SU43114A1 - Installation for continuous thermal processing of shale - Google Patents

Description

The existing designs of coal coking chambers due to the significant physicochemical distinction of shale cannot be used for thermal processing of the latter without a fundamental change in the design of the chamber itself.

The main difference between slate, its non-caking and the absence of shrinkage during distillation, puts it in a special place among all known fuels. In addition, as a result of experimental and research work, it was established that shale ash, at known temperature conditions of shale burning, is a high-value new building material.

Suffice it to say that the ash content of shale is in the average not lower

in order to question the use of;

Ash was responsible IBHO exceptional place in the shale problem.

The insignificant caloric content of shale — on average, 2500–3000 calories / kg makes the task of its economic use particularly difficult, since the basic organic matter of shale, kerogen, is a valuable raw material for producing synthetic liquid injections.

(32)

With the high-temperature decomposition of shale, in addition to the main products, high-calorie gas and tar, there is mainly a significant amount (50 - 55 Ou) of low-grade (Q 900 - 1100 cal / kg) shale coke, the use of which is very difficult. Recent work has established that shale coke has a high reactivity, which puts insurmountable obstacles to its quenching. Among the possible ways to use coke, it can be suggested that it be burned under the boilers or further gasified to ash, subject to the conditional addition of fresh slate.

The combustion of shale coke on the grate, due to the inability to withstand the desired temperature, may ultimately cause sintering or even ash melting.

Considered with the mandatory pre-quenching of coke with notably significant heat losses:

1) the physical heat of coke

chambers 1000 °,. . ZOOKaAJKt

2) partial burning with

extinguishing and transporting lOVo100 cal I kg

3) loss due to moistening of coke during quenching 70 "

4) losses on the grid in the lattice (or underburning) 3% 30 „

Total , . . 500 KuAJKz

in the order of 35%, we will have ash of degraded quality, since the fused ash gives bound calcium silicates and, consequently, lower burning ability.

The proposed design is characterized by the following features:

1. The distillation chamber is made of two separate inclined chambers.

2. The transfer of hot coke to the gas generator is performed directly, which automates all the work of the chamber furnace with the gas generator and increases the thermal

ckofeementent beneficial action.

3. The proposed unit can be used for all types of solid fuels.

4.Under the gas generator has a peculiar design, allowing you to produce automatic dry ash removal.

Approximate installation of the furnace on eight chambers with a capacity of 200 tons / day. depicted in FIG. 1 in cross and in FIG. 2 in longitudinal cuts.

The main unit of the furnace-chamber 1 of distillation is two paired inclined chambers with an inclination relative to the vertical of 27-30 ° from the most likely angle of repose of a non-coking piece of shale. The middle wall 2 of the distillation chamber is the boundary that divides the chamber into two separate chambers. This wall is located in the middle part of the chamber and, not income to the lower neck, excludes the reciprocal connection between the charge of each half, i.e., the thrust that occurs in the conical part of the bunker. Distillation chamber - continuous with mechanical loading and unloading.

A series of experiments performed at temperature conditions of heating in the order of 1000 ° inside the chamber suggests that the most economical time limit for coking itself can be taken 12 hours. The gas production curves and the percentage of carbon monoxide already after 10 hours show an increase in the CO yield, which is the product of the dissociation of carbonates of the mineral part of the shale, thereby indicating that the charge has heated up to 800-900 °.

Directly under the distillation chamber 1 is a gas generator 3, serving two adjacent chambers. Coke enters the gas generator red-hot to 1000 °, so it is highly desirable to produce its gasification in a high layer.

The capacity of 1 m of the generator’s cross section for shale averages 200 KiJM per hour. For hot slate coke, the capacity of 1 m can be increased to 250-300. This generator voltage is not the limit, since, having such favorable conditions, it is reasonable to increase the forcing voltage to blow and superheated steam and, therefore, additionally use shale fines (crushing waste). The generator has a disk rotating tutirovanny under 4 with a cap according to the type of Kerpeli generator with eccentricity. The disk under is set on a roller drive. On one side of the generator, a shut-off device is installed at the hearth, which dumps the scorched ash into a scraper conveyor transporting the ash to the bunker storage. Having given one or another number of rotations of the generator hearth, it is possible to easily and conveniently adjust the quality of the ash produced, so as to prevent its melting. In addition, the steam in the generator helps this condition, making it possible to reduce or, conversely, increase the coke heat. It should be noted that the parodut will not have any effect on the ash, as according to the works of Ing. Shemkova (VNIGI) ash quality is even improved under these conditions.

The resulting gas is discharged into the common flue 5, from where it enters the channel and then into the heating chambers.

The channel has trapping bags.

fly ash, from where it is discharged through the drain hoses into a common ash conveyor. Excess gas enters the magnetic gas pipeline and is transported through coolers to a gas tank. Do not drive the calculated data on gas, we can assume that the resulting gas will have a calorific value of about 1100-1200 ka-g / l, since it will largely contain the products of dissociated steam H and CO, i.e. represent water gas diluted with air gas.

Each heating chamber has in the lower part an individual supply of cold combustion air. If there is a sufficient pyrometric effect (there is a heated gas of 700-800 ° C), heating of the combustion air is not provided.

The heating channels 6 are arranged in series horizontally and in the upper part are retracted into a common chimney 9, which serves one unit of distillation chambers, i.e. eight pieces.

The waste gases of each coking plant have a temperature of about 1000 °, therefore their use is necessary.

In the proposed design, one regenerator 10 with two switching chambers is installed on one furnace of eight chambers; flue gases after the regenerator with a temperature of 800 ° are directed to a special horizontal steam boiler 11, and then to the exhaust in a chimney.

The resulting steam with pressure up to 6 - 8 atm. it is used for the needs of the installation itself, i.e. for blowing into the gas generators.

Steam, transient throttle valve with a pressure not exceeding 1.5 atm. (manometric), sent to the regenerator and already overheated is used to blow in the generators.

The resulting dry shale gas is discharged through an outlet pipe 12 and passes through the usual primary cleaning route, i.e., hydraulic scrubbing, etc.

The proposed method of non-stop processing of oil shale excludes:

1) transport, tusk of hot coke and its storage;

2) independent generating station;

3) increases the overall efficiency of the installation;

4) makes it possible to get the ashes of the desired quality.

The subject matter of the invention.

1. An installation for non-stop thermal processing of shale, consisting of a distillation furnace associated at the bottom with a gas generator, characterized in that the coking chamber 1, which has a flat downward prism, is provided with a transverse vertical separation wall 2 that does not reach the throat.

2. The form of the furnace, in accordance with claim 1, characterized in that the heating wall of the distillation chamber is provided with a number of horizontal fire fluxes (ports 6, interconnected in order).

3. In the furnace, according to p. 1, use of a regenerator 10 for superheating steam and a waste heat boiler for heat recovery of waste waste products.