Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
  • C10J3/02—Fixed-bed gasification of lump fuel
  • C10J3/20—Apparatus; Plants
  • C10J3/34—Grates; Mechanical ash-removing devices
  • C10J3/40—Movable grates
  • C10J3/42—Rotary grates

Definitions

• the invention relates to a method and the associated devices for the
• Carburettors for fixed-bed gasification are operated at high power for economic reasons.
• Crucial for the achievable performance of the carburetor is the most uniform flow through the bed. This is characterized by a stepwise expression of the reaction zones in the bed of the fixed bed in the fixed bed gasifier. From bottom to top, ideally, the reaction zones are the oxidation (fire zone), the gasification (gasification zone), the pyrolysis (pyrolysis zone) and the preheating and drying (drying zone). If there is an uneven flow through the bed with preferential flow near the wall or in channels, the reaction zones are discarded.
• the fire zone can be locally far up to the area of the actual
• Drying zone migrate, the CO2 content of the raw gas increases and it is increasingly discharged dust with the raw gas.
• a high dust discharge represents a loss of gasification substance and complicates the treatment of the raw gas and the hydrocarbons formed during the degassing.
• the amount of dust produced is determined essentially by the primary fines introduced with the gasification substance and the formation of secondary fines during the heating, drying, degassing and gasification of the gasification substance. Due to high temperature gradients, the particles of the gasification material are exposed to high thermal stresses, especially in the sub-processes of heating, drying and degassing, which lead to the disintegration of the particles and thus to the secondary formation of fine particles. Furthermore, fine grain is created by the mechanical stress of the particles during the downward movement of the bed.
• the thermal and mechanical stability of the gasification substances is of crucial importance for the formation of fine particles and the discharge of dust and thus for achievable specific gasifier capacities.
• the resistance to thermal and mechanical stresses decreases in order
• Soft lignite are mostly used as lignite briquettes. These decompose particularly strong in the top of the carburetor and produce much fine grain. The forming bed is therefore unstable even at low specific carburetor and it comes to the intermittent discharge of large amounts of dust.
• Lumpy raw lignite coal with raw coal water contents up to 50% can not be used for reasons of unavailable regular flow in fixed bed gasifiers so far.
• Gasification agent outlets feed the lowest proportion of gasification agents in the bed. Thus, at most the area proportions of the bed to be flowed through section is met. Irregularities arising from the
• Proposal DD260192A3 finally recommends a specific expression of
• a rotary grate is described, in which the distances of the Vergasungsffenauslässe are chosen so large that should form a flow channel at defined, stepped rotation of the grate in the holding period over each Vergasungsffenauslass.
• Low-pressure gas generators are operated with air and subordinate to water vapor as a gasification agent at low pressures to ambient pressure of at most 50 mbar water column.
• the flow resistance of the gasification agent passage through the rotary grate must be strongly limited in relation to the pressure loss of the charge, i. the cross sections of the gasification agent outlets of the rotary grate are designed to be correspondingly large.
• the rotary grate can not take over the distribution of the gasification agent over the cross section of the bed, but the distribution takes place
• DE656988A aims to achieve a uniform distribution of the vapor-air mixture over the entire cross-section of the gas generator shaft, wherein the distribution does not take place via the grate openings, but outside throttle points, which are assigned to grate segments.
• the special throttle points which are assigned to grate segments.
• the object of the invention is seen to act uniformly on the openings of the rotary grate. Apart from the fact that no uniform distribution over the cross section of the bed can be achieved by means of the rotary grate, not even the uniform distribution over the sectors of the rotary grate is achieved, since even over the sectors no higher form can be achieved. DE656988A therefore offers no help, a homogenization of the flow through the bed over the cross section of a lean gas generator or a
• Rotary grate generators basically at the highest possible temperatures in the Oxidation zone operated to granulate the ashes and to keep the flow resistance of the ash zone, of all zones of the worst-flowing zone, as low as possible. Transferred to the in
• annular gas collection channel or distributed over the carburetor cross section a number of Gassammei lenders to produce a uniform bulk movement and gas flow.
• the dust discharge is also in the gasification of chunky coal, whose grain sizes about 5 to 50 mm, in some cases up to 100 mm amount, a hitherto unsolved problem.
• Coarse-grained particles with grain sizes up to 6 mm are also discharged with the raw gas (Bunt 2006). Coarse-grained particles of this particle size can only from gas strands, which emerge with flow rates of several meters per second (m / s) from the fixed bed in the form of flow channels, or by the formation of local fluidized beds on the surface of the fixed bed, the local flow rates of approx. 1 m / s, be entrained in the gas outlet. Locally increased exit velocities are also caused by imbalances and atypically high levels of the firebed, as described by J.R. Colorful and F.B. Described by Waanders and other authors (Bunt,
• the bulk of the raw gas flows either over a relatively small
• one-sided flows cause local concentrations of the reaction zones.
• the processes of drying and degassing proceed at an increased rate, so that these zones have a lower thickness than in the rest of the area Carburetor cross section.
