EP0851906A1

EP0851906A1 - Method for gasification processing of solid combustible municipal refuse and the like

Info

Publication number: EP0851906A1
Application number: EP95924899A
Authority: EP
Inventors: Georgi Manelis; Evgeni Poliantchik; Nadezhda Tchervonnaia; Alexandr Ioudanov; Viatcheslav Tcheremisine; Alexandr Tchervonny; Viktor Foursov; Nikolai Alkov; Vladimir Rafeev
Original assignee: ENVIROTEC GROUP Ltd
Current assignee: ENVIROTEC GROUP Ltd
Priority date: 1994-06-23
Filing date: 1995-06-22
Publication date: 1998-07-08
Also published as: AU2922895A; WO1996000267A1

Abstract

Municipal refuse (F) optionally containing added combustible or non-combustible solids (S) is processed in a reactor (4) having a counterflow of air (L) optionally containing added water (W). The gaseous product (G) and a solid residue (R) are removed. The gasifying agent (L, W) is preheated by the combustion residue at the bottom of the reactor, whereafter the combustible gaseous product (G) preheats and dries the waste before removal from the reactor. The maximum combustion temperature in the reactor is held at 700-1400 DEG C, and the temperature of the gaseous product is kept below a maximum of 250-400 DEG C by adjusting the mass fraction (a) of oxygen in the gasifying agent, the mass fraction (b) of non-combustible material in the feedstock, and the mass fraction (c) of combustible material in the feedstock, while maintaining a ratio A = a.b/c of 0.1-4.0. The yield and thermal efficiency of the method may thus be enhanced.

Description

"Process for treating solid combustible municipal waste or the like by gasification

DESCRIPTION The treatment of municipal waste is an important problem because the waste accumulates in ever increasing quantities, while there is currently no process for treating or eliminating it that is both economical and ecological. Most of the waste continues to accumulate in landfills, which foreshadows environmental problems for the future. Existing incinerators to treat municipal waste treat only a small part of it. The existing processes currently require heavy investment due in particular to smoke purification systems, which are expensive but necessary to make these incinerators comply with anti-pollution standards. The present invention relates to the treatment of municipal solid waste which contains paper, wood, rubber, textiles and other fuels, by pyrolysis / gasification of their combustible part and obtaining pyrolysis products and combustible gas.

A number of methods are known for treating municipal solid waste by combustion. The most widely used is the process of direct combustion of municipal solid waste on mobile grids of special design in an air flow. This process results in air pollution which can only be eliminated by a complex and costly treatment of the fumes. The processes which go through a preliminary gasification of the waste are more promising because the combustible gas obtained is usually much easier to purify than the fumes, if only because of its smaller volume. US-A-2 796 390 and US-A-2 798 032 describe, with regard to the treatment of oil shales, examples of processes which successively implement, layer by layer, the combustion / gasification of solid organic waste in vertical ovens in a counter-current of oxidizing gas.

The general principle of counter-current gasification for solid organic fuels is as follows: - The gasification agent feeds the reactor against the current with solid organic fuel so that the oxidizing gas passes at least partially through a layer solid incombustible product from gasification (ash). This provides an area where the oxidizing gas is preheated and the ash is cooled before being discharged.

- The gasifying agent containing oxygen and, if necessary, water and / or carbon dioxide enters a combustion zone, where the oxygen reacts with the solid carbonaceous fuel (coal) at a temperature which is typically from 900 to 1500 ° C.

- Oxygen is completely consumed in combustion and the hot gaseous products of combustion (including carbon dioxide) pass through another layer of solid fuel where the reduction zone is established, i.e. say that water and carbon dioxide react with carbonaceous fuel to produce combustible gases. The heat from the hot combustion gases is consumed in these reduction reactions. The temperature of the gas flow decreases as the gas flows through the solid fuel, as the gas transfers its sensible heat to solid fuels. Organic fuel heated by the flow of gas is pyrolysis, producing coal, tar, oils and combustible gases. The gaseous product flows through the freshly loaded fuel, so that the produced gas is cooled and the fuel preheated and dried. Finally, the gas produced (entraining aqueous vapors and hydrocarbons, oils and tars) is withdrawn for later use or treatment.

