[0001] This invention relates to a process for the refining of a raw gas produced from a
carbonaceous material by means of a gasification process in which the refing takes
place in a secondary stage separated from the gasifier of the gasification process.
[0002] A raw gas produced from different kinds of biofuels and used as a fuel gas is a valuable
oil substitute for demanding applications in which the process demands make direct
solid fuel fireing impossible, e.g. fireing of lime kilns or conversion of existing
oil fired boilers.
[0003] For other types of applications, e.g. so-called cogeneration (of electrical power
and heat) by use of diesel engines, very high demands on the gas purity concerning
primarily tars and dust are set. Moreover, environmental aspects often lead to demands
on low concentrations of compounds which when combusted form harmful emissions, such
as NO
x, SO
x and various chlorinated compounds. The last mentioned is valid especially for a gas
produced from refuse derived fuel, RDF. These demands on the gas purity can be satisfied
by the raw gas being refined by an appropriate method.
[0004] Gasification of RDF with subsequent refining of the raw gas means an environmentally
favourable method for energy recovery from wastes by utilization of refined gas in
existing boilers or for cogeneration in diesel engines and/or boilers.
[0005] Besides, utilization of raw gas often is connected with other technical problems.
[0006] At temperatures below 1200°C tar is always present in a raw gas produced by gasification
of a carbonaceous material, e.g. coal, peat, bark, wood or RDF, which limits the
utilization to combustion of hot gas in direct or close connection to the gasifier.
Operational disturbances caused by tarcoating on apparatuses and armatures are a great
problem which limits the availability. During combustion of hot gas, nitrogen and
in certain cases also sulphur (e.g. from peat) bound in tars, as well as ammonia,
H₂S (peat) or CHl (from RDF), furthermore give rise to emissions which are harmful
to the environment (NO
x, SO
x and HCl, respectively, and chlorinated hydrocarbons, i.a. dioxines).
[0007] Despite extensive research concerning tar and ammonia conversion, so far no process
which in an industrial scale can achieve sufficiently far-reaching raw gas refining
has been developed. The traditional way of reducing tar contents in a raw gas is by
means of wet scrubbing, but aerosol formation in the scrubber makes the tar removal
inefficient. Furthermore, a process water with high contents of organic compounds
and ammonia is obtained. Consequently, this water in its turn must be cleaned before
being discharged to a sewerage. When gasifying RDF the process water also contains
high concentrations of dissolved hydrochloric acid and/or ammonium chloride. When
gasifying more sulphur rich fuels, e.g. peat or coal, the raw gas also has to be purified
to remove hydrogen sulphide.
[0008] The object of the presented invention is to provide a raw gas refining process, by
means of which the above mentioned problems will be solved to a great extent.
[0009] This object is achieved by the process according to the invention having the features
defined in the enclosed claims.
[0010] The invention thus concerns a process for the refining of a tar and ammonia containing
raw gas, in special cases also containing considerable quantities of hydrogen chloride,
the gas being produced by means of an arbitrary gasification process from a carbonaceous
material, e.g. bark, wood, peat or Refuse Derived Fuel, RDF, wherein in a secondary
stage conversion takes place in contact with an appropriate active (catalytic and
possible absorbing) material, e.g. dolomite, of the tar and ammonia present in the
raw gas, preferably to such a level that the remaining contents are below 500 and
300 mg/Nm³ respectively. In special cases absorption of hydrogen chloride to almost
thermodynamic equilibrium simultaneously takes place. The secondary stage consists
of a Circulating Fast Fluidized Bed (CFB) with a bed material at least mainly in
form of an active material, e.g. dolomite. With this arrangement the secondary stage
also could be integrated with an arbitrary CFB-gasifier, only preceded by a primary
particle separator, or another type of gasifier.
[0011] We have found that sufficient conversion of tars and ammonia and in special cases
simultaneous absorption of hydrogen chloride can be achieved, by first separating
the tar containing gas from pyrolysing larger fuel particles in the gasifying stage
and then in a separate secondary stage in the form of a circulating fast fluidized
bed contacting the gas with a suitable active material, such as dolomite, at suitable
process parameters.
[0012] If the carbonaceous material also contains sulphur in considerable amounts, which
e.g. is the case for peat, absorption of hydrogen sulphide on the catalytic and absorbing
material will of course also take place.
