JPS58207939A - Gasification of sulfur-containing fuel - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

DETAILED DESCRIPTION OF THE INVENTION (Background Art) The present invention relates to the production of rat-sulfur-containing fuel, in particular:
This invention relates to a method for gasification using a fluidized bed made of particulate material.

The Environment Agency and various national authorities have established implementation standards that set maximum allowable sulfur dioxide emission levels for power plants that use fossil fuels. It is planned to remove sulfur dioxide from nuclear gases before the exhaust gases are dissipated into the atmosphere.

However, because a large amount of gas enriched with dilute sulfur dioxide flows into the boiler outlet, the exhaust gas purification equipment becomes large and has a high capacity.

Although it is possible to treat the exhaust gas from the stack to control the amount of sulfur dioxide released, it is advantageous to desulfurize the fuel before it is combusted in the boiler because the volume of gas required for treatment is reduced. be.

For this purpose, the technology of fuel gasification treatment has been developed2, which involves the partial combustion of a fuel, such as heavy oil or granular coal, in the f#, formation layer of lime particles. Desulfurization is carried out through reaction with lime particles, and the combustible off-gas produced is used in an external device, such as a commercially available sparker-fired boiler. 7! r00”F(
El! ;℃) to 1too″F (t7/℃)
Maximum desulfurization efficiency can be obtained if the desulfurization efficiency is controlled within the range of
The temperature is /1,00? (g7/°C), the sulfur retention capacity of lime decreases rapidly. However, at this relatively low temperature, there is a limit to the efficiency of the gasification process, making it difficult to operate at an industrially practical speed. The object of the present invention is to provide a fluidized bed that is free of sulfur, and to provide a process for producing sulfur that produces a product gas that is virtually free of sulfur.

Furthermore, it is an object of the invention to provide a process of the above-mentioned type in which the gasification process can be carried out at very high temperatures without reducing the desulfurization.

Furthermore, it is an object of the present invention to provide a process of the type described above, in which a fluidized bed consisting of particulate material containing calcium is reacted with the sulfur of the product gas.

A further object of the present invention is that the particle material contains silicate, which allows the processing temperature to be maintained at a relatively high temperature and improves the desulfurization efficiency without reducing desulfurization. The object of the present invention is to provide a method of the type described above.

According to the method of the present invention, a fluidized bed of particulate material is formed, which particulate material contains calcium that reacts with the sulfur produced when the fuel is gasified, and the fluidized bed also contains silica. This allows the fluidized bed to be operated at temperatures that improve sulfur conversion efficiency without reducing tfP recovery.

The foregoing description and objects, features and advantages will be better understood by reference to the following detailed description of preferred embodiments of the invention in conjunction with the accompanying drawings. .

(Explanation of Examples J) The ItI# mold of the present invention will be described with reference to the gasification apparatus 10 shown in FIGS. 1 and 2.

Gasification! i[10d, i.e. the grid 12
, front wall 14, rear wall 11, and lattice 12 to roof 18
It is provided with a full-bodied side wall 17 (see FIG. 2) extending over the entire length. The vertical part 20 is the front part &! ! 14 and the rear wall 16 to cover the inside of the gas cover.
and a reproduction section 24. floor 12, walls 14 and 1
6. The roof 18 and the vertical portion 20ri are all heat-insulated using a well-known method.

An air duct 26 extends below the floor and has an inlet 28 for receiving air from outside. A plurality of T-shaped air distribution piping devices 30 extend through the floor, the devices 30r
i. Air is received from the duct 26 and the air IF converter 2
2 and the reproduction section 24. As best seen in FIG. 2, each tube fold fl 130 includes a vertical tube 3Ua extending through an opening in the floor 12 and a horizontal gaob connected to the vertical tube and receiving air therefrom. Although not shown, the horizontal pipe 30b has a series of holes M formed on its upper surface to distribute air to the gasification section 22 and the regeneration section 24.

A plurality of fuel distribution piping holes 32 extend through other openings in the floor 12 to the gasification s24, and the fuel distribution piping system f1t,
The valleys of 32 pass through the horizontal pipe 32a extending in the f direction of the floor 12, and are connected to the horizontal pipes t and Ha. 'f32b
t- Prepare.

The ends of the valley water pipes 32a each extend through the II wall 17 and connect to a fuel source (not shown) such as petroleum or granulated coal.
It is becoming more persistent.

A supply device 346 extends back up the wall 17 and supplies particulate material containing calcium and silica to the gasification section 22. For example, the material may have the following composition: Portland cement.

CaO6θ~l, 591 M2036% Fi20:s J% 5LO2-2/~26% Na2O/ 5032% MgO, 2% The presence of silica in the above-mentioned composition causes unexpected results and impedes sulfur recovery. The gasification process can be carried out at higher temperatures than when using silica-free compositions without loss.

Compositions containing calcium and silica are not limited to the specific examples described above. That is, for the amount of calcium required to react with sulfur and remove a given amount of sulfur from the hydrogen-sulfur gas, sufficient silicate power exists to perform a similar treatment using only lime or limestone. 4I & the above composition -': as long as it is possible to carry out the sulfur treatment at higher temperatures without reducing the recovery of sulfur.

Things can change. For example, as an alternative composition, the particulate material may be comprised of a mixture of calcium and silica in approximately the same proportions as described above. For example, by introducing water and using a rotating dinuk, screen, etc.,
It is preferable to harden into a ball or an islet shape. This improves processing efficiency without impairing material handling.

The gas conversion part 22 is provided with a +111 wall 36,
The separation wall 36ri connects the section 22 to the channel (22).
a and 22I) (see Figure 2).