Municipal waste belongs to pyrolysable solid fuels with a high ash content which can be treated by gasification against the current. Municipal solid waste usually contains substantial amounts of fuel, namely paper, wood, rubber, textiles, plastics, organic food waste, etc. which can be treated to provide combustible gas. Solid combustion products that are removed from the combustion zone are generally environmentally sustainable.

According to US-A-4 732 091 the fuel, which may include municipal solid waste, is loaded into the upper part of a vertical oven. The waste progresses in the oven at a rate which is controlled by a system of movable grates, through a succession of chambers where the fuel pyrolyses then burns in a counter-current of air-vapor gasification agent. The process allows the gasification of waste, grids used to deagglomerate the load during treatment, so as to ensure its permeability to gases, and serving to control the rate of supply of waste to successive zones. The presence of mobile grilles is the main drawback of this process. In high temperature areas, the grates will inevitably wear out quickly. In addition, the dust particles will settle on the mobile reactor structures and prevent them from operating freely. The gaseous product leaves the reactor at a temperature of about 430 to 540 ° C. The temperature in the combustion zone is around 870 to 930 ° C.

The general problem of known gasification processes is their low yield, in particular for treating waste whose composition varies. Another general problem of the known processes is the high temperature of the gaseous product, which prevents its direct purification, while this gaseous product usually contains acid components (for example sulfuric acid, hydrochloric acid, hydrofluoric acid) which is necessary. remove before burning the product gas. At temperatures above 300 ° C, the tar in the product gas tends to settle in the gas lines as it polymerizes.

The aim of the present invention is to propose a process for the incineration of municipal solid waste, including waste having a low calorific value, without additional energy supply and producing products which are harmless for the environment (after final treatment ). According to the invention, a method is proposed for treating, by gasification, municipal solid waste or the like, comprising the following steps:

- the waste is loaded into a reactor;

- A gasification agent containing oxygen is injected into the reactor through a region of this reactor where the solid products of the treatment are deposited;

- The solid products from the treatment are discharged from this reactor; and - a gaseous product resulting from drying, pyrolysis and gasification is removed from this reactor, the gasification of waste resulting from the successive passage of this waste through:

- a heating and drying zone, • - a pyrolysis zone, - a combustion zone (oxidation),

- and a cooling zone, characterized by a temperature regulation process comprising maintaining the maximum temperature in the reactor in a temperature range between 700 and 1400 ° C, by adjusting at least one parameter chosen from the mass fraction ( a) oxygen in the gasifying agent, the mass fraction (b) of the incombustibles in the charge, and the mass fraction (c) of fuel in the charge, while maintaining the ratio A = ab / c in the value range 0.1 <A <4.0.

Preferably, the maximum temperature is maintained in the range from 1000 to 1200 ° C. Preferably also, the maximum temperature regulation is carried out while maintaining the ratio A in the range 0.15 <A <1.0. For the usual composition of fuels in municipal waste similar to that found in European countries, it is preferable to comply with 0.2 <A <0.5. In addition to adjusting at least one of the three parameters entering into the calculation of the ratio A, it is also recommended to regulate the flow rate of the gasifying agent. Typically, the flow rate of the oxidizing gas is between 200 and 2000 kg / h / m2 of cross section of the reactor in the combustion zone. The mass fraction of the fuels in the waste as regulated according to the invention will typically be between 20 and 50%.

It is also preferable to adjust the parameters so as also to regulate the temperature of the gaseous product so that it is less than 400 ° C., preferably less than 250 ° C., at the outlet of the reactor, because if the gaseous product leaves the reactor at about 250 ° C or less, the condensation and polymerization of tars in the conduits is significantly reduced. The method according to the invention is suitable for gasifying solid municipal waste containing fuels (between approximately 10 and 90% by weight), water (between approximately 10 and 70% by weight), and a portion of solid non-combustibles ( between about 10 and 80% by weight).