• the accelerated process requires a higher thermal load of the gasification substance and thus a stronger decay and an increased formation of secondary fine grain.
• This fine grain which is discharged at the high flow rate through the gas outlet from the bed and the carburetor as dust, limits the performance of the carburetor.
• Remedy for equalization of the gas flow is to be created by a static coal distributor according to DE112005002983B4, with which the raw gas is sucked from an annular zone in the Gassammeiraum, resulting in a
• the gas exit surface and the bed cross-sectional area are defined herein as cross-sectional areas perpendicular to the axis of the carburetor.
• the gas outlet surface, which forms below the Gassammeiraumes is, according to DE112005002983B4 of the
• the lateral raw gas outlet is for this purpose by a Rohgasabzug or gas extraction duct further up in the
• Fire bed to hot spots in the center of the carburetor or near the wall of the carburetor can be fixed.
• the result are power limitations to excessive dust emissions and / or the formation of large fusion networks or even
• the aim of the invention is to increase the specific power for fixed bed gasifier.
• the invention is based on the object, a method and the associated
• the object is achieved by a method for fixed bed gasification for static and / or dynamic homogenization of the flow and increase the specific carburetor in a fixed bed gasifier with a static coal distribution in the form of a cylindrical Ein rehabilitationschachtes whose top edge with the dome of the fixed bed gasifier is connected, with a continuously or non-continuously rotating rotary grate, which can be designed as a stepped grate, both non-reversible or reversible operable, and
• Has gasification agent outlet openings which open into bulk-free annular spaces, characterized in that the gasification agent of different sectors of the rotary grate (rotary grate sectors) with different sector loads
• the raw gas quantities at the upper limit of the bed to the gas collection room are statically forced or reduced in relation to the sector area ratios, the raw gas quantities withdrawn from at least two manhole areas corresponding to the ratio of maximum to minimum sector area ratio> 1, 1 and preferred > 1, 5 differ from each other, or
• Rohgäsmengen at the upper limit of the bed to Gassammeiraum having over the circumference of the bed at least one radially directed increase (comb) and a radially oriented recess (valley), according to the
• the fixed-bed gasifier is operated with the Einticianschacht with a constant in height, inclined and / or serrated or wavy lower edge so that the bed area ratio as the ratio of the horizontal projection of the entire gas outlet surface at the boundary to the gas collection space to the bed cross-sectional area of the bed is> 0.25, preferably> 0.33.
• the cylindrical bed is limited in by the carburetor inner wall
• Gas collection chamber is assigned to the cross-sectional area of the entire bed, which is referred to as bed area ratio.
• the method for fixed bed gasification is performed so that the gasification agent of different sectors of the rotary grate (rotary grate sectors) with different sector loads (in terms of quantity forced or reduced) into the stainless steel cylinder sectors of the bed of the bed (rust bed sectors) or areas of these sectors is dynamically forced or reduced fed, the sector loads of the forced rotary grate sectors are 20 to 100% higher than the sector loads of reduced rotary grate sectors, and wherein the residence times of the rotary grate sectors in the grate bed sectors are kept the same or varied, and
• the raw gas quantities at the upper limit of the bed to the gas collection room are statically forced or reduced in relation to the sector area ratios, the raw gas quantities withdrawn from at least two manhole areas corresponding to the ratio of maximum to minimum sector area ratio> 1, 1 and preferred > 1, 5 differ from each other, or
• the fixed-bed gasifier is operated with the Einticianschacht with a constant in height, inclined and / or serrated or wavy lower edge so that the bed area ratio as the ratio of the horizontal projection of the entire gas outlet surface at the boundary to the gas collecting space to the bed cross-sectional area of the bed is> 0.25, preferably> 0.33,
• the dynamic forcing generated by the rotary grate or reduction of the loading of the rust bed sectors with gasification agent with the static forcing generated by the Einticianschacht or reducing the flow in the shaft filling sectors by forming different sector area ratios or by the formation of combs and Tuning is done so that at least one generated by an increased sector load dynamic forcing in a grate filling sector and at least one generated by a maximum sector area ratio and / or by a comb of the hanging shaft static forcing in a manhole land sector geometrically corresponding, the horizontal projections of the dynamically forced grate filling sectors and the statically forced manhole sectors coincide or alternate in their angular positions, or preferably three dyna In the horizontal projection, mixed forced rust bed sectors coincide with three statically forced manhole bed sectors in the angular positions.
• the fixed bed pressure gasification takes place for static and dynamic
• Rotary grate sectors and that the residence time of the rotary grate sectors in the area of the grate bed sectors is kept the same or varied
• the rotary grate and the manhole are two elements of a functional unit, which consists in that the flow of the rotary grate circular sectors of the bed of the bed (rust-bed sectors) and the circular sectors of the bed close to the bed of the bed (shaft-bed sectors) of both elements coordinated and sektorgenau is forced and reduced, whereby the flow through