The separation wall 36 extends from the partition 20 to the dark chain acid of the rear wall 16 and forms a passageway 22c connecting the channels 22a and 22b.

The population slot 38 and the exit slot 40 are connected to the partition 20 (29), and the population slot 38 connects the chamber 22a and the regeneration unit 24 to 1! ! As a result of this arrangement, the particulate material introduced into the gasification section 22 via the feeder fi 34 and the fuel Distribution tg*a
The fuel (for example, oil) introduced into the gasification section 22 through the gasification section 22b is mixed with a
and the regeneration section 2 from the chamber 22b through the slot 38.
4 continuously flows into the slot 4 from its bulge 24.
0 into chamber 22b for recirculation.

A pair of outlets 42 and 44 are provided in the roof 18;
These outlets communicate with the upper part of the gasification section 22 and the regeneration section 24, each with q! The sulfur gas and sulfur gas produced in the r section are discharged.

In operation of the device, a certain amount of particulate material enters the gasification section 2.
It is placed in 2. And the temperature of the layer is the fuel distribution f device 3
By controlling the fuel entering the layer from 2) is approximately 9g0℃
(1g00a).

Air is distributed from duct 26 at a rate below chemistry!
Introduced into the gasification section through device 30, the air fluidizes the bed material and reduces combustion and heat generation. On the other hand, flue gas is used as an inert heat-absorbing medium to control the processing temperature so that it does not become too high.

The amount of fuel and air introduced is c1! ! By adjusting the gasification rate, the stoichiometry is approximately 2 at a gasification rate of $22! ;'la to 30% of the fuel and the fuel is partially combusted, and this combustion provides enough heat to partially combust the fuel and optionally vaporize or decompose the remaining oil.

This partial combustion forms hydrogen sulfide, which reacts with calcium in the layer material to form calcium sulfide. The gas product of this process is essentially sulfur- and panazum-free fuel gas, with approximately 200 sTU
/ft3 (1,7 units/m") of heat generation tfI: This gas rises by natural convection, exits the gasifier through outlet 4z, and enters the gaylor. and other external devices.

The air from the duct 26 escapes the air distribution piping device 30 and is also introduced into the regeneration section z4, making the atmosphere oxygen-rich. The sulfurized lucium formed in the gasification section 22 is circulated through the regeneration section 24i as described above. While generating off-gas with sulfur dioxide concentration,
Oxidizing power Changes to lucium rum.

Ca5O+ CaS + 02→JCaO+, 2S0
2 The sulfur dioxide produced by the above reaction is transferred to the regeneration section 24.
is discharged from the gas through outlet 44 and recovered from the gas stream in the form of elemental sulfur by an external device. On the other hand, the calcium oxide is recycled to the gasification section 22 and reused as a sulfur absorbent.

The l-material from the reaction source is continuously removed through a drain pipe or the like (not shown), and the l-
By replenishing the material, the sulfur retention capacity in the oxidized portion 22 is maintained. The amount of particulate material required will vary depending on the amount of sulfur to be removed from the gas. , this no amount of material! - by varying the amount of particulate material introduced into II and the t of reactive source material removed from the bed.
f) As a result, the presence of calcium in the layer material substantially eliminates the presence of sulfur, which naturally causes the formation of sulfur at a much higher rate. On the other hand, due to the presence of the nori knife, the gasification process can be carried out at a relatively high temperature where high sulfur conversion efficiency can be achieved without reducing the amount of sulfur recovered. Without departing from the purpose, some /& members in the above embodiments are aT functions. For example, F+ is not limited to oil, but may also be grains, coal throat and curved fuels, in which case the -E, family is added to the gasifier along with the air flow. be introduced.

Modifications, changes, and substitutions of the scope are mentioned in the above disclosure, and some of the above and the following may be used in the meeting. Therefore, the terms of the patent claims should be interpreted broadly and in a way that meets the objectives & C of the present invention. .

[Brief explanation of drawings]

Figure I/ is a cross-sectional view of the oxidation equipment used in the present invention, and Figure A2 is a cross-sectional view cut along the line Coats in Figure A2. Description of symbols IO...tf gasifier z...grid 14...front wall 16...rear wall 22...gasification section 24...regeneration section 16...air duct 30...・Air distribution piping device

Claims (1)

[Scope of Claims]
A sulfur-containing M fuel is introduced into the layer, air is passed through the layer to fluidize the layer to promote combustion of the fuel, and the fuel is gasified by introducing the fuel and controlling the air circulation. releasing sulfur-containing gas from the fuel, selecting an amount of calcium in the material to react the calcium with the sulfur to remove a majority of the sulfur from the gas; Gasification of a sulfur-containing fuel, characterized in that the silica is selected to cause sulfurization to occur with a higher degree of performance than when silica is not included and without a reduction in desulfurization. Method. @ The weight of calcium in the material is from 6 ozb to bs
9. The method described in item 7 above, wherein the % sign is melting between %υ. (j) The gItD method described in item 1 above, characterized in that the silica content in the material is between 27 and 27. (To) The ratio of calcium to silica in the material. is 6 in weight
4 to be in the range of 21 to 26 versus 0 to 6S? 7. The method described in item 7 above. (6) The method according to item 1, which includes the step of clumping the material into a sphere or pellet before introducing the material into the layer. (6) The temperature of the layer is approximately /g00' F (7g2℃)
2. The method according to item 1 above, wherein the % imitation is maintained at . (η) The method according to item 1 above, characterized in that the flow of air that presses against the layer is a chemical reaction that suppresses combustion and heat generation.