[0013] The amount of active material which is required in relation to the raw gas amount
is determined by the required space-velocity for catalytic conversion of tars and
ammonia and depends on several parameters such as the temperature, the residence time
of the gas, the particle size of the active material, the partial pressure of reactants
and the degree of deactivation of the active material. Too low temperature and/or
CO₂ partial pressure can result in the tar conversion causing carbon deposition on
the active surface, which results in deactivation. If this occurs the material can
be activated by treatment with an oxidizing gas, e.g. air and/or steam. Absorption
of HCl (and/or H₂S) takes place so rapidly at the temperatures of interest that these
reactions become almost determined by the equilibrium and result in a consumption
of active material corresponding to the formed solid chloride (and sulphide resp.).
[0014] We have thus found that absorption of chloride (and in certain cases also of hydrogen
sulphide) on an active material such as dolomite is a rapid reaction and requires
presence of a considerably less amount of active material in relation to the gas
flow than catalytic conversion of tars and ammonia.
[0015] Utilization of a secondary stage in the form of a fast circulating fluidized bed
(CFB) means considerable advantages.
[0016] Such a bed is able to handle dust entrained from the gasifier, gives very uniform
temperatures in the reaction zone and also gives a homogeneous contact between gas
and bed material, that is to say little risk for variations in conversion/absorption
degree. Further, the particle size can be varied downwards to a great extent, for
those cases in which this is needed to give increased conversion at a given temperature
and space-velocity. Considerable erosion of the bed material also results in increased
accessible active surface. Also, a secondary stage designed as a CFB with advantage
can be integrated with an arbitrary CFB gasifier, which merely has a primary particle
separator, or another type of gasifier. One also achieves relatively small diameters
when scaling up, since the gas velocities can be kept relatively high, up to about
10 m/s, preferably up to 6 m/s.
[0017] In case the gasifier consists of a CFB gasifier, a connection directly after primary
dust separation can thus be made. If an active material is used as a bed material
in the CFB gasifier, the secondary stage can in an advantageous manner be integrated
with the gasifier, e.g. so that dust from a secondary particle separator after the
secondary stage is totally or partly recycled to the gasifier. In this way, the total
losses of bed material also become lower, and one also obtains the advantage of using
only one type of bed material.
[0018] The necessary amount of active material in the reactor shaft of the secondary stage
for sufficient catalytic conversion of tar and ammonia is controlled by the totally
added amount and by controlled recirculation of bed material. Required conversion
determines suitable combination of temperature, particle size and amount of active
material. Because of abrasion, deactivation and/or absorption of HCl (and possibly
H₂S) consumed active material is replaced by adding corresponding amounts of fresh
active material and/or activated such material. The residence time of the gas can
be controlled by the combination diameter/height above the gas inlet.
[0019] In those special cases, when HCl is present in the raw gas in considerable amounts,
the active material entrained by the outlet gas from the secondary stage means that
the HCl absorption is improved, since thermodynamically it becomes more far-reaching
at lower temperatures, under the condition that the refined gas is cooled down to
an essentially lower temperature before final dust removal.
[0020] In the following the invention will be described by way of a non-limiting embodiment
while referring to the enclosed drawing, which schematically shows a gasification
and gas refining system which embodies the present invention.
[0021] In the system shown in the drawing carbonaceous material 1 is conveyed to a gasifier
3, which consists of a circulating fast fluidized bed (CFB). This comprises a reactor
51, a primary separator 52 and recirculation means 53 for bed material separated in
the primary separator. The bed material consists of an active catalytic and absorbing
material, preferably in the form of dolomite, mixed with ungasified carbonaceous
material, char. The primary separator 52 is a mechanical separator of non-centrifugal
type, suitably a U-beam separator, in accordance with what is described in our European
Patent EP 0 103 613, relating to a CFB boiler and hereby referred to.
[0022] The hot raw gas 2 produced in the gasifier 3 is withdrawn directly from the primary
separator 52 and is fed directly to a gas cleaning secondary stage 25 without any
additional dust removal. The secondary stage 25 is designed as a circulating fast
fluidized bed (CFB) 26 and has the same kind of active bed material as the gasifier
3.
