rub the Turk

strength,% 80

Coke yield,% 64.2

Similarly, the processing is subjected to grade G coal with a particle size of 13–25 mm, shchitty, including 70% grade G coal, 15% grade OS and 15% grade T (W 8%, V 30.7%, 7 mm), as well as brass sets 15 mm obtained from grade G coal by cold pressing using coal tar as a binder

The gas used for producing briquettes with a particle size of 0-3 mm is characterized by the following quality indicators: W 9.2%; A 7.2%;

5 0 5

0

five

0

five

0

five

1300 ° C

, 6% 5, 4%; ,five%; at 6.0 mm,

Characteristics of the products obtained are given in table. 1, V. table. 2 shows data on the electric coke coke from gas coal and the charge obtained by varying the pressure drop in the area of coal preheating to the coke electric broker zone from 20 to 65 Pa / m. From the table. 2 data shows that with a pressure difference in the range of 30 .55 Pa / m, a stable yield of reducing gas of 1480-1485 is observed during the processing of coal gas and 1360-1368 nm / ton of reducing gas during processing of the charge

In tab. Table 3 presents the generalized data on gas coal processing and pulping with a humidity of 5–12%. The calcining and conversion of direct coke oven gas was carried out at 1300 C.

From the data table. 3 it follows that when the moisture content of coal is below 7%, soot appears in the conversion products as a result of the partial pyrolysis of coke oven gas hydrocarbons on the heated coke due to the lack of moisture required for the conversion process. The formation of carbon black leads to the loss of the initial hydrocarbon feedstock, reduces the gas permeability of the mass of coke and reduces the technological process. Therefore, the lower limit of the moisture content of the coal used to carry out the method is defined as 7%.

An excess of moisture leads to a partial gasification of coke and a decrease in its quantitative yield. This is confirmed by the results given in table. 3j and also in FIG. 2. On the basis of the dependence, the limiting value of the moisture content of the coal for carrying out the method is determined from the inflection point of the curve corresponding to the moisture content of the coal 10%. The use of coal with a moisture content of more than 10% leads to a decrease in the yield of coke,

In tabLo 4 is given a comparative assessment of the proposed and known methods of processing briquettes with a diameter of 15 MMj obtained from gas coal

From given in tabls. -4 data imply that when processing coal by the proposed method, yield voem ™

settling gas is more than 2.0 times better compared with the results obtained during the processing of coal by a known method (1480 and 691 coal, respectively).

According to the proposed method, a reducing gas is obtained containing 98.8% of the sum of the components of CO and H, while the known content of the reducing components in the gas is 2.8%

According to the proposed method, full conversion of hydrocarbons of direct coking of gas is provided, the residual methane content is almost negligible (0.2%). In the converted gas obtained by a known method, 2.1% of methane is contained.

With an almost equal quantitative yield of coke, obtained by the compared methods, the mechanical properties of coke, obtained by the proposed method, are higher.

The economic feasibility of using the method of processing direct coke oven gas is due to the use of cheap low-leakage1458374 6

coals of low metamorphism and the possibility of reducing coke consumption in blast furnaces by using reducing gas.

Claims (1)

Invention Formula A method of producing coke and reducing gas, including feeding lump coal or coal briquettes into a vertical furnace, preheating them, coking, then coke electric carts in the presence of water vapor and coke gas, withdrawing the reducing gas and cooling the coke, characterized in that exhaust gas and process simplification process coal or coal briquettes with a moisture content of 7–10%, reducing gases are removed from the lower part of the electric breaker zone and create a pressure drop along the height of the furnace from the preheating zone of the coal to the zone of the electro-coke coke 30-35 Pa / m, 1420 1365 1480 98.2 0.25 0.2 Ots. 98.8 0.20 0.2 Ots. 98.8 0.20 0.3 Ots. T a blitz 1 64.7 72.0 84.0 9010 70.1 76.8 93.0 87-10 64.2 62.1 84.0 94-10 Indicators Recyclable material Pressure drop in the coal heating system in the area from the coal preheating zone to the coke electric broker zone, Pa / m 20 Vdsod in the stationary hectare for, Output camHj g / m The content in the reducing gas CH4,% Coal 1Pyhta Coal Charge Charcoal Charcoal 13701394146014811485148014731430 129513101340136513681360 13481350 2,40,80,30,00,00,00,00,0 2,10,5Oi20,00,00,00,00,0 0,100,150,180,190,200,250,653,4 0.10 O, 00,140,180,170,200,503.2 The content in the reducing gas vapor resin, g / m Charcoal Charcoal 0.0 0.0 0.0 0.0 0.0 0.0 0.6 0.6 4.2 0.0 0.0 0.0 0.0 0.0 0.0 3.8 table 2 25 T27 I 30 J50 55 | 57 65 11.00.0 12.00.0 The proposed 1480 98,8 0,2 0,3 0,0 0,2 64 64 62,1 84,0 94-10 Known 691. 96.0 2.1 1.1 0.6 0.2 64.5 53.0 77.3 1710 0.0 63.3 0.0 62.9 68.8 68.2 Table 4 7 / ffoHC AU u / t / xmM And 7  %  6s I 63 S1 & fe.2 ff0 / tc / 3 angle) f rO12 3 / f & j ffffc / A,%