According to the invention, solid municipal waste is loaded into a reactor (for example a vertical reactor) in order to successively dry the waste, then pyrolysis and gasify its fuels. An oxidizing gas containing oxygen, for example air, is injected into this reactor through the region of the reactor where the solid residues of the treatment are deposited, so that the gas flow is oriented substantially against the current of load.

The charge passes through the succession of zones which will now be described.

First a drying zone, where the temperature of the load rises to 200 ° C by heat exchange with the flow of gaseous products. In this zone, the charge is dried while the gas flow cools before being withdrawn from the reactor. The gases produced by drying, pyrolysis and gasification are withdrawn in this zone as a gaseous product. Then the charge enters a pyrolysis and coking zone where the temperature of the charge increases from 200 to 800 ° C by heat exchange with the flow of hot gas, and fuels of the charge are pyrolyzed to finally give a charcoal. The charge containing the residual carbonaceous fuel then enters a combustion and gasification zone where the temperature of the charge is between 700 and 1400 ° C. In this area, the coal reacts with the hot oxidizing gas to provide combustible gas. The solid residue of combustion enters a cooling zone where it is cooled by the counter-current of oxidizing gas, from the combustion temperature to the discharge temperature. The oxidizing gas counter-current is heated to a temperature close to the combustion temperature before entering the combustion zone. Finally, the solid combustion residues (treatment products) are discharged from the reactor.

The aforementioned classification of the zones is to some extent arbitrary and these zones can be defined in another way, for example according to the temperature of the gases, the composition and the state of the products participating in the reactions, etc. But whatever the particular choice of these zones, an important point is that due to the countercurrent flow of gases and solids the gasification agent (oxidizing gas) is preheated by the solid residues of combustion and that then the hot gaseous products of combustion and gasification give up their heat to the initial charge.

It should also be noted that the flow against the current does not necessarily imply a spatial displacement of the load. In particular, the process can be carried out in a continuous mode, by continuously or intermittently loading the feed into the reactor and by discharging the solid residues from the reactor while the feed is consumed in the process. In this particular case, in fact, the load being treated moves, preferably under the action of gravity, against the flow of the gas stream. Alternatively, the process can be carried out cyclically in a fixed bed implementation mode, the reactor being loaded and unloaded in batches during periods of shutdown. In this case, said succession of zones moves along the charge and it is said that the charge enters a zone when this zone reaches a particular region of the reactor.

When the temperature of the gaseous product exceeds the prescribed limits, the ratio A defined according to the invention is increased and / or the rate of supply of oxidizing gas is decreased. When the maximum temperature in the reactor exceeds the prescribed limits, the ratio A is decreased and / or the gas supply rate is decreased; and finally when the maximum temperature in the reactor becomes lower than the prescribed limits, the ratio A and / or the oxidizing gas feed rate and / or the mass fraction of fuel in the feed is increased.

In particular, the ratio A can be adjusted by introducing into the waste solid non-combustible materials or objects, preferably non-fusible, preferably having a size less than 250 mm, or a solid fuel in pieces. This last possibility corresponds to the extreme case of the treatment of wet waste very poor in fuels. Solid combustion residues can be reprocessed and a fraction thereof used as additional solid incombustibles to regulate the composition of the charge. The quantity of non-combustible and combustible materials that can be introduced into the reactor in addition to the initial charge can reach up to 200% and respectively 30% of the weight of the initial waste. The waste can also be prepared by fragmenting or shredding it to make it more uniform in size so that the loaded waste contains only pieces of a size less than 350 mm. This pre-treatment, although optional, can significantly improve the gas permeability of the load and homogeneity of the corresponding zones.