[0023] The raw gas 2 is supplied to the secondary stage 25 so that it constitutes a fluidizing
gas.
[0024] The secondary stage 25 is designed with a long and narrow reactor shaft with arbitrary
cross section (e.g. circular or square). Bed material which follows with the gas
stream out form the top of the reactor shaft is separated to a major part in a primary
particle separator 27, preferably a U-beam separator of the same kind as the U-beam
separator of the gasifier, followed by a secondary separator 28, preferably a cyclone.
The material 30 separated in the primary particle separator is recycled to the lower
part of the circulating bed 26 through a recirculation facility. The material 29
separated in the secondary particle separator 28 is added mainly to the lower part
of the gasifier 3, stream 31. When needed, a part of the material stream 29 also can
be supplied to the lower part of the circulating bed 26, stream 34, and/or be discharged
out of the system, stream 43.
[0025] For feeding fresh catalytic and absorbing material 14 to the secondary stage 25 a
side feeding device 15 located on a suitable height is used. Consumed and/or deactivated
bed material 35 is discharged by means of a discharging device 36 located in connection
with the bottom of the secondary stage 25.
[0026] The active material used in the secondary stage in this example consists of a calcium-magnesium
carbonate containing material, preferably dolomite, with a particle size smaller
than 2 mm, preferably smaller than 1 mm, which in combination with the passing gas
forms the fast circulating fluidized bed 26.
[0027] The gas velocity in the upper section of the reactor shaft, calculated on the free
cross section, is adjusted so that it is below 10 m/s, preferably not above 6 m/s.
[0028] The fluidizing gas of the fast circulating bed 26 consists of the raw gas 2 and
added oxidizing gas 13, e.g. air. When needed additional oxidizing gas 33 can be added
to the secondary stage 25 on one or on several other suitable, higher located levels.
[0029] Conversion of tar and ammonia contained in the raw gas 2 and absorption of chloride
contained in the raw gas take place by means of contact with the catalytic and absorbing
material in the circulating bed 26 within a temperature interval of 600-1000°C, preferably
700-900°C or most preferably 850-950°C. The required temperature level is maintained
by burning combustible gas components inside the secondary stage 25, which is controlled
by adjustment of the amount of added oxidizing gas, streams 13 and 33.
[0030] The average suspension density in the reactor shaft of the secondary stage 25 is
maintained within an interval of 20-300 kg/m³, preferably within an interval of 80-250
kg/m³, so that a necessary contact between the passing gas and the active material
is obtained. This is achieved by adjusting the total amount of circulating material
in combination with controlling the flow rate of recycled material 30 and 34.
[0031] The residence time of the gas in the reactor shaft, calculated on an empty reactor
shaft, is maintained within an interval of 0.2-20 s, preferably within an interval
of 0.5-7 s.
[0032] When needed, activation of deactivated catalytic and absorbing material can be performed
by adding oxidizing gas 32, e.g. air, to the material which is recycled to the lower
part of the circulating bed, streams 30 and 34. The amount of added oxidizing gas
32 is controlled so that the activation takes place within a temperature interval
of 600-1000°C, preferably within an interval of 750-900°C.
[0033] Before starting operation of the process heating of the secondary stage 25 including
its bed material takes place by means of combustion of LP gas 24 therein.
[0034] The refined gas stream 4 leaving the secondary separator 28 of the secondary stage
25 is relieved from entrained finely divided bed material and steam in the subsequent
gas treatment stages.
[0035] The gas passes through two heat exchangers. In the first heat exchanger 37 heat exchange
takes place with oxidizing gas, stream 10, intended for both the gasifier 3 and the
secondary stage 25, so that preheated oxidizing gas 11 at the outlet from the heat
exchanger 37 has a suitable temperature, preferably about 400°C. The preheated oxidizing
gas 11 is used both in the gasifier 3 (among others as fluidizing gas), stream 12,
and in the secondary stage 25, streams 13, 32 and 33.
[0036] In the subsequent second heat exchanger 38 the temperature of the gas 5 is lowered
to a level which permits the outlet gas 6 to be further cleaned by using e.g. standard
textile filters or a cyclone for further dust removal, at 39, i.e. preferably down
to 150-300°C. The removed dust 18 is withdrawn from the dust removal stage 39.
