[0001] The present invention refers to a continuous-type gasifier, in particular for biomasses
and urban and industrial wastes.
[0002] As known, in general, gasifiers exploit a pyrolysis reaction through heating with
reduced amounts of oxygen to convert the original solid fuel originario into a fuel
gas (syngas) by means of partial combustion.
[0003] In particular, the gasification process always proceeds through three steps:
- pyrolysis, namely transforming, by thermal cracking, the solid material into gaseous
products and carbon residuals;
- combustion of part of the pyrolysis products with an oxidising agent (air, oxygen);
- gasification of the carbon residual produced by pyrolysis at the expense of heat of
the combustion products.
[0004] In the first step, there is a thermal demolition of the molecules of products to
be treated, forming gaseous products with various molecular weights and carbon residuals.
Combustion generates the necessary heat to perform the pyrolysis and to transform
the pyrolysis products into light gases (CO, H
2, CH
4). In this step, there must also occur a thermal cracking of the gaseous pyrolysis
products with high molecular weight, which, when using the gas, can give rise to condensation
of liquids and tars.
[0005] In past years, many technologies have been developed for gasifying various solid
fuels. For medium-small sized plants, the most commonly used technology is the moving-bed
technology of the "down-draft" type. In this system, the solid is supplied from the
top in the reactor in order to form a solid bed which slowly advances downwards.
[0006] The reactor, in its upper part, is airtight, in such a way as to force gases inserted
or produced in the reactor itself to go out through the lower bed part, where instead
openings are left. At a certain height, air or oxygen are inserted through nozzles
placed on the periphery of the reactor. Inserted air implies the partial combustion
of the pyrolysis gas in the neighbourhood of points for introducing air. The developed
heat causes the pyrolysis of the material present immediately above the area for introducing
air. Volatile pyrolysis products flow downwards, crossing the area where combustion
occurs and taking part therein.
[0007] The pyrolysis gas combustion therefore brings about the formation of high amounts
of CO
2 and H
2O. In the combustion area, the temperature can locally get to exceed 1200-1300°C.
[0008] Hot gases, in order to go out of the reactor, must therefore cross the lower bed
part, composed of the carbon residual. Under such situation, the following endothermal
gasification reactions occur for carbon:
C+CO
2=
2CO (1)
C+H
2O=CO+H
2 (2)
[0009] Other reactions which bring about the formation of light hydrocarbons (natural gas,
for example), both for kinetic and for thermodynamic reasons, have a more limited
effect.
[0010] Carbon residuals, partily gasified, are withdrawn together with ashes through a grid
placed at the reactor base. Through the same grid, also gases produced by the gasifier
are withdrawn, which therefore go out at a temperature of at least 800°C.
[0011] The above described known reactor, however, still suffers from a series of limitations,
such as the following:
- air is generally inserted from the reactor sides, in an area occupied by the bed of
fuel material. Its penetration into the bed is therefore limited and consequently
also the combustion area remains limited. A relatively cold area therefore can be
created next to the gasifier axis, such area being able to be crossed by gases and
tars produced by pyrolysis without subjecting them to cracking, thereby partly finding
them in the final gas. The importance of such critical aspects highly increases when
the plant sizes increase. Ofter the gasifiers, downstream of entering air, have a
smaller section to make it easier to mix gas, but at the same time a smaller section
favours the creation of solid bridges which block the downward flow of the bed;
- carbon residuals react according to above reactions (1) and (2) quickly reducing the
gas temperature. In the lower bed areas, such temperature is often too low to allow
the reactions (1) and (2) to occur quickly enough, taking to the complete exhausting
of the residuals. In addition to this, always in the lower bed area, gas often reaches
conditions which are near the thermodynamic balance, and anyway does not succeed in
converting carbon into CO, apart from kinetic aspects.
[0012] Consequence of the previous considerations is that normally a relevant amount of
carbon residual is withdrawn from the reactor together with ashes. This aspect, in
addition to impairing the process efficiency, does not allow reaching the specific
requests of EC legislations (Directive 200/76 CE) in terms of maximum content of carbon
in ashes produced by the thermal treatment of wastes. Also under the most favourable
working conditions, the amount of produced tar is on the order of 0.5-1 g/Nm
3 of gas.
[0013] Moreover, in case of materials producing a fragile and fine carbon residual like
the one originated by pyrolysis of wastes or very subdivided biomasses (straw, cutting,
etc.), a bed of very fine solid particles is formed at the gasifier base, which makes
the flow of outgoing gases, in the gasification phase, very problematic.