The ratio A can also be adjusted by acting on the composition of the oxidizing gas, for example by making this gas richer or poorer in oxygen, by introducing water (liquid or vapor), carbon dioxide, etc. The use of carbon dioxide and water to regulate the oxygen content of the oxidizing gas can also have the advantage that their presence in the combustion / gasification zone displaces corresponding chemical equilibria in the direction of a stronger fuel gas production

(mainly carbon monoxide and hydrogen), which improves the calorific value of the gas produced and the efficiency of the process. In particular, carbon dioxide and water can be taken from the gaseous product. For example carbon dioxide can be obtained as a derivative product when the combustible gas is freed from sulfuric acid

(by purification by amines) and water can be obtained by condensation from the gas. To consume the water produced as a residue by the process, for example during the purification of the gaseous product, it can be injected into the combustion zone or the cooling zone where the temperature remains high (more than 400 ° C. for solids) and where an oxidizing environment prevails, which destroys the organic pollutants contained in this water. This water supply mode provides at the same time an additional means for urgently adjusting the maximum temperature in the reactor, in case the temperature exceeds the prescribed limits.

To purify the gas produced from sulfur (and other acid components such as chlorine, fluorine, etc.), a component (such as limestone or dolomite) can be introduced into the waste which reacts chemically with the acid compounds to give products which are then removed with the solid residue from the combustion.

The aforementioned report A constitutes the basic parameter for implementing the method. Indeed, the optimized process must satisfy (when this is simultaneously possible) the following criteria:

- a) high energy efficiency

- b) rapid processing rate

- c) high calorific value of the gaseous product

- d) low temperature of the gaseous product; and - e) low temperature of the solid residue.

We see that criteria (a) and (c to e) are consistent. Indeed, a high energy yield means that the energy value transmitted to the gaseous products is high and that the sensible heat of the products leaving the reactor is low. In addition, products are easier to handle when they are at low temperatures. At the same time, the criteria

(a) and (c) are simultaneously satisfied when the treatment temperature is high, that is to say when the reaction rates in the combustion zone are high and the chemical equilibria shifted in the direction of gas formation combustible. Typically temperatures above 1000 ° C. are of great interest, the maximum temperature being limited by the risks of fusion of the structures of the reactor and / or of the solids inside the reactor.

So the question is how to combine a high combustion temperature with low temperatures of solid and gaseous products. The principle of the counter-current in itself partially answers the question, since it ensures a heat exchange between the products by allowing them to release a substantial part of their sensible heat before leaving the reactor. However, the problem is not at all resolved by the prior art. The important point is that parameters that the invention intends to regulate, namely the mass fraction of oxygen in the oxidizing gas, the mass fraction of non-combustibles in the waste and the mass fraction of fuels in the waste do not allow optimal treatment ( according to the above criteria) if they are regulated one by one and not in a concerted manner.

It has been discovered that the above parameters combine to form the ratio A playing a substantial role. Indeed, the ratio (a / c) basically includes the inverse ratio of the consumption of waste to that of the gasification agent correlated to the stoichiometric ratio of oxygen and fuel consumption, which cannot vary significantly. At the same time, the mass content of the incombustibles governs the intensity of the heat exchange of the gasifying agent supplying the cooling zone and recovering the sensible heat from the solid residues. Thus, only a concerted adjustment of the three parameters entering into report A can make it possible to optimize the process. A concerted adjustment can mean that only one or two of the three parameters are actually adjusted, provided that this is done taking into account the resulting value for the ratio "A".

The effect of the absolute feed rate of the gasifying agent is that the maximum combustion temperature increases if the feed rate is higher. There are two reasons for this. The first relates to the share of heat losses in the general energy balance. Heat losses become lower when the processing rates are higher. The second relates to the kinetics of endothermic reactions in the combustion zone. At the same time, increasing the supply rate of oxidizing gas increases (the other parameters being fixed) the temperature of the gaseous product.

The mass content of fuels, which is an indirect measure of the calorific value of waste, must be taken into account and possibly regulated to be increased in extreme cases of excessively wet waste. It can be improved by additional introduction of solid fuels (insofar as this does not contravene the regulation taking account of "A") or, otherwise, by drying the waste prior to its gasification. Other features and advantages of the invention will emerge from the description below relating to non-limiting examples. In the appended drawings: FIG. 1 is a graph showing different temperatures in the process as a function of the ratio "A"; and - Figure 2 is a schematic view of a device for implementing the method according to the invention.

