WO2012069952A2

WO2012069952A2 - Macroapparatus for the production and treatment of gas

Info

Publication number: WO2012069952A2
Application number: PCT/IB2011/055064
Authority: WO
Inventors: Giovanni Cappello
Original assignee: A.G.T. S.R.L.
Priority date: 2010-11-23
Filing date: 2011-11-14
Publication date: 2012-05-31
Also published as: ITMI20102156A1; IT1403250B1; EP2643435A2; WO2012069952A3

Abstract

The invention relates to a plant 100 and a method for the production of energy from biomass BM. In the plant, a macroapparatus 10 comprises: a gasifier 12, a dedusting unit 14; an evaporative cooler 20; a scrubber 30; and a purifier 60. The cooler and the scrubber each comprise means for spraying an aqueous mixture MA into the gas G, a basin for storing a quantity of condensed aqueous mixture, a recirculation circuit for removing the aqueous mixture from the basin and supplying it to the spraying means, and a bleed for removing the condensed pollutants and conveying them to the gasifier 12. The scrubber also comprises a heat exchanger along the recirculation circuit. The purifier comprises: means for spraying the aqueous mixture removed from the cooler basin into an oxygenated gas A; means for heating the wet oxygenated gas AU above 200°C; and a catalytic oxidizer 68 for promoting oxidation of the pollutants suspended in the wet oxygenated gas AU.

Description

MACRO APPARATUS FOR THE PRODUCTION AND TREATMENT OF GAS

DESCRIPTION

The present invention relates to a macroapparatus for the production, cooling and cleaning of gas produced by a gasifier. The gasifier is suitable for producing fuel gas from biomass of different origin or from mineral coal. The cleaning apparatus is designed to purify the fuel gas produced by the gasifier.

For some time plants for the gasification of biomass, i.e. plants designed to produce fuel gas from biomass, have been known. The largest fraction of biomass (80-98%) consists of carbon (C), hydrogen (H) and oxygen (O) which are organized as different types of molecules. The remaining fraction of biomass (2-20%) consists of other molecules and other inorganic elements including in particular silicon (Si), potassium (K), calcium (Ca) and magnesium (Mg).

In a manner known per se, the main reactions which occur during gasification are as follows:

C + 0.→ CO₂ (combustion)

C + ½ O₂→ CO (partial oxidation)

C + H₂O(g)→ CO + H₂ (coal reforming)

C + CO₂→ 2CO (Boudouard reaction)

C + 2H₂→ CH₄ (methanation)

CO + H₂O(g)→ CO₂ + H₂ (water/gas shift reaction).

These reactions produce, in the presence of air, a gas (called "producer gas") composed of a mixture consisting in dry form of about 50% N₂, 20% CO, 15% H₂, 10% CO₂ and 5% CH₄. If the reactions take place without the presence of air, the final mixture does not contain N₂ and is referred to by the name of "synthesis gas" or syngas.

Various types of gasification plants are known, these differing on the basis of the reactor structure, the path followed by the gas within the reactor, the type of filtration apparatus used, etc.

Gasification plants of the known type are not, however, without defects.

The present-day gasification plants may be classified as two main types. The plants of the first type are constructed mainly for experimental purposes, are characterized by large dimensions (power output typically greater than 1 Megawatt) and use sophisticated technology. These dimensions and the fact that they are built generally on a "one-off basis" mean that these plants are not suitable for large-scale commercialization.

The plants of the second type are characterized by small dimensions, use rudimentary technology and are suitable in particular for rural environments in developing countries. The technological backwardness of these plants is such that they cannot be used on a large scale in the Western energy market.

In the 1940s extremely compact gasification plants were built. These plants were generally mounted on motor vehicles in order to compensate for the absence of petroleum-derived products. These plants in fact enabled internal combustion engines to be run using wood or wood charcoal. They were characterized by small dimensions, but were inefficient, produced a gas of unacceptable quality by modern standards and generally created serious problems in terms of environmental pollution.

Present-day internal combustion engines require gas of a very high quality. In general, further - relatively severe - restrictions are also applicable with regard to the maximum temperature of the supply gas, its relative humidity and the dewpoint of the tars present therein.

Achieving such a quality of gas, and in particular lowering the temperature of the gas used to fuel an engine, results in the formation of condensation water. This water is heavily contaminated with organic substances (phenols, ammonia, benzenes, etc.) and therefore gives rise to major problems with regard to the treatment and elimination of said substances.

The object of the present invention is therefore to provide an apparatus for cooling and cleaning the gas produced by a gasifier, which is able to overcome at least partly the drawbacks mentioned with reference to the prior art.

In particular, a task of the present invention is to provide an apparatus for cooling and cleaning the gas, which has compact overall dimensions and which can be built at a low cost and easily implemented on an industrial scale.

Moreover, a task of the invention is to provide an apparatus and a method which are able to produce high-quality gas at a temperature sufficiently low for use also in present- day internal combustion engines. Another task of the invention is to solve the problem of disposal of the polluted water which is formed during cooling of the gas and the tars produced.

This object and these tasks are achieved by means of a macroapparatus according to Claim 1 , by means of plant according to Claim 11 and by means of a method according to Claim 14.

In order to understand better the invention and to appreciate its advantages, a number of exemplary and non-limiting embodiments thereof are described below with reference to the accompanying drawings in which:

Figure 1 is a schematic view of a plant for the production of energy from biomass, comprising the macroapparatus for the production and treatment of the gas and disposal of the polluted water according to the invention;

Figure 2 is a schematic view of another plant according to invention;

Figure 3 is a schematic view of a further plant according to the invention;

Figure 4 is a diagram which illustrates the behaviour of certain types of tars upon variation in the temperature;

Figure 5 shows a perspective view of the assembly consisting of the evaporative cooler and the evaporator forming part of an embodiment of the macroapparatus according to the invention;

Figure 6 shows a plan view of the assembly according to Figure 5;

Figure 7 shows a side view of the assembly according to Figure 5;

Figure 8 shows a cross-sectional view along the line VIII- VIII of Figure 6;

Figure 9 shows a cross-sectional view of an embodiment of the gasifier forming part of the macroapparatus according to the invention, in the closed configuration;

Figure 10 shows a cross-sectional view of the gasifier of Figure 9 in the open configuration;

Figure 11 shows an enlarged view of the detail indicated by XI in Figure 9;

Figure 12 shows an enlarged view of the detail indicated by XII in Figure 10;

Figure 13 shows the diagram of a catalytic oxidizer;

Figure 14 shows the behaviour of the catalytic oxidizer upon variation in the temperature of the gas.

In the remainder of the description reference will often be made to the concepts "up", "top" or the like, and respectively to the concepts "low", "bottom" or the like. These concepts are to be understood as referring solely to the apparatus correctly assembled for operation and therefore subject to the force of gravity.

Reference will also be made, during the description of the path followed by the gas, to the concepts "upstream" and "downstream". "Upstream" is understood as meaning a position along the path, relatively close to the reactor inlet through which the biomass and the air necessary for the reactions are fed. On the other hand, "downstream" is understood as meaning a position along the path relatively far from the reactor inlet. In the accompanying figures, the reference number 100 denotes overall a plant for the production of energy from fuel, in particular from biomass BM. The plant 100 comprises firstly a macroapparatus 10 for the production and treatment of the gas G. In accordance with the embodiment shown in Figure 1 , the plant 100 also comprises, downstream of the macroapparatus 10, other components which will be described below. These further components preferably include an electrostatic filter 40 and a unit 80 for using the gas G.