[0015] NL-A-8 200 417 provides for an upper stirrer from which air is entered and a lower grid supporting
the solid. Below the grid ashes accumulate, and are then withdrawn from the opening
20 (figure 1). The exhausting section 9 is not crossed by any gas which can favour
the actual exhausting. In the present invention, pre-heated air is entered, whose
purpose is enabling the esothermal gasification reactions of the whole exhausting
section.
[0016] In addition to this, pre-heated air is entered from the bottom in order to impair
the bad packing.
[0017] In addition to this, in the present invention, between exhausting section and grid,
an empty area from solid is always created, which can allow the possible movement
of the bed in the exhausting area. In the present invention it is further specified
that fluid entered by the stirrer is pre-heated, and the stirrer blades must be coated
with a refractory material to allow using pre-heated air. Such features are not mentioned
in
NL-A-8 200 417.
[0018] Like in the previous case, in patent
CA-A1-2 432 202, in the exhausting section (figure 1, 44) nothing is entered which can favour the
charcoal exhaust. The described exhausting section therefore is nothing but the common
gasifying area, always present in downdraft gasifiers. Between area 44 and upper area
38, the empty space which is provided in the present invention is instead not present.
Nor
CA-A1-2 432 202 mentions methods to make the combustion more stable, such as air pre-heating and
following protection of blades with thermal insulation.
[0019] With respect to these prior documents, the present invention discloses the lower
gasifier part, which must behave like a counter-current gasifier: it is therefore
of the utmost importance that, in its lower part, air is entered: this allows the
exhausting section to operate. The arrangement for which the gas outlet is below the
grid but above the exhausting section (not inside it, like in
NL-A-8 200 417) allows withdrawing gas without compelling it to cross the exhausted and very fine
solid.
[0020] Therefore, object of the present invention is solving the above prior art problems
by providing a continuous-type gasifier, in particular for biomasses and urban and
industrial wastes, which is more efficient with respect to what is proposed by the
prior art, allowing, in particular, a better exploitation of carbon residuals, substantially
reducing their amount present in ashes.
[0021] Another object of the present invention is providing a continuous-type gasifier,
in particular for biomasses and urban and industrial wastes, in which, also next to
the axial area of the reaction chamber, an adequate temperature is kept for guaranteeing
the cracking of gas and of tars produced by pyrolysis which cross such area.
[0022] Moreover, an object of the present invention is providing a continuous-type gasifier,
in particular for biomasses and urban and industrial wastes, able to guarantee the
complete exhaustion of the carbon residual due to esothermal combustion reactions,
reaching, in the hottest bed areas, temperatures much greater than 1000 °C.
[0023] The above and other objects and advantages of the invention, as will appear from
the following description, are obtained with a continuous-type gasifier, in particular
for biomasses and urban and industrial wastes, as claimed in claim 1. Preferred embodiments
and non-trivial variations of the present invention are the subject matter of the
dependent claims.
[0024] It is intended that all enclosed claims are an integral part of the present description.
[0025] It will be immediately obvious that numerous variations and modifications (for example
related to shape, sizes, arrangements and parts with equivalent functionality) could
be made to what is described, without departing from the scope of the invention as
appears from the enclosed claims.
[0026] The present invention will be better described by some preferred embodiments thereof,
provided as a non-limiting example, with reference to the enclosed drawings, in which:
- Figure 1 shows a schematic, side sectional view of a preferred embodiment of the gasifier
according to the present invention; and
- Figure 2 shows a schematic diagram illustrating the flows of material/energy in a
plant equipped with a gasifier according to the present invention.
[0027] With reference to Figure 1, it is possible to note that a preferred embodiment of
the continuous-type gasifier 1 of the "down-draft" type, in particular for biomasses
and urban and industrial wastes, according to the present invention comprises at least
one reaction chamber 3 divided into at least one upper portion 3a and at least one
lower exhaustion portion 3b by at least one mobile grid 21 for withdrawing charcoal
and supporting the solid bed, such reaction chamber 3 having at least one first upper
end equipped with at least one opening 5 for introducing substances to be gasified
inside such chamber 3, such chamber 3 being internally equipped with at least one
rotary stirring shaft 13, having a substantially vertical rotation axis, such shaft
13 being equipped with a plurality of delivery openings 15 inside such chamber 3 for
at least one comburent fluid like, for example, air or air enriched with technical
oxygen, suitably pre-heated at such a temperature as to guarantee triggering oxidation
reactions.