Figure 1 shows the dependence of the combustion temperature in an air flow, of a sample of waste comprising coal mixed with firebrick. Curve I is the calculated combustion temperature, curve II the calculated temperature of the gases leaving the reactor, and curve III the temperature of the solid residue, all three calculated for a long and isolated reactor. The abscissas represent the ratio (A). Points are experimental values for the combustion temperature in a fixed bed laboratory reactor.

It can be seen that the combustion temperatures are extremely dependent on the fuel composition and that a maximum value is reached for a certain fuel content.

In the embodiment shown as For example in FIG. 2, waste containing fuel "F" is fragmented in a shredder 1 then mixed with solid incombustibles "S" in a mixer 2 and loaded into a vertical furnace type reactor 4 via an air lock 3. The charge stacked under the effect of its own weight in the reactor 4 passes successively through drying 5, pyrolysis 6, combustion 7 and cooling 8 zones. The solid residue of combustion "R "is continuously discharged through the air lock 9 at a rate which is adjusted so as to regulate the movement of the charge downwards and thus stabilize the combustion zone at a certain level above the bottom of the reactor . The solid residue is sorted on a sieve 10, part of this residue being recycled as a solid additive "S" and the other being discharged. The air supply "L" is provided by a compressor 11 in the lower region of the reactor. The gaseous product "G" is drawn off in the upper region of the reactor and directed to a condenser 12 in which water "W" is condensed to be sent to the cooling zone to incinerate the organic pollutants dissolved therein. The gaseous product is sent to a further treatment which can include a purification and finally combustion in a boiler or a similar thermal load. The temperatures in the respective zones are continuously monitored and at least some of the parameters a, b, c mentioned above, as well as the oxidizing gas flow are adjusted while maintaining the ratio A within the prescribed limits when these temperatures deviate from their respective prescribed optimum range.

The present invention, unlike the known methods, makes it possible to efficiently gasify solid municipal waste by producing a large quantity of combustible gas, with a high energy yield. The low temperature of the gaseous product facilitates the purification of the gaseous product and prevents the polymerization of unsaturated pyrolysis oils in the conduits. At the same time, the high combustion temperature ensures a high calorific value for the non-condensed gaseous products, and a rapid treatment rate.

The present invention has just been described in a nonlimiting manner and other improvements are possible within its general framework.

Example

The present invention is further illustrated by the following example.

The incineration / gasification of waste was modeled using a fixed bed laboratory facility. The reactor was originally a refractory-coated tube having a length of 1600 mm and an inner diameter of 250 mm. The temperature along the reactor and the pressure inside it were continuously monitored. The lower region of the reactor was supplied with air or an air-vapor mixture. The gaseous product was drawn from the upper region of the reactor and sent to a water-cooled condenser, in which water and the liquid hydrocarbons were recovered from the gaseous product. The uncondensed gaseous fuel was sent to an afterburner.

The waste sample contained, in% by weight:

- food (plant) residues 35% - cardboard and paper 30%

- wood 2%

- textiles 5%

- metal 3%

- rubber and plastic 6% - glass 7%

- rock and sand 12%

This mixture was further humidified to a 40% total humidity, then it was conditioned by adding 50% by weight of pieces of refractory bricks with a size between 30 and 70 mm. During treatment, the waste burned steadily. The maximum temperature in the combustion zone was 1370 ° C, the gas produced had a temperature below 200 ° C except for a short period just before the reactor was shut down. The temperature of the solid residue in the cooling zone was 250 ° C. The weighing showed that the ash content of the waste sample was 28% (refractory bricks excluded). The recovered liquid mainly contained water, only a small fraction of about 3% of this liquid was a mixture of liquid hydrocarbons (pyrolysis oils). The uncondensed gas burned steadily in the afterburner, producing no apparent soot, dust, or smoke.