The macroapparatus 10 according to the invention comprises:

- a gasifier 12 suitable for receiving a flow of oxygenated gas and fuel BM and emitting a flow of gas G;

- a line suitable for conveying the flow of gas G from the gasifier 12 to a dedusting unit 14;

- a dedusting unit 14;

- a line suitable for conveying the flow of gas G from the dedusting unit 14 to an evaporative cooler 20;

- an evaporative cooler 20 suitable for treating the flow of gas G, comprising:

- means 21 for spraying an aqueous mixture MA into the flow of gas G,

- a basin 22 suitable for allowing settling and storage, in the evaporative cooler 20, of a quantity of aqueous mixture MA in the condensed state,

- a recirculation circuit 23 suitable for removing the aqueous mixture MA from the basin 22 and supplying it to the spraying means 21 of the evaporative cooler 20; and

- a /bleeder pipe 24 suitable for removing the condensed pollutants from the bottom of the basin 22 and conveying them to the gasifier 12;

- a line suitable for conveying the flow of gas G from the evaporative cooler 20 to a scrubber 30;

- a scrubber 30 suitable for treating the flow of gas G, comprising:

- means 31 for spraying an aqueous mixture MA into the flow of gas G;

- a basin 32 suitable for allowing settling and storage, in the scrubber 30, of a quantity of aqueous mixture MA in the condensed state;

- a recirculation circuit 33 suitable for removing part of the aqueous mixture MA from the basin 32 and supplying it to the spraying means 31 ;

- a bleeder pipe 34 suitable for removing the condensed pollutants from the bottom of the basin 32 and conveying them to the gasifier 12;

- a heat exchanger 35 located along the recirculation circuit 33 of the scrubber 30; and

- a compensation pipe 37 suitable for removing part of the aqueous mixture MA from the basin 32 and supplying it to the basin 22 of the evaporative cooler 20;

- a line suitable for conveying the flow of gas G from the scrubber 30 outside of the macroapparatus 10.

Finally, the macroapparatus 10 according to the invention comprises a purifier 60 suitable for receiving a flow of oxygenated gas A and aqueous mixture MA and for emitting a flow of purified wet oxygenated gas AU, the purifier 60 comprising in turn:

- a line 61 for supplying a flow of oxygenated gas A;

- an evaporator 63 having means 630 for spraying an aqueous mixture MA into the flow of oxygenated gas A;

- a pipe 65 suitable for removing a quantity of aqueous mixture MA from the basin 22 of the evaporative cooler 20 and supplying the aqueous mixture MA to the spraying means 630 of the evaporator 63;

- a line 62' suitable for conveying the wet oxygenated gas AU from the evaporator 63 to heating means 67;

- means 67 for heating the wet oxygenated gas AU, suitable for raising its temperature to beyond 200°C;

- a line 62" suitable for conveying the wet oxygenated gas AU to a catalytic oxidizer 68; - a catalytic oxidizer 68 suitable for promoting oxidation of the organic pollutants suspended in the wet oxygenated gas AU; and

- a line suitable for introducing into the atmosphere the wet oxygenated gas AU purified downstream of the catalytic oxidizer 68.

The macroapparatus 10 described above may preferably comprise one or more of the following auxiliary components:

- a pipe 27 suitable for introducing water from the outside into the macroapparatus 10, for example supplying it to the spraying means 21 or to the basin 22 of the evaporative cooler 20;

- a discharge pipe 36 suitable for removing the excess aqueous mixture MA from the basin 32 of the scrubber 30 and conveying it externally; and/or

- a recirculation circuit 64 suitable for removing any condensed aqueous mixture MA from the bottom of the evaporator 63 and conveying it to the basin 22 of the evaporative cooler 20.

Patent application WO 2008/096387, in the name of the same applicant, describes a gasification plant which, in the general configuration and in the aspects known per se, is similar to the plant 100 considered here. Reference should be made to this document for those aspects which are not dealt with in detail in the description below.

The gasifier 12 is suitable, in a manner known per se, for treating different fuels such as biomass of various kinds, charcoal or mineral coal.

The gasifier 12 is preferably of the downdraft (or downdraught) type known per se. In this type of gasifier the fuel BM is introduced into the reactor from above, the gasification reactions occur in the bottom part of the reactor and the gas produced is removed from the bottom of the reactor. This type of gasifier therefore differs from other - so-called updraft - gasifiers in which the gas produced is removed from the top of the reactor.

The downdraft gasifier offers a number of notable advantages during the gasification of biomass. In particular it produces a gas with a limited tar content, thus facilitating the subsequent cleaning thereof. Moreover, the downdraft gasifier, as a by-product of gasification of biomass, produces a carbonaceous residue, known as charcoal, the demand for which is constantly increasing. Said charcoal is in fact used to improve the fertility of terrain (in this sense it is known as "biochar") and in particular to fix in an extremely stable manner the carbon present in the biomass. This carbon originates from the carbon dioxide (CO₂) drawn from the atmosphere by the biomass.

The gasifier 12 is preferably of the downdraft open-top or open-core type known per se. In this type of gasifier, the oxygen which is needed for the reactions of combustion and partial oxidation of the carbon is generally provided by the air which is drawn in from the environment at atmospheric pressure via the top inlet of the reactor. This type of gasifier therefore differs from other types in which the oxygen which is necessary for the combustion/gasification reactions is supplied at a pressure greater than atmospheric pressure by a suitable plant or is injected at given points directly inside the reactor. This solution is adopted for example in the so-called Imbert gasifier.

In accordance with other possible embodiments aimed at achieving a greater percentage amount of oxygen 0₂ in the air drawn in by the gasifier 12 a plant for supplying oxygen 0₂ under pressure, for example a cylinder or other pressurised oxygen storage vessel, is envisaged. With these embodiments there exists the possibility of potentially increasing, as required, the percentage amount of oxygen 0₂ in the air flow which is drawn in. The composition of the drawn air may therefore vary between that of ambient air (i.e. a mixture containing about 20% oxygen) and that of pure oxygen (100% 0₂), the intermediate compositions generally being able to be defined as oxygenated air. The increase in the percentage amount of oxygen may be useful in certain particular operating conditions of the gasifier 12 for more effective gasification of certain particular fuels, for example sludges. The expression "oxygenated gas" used below refers generally to ambient air, oxygenated air or pure oxygen.

Finally, this type of gasifier generally has cylindrical reactors with a constant cross- section, without throats or constrictions (throatless), which allow the use of low density biomass BM.

The open-core gasifier has the advantage of being very simple and economical in terms of construction and management. Moreover, with the open-core gasifier it is possible to gasify biomass with low-melting ash having a very low density such as biomass of the herbaceous type.

Figures 9 to 12 show a particular embodiment of the gasifier 12 included in the macroapparatus 10 according to the invention.

According to this embodiment, the gasifier 12 comprises means 120 for raising the outer jacket 121.

Figure 9 shows the gasifier 12 in the closed configuration. This configuration is the configuration which is maintained during operation of the gasifier 12, but also during the normal non-operative periods. In this configuration, the outer jacket 121 therefore separates the inside of the gasifier 12 from the external environment.

Figure 10 shows the same gasifier according to Figure 9, but in its open configuration. This configuration is the configuration which is maintained during maintenance of the gasifier, typically during the removal of foreign bodies 123. In this configuration, the outer jacket 121 is raised and therefore defines an opening which establishes communication between the inside of the gasifier 12 and the external environment. A fairly common occurrence is the involuntary introduction into the gasifier 12, during introduction of the biomass BM, of foreign bodies 123. These foreign bodies 123 are typically bodies which, owing to their physical and chemical nature, are unable to take part in the gasification reactions, i.e. typically stones or metal waste. For this reason, the foreign bodies 123 pass through all the zones of the gasifier 12, their structure and mass remaining more or less unchanged, and are deposited finally on the bottom grille 122 supporting the biomass BM.

The accumulation of foreign bodies 123 on the bottom grille 122 may in the long run result in an unacceptable alteration in the process conditions, for example owing to the constriction which they form in the flow cross-section of the gas G leaving the gasifier. In the light of the above, it is therefore required to remove periodically the foreign bodies 123 from the bottom grille 122.

In this connection, operation of the gasifiers of the known type must be periodically interrupted in order to allow disassembly of the outer casing of the reactor so that the grille can be accessed. This solution, although widely used, results in long downtimes of the plant, said downtimes being necessary in order to allow cooling of the reactor and enable the operating staff to disassemble the reactor, remove the foreign bodies 132 and restore the working configuration of the reactor. As the person skilled in the art can easily understand, these long downtimes have a negative impact on the productivity of the plant.

With the embodiment of the gasifier 12 shown in Figures 9 to 12 it is instead possible to complete the operation of removal of the foreign bodies 123 in an extremely simple manner. The raising means 120 in fact allow the outer jacket 121 of the reactor to be raised so that there is direct access to the bottom grille 122. Removal of the foreign bodies 123 may thus be performed in a simple and rapid manner, without the need for lengthy stoppage of the plant.

Figures 11 and 12 show a detail of the raising means 120, in the closed operating configuration and in the open maintenance configuration, respectively. In the specific embodiment shown in the figures, the raising means 120 comprise a plurality of jacks which are arranged on the outer perimeter of the jacket 121.