[0028] Preferably, such shaft 13 is equipped with at least one internal axial duct 14 communicating
such openings 15 with at least one source means of such comburent fluid through, for
example, at least one opening 16 for introducing such comburent fluid inside such
duct 14. Preferably, the shaft 13 is equipped with internal thermal protecting means
in such a way as not to disperse sensitive heat of the pre-heated fluid which passes
therein. Still more preferably, the shaft 13 is equipped, at least at the bottom,
with a stirring end 17 equipped with a plurality of such openings 15.
[0029] Preferably, the stirring ends 17 are externally equipped with at least one layer
of refractory, thermally protecting material whose purpose is protecting the internal
metallic parts from high temperatures generated due to oxidation reactions and the
use of a strongly pre-heated comburent fluid.
[0030] The gasifier 1 according to the present invention further comprises at least one
mobile grid 21 for withdrawing charcoal and supporting the solid bed, such grid 21
being arranged below the lower end of such shaft 13.
[0031] Advantageously, the mobile grid 21 and the shaft 13 can have wholly independent mutual
movements: in particular, the movement of the grid 21 can be both alternate vertical
and rotary, and, when it is rotary, preferably the grid 21 and the shaft 13 will have
an opposite rotation direction.
[0032] The gasifier 1 according to the present invention further comprises at least one
opening 23 for outputting the fuel gas produced inside the reaction chamber 3, such
opening 23 being preferably arranged below such grid 21.
[0033] The lower exhaustion portion 3b is therefore arranged below the grid 21 and preferably
has its perimeter walls equipped with means 25 for introducing at least one fluid
for exhausting the charcoal (for example air) pre-heated at a temperature of at least
450-500 °C, so that, due to the combustion reactions, peak temperatures greater than
1200 °C are reached, following its combustion, such lower portion 3b being coated
with at least one layer of a refractory material and having preferably a tapered shape
towards a lower end equipped with means for withdrawing ashes 27.
[0034] Obviously, entering substances to be gasified inside the reaction chamber 3 can occur
through suitable loading means known in the art, such as, for example, at least one
hopper or, still more preferably, at least one loading chamber 7 connected to such
opening 5 by interposing at least one first valve means 9 cooperating with at least
one second valve means 11 placed as closure of at least one loading opening of such
loading chamber 7, such valve means 9, 11 having an alternate opening/closing operation,
in order to guarantee the necessary tightness to force gases entered or produced in
the reaction chamber 3a to go out through the grid 21 openings.
[0035] Therefore, due to the features of the gasifier 1 according to the present invention
as described above, it is possible to advantageously obtain the following technical
results:
- the part of solid bed affected by pyrolysis and therefore softening of plastics possibly
present therein is continuously moved by the shaft 13 to avoid forming bridges and
agglomerates due to the plastic material being present;
- the comburent fluid is uniformly distributed inside the reaction chamber 3 through
the openings 15 in order to make it useless to employ the restriction generally adopted
in prior art down-draft gasifiers, and to make the hot combustion area wider. It must
be noted that pre-heating of the comburent fluid is necessary to obtain a stable combustion,
since the points for inserting the comburent are mobile and a continuous bed ignition
is therefore required: moreover, the entered amount of comburent fluid, not having
to wholly gasify the residual, is lower with respect to prior art systems with the
same potentiality, and therefore also generated heat is lower: from this, a further
pre-heating of the comburent fluid is needed. Finally, heating allows recovering energy;
- under the combustion area (which occurs mostly with pyrolysis gas) a bed of carbon
residual is formed, which is only partly consumed by gasification reactions with CO2 and H2O and which is supported by the mobile grid 21 that, through its movement, drops the
solid with a fixed flow-rate;
- carbon residual and ash falling through the grid 21 accumulate in the lower exhaustion
portion (3b) below, where they are completely exhausted due to the insertion of exhausting
fluid from below, such fluid being preferably pre-heated air at a temperature of at
least 450-500°C: in this way, Directive 2000/76/CE is complied with, which strongly
limits the presence of carbon residual in ashed.
[0036] As application example of the gasifier 1 according to the present invention, herein
below some performances are given for a plant like the one in Figure 2, such plant
comprising in line:
- at least one system 101 for crushing supplied wastes;
- at least one de-ironing device 103;
- at least one means 105 for storing the sterilised wastes;
- at least one supplying means 107 for wastes from such storage means 105 to the loading
chamber 7 of the gasifier 1;
- at least one gasifier 1 according to the present invention;
- at least one means 109 for washing gas with an organic liquid phase for removing residual
tars and one washing means 110 with a basic acqueous solution for removing acid gases;
- at least one gas-meter 111;
- at least one motor 113 supplied by such fuel gas with exhausting means.