Claims

CLAIMS 1. Process for the gasification treatment of municipal solid waste or the like comprising the following steps: - the waste (F) is loaded into a reactor;

- A gasification agent (L, W) containing oxygen is injected into the reactor through a region of this reactor where the solid products of the treatment are deposited; - The solid treatment products (R) are discharged from this reactor; and

- a gaseous product (G) resulting from drying, pyrolysis and gasification is removed from this reactor, the gasification of the waste resulting from the successive passage of this waste into:

- a heating and drying area, (5),

- a pyrolysis zone, (6),

- a combustion zone (oxidation), (7), - and a cooling zone, (8), characterized by a temperature regulation process comprising maintaining the maximum temperature in the reactor in a temperature range between 700 and 1400 ° C, by setting at least one parameter chosen from the mass fraction (a) of oxygen in the gasification agent, the mass fraction (b) of the incombustibles in the feed, and the mass fraction (c ) of fuels in the load, while maintaining the ratio A = ab / c in the range of value 0.1 <A <4.0.

2. Method according to claim 1, characterized in that the maximum temperature is maintained in the range 1000 - 1200 ° C.

3. Method according to claim 1 or 2, characterized in that the ratio "A" is maintained substantially in the range of values 0.15 <A <1.0.

4. Method according to claim 1 or 2, characterized in that the ratio "A" is maintained appreciably in the range of values 0.2 <A <0.5

5. Method according to any one of claims 1 to 4, characterized in that said temperature regulation comprises maintaining the temperature of the gaseous product (G) below 400 ° C at the outlet of the reactor.

6. Method according to any one of claims 1 to 4, characterized in that said temperature regulation comprises maintaining the temperature of the gaseous product (G) below 250 ° C at the outlet of the reactor.

7. Method according to any one of claims 1 to 6, characterized in that the step consisting in adjusting at least one parameter comprises adjusting the fraction by mass (c) of the fuels in the waste by selectively introducing into the waste pieces of non-fusible non-combustible material (S) in an amount up to 200% by weight of initial waste (F).

8. Method according to claim 7, characterized in that a compound adapted to rid the gaseous product (G) of harmful components is introduced into the waste.

9. Method according to claim 8, characterized in that the component adapted to rid the gaseous product is of a type which binds chemically with said harmful compounds, giving products which are discharged from the reactor in the state incorporated in the solid products of the treatment (R).

10. Method according to any one of claims 1 to 9, characterized in that the step consisting in adjusting at least one parameter comprises adjusting the fraction by mass (c) of fuels in the waste by selective introduction into the waste solid fuel in pieces in an amount up to 30% by weight of the initial waste.

11. Method according to any one of claims 1 to 6, characterized in that the step consisting in adjusting at least one parameter comprises adjusting the fraction by mass (C) of fuels in the waste by mixing the initial waste ( F) selectively with non-combustible and combustible solid materials before loading the waste into the reactor.

12. Method according to any one of claims 1 to 10, characterized in that the step consisting in adjusting at least one parameter comprises the adjustment of a second parameter constituted by the flow of gasification agent (W, L) .

13. Method according to any one of claims 1 to 12, characterized in that water (W) and / or carbon dioxide is introduced into the gasification agent (W, L).

14. Method according to any one of claims 1 to 12, characterized in that water is injected into said combustion zone (7) and / or said cooling zone (8), where the temperature of the solids exceeds 400 ° C.

15. Method according to any one of claims 1 to 14, characterized in that the waste is prepared in pieces of size less than 350 mm before loading the waste into the reactor.

16. Method according to any one of claims 1 to 15, characterized in that the waste is treated in batches, by loading the waste (F) and discharging the solid treatment products (R) during periods of stoppage of the reactor.

17. Method according to any one of claims 1 to 15, characterized in that the waste is treated continuously, by loading the waste (F) into the reactor and discharging the solid products from the treatment (R) continuously or intermittently without interrupting the process.