[0037] As mentioned before, the gas stream 4 contains entrained finely divided active material
which follows with the gas stream out of the secondary separator 28. In special cases,
e.g. in connection with gasification of RDF, the raw gas 2 from the gasifier contains
considerable amounts of HCl. Since absorption of HCl on calcareous materials, such
as dolomite, is favoured by sinking temperature, the gas cooling in the heat exchangers
37 and 38 contributes to increase the degree of absorption of residual HCl on the
entrained material.
[0038] The almost dust-free gas 7, which leaves the dust removal stage 39, is fed to a
scrubber 40, in which it is relieved from moisture and other water soluble components.
In the scrubber 40 both moistening of the gas stream 7 and condensation of steam
take place. At the current conditions also precipitation of almost all of the residual
fines and absorption of water soluble gas components, e.g. NH₃, HCl and/or NH₄Cl,
take place.
[0039] The water stream 20 leaving the scrubber 40 is recirculated by a pump 41, whereby
it is cooled in a heat exchanger 42, so that the temperature of the water 19 recycled
to the scrubber 40 is kept within the interval 15-20°C. Excess water 21 is drained
from the water circuit.
[0040] The gas 8 leaving the scrubber can for industrial applications be regarded as pure,
i.e. it is almost free from tars, ammonia, dust, HCl and H₂S. However, at the present
outlet temperatures (about 30°C) it is saturated with steam. Depending on the application,
in order to decrease the relative humidity, the gas stream 8 can be preheated or
passed through an additional drying stage in order to reduce its moisture content.
The pure gas satisfies the requirements for engine operation, e.g. by means of turbocharged
diesel engines, and can be burned without any subsequent exhaust gas cleaning.
[0041] For more simple applications, e.g. heat generation in boilers, the scrubber 40 can
be omitted, so that the refined gas can be utilized either directly after the heat
exchanger 37, stream 22, or after the dust separator 39, stream 23.
[0042] In the described example the secondary stage 25 has been integrated with a gasifier
3 based on CFB technology. The gasifier 3 can produce the raw gas 2 from several different
kinds of fuels, e.g. coarse bark, peat or refuse derived fuels RDF. As bed material
in the circulating bed of the gasifier 3 it is, as mentioned, convenient to use a
catalytic and absorbing material of the same type as in the secondary stage 25.
[0043] The total pressure drop of the oxidizing gas supplied, e.g. air, at the passage through
the production loop, is slightly above 1 bar. This sets requirements on using a compressor
16, which increases the oxidizing gas pressure in stream 9 to the pressure level in
stream 10 necessary in view of the purpose involved.
1. A process for the refining of a raw gas produced from a carbonaceous material by
means of a gasification process, wherein the refining takes place in a secondary stage
separated from the gasifying process, characterized in that in order to reduce the gas contents of tar in form of organic compounds condensible
at lower temperatures such as ambient temperatures, and of ammonia the refining is
carried out in a secondary stage in the form of a fast circulating fluidized bed,
the bed material of which at least to a major part consisting of an active material
in the form of a material that is catalytic for tar and ammonia conversion, possibly
in combination with a contemporaneous addition of oxidizing gas, preferably an oxygen
containing gas and/or steam, while adjusting the constantly present amount of catalytic
material, its particle size, the design of the secondary stage with respect to contact
between gas and solid material, the operating temperature, the amount of possibly
added oxidizing gas and the residence time of the gas, such that a catalytic conversion
of tar and ammonia present in the raw gas takes place, preferably to concentrations
in the refined gas below 500 and 300 mg/Nm³ respectively.
2. A process according to claim 1, characterized by utilizing in order also to decrease the content of hydrogen chloride in the gas,
an active material which also can absorb chloride, the operating temperature also
being adjusted and intermittent or continuous feeding of fresh catalytic and absorbing
material in sufficient amounts taking place so that hydrogen chloride present in the
raw gas will be absorbed on the material, preferably sufficiently far-reaching so
that the concentrations of hydrogen chloride in the refined gas will correspond to
an almost thermodynamic equilibrium, while at the same time a sufficient amount of
constantly present material active for catalytic conversion is maintained, a corresponding
amount of the material containing absorbed chloride being discharged from the secondary
stage intermittently or continuously.