As already mentioned above, the chemical reactions which take place inside the downdraft reactors do not manage to produce complete gasification of the biomass BM and therefore release, in addition to the produced gas flow G, solid residue in the form of charcoal dust. As described above, this charcoal dust may be used for interesting applications from an agricultural and/or environmental point of view. As an alternative to said applications, the charcoal may be further exploited for energy-related purposes. In accordance with certain embodiments, such as that shown in Figure 3, the macroapparatus 10 also comprises an auxiliary gasifier 125 which is suitable for the gasification of the charcoal dust C which is discharged from the first gasifier 12 as residue of the gasification reactions of the biomass BM.

The auxiliary gasifier 125 is preferably of the type suitable for gasification of dust-like masses and typically may have an updraft and open-core structure.

In accordance with this embodiment of the macroapparatus 10, the auxiliary gasifier 125 comprises a line 69 suitable for supplying the wet oxygenated gas AU output by the evaporator 63 of the purifier 60. The advantages arising from the use of the wet oxygenated gas AU inside the auxiliary gasifier 125 will be described below. Another line 126 is designed to convey the gases produced by gasification of the charcoal C from the auxiliary gasifier 125 to the main gasifier 12.

According to certain embodiments, not shown in the accompanying figures, the macroapparatus 10 also comprises means for evacuation of the dust and/or ash which collects, respectively, inside the gasifier 12, the dedusting unit 14 and (if present) the auxiliary gasifier 125.

These means comprise advantageously one or more screw conveyors which are designed to remove the dust and/or ash and to convey them to special collection or storage containers. Moreover, the dust and/or ash evacuation means preferably comprise valves which are designed to allow the dust and/or ash to be removed from the macroapparatus 10, without at the same time allowing the entry of ambient air inside the macroapparatus 10. These valves are particularly advantageous in the case where the inside of the plant 100 is kept under a vacuum in order to obtain the movement of the gas G along the plant itself. In this case, the absence of the valve on the dust outlet from the gasifier would result in the entry of air and the consequent explosion of the gasifier 12 itself.

The gas G leaving the gasifier 12 has a temperature of about 400°C - 800°C and conveys a considerable quantity of pollutants. The main pollutants are dust from charcoal, ash and tars in the vaporized or atomized state. The gas G, in order to be effectively used in a user unit 80, must be as far as possible free of pollutants and must be cooled down to a temperature below 70C° and preferably below 60C°.

The unit 14 for dedusting the gas G may for example comprise a cyclone (see for example the scheme in Figure 1) or a high-temperature ceramic filter (not shown). Both these solutions are not described here in detail since they are well known per se to the person skilled in the art.

The evaporative cooler 20 is designed to obtain initial cooling of the gas G by means of evaporation of a water-based mixture MA until the gas G is saturated. In other words, the spraying means 21 situated inside the evaporative cooler 20 spray the aqueous mixture MA into the flow of gas G. Part of this mixture MA evaporates, absorbing the heat and therefore lowering the temperature of the flow of gas G. This mechanism functions efficiently until the vapours produced by the evaporation of the aqueous mixture MA saturate the gas G.

In the embodiments described below it is considered that the aqueous mixture MA comprises mainly water, polar (hence water-soluble) tars and non-polar (non-soluble) tars.

In other possible embodiments of the apparatus 10 the aqueous mixture MA could also comprise other additives which are suitable for solving specific contingent problems. These additives may be in the form of a solution, emulsion, suspension or in any case mixed with water. One of these additives may, for example, comprise particles of calcium hydroxide Ca(OH)₂ which, in an aqueous suspension, form so-called lime milk. The use of lime milk allows neutralization of any acid compounds present in the gas G. Another useful additive could in some cases be an anti-foaming agent.

In general, the aqueous mixture MA also comprises traces of the other elements present in the gas G, such as carbon (C) in the form of charcoal and other inorganic elements in the form of ash such as silicon (Si), potassium (K), calcium (Ca) or magnesium (Mg). As already described above, the spraying means 21 may advantageously comprise a connection 27 to the water mains or to some other water supply outside the plant 100. It is thus possible to compensate for any water losses occurring in the evaporative cooler 20 or downstream thereof.

The evaporative cooler 20 also comprises a basin 22 which stores a quantity of aqueous mixture MA in the condensed state. The presence of the mixture MA in the liquid phase ensures effective saturation of the gas G passing through the evaporative cooler 20, but in particular is necessary in order to be able to achieve effective washing of the gas G. A quantity of aqueous mixture MA much greater than that required to saturate the gas G is injected into the evaporative cooler 20 by the spraying means 21. The excess quantity of aqueous mixture MA which therefore passes through the gas G in the liquid state results in removal of the suspended condensed tars and the fine dust which cannot be retained by the dedusting means 14. Obviously the aqueous mixture MA which is sprayed in excess of that producing saturation of the gas G, and which therefore remains in the liquid state, is collected inside the basin 22.

The temperature of the gas G leaving the evaporative cooler 20 depends on the concentration of tars in the aqueous mixture MA and the type of said tars. At the end of an initial transient state, the operating parameters of the evaporative cooler 20 stabilize. If the evaporative cooler 20 is correctly dimensioned, the saturated gas G and the condensed aqueous mixture MA have practically the same temperature. In this operating condition, cooling of the gas G occurs almost exclusively by means of absorption of latent evaporation heat by the aqueous mixture MA. If pure water were used in place of the aqueous mixture MA, the equilibrium temperature inside the evaporative cooler 20 would stabilize at about 80°C. With an increase in the concentration of tars in the aqueous mixture MA the ebullioscopic constant of the aqueous mixture MA also increases and therefore the equilibrium temperature rises.

The basin 22 of the evaporative cooler 20 is preferably formed so that it is possible to achieve efficient sedimentation of the non-soluble tars in the aqueous mixture MA, the charcoal dust and the ash produced by the gasifier 12 and not eliminated by the dedusting unit 14 so that the concentration thereof suspended in the aqueous mixture MA is as low as possible. These separated tars and dusts are then discharged via the pipe 24 to the gasifier 12 for gasification and subsequent elimination.

At the tar concentration levels in the mixture considered advantageous for operation of the evaporative cooler 20, the equilibrium temperature is preferably between 75 °C and 90°C. This temperature is achieved by favouring the sedimentation of a given quantity of non-soluble tars in the aqueous mixture present in the basin 22. In this case the aqueous mixture MA has a particularly low viscosity which favours the use of low-cost centrifugal pumps. If the concentration of water in the mixture MA should decrease, the evaporative cooling effect would gradually decrease causing a rise in temperature of the mixture.

The use of evaporative cooling of the gas G, which occurs generally at temperatures higher than 80°C, eliminates the need to cool the aqueous mixture MA by means of a heat exchanger located along the recirculation circuit 23 supplying the spraying means 21.

A heat exchanger located along this recirculation circuit 23 would in fact be easily soiled and would therefore require frequent maintenance. The aqueous mixture MA contains in fact a large quantity of tars which complicate and increase the cost of any heat exchange in a conventional heat exchanger, for example of the tube bundle type. Moreover, in order to obtain a suitable heat exchange action, the surfaces of the heat exchanger should be substantially colder than the aqueous mixture MA flowing over them. This would thus cause a localized increase in the viscosity of the aqueous mixture MA, with consequent problems, both of a thermal nature (poorer heat transmission) and of a hydraulic nature (clogging of the exchanger).

Figure 4 is a diagram which illustrates the behaviour of different tar fractions upon variation in the temperature. As can be seen, the different tar fractions have behaviours which are markedly different at the same temperature.

In particular, at an equilibrium temperature plausible for operation of the evaporative cooler 20, for example at the temperature of 85°C, different phases coexist. There are lighter tars (aromatic tars) which are entirely in the vapour phase, other tars (light polyaromatic and heterocyclic tars) which are partly in the vapour phase and partly in the condensed phase and, finally, there are heavier tars (heavy polyaromatic tars) which are completely in the condensed phase.

The condensed tars are collected in the basin 22 together with water, forming the aqueous mixture MA. The aqueous mixture MA comprises both polar tars which pass into solution and non-polar tars which generally have a density greater than water and which, if left to settle suitably, form layers on the bottom of the basin 22.

The bleeder pipe 24 is designed to remove from the bottom of the basin 22 most of the sedimented tars which collect there. They must be removed from the basin 22 in order to maintain the correct quantity of mixture MA inside the evaporative cooler 20. Moreover, the condensed tars present in the mixture MA may be usefully conveyed back to the inlet of the gasifier 12 and subjected again to the oxidation and gasification processes. Tars are in fact colloidal systems comprising a large quantity of organic substances, in particular heterocyclic and aromatic polycyclic hydrocarbons. From the tars it is therefore possible to extract a further quantity of gas G.

In the accompanying Figures 1 to 3, the evaporative cooler 20 is shown in the form of a duct along which the flow of gas G travels in a substantially horizontal direction. Inside the duct the aqueous mixture MA is sprayed in the same direction as that of the gas flow. The basin 22 is formed at a bottom point of the duct and the condensed mixture MA collects there by means of gravity.

In accordance with that shown in the accompanying Figures 5 to 8, the evaporative cooler 20 may have the structure of a duct along which the flow of gas G travels in a substantially vertical direction. Inside this duct the aqueous mixture MA is sprayed for example in the same direction as that of the flow of gas G. The basin 22 is formed at the bottom of the duct and the condensed mixture MA collects there by means of gravity, in a similar manner to that described above.

The evaporative cooler 20 preferably comprises shredder means 25 for breaking up the encrustations which form inside it during treatment of the flow of gas G.

The shredder means 25 are preferably situated between the upper zone where spraying of the aqueous mixture MA take place and the basin 22 inside which the aqueous mixture MA collects in the condensed state.

The shredder means 25 preferably comprise a series of blades 250 movable with respect to a grille 251. In accordance with the embodiment shown in Figure 8, the blades 250 are mounted radially on a rotating shaft arranged in the vicinity of the surface of the grille 251. In accordance with this embodiment, following rotation of the shaft, the blades 250 periodically pass through the surface of the grille 251.

Below it is described how a number of undeniable advantages may be achieved with this solution. Firstly it must be mentioned here that, in this zone of the plant 100, the flow of gas G conveys along with it a large quantity of pollutants since it has been treated only by the dedusting unit 14. Most of the pollutants (whether they be in the form of vapours, aerosols or fine dust) are preferably removed further downstream, typically inside the electrostatic precipitator 40 (described in detail below).

Inside the evaporative cooler 20 the flow of gas G undergoes a drastic reduction in temperature: from about 400-800°C to about 75-100°C, preferably about 80° C. Owing to said cooling, some of the tars condense to form droplets which, in turn, act as aggregation nuclei for the dust present in the gas G.

The phenomenon described above therefore produces, in the zone where the flow of hot gas G encounters the flow of sprayed aqueous mixture MA, the formation of solid or semi-solid encrustations which may also be of considerable size. These encrustations, separating from the walls of the evaporative cooler 20, may also be conveyed into the basin 22 and prevent correct operation thereof. The encrustations are in fact of a size such as to cause blockage of the bleeder pipe 24 and/or the recirculation circuit 23 in a very short amount of time.

The shredder means 25 reduce instead the size of these encrustations so as to allow them to flow out correctly through the bleeder pipe 24. In particular, during operation of the evaporative cooler 20, the encrustations are deposited by means of gravity onto the grille 251 where the regular passing movement of the blades 250 breaks them down into parts sufficiently small for them to be able to fall through the grille 250 and then be conveyed together with the liquid tars through the bleeder pipe 24.

As may be noted in Figure 8, in this particular embodiment of the evaporative cooler 20, a screw conveyor 220 is provided on the bottom of the basin 22 so as to be able to remove all the pollutants which collect there (whether they be more or less fluid tars or pieces of the encrustations previously broken up by the shredder means 25).

The basin 22 also comprises an outlet suitable for removing the aqueous mixture MA. This outlet is situated in a position within the stored quantity of aqueous mixture MA so as not to draw off either the heavier pollutants which are deposited on the bottom of the basin 22 or the foam and the lighter pollutants which float on the surface of the aqueous mixture MA. The outlet supplies the recirculation circuit 23 which delivers the aqueous mixture MA to the spraying means 21 of the evaporative cooler 20. Moreover the outlet also supplies the pipe 65 which delivers the aqueous mixture MA to the spraying means 630 of the evaporator 60.

As already mentioned above, the scrubber 30 comprises a heat exchanger 35 situated along the recirculation circuit 33. The heat exchanger 35 is designed to cool the aqueous mixture MA along the path which it follows towards the spraying means 31 , so that the aqueous mixture MA may in turn cool the gas G inside the scrubber 30.

Moreover, the scrubber 30 may advantageously comprise a discharge pipe 36 suitable for removing the excess aqueous mixture MA from the basin 32 and conveying it externally.

Inside the scrubber 30 the gas G is cooled down to the temperature required for correct operation of the gas user unit 80, which temperature is typically between 40°C and 50°C. During the process of cooling of the gas G, most of the water and the tars which are present in the gas G in the vapour phase upon leaving the evaporative cooler 20 are condensed. These condensed products accumulate in the basin 32 forming the aqueous mixture MA. This aqueous mixture MA is continuously removed and pumped to the evaporative cooler 20 via the proper compensation pipe 37.

In this connection it should be noted that in the evaporative cooler 20 the quantity of mixture MA present in the condensed state in the basin 22 gradually diminishes owing to its continuous evaporation within the flow of gas G. On the other hand, inside the scrubber 30 the quantity of mixture MA present in the condensed state in the basin 32 increases gradually owing to the continuous condensation of the vapours present in the gas G during cooling. In the macroapparatus 10 according to the invention the excess amount of aqueous mixture MA present in the basin 32 is therefore used in order to supplement in a continuous manner the losses of mixture MA inside the basin 22.

If the temperature of the gas G leaving the scrubber 30 is higher than that of the dewpoint of the gas G, the condensed water inside the basin 32 is less than the water evaporated inside the evaporative cooler 20. In these operating conditions, even displacing continuously the aqueous mixture MA from the basin 32 to the basin 22, it is required to introduce water into the macroapparatus 10 drawing upon an external supply via the line 27.

If the temperature of the gas G leaving the scrubber 30 is the same as the temperature of the dewpoint of the gas G, the condensed water in the basin 32 is equal to the evaporated water in the evaporative cooler 20. In these operating conditions, by displacing continuously the aqueous mixture MA from the basin 32 to the basin 22, the macroapparatus 10 is in hydric equilibrium.

If the temperature of the gas G leaving the scrubber 30 is lower than that of the dewpoint of the gas G, the condensed water in the basin 32 is greater than the evaporated water in the evaporative cooler 20. In these operating conditions, even displacing continuously the aqueous mixture MA from the basin 32 to the basin 22, it is required to dispose of water from the macroapparatus 10 externally. This water disposal may be effectively performed by means of the purifier 60, as previously mentioned and as will be described in greater detail below.

According to certain embodiments of the invention, the macroapparatus 10 comprises a heat exchanger instead of the scrubber 30. This heat exchanger is preferably of the tube- bundle type in which the hot gas G exchanges heat with a service liquid.

Moreover, the evaporative cooling of the gas G produces a supply of water at a high temperature, generally equal to or greater than 80°C; this supply allows water vapour to be produced in an economic and in particular very convenient manner from an energy point of view, for example by means of the evaporator 63 of the purifier 60.

The water vapour may be usefully evacuated externally in order to improve the conditions of the process and in particular allow lowering of the temperature of the gas G below its dewpoint, as will be described below.

The purifier 60 is thus able to dispose of any excess aqueous mixture MA. Said disposal represents a problem for plants of the known type since the aqueous mixture MA which must be disposed of is contaminated by a large quantity of pollutants which are dangerous both for man and for the environment.

As already mentioned above, downstream of the evaporator 63 the purifier 60 comprises means 67 for heating the wet oxygenated gas flow AU. These means may assume different embodiments. They may comprise for example a heat exchanger 670 in which the wet oxygenated gas AU may absorb heat from another hot fluid, for example from the gas G leaving the gasifier 12. Alternatively, the means 67 may comprise a manifold 671 which causes the wet oxygenated gas AU to merge with another flow of hot gases directed towards the catalytic oxidizer. These embodiments of the heating means 67 are described in greater detail below.

Since the temperature of the aqueous mixture MA sprayed into the evaporator 63 is about 80°C, the mass of water which evaporates is equal to about 0.5 kg for each kilogram of oxygenated gas A, for example air.

This evaporation inside the purifier 60 allows elimination of the excess liquid water which condenses inside the macroapparatus 10 in the case where the gas G is to be cooled to below its dewpoint temperature, typically below about 60°C. During this step moreover a quantity of heat made available at a low temperature, and therefore not able to used for other purposes, is used.

The pollutants present in the aqueous mixture MA are typically hydrocarbons such as phenols, benzenes, toluenes, xylenes or naphthalenes, so that the disposal of the excess mixture MA is difficult and costly.

By way of example, the presence of phenols within the aqueous mixture suppresses the bacterial flora present normally in the systems for civil and industrial water treatment systems, not allowing in fact the disposal of the aqueous mixture MA via the sewage system. The wet oxygenated gas AU containing hydrocarbons in the vapour state leaving the evaporator 63 has typically a temperature close to the temperature of the water of the aqueous mixture MA present in the basin 22 (about 80°C) and must be heated to above 200°C, preferably above 300°C so as to be then usefully conveyed to the catalytic oxidizer 68 (see the graph in Figure 14 in this connection). Inside the catalytic oxidizer 68 the hydrocarbons HC present in the wet oxygenated gas flow are converted, in a manner known per se, into H₂0 and C0₂. At the outlet of the catalytic oxidizer 68 the wet oxygenated gas flow AU, since it contains no longer hydrocarbons, but only water vapour H₂0(g) and C0₂, may be readily discharged into the atmosphere without any danger for the environment and for health (see the diagram in Figure 13 in this connection).

The flow of wet oxygenated gas AU may be generated in different ways. One extremely simple way is that of using a fan 66 mounted so as to draw air from the environment and blow it into the line 61 leading to the purifier 60. As an alternative or in addition to the fan 66, another fan (not shown) may be mounted so as to draw the oxygenated gas AU already treated by the evaporator 63 and/or the catalytic oxidizer 68. These solutions envisage therefore the use of ambient air as oxygenated gas A.

In accordance with other possible embodiments, intended to obtain a greater percentage of oxygen 0₂ in the oxygenated gas A, a system for supplying oxygen 0₂ under pressure, for example a gas cylinder or other pressurized oxygen tank, is provided alongside or instead of the fans. These embodiments potentially enable the percentage of oxygen 0₂ in the oxygenated gas flow to be increased as required. The composition of the oxygenated gas A may therefore vary between that of air (i.e. a mixture containing about 20% oxygen) and that of pure oxygen (100% 0₂), the intermediate compositions being generally definable as oxygenated air. The increase in the percentage of oxygen may be useful in certain particular cases of operation of the catalytic oxidizer 68 for more efficient distribution of the hydrocarbons HC.

Figure 1 shows a first embodiment of the purifier 60 for disposal of the aqueous mixture MA and the associated pollutants. According to this embodiment the means 67 for heating the wet oxygenated gas AU comprise a heat exchanger 670. This heat exchanger 670 is suitable for generating a heat exchange between the flow of gas G output from the gasifier 12 (which is typically at a temperature of about 600°C) and the wet oxygenated gas flow AU output from the evaporator 63 (which is typically at a temperature of about 80°C).

The heat exchanger 670 is not particularly subject to contamination due to condensation of the tars and the coal dust present in the gas G since the quantity of heat to be exchanged in order to raise the temperature of the wet oxygenated gas AU from about 80°C to about 300°C is limited with respect to all the sensible heat available in the gas G. In view of the above there is minimum cooling of the gas G and, consequently, minimum condensation of the tars and adhesion of the dust. The catalytic oxidizer 68 is therefore situated downstream of the heat exchanger 670 and the wet oxygenated gas AU reaches it at a temperature of about 300°C. After passing into the catalytic oxidizer 68, the flow of wet oxygenated gas AU, now clean, is introduced directly into the atmosphere.

Figure 2 shows a second embodiment of the purifier 60 for disposal of the aqueous mixture MA and associated pollutants. This embodiment is suitable for use in plants 100 where the unit 80 using the gas G is a thermal unit, typical an internal combustion engine or a burner. According to this embodiment, the means for heating the wet oxygenated gas AU comprise a manifold 671 suitable for causing merging of the flow of wet oxygenated gas AU (which is typically at a temperature of about 80°C) with the flow of exhaust gases from the user unit 80 (typically having a temperature of about 400-500°C).

The wet oxygenated gas AU is thus mixed with the exhaust gases of the user unit 80 and the gaseous mixture thus obtained is then supplied to the catalytic oxidizer 68 and then dispersed into the atmosphere.

This solution is particularly advantageous in the case where, as commonly occurs in the case of commercially available internal combustion engines, the user unit 68 is already equipped with its own catalytic oxidizer 68. There is therefore preferably just one common catalytic oxidizer 68 for the purifier 60 and the user unit 80.

According to this configuration, the quantity of sensible heat present in the exhaust gases and the corresponding temperature level are able to ensure that the final gaseous mixture, obtained from introduction of the wet oxygenated gas AU into the exhaust gases, has a temperature higher than 200°C, typically higher than 300°C. At this temperature, it is therefore possible, by means of the catalytic oxidizer 68, to eliminate the hydrocarbons present in the gaseous mixture and therefore prevent them from being definitively introduced into the atmosphere.

Figure 3 shows a further embodiment of the plant 100, comprising a different system for disposal of the aqueous mixture MA and the associated pollutants. According to this embodiment, the macroapparatus 10 further comprises auxiliary gasifier 125 described above.

According to this embodiment, part of the wet oxygenated gas at the temperature of about 80°C is conveyed to the auxiliary gasifier 125, while the remainder is conveyed to the heating means 67 and then to the catalytic oxidizer 68. In this type of plant, the means 67 for heating the wet oxygenated gas AU may comprise both a heat exchanger 670 as in the plant of Figure 1 and a manifold 671 as in the plant according to Figure 2. For this reason, in Figure 3 the means 67 for heating the wet oxygenated gas AU are shown very schematically.

The gases produced by the gasification of the charcoal C in the auxiliary gasifier 125 (i.e. H₂, H₂O, N₂, CO, CO₂) are conveyed via a proper line 126 into the top part of the reactor of the gasifier 12. These products have a temperature of about 400-800°C and, by mixing with the comburent oxygenated gas flow which enters into the gasifier 12, assist the gasification reactions described above, in particular the coal reforming reaction, the Boudouard reaction and the methanation reaction.

The coal reforming reaction, which is favoured by the presence of water vapour H₂0_(g) in the oxidation zone of the reactor as well as the Boudouard reaction (also described above) are highly endothermic reactions. These reactions therefore absorb the heat released by the other exothermic reactions which occur inside the gasifier 12 (typically the reactions produced by combustion of the carbon and the pyrolysis gases) and thus limit the temperatures in the oxidation zones to values in the region of 800°C-900°C. These considerations, which are important for the gasifier 12, are even more important for the auxiliary gasifier 125, owing to the fact that it operates substantially in the presence of carbon C alone. The generalized combustion reaction of the carbon C could result in extremely high temperatures, in excess of 1500°C, being reached inside the auxiliary gasifier 125. The introduction of water vapour H₂0_(g) into this type of reactor and the consequent generation of endothermic reactions is therefore even more important in order to limit the temperature inside the reactor.

As already explained above, the aqueous mixture MA, removed from the basin 22 and sprayed into the evaporator 63 of the purifier 60 at a temperature equal to or greater than 80°C, enables a significant flow of oxygenated gas A to be easily saturated with water vapour H₂0_(g). It is thus possible to convey a significant amount of water vapour H₂0_(g) inside the auxiliary gasifier 125. Moreover, as already explained above, the heat required to obtain evaporation of the water which saturates the flow of oxygenated gas A is provided by cooling the aqueous mixture MA.

This heat, owing to the relatively low temperature at which it is available, may not generally find a useful application. On the other hand, in the case of the macroapparatus 10 according to the invention, this heat may be used to improve gasification of the charcoal C in the auxiliary gasifier 125. All this enables the energetic efficiency and the overall quality of the entire gasification process to be increased. The increase in the energetic efficiency may be as high as about 15%-20% depending on the type of biomass BM and its ash content, this meaning a reduction in the specific consumption of biomass BM of up to about 15-20% and an increase in the amount of hydrogen H₂ contained in the gas G produced by the plant.

This increase in the energetic efficiency is due to the use of part of the carbon content of the biomass BM which cannot be completely used in the main downdraft gasifier 12. In fact the final residue of the auxiliary updraft gasifier 125 is formed solely by inorganic ashes.

It should be noted here that another solution is known for generating steam, said solution being historically used in mineral coal gasifiers. This known solution makes use of the high-temperature heat which is available on the outer walls of the reactor. A solution of this type, however, does not produce advantages in energy terms since the heat required for evaporation of the water is extracted from the gasification reactions. Figures 5 to 8 show an embodiment of the evaporative cooler 20 and the evaporator 63 of the purifier 60 which are integrated in a single assembly 50. This embodiment of the invention is particularly advantageous. It in fact enables the heat dispersion to be minimized along the line supplying the aqueous mixture MA from the basin 22 to the spraying means 630 of the evaporator 63. To ensure optimum operation of the invention, the aqueous mixture MA must in fact be sprayed at the highest possible temperature from among those already available inside the plant 100. The high temperature of the aqueous mixture MA (equal usually to about 80°C) ensures efficient saturation of the flow of oxygenated gas A. In view of the above, the use of heat made available by the plant 100 avoids having to resort to external heat sources which would result in a drastic reduction in the overall energetic efficiency of the process.

In accordance with the embodiments shown in the accompanying figures, the plant 100 also comprises an electrostatic precipitator 40 suitable for treating the flow of gas G already treated by the macroapparatus 10. The gas G leaving the macroapparatus 10 has in fact undergone the desired cooling and initial dedusting, but still contains several pollutants in suspended form. These pollutants (fine dusts, tars in aerosol and vapour form) may be advantageously removed from the gas G by means of an electrostatic precipitator 40.

In particular, the plant 100 preferably comprises a wet electrostatic precipitator (WESP) 40 of the type known per se. Said precipitator comprises ducts inside which an electrostatic field is maintained. In particular, the electrostatic precipitator 40 comprises preferably tubular structures inside each of which an electrode is arranged. An electrostatic field may thus be formed inside each tubular structure, between the walls and the central electrode.

Moreover, the precipitator 40 may comprise preferably:

- a tank 42 suitable for collecting the tars and the water removed from the gas G;

- a bleeder pipe 44 suitable for removing the condensed tars from the bottom of the tank 42 and conveying them to the gasifier 12;

- a discharge pipe 46 suitable for removing the excess aqueous mixture from the tank 42 and conveying it towards the basin 32; and

- an output line 18 suitable for conveying the flow of clean gas G to a user unit 80.

The electrostatic precipitator 40 allows the gas G to be cleaned of the suspended pollutants so as to obtain the desired quality for the user unit 80. Cleaning of the gas is performed, in a manner known per se, by means of electrostatic attraction exerted on the pollutants by the walls of the precipitator 40.

Immediately upstream of the electrostatic precipitator 40, cooling of the gas G inside the scrubber 30 causes condensation of the vapours still present inside it. The formation of water droplets provides condensation nuclei for the tar molecules and, vice versa, the formation of tar droplets provides condensation nuclei for the water molecules. In this way the aqueous mixture MA is converted from the vapour phase to the liquid phase, thus forming a tar and water aerosol.

Once it has reached the inside of the electrostatic precipitator 40, the aerosol suspended in the gas G is attracted towards the walls of the precipitator itself by the effect of the electrostatic field maintained within it. The aerosol therefore adheres to the walls of the precipitator 40 and, flowing along the walls, is collected inside the tank 42.

With reference again to the diagrams shown in Figures 1 to 3, it is possible to note how the condensed liquids, which are removed from the gas G inside the electrostatic precipitator 40, are collected inside the tank 42 also provided with a bleeder pipe 44. In a similar manner to that already described above with reference to the bleeder pipes of the basins 22 and 32 of the evaporative cooler 20 and the scrubber 30, respectively, the bleeder pipe 44 also allows removal from the bottom of the tank 42 of at least part of the aqueous mixture MA. The mixture removed contains water, polar tars in solution form and in particular non-polar (water-insoluble) tars which collect on the bottom of the tank 42. For this reason, the bleeder pipe 44 draws advantageously from a bottom point of the tank 42 where the heavier non-polar tars spontaneously collect by means of gravity. The tars, both polar and non-polar, may be usefully conveyed back to the inlet of the gasifier 12 and undergo again the oxidation and gasification processes.

The lighter tar fraction remains volatile in the gas G also at the exit temperature from the electrostatic precipitator 40. This tar fraction is therefore conveyed together with the flow of the gas G to the subsequent user applications. Typically the use of the gas G envisages a combustion step, to which the light tars may also usefully contribute in view of their chemical nature.

The tank 42 of the precipitator 40 comprises finally a discharge pipe 46. This pipe is suitable for removing any excess aqueous mixture MA from the tank 42 and conveying it towards the basin 32. According to certain embodiments, the electrostatic precipitator 40 comprises a thermal insulation able to prevent as far as possible heat exchange with the external environment. The gas G flows inside the electrostatic precipitator 40 at a temperature generally greater than the ambient temperature, usually at a temperature of between 40°C and 60°C. In these conditions the gas G would tend to release heat spontaneously to the external environment, cooling and triggering further condensation phenomena. These phenomena are therefore limited owing to the thermal insulation of the electrostatic precipitator 40.

According to certain embodiments the plant 100 also comprises means 70 for heating the gas G again after cooling it. These means 70, if present, may for example be associated with the output line 18.

Cooling of the gas G, in particular inside the evaporative cooler and the scrubber 30, causes condensation of most of the water and the tars present therein in the form of vapour. The gas G, however, remains saturated with vapours, i.e. it remains with a relative humidity of 100%. In these conditions even a slight drop in temperature of the gas G causes condensation of the vapours and the consequent formation of mist within the gas G. The occurrence of such a drop in temperature is highly likely along the line 18 which conveys the gas G from the electrostatic precipitator 40 to the external user unit 80. The consequent condensation and formation of mist would therefore risk soiling the line 18 and the user unit 80 itself.

In order to overcome the abovementioned drawbacks, according to certain embodiments of the invention, the temperature of the gas G may be raised again a few degrees (for example 10-20C⁰). A reduction in the relative humidity which falls below 100% is thus obtained. In these changed conditions the gas G may be subject to slight temperature fluctuations, but without this giving rise to the formation of mist.

The heating means 70 may advantageously make use of the heat provided by other sections of the plant 100, such as the evaporative cooler 20 or the gas user unit 80 (which preferably comprises an internal combustion engine or other form of burner). The circuit may be formed in a manner known per se, for example may be advantageously a closed circuit inside which a predetermined quantity of heating liquid circulates. Each of the bleeder pipes 24, 34 and 44 (if present) and each of the recirculating circuits 23, 33 and 64, as well as the pipe 65, preferably comprises a pump suitable for moving the aqueous mixture MA even when it is rich in heavy tars such as those which must be conveyed back to the inlet of the gasifier 12. These pumps may be preferably centrifugal pumps, gear pumps or peristaltic pumps suitable for moving fluids which may also be very viscous. According to certain embodiments, the pump situated in the recirculation circuits 23 and 33 which respectively supply the spraying means 21 and 31 of the evaporative cooler 20 and the scrubber 30 may be advantageously centrifugal pumps. This type of pump is in fact suitable for providing a considerable throughput of aqueous mixture MA provided that it has a sufficiently low viscosity.

According to certain possible embodiments, the discharge pipes 36 and 46 may advantageously comprise a settling tank suitable for separating further by means of gravity the tars from the water. The tars recovered from the bottom of the settling tank may then be removed for storage or for conveying them back to the gasifier 12.

According to certain possible embodiments, the plant 100 also comprises a blower mounted on the line 18 and able to move the gas G through the entire plant 100, from the gasifier 12, via the dedusting unit 14, the evaporative cooler 20, the scrubber 30 and the electrostatic precipitator 40 (if present) as far as the line 18 and beyond.

According to certain possible embodiments, the plant 100 comprises, finally, a gas user unit 80.

According to the embodiment of the plant 100 shown in the accompanying Figures 2 and 3, the gas user unit 80 comprises an internal combustion engine to which a generator for the production of electric energy may be typically connected.

In particular, it should be noted that, owing to its excellent quality, the gas G output from the plant 100 according to the invention can be used to fuel modern reciprocating engines (both Otto cycle and Diesel cycle engines) and/or gas turbine engines.

According to other possible embodiments, the gas user unit 80 may comprise: burners and/or boilers for heating and/or for the production of sanitary hot water; headers for conveying the gas in a supply network; compressors for storing the gas in cylinders or tanks; units for filtering the gas by means of molecular filters or membranes for dividing up the producer gas into its individual constituent gases (H₂, CO, N₂, etc.); units for the production of liquid fuels by means of catalytic processes such as the Fischer-Tropsch process; and any other type of gas user unit 80 known per se.

The invention also relates to a method for the production and treatment of the gas G. The method comprises, in normal operating conditions, the steps of:

- providing a macroapparatus 10 in accordance with that described above;

- providing a flow of wet oxygenated gas and fuel BM to the gasifier 12;

- conveying the flow of gas G from the gasifier 12 to the dedusting unit 14;

- conveying the flow of gas G from the dedusting unit 14 to the evaporative cooler 20;

- spraying inside the evaporative cooler 20 the aqueous mixture MA into the flow of gas G so as to perform washing of the gas G and a first cooling step for absorption of the latent evaporation heat in the aqueous mixture MA;

- storage and settling, inside the basin 22 of the evaporative cooler 20, of a quantity of aqueous mixture MA in the condensed state;

- removing the aqueous mixture MA from the basin 22 and supplying it to the spraying means 21 of the evaporative cooler 20;

- removing the condensed pollutants from the bottom of the basin 22 and conveying them to the gasifier 12;

- conveying the flow of gas G from the evaporative cooler 20 to the scrubber 30;

- spraying inside the scrubber 30 the aqueous mixture MA into the flow of gas G so as to perform a second cooling step for removal of heat by the aqueous mixture MA;

- storing and settling, inside the basin 32 of the scrubber 30, of a quantity of aqueous mixture MA in the condensed state;

- removing from the basin 22 part of the aqueous mixture MA and supplying it to the spraying means 31 ;

- removing from the basin 32 part of the aqueous mixture MA and supplying it to the basin 22 of the evaporative cooler 20;

- removing from the bottom of the basin 32 the condensed pollutants and conveying them to the gasifier 12;

- cooling by means of the heat exchanger 35 the aqueous mixture MA along the path from the basin 32 to the spraying means 31 ;

- introducing a flow of oxygenated gas A into the evaporator 63 of the purifier 60; - removing a quantity of aqueous mixture MA from the basin 22 of the evaporative cooler 20;

- spraying inside the evaporator 63 the aqueous mixture MA removed from the basin 22 into the flow of oxygenated gas A so as to obtain a flow of wet oxygenated gas AU;

- heating the wet oxygenated gas AU in the heating means 67 up to a temperature higher than 200°C;

- conveying the hot wet oxygenated gas AU to the catalytic oxidizer 68;

- promoting, inside the catalytic oxidizer 68, oxidation of the organic pollutants suspended in the wet oxygenated gas AU;

- introducing into the atmosphere the cleaned wet oxygenated gas AU; and

- conveying the flow of gas G from the scrubber 30 outside of the macroapparatus 10. According to a mode of implementation of the invention, the first cooling step lowers the temperature of the gas G from the 400-800°C at which it leaves the gasifier 12 to 75- 90°C. This first cooling step therefore involves absorption of a large quantity of heat, present in the gas G in the form of sensible heat. In the method according to the invention, the aqueous mixture MA removes preferably from the gas G a large quantity of heat, absorbing it in the form of latent evaporation heat, while a minimum part is absorbed in the form of sensible heat. During this first (evaporative) step there is therefore no exchange of heat towards the outside of the system and the heat therefore remains inside the flow of vapour-saturated gas G.

According to a mode of implementation of the method, the second cooling step lowers the temperature of the gas G from the 75-90°C at which it leaves the evaporative cooler 20 to the 40-60°C which are optimum for operation of the user unit 80. This second step of cooling of the gas G involves removal of a large quantity of heat present in the form of latent heat in the vapours generated by the aqueous mixture MA (water vapour and light tars in the vapour phase) and mixed with the gas G. In the method according to the invention, the aqueous mixture MA removes preferably the heat, absorbing it in the form of sensible heat and therefore increasing its own temperature. During this second (condensation) step there is therefore an exchange of heat with the outside of the system via the exchanger 35.

The present invention also relates to a gasifier 12 of the downdraft open-core type comprising means 120 for raising the outer jacket 121. These raising means, as already described above in connection with the gasifier 12 forming part of the macroapparatus 10, are suitable for converting the outer jacket 121 from a closed operating configuration into an open maintenance configuration.

The present invention also relates to an assembly 50 similar to that described above in connection with Figures 5 to 8 and forming part of the macroapparatus 10. In particular, the assembly 50 comprises an evaporative cooler 20 and an evaporator 63.

The evaporative cooler 20 of the assembly 50 is suitable for treating a flow of gas G and comprises:

- means 21 for spraying an aqueous mixture MA into the flow of gas G;

- a basin 22 suitable for allowing settling and storage, in the evaporative cooler 20, of a quantity of aqueous mixture MA in the condensed state;

- a bleeder pipe 24 suitable for removing the condensed pollutants from the bottom of the basin 22 and conveying them externally.

The evaporator 63 of the assembly 50 comprises:

- a line 61 for supplying a flow of oxygenated gas A;

- means 630 for spraying an aqueous mixture MA into the flow of oxygenated gas A;

- a pipe 65 suitable for removing a quantity of aqueous mixture MA from the basin 22 of the evaporative cooler 20 and for supplying the aqueous mixture MA to the spraying means 630;

- a line 62, suitable for conveying the wet oxygenated gas AU externally.

The present invention also relates to an evaporative cooler 20 similar to that described above in relation to Figures 5 to 8 and forming part of the macroapparatus 10. In particular the evaporative cooler 20 suitable for treating a flow of gas G comprises:

- means 21 for spraying an aqueous mixture MA into the flow of gas G,

- a recirculation circuit 23 suitable for removing the aqueous mixture MA from the basin 22 and supplying it to the spraying means 21 of the evaporative cooler 20; and - a bleeder pipe 24 suitable for removing the condensed pollutants from the bottom of the basin 22 and conveying them externally;

- shredder means 25 for breaking up the incrustations which form inside the evaporative cooler 20 during treatment of the gas flow G.

According to an embodiment of the evaporative cooler 20, the shredder means 25 are included between the zone where spraying of the aqueous mixture MA occurs and the basin 22 inside which the aqueous mixture MA is collected. Preferably these shredder means 25 comprise a series of cutters 250 which are movable with respect to a grille 251.

From that stated above it will be clear to the person skilled in the art how the plant 100 in its entirety, the macroapparatus 10 in particular and the method according to the invention overcome the disadvantages highlighted in relation to the prior art.

It is clear that the specific characteristics are described in relation to the various embodiments of the plant 100 by way of a non-limiting example.

Obviously, a person skilled in the art, in order to satisfy any specific requirements which might arise, may make to the macroapparatus 10 and/or the plant 100 according to the present invention further modifications and variations, all of which moreover contained within the scope of protection of the invention, as defined by the following claims.

Claims

1. An assembly (50) comprising an evaporative cooler (20) and an evaporator (63), wherein the evaporative cooler (20) is suitable for treating a flow of gas G and comprises:

- means (21) for spraying an aqueous mixture MA into the flow of gas G;

- a basin (22) suitable for allowing settling and storage of a quantity of aqueous mixture MA in the condensed state;

- a recirculation circuit (23) suitable for removing the aqueous mixture MA from the basin (22) and supplying it to the spraying means (21) of the evaporative cooler (20); and

- a bleeder pipe (24) suitable for removing the condensed pollutants from the bottom of the basin (22) and conveying them externally;

and wherein the evaporator (63) comprises:

- a line (61) for supplying a flow of oxygenated gas A;

- means (630) for spraying an aqueous mixture MA into the flow of oxygenated gas A;

- a pipe (65) suitable for removing a quantity of aqueous mixture MA from the basin (22) of the evaporative cooler (20) and for supplying the aqueous mixture MA to the spraying means (630);

- a line (62') suitable for conveying the wet oxygenated gas AU externally.

2. The assembly (50) according to claim 1, wherein the evaporative cooler (20) further comprises shredder means (25) for breaking up the encrustations which form inside the evaporative cooler (20) during treatment of the flow of gas G.

3. The assembly (50) according to claim 2, wherein the shredder means (25) are situated between the zone where spraying of the aqueous mixture MA occurs and the basin (22) inside which the aqueous mixture MA is collected and wherein the shredder means (25) comprise a series of cutters (250) movable with respect to a grille (251).

4. A macroapparatus (10) for the production and treatment of gas G, comprising:

- a gasifier (12) suitable for receiving a flow of oxygenized gas and fuel BM and for emitting a flow of gas G;

- a line suitable for conveying the flow of gas G from the gasifier (12) to a dedusting unit (14);

- a dedusting unit (14);

- a line suitable for conveying the flow of gas G from the dedusting unit (14) to an evaporative cooler (20);

- an evaporative cooler (20) suitable for treating the flow of gas G, comprising:

- means (21) for spraying an aqueous mixture MA into the flow of gas G,

- a basin (22) suitable for allowing settling and storage in the evaporative cooler (20) of a quantity of aqueous mixture MA in the condensed state,

- a recirculation circuit (23) suitable for removing from the basin (22) the aqueous mixture MA and for supplying it to the spraying means (21) of the evaporative cooler (20); and

- a bleeder tube (24) suitable for removing the condensed pollutants from the bottom of the basin (22) and conveying them to the gasifier (12);

- a line suitable for conveying the flow of gas G from the evaporative cooler (20) to a scrubber (30);

- a scrubber (30) suitable for treating the flow of gas G, comprising:

- means (31) for spraying an aqueous mixture MA into the flow of gas G;

- a basin (32) suitable for allowing settling and storage, in the scrubber (30), of a quantity of aqueous mixture MA in the condensed state;

- a recirculation circuit (33) suitable for removing from the basin (32) part of the aqueous mixture MA and for supplying it to the spraying means (31);

- a bleeder pipe (34) suitable for removing the condensed pollutants from the bottom of the basin (32) and conveying them to the gasifier (12);

- a heat exchanger (35) placed along the recirculation circuit (33) of the scrubber (30); and

- a compensation pipe (37) suitable for removing from the basin (32) part of the aqueous mixture MA and supplying it to the basin (22) of the evaporative cooler (20);

- a line suitable for conveying the flow of gas G from the scrubber (30) to the outside of the macroapparatus (10);

the macroapparatus (10) further comprising a purifier (60) suitable for receiving a flow of oxygenized gas A and of aqueous mixture MA and for emitting a flow of cleaned wet oxygenated gas AU, the purifier (60) comprising:

- a line (61) for supplying a flow of oxygenated gas A;

- an evaporator (63) having means (630) for spraying an aqueous mixture MA into the flow of oxygenated gas A;

- a pipe (65) suitable for drawing a quantity of aqueous mixture MA from the basin (22) of the evaporative cooler (20) and for supplying the aqueous mixture MA to the spraying means (630) of the evaporator (63);

- a line (62') suitable for conveying the wet oxygenated gas AU from the evaporator (63) to heating means (67).

- means (67) for heating the wet oxygenated gas A, suitable for raising its temperature above 200°C;

- a line (62") suitable for conveying the wet oxygenated gas AU to a catalytic oxidizer (68);

- a catalytic oxidizer (68) suitable for promoting oxidation of the pollutants suspended in the wet oxygenated gas AU; and

- a line suitable for introducing into the atmosphere the cleaned wet oxygenated gas AU downstream of the catalytic oxidizer (68).

5. The macroapparatus (10) according to claim 4, wherein the gasifier (12) is of the downdraft open-core type.

6. The macroapparatus (10) according to claim 4 or 5, further comprising an auxiliary gasifier (125) suitable for gasification of the charcoal dust C which is output from the gasifier (12).

7. The macroapparatus (10) according to the preceding claim, wherein the auxiliary gasifier (125) is of the updraft open-core type.

8. The macroapparatus (10) according to claim 6 or 7, further comprising a line (69) suitable for supplying to the auxiliary gasifier (125) the wet oxygenated gas AU which is output from the evaporator (63) and a line (126) suitable for supplying to the gasifier (12) the gases produced by gasification of the charcoal C in the auxiliary gasifier (125).

9. The macroapparatus (10) according to any one of claims 4 to 8, wherein the evaporative cooler (20) comprises shredder means (25) for breaking up the solid or semi- solid encrustations forming inside it during treatment of the flow of gas G.

10. The macroapparatus (10) according to the preceding claim, wherein the evaporative cooler (20) comprises at least one screw conveyor (220) suitable for removing from the bottom of the basin (22) the pollutants collecting there, said pollutants comprising more or less fluid tars and/or pieces of solid or semi-solid encrustations broken up by the shredder means (25).

1 1. The macroapparatus (10) according to any one of claims 4 to 10, wherein the means (67) for heating the wet oxygenated gas flow AU inside the purifier (60) comprise a heat exchanger (670) where the wet oxygenated gas AU may absorb heat from the gas G leaving the gasifier (12).

12. The macroapparatus (10) according to any one of claims 4 to 11, wherein the means (67) for heating the flow of wet oxygenated gas AU inside the purifier (60) comprise a manifold (671) for causing merging of the wet oxygenated gas AU with another flow of hot gases directed towards the catalytic oxidizer (68).

13. The macroapparatus (10) according to any one of the claims 4 to 12, wherein the gasifier (12) comprises means (120) for raising the outer jacket (121), so as to move the outer jacket (121) from a closed operating configuration into an open maintenance configuration.

14. A plant (100) for production and treatment of gas G, comprising a macroapparatus (10) according to any one of the claims 4 to 13, an electrostatic precipitator (40) and a user unit (80).

15. The plant (100) according to the preceding claim, wherein said user unit (80) comprises an internal combustion engine and/or a burner and a catalytic oxidizer (68), the catalytic oxidizer (68) being in common with the purifier (60) of the macroapparatus (10).

16. The plant (100) according to claim 14 or 15, wherein the electrostatic precipitator (40) comprises a thermal insulation suitable for preventing heat exchange between the gas G and the outer environment.

17. A method for production and treatment of gas G, comprising, in normal operating conditions, the steps of:

- providing a macroapparatus (10) according to any one of the claims 4 to 13;

- supplying a flow of oxygenated gas and fuel BM to the gasifier (12); - conveying the flow of gas G from the gasifier (12) to the dedusting unit (14);

- conveying the flow of gas G from the dedusting unit (14) to the evaporative cooler (20);

- spraying inside the evaporative cooler (20) an aqueous mixture MA into the flow of gas G so as to obtain washing of the gas G and a first cooling step due to heat absorption in the aqueous mixture MA;

- storing and settling, in the basin (22) of the evaporative cooler (20), a quantity of aqueous mixture MA in the condensed state;

- removing from the basin (22) the aqueous mixture MA and supplying it to the spraying means (21) of the evaporative cooler (20);

- removing from the bottom of the basin (22) the condensed pollutants and conveying them to the gasifier (12);

- conveying the flow of gas G from the evaporative cooler (20) to the scrubber (30);

- spraying inside the scrubber (30) the aqueous mixture MA into the flow of gas G so as to obtain a second cooling step due to heat removal by the aqueous mixture MA;

- storing and settling, in the basin (32) of the scrubber (30), a quantity of aqueous mixture MA in the condensed state;

- removing from the basin (32) part of the aqueous mixture MA and supplying it to the spraying means (31);

- removing from the basin (32) part of the aqueous mixture MA and supplying it to the basin (22) of the evaporative cooler (20);

- removing from the bottom of the basin (32) the condensed pollutants and conveying them to the gasifier (12);

- cooling by means of the heat exchanger (35) the aqueous mixture MA along its path from the basin (32) to the spraying means (31);

- introducing a flow of oxygenated gas A into the evaporator (63) of the purifier (60);

- removing a quantity of aqueous mixture MA from the basin (22) of the evaporative cooler (20);

- spraying, inside the evaporator (63), the aqueous mixture MA removed from the basin (22) into the flow of oxygenated gas A so as to obtain a flow of wet oxygenated gas AU;

- heating the wet oxygenated gas AU in the heating means 67 up to a temperature higher than 200°C; - conveying the hot wet oxygenated gas AU to the catalytic oxidizer (68);

- promoting, inside the catalytic oxidizer (68), oxidation of the organic pollutants suspended in the wet oxygenated gas AU;

- introducing into the atmosphere the cleaned wet oxygenated gas AU; and

- conveying the flow of gas G from the scrubber (30) outside of the macroapparatus (10).

18. A gasifier (12) of the downdraft open-core type, characterized in that it comprises means (120) for raising the outer jacket (121), so as to move the outer jacket (121) from a closed operating configuration into an open maintenance configuration.