[0037] The above plant 100 has been supplied with wastes at 515 Kg/h (the gasifier 1 is
therefore supplied with the de-ironed wastes equal to 500 kg/h) having the properties
included in the following Table 1.
Table 1: elementary composition and PCI of wastes
Heat power (kcal/kg) as it is |
4000 |
INERTS/metals |
16.8% |
Total humidity |
10.4% |
Elementary composition (dry ash free), percentage in weight |
|
C |
57.6 % |
H |
7.4 % |
OR |
34.2 % |
N |
0.8 % |
[0038] In this way, it is possible to obtain a fuel gas with a heat power lower at least
by 1250 kcal/ Nm
3 (on humid gas).
[0039] The following Table 2 includes the major features of the various flows of material/energy
in the sections of plant 100 designated with related letter-type references A to I:
Table 2
Currents |
A |
B |
C |
D |
E |
F |
Composition |
|
|
|
|
|
|
H2O % vol |
0 |
0 |
0 |
0 |
6.3 |
6.3 |
O2 % vol |
21 |
90 |
21 |
0.21 |
0 |
0 |
N2 % vol |
79 |
10 |
79 |
0.79 |
44 |
44 |
H2 % vol |
0 |
0 |
0 |
0 |
20.5 |
20.5 |
CH4 % vol |
0 |
0 |
0 |
0 |
0 |
0 |
CO % vol |
0 |
0 |
0 |
0 |
23.3 |
23.3 |
CO2 % vol |
0 |
0 |
0 |
0 |
5.5 |
5.5 |
Flow-rate kg/h |
950 |
0 |
125 |
845 |
1400 |
1400 |
Temperature °C |
25 |
25 |
500 |
500 |
880 |
620 |
[0040] The following Table 3 instead includes the major parameters linked to the energy
balance of the plant 100:
Table 3
Balances at massification section |
|
|
Power given by direct waste combustion |
2340 |
kW |
Lost heat with hot ashes |
25 |
kW |
Dissipated heat for gas cooling down to 25°C |
260 |
kW |
Miscellaneous losses |
55 |
kW |
Thermal power from direct gas combustion |
2000 |
kW |
1. Continuous-type gasifier (1) of the "downdraft" type, in particular for biomasses
and urban and industrial wastes, comprising at least one reaction chamber (3) divided
into at least one upper portion (3a) and at least one lower exhaustion portion (3b)
by at least one mobile grid (21) for withdrawing charcoal and supporting a solid bed,
said reaction chamber (3) having at least one first upper end equipped with at least
one opening (5) for introducing substances to be gasified inside said chamber (3),
said chamber (3) being internally equipped with at least one rotary stirring shaft
(13), said shaft (13) being equipped with a plurality of openings (15) for delivering
inside said chamber (3) at least one comburent fluid pre-heated at a temperature sufficient
to guarantee triggering oxidation reactions, characterised in that it comprises at least one opening (23) for outputting a fuel gas produced inside
said reaction chamber (3), said opening (23) being arranged below said grid (21),
and in that said lower exhaustion portion (3b) arranged below said grid (21) has perimeter walls
equipped with means (25) for introducing a comburent fluid for exhausting said charcoal
in order to reach, due to combustion reactions, peak temperatures greater than 1200
°C, said lower portion (3b) being coated with at least one layer of a refractory material
and having a tapered shape towards a lower end equipped with means for withdrawing
ashes (27).
2. Gasifier (1) according to the previous claim, characterised in that said comburent fluid is air or air enriched with technical oxygen.
3. Gasifier (1) according to claim 1, characterised in that said shaft (13) is equipped with at least one internal axial duct (14) communicating
said openings (15) with at least one source means of said pre-heated comburent fluid
through at least one opening (16) for introducing said comburent fluid inside said
duct (14).
4. Gasifier (1) according to claim 1, characterised in that said shaft (13) is equipped at least on its bottom with a stirring end (17) equipped
with a plurality of said openings (15), said stirring end (17) being externally equipped
with at least one layer of refractory material for thermal protection.
5. Gasifier (1) according to claim 1, characterised in that said mobile grid (21) is arranged below a lower end of said shaft (13).
6. Gasifier (1) according to the previous claim, characterised in that said grid (21) and said shaft (13) have mutually independent movements.
7. Gasifier (1) according to the previous claim, characterised in that said movement of said grid (21) is alternate vertical or rotary.
8. Gasifier (1) according to the previous claim, characterised in that also said shaft (13) has a rotary movement but with a rotation direction opposite
to the rotation direction of said grid (21).