3. A process according to claim 1 or claim 2, characterized in that the operating temperature of the secondary stage is adjusted within the
interval of 600-1000°C, preferably within the interval of 850-950°C.
4. A process according to any one of claims 1, 2 or 3, characterized in that the operating temperature of the secondary stage is controlled by added amounts
of oxygen containing gas.
5. A process according to any one of the preceding claims, characterized in that the active material consists of a magnesium-calcium carbonate containing
material, preferably dolomite, and/or the corresponding calcined (burnt) product.
6. A process according to any one of the preceding claims, characterized in that active material deactivated as a result of carbon deposition or by any other
reason intermittently or continuously is discharged from the secondary stage and
is replaced by equivalent amounts of fresh and/or activated material.
7. A process according to claim 6, characterized in that deactivated active material discharged from the secondary stage is activated
by treatment with an oxidizing gas, preferably an oxygen containing gas and/or steam,
in a separate activating stage, thus activated material being returned to the secondary
stage.
8. A process according to any one of the preceding claims, characterized in that active material deactivated as a result of carbon deposition or by any other
reason is activated by treatment with an oxidizing gas, preferably an oxygen containing
gas and/or steam, in the system recirculating separated bed material of the secondary
stage.
9. A process according to claim 7 or claim 8, characterized in that the activation takes place at an operating temperature within the interval
of 600-1000°C, preferably within the interval of 750-900°C.
10. A process according to any one of claims 7, 8 or 9, characterized in that the operating temperature of the activation is controlled by means of added
amounts of gas containing oxygen.
11. A process according to any one of the preceding claims, characterized in that the raw gas is supplied to the secondary stage directly from the gasifier
without any intermediate dust removal.
12. A process according to claim 11, wherein the gasifier comprises a fast circulating
fluidized bed, characterized in that the raw gas is supplied to the secondary stage directly from the primary
separator of the gasifier without any additional dust separation.
13. A process according to any one of the preceding claims, characterized in that the fluidizing gas of the secondary stage comprises the raw gas and possibly
an oxidizing gas.
14. A process according to claim 12, characterized in that oxidizing gas which does not constitute a fluidizing gas, is added to the
reactor of the secondary stage at one or several levels above the fluidizing gas supply.
15. A process according to any one of the preceding claims, characterized by chosing the total amount of active material present in the secondary stage and
controlling the recirculation flow of bed material for providing a suspension density
of the circulating fast fluidized bed such that the desirable contact between the
passing gas and the active material, for the catalytic conversion, is accomplished.
16. A process according to any one of the preceding claims, characterized in that the gas velocity in the secon dary stage calculated on an empty reactor
shaft, is maintained below 10 m/s, preferably below 6 m/s.
17. A process according to any one of the preceding claims, characterized in that the particle size of the catalytic and absorbing material is smaller than
2 mm, preferably smaller than 1 mm.
18. A process according to any one of the preceding claims, characterized in that the average suspension density in the reactor shaft is maintained within
the interval of 20-300 kg/m³, preferably within the interval of 80-250 kg/m³.
19. A process according to any one of the preceding claims, characterized in that the residence time of the gas calculated on an empty reactor shaft, is kept
within the interval of 0.2-20 s, preferably within the interval of 0.5-7 s.
20. A process according to any one of the preceding claims, characterized in that the hydrogen chloride content in the refined gas, which leaves the secondary
stage, is lowered further by means of absorption on the catalytic and absorbing material
remaining in the gas after the particle separation of the secondary stage, wherein
the gas after the secondary stage first is cooled to a considerably lower temperature,
preferably to a temperature between 150 and 300°C, and then is subject to additional
dust separation.
21. A process according to any one of the preceding claims, characterized in that the raw gas feeding of the secondary stage is connected directly to the
primary particle separator of a gasifier having a fast circulating fluidized bed,
in which the circulating bed material consists of an active material of the same type
as in the secondary stage, in that dust separated in the secondary stage, preferably
in a secondary particle separator, at least partly is recycled to the lower part of
the gasifying reactor, and in that bed material entrained with the raw gas from the
gasifier and material possibly discharged from the bottom of the gasifier are replaced
by the material recycled to the gasifying reactor from the secondary stage in combination
with fresh catalytic and absorbing material which is added to the gasifier intermittently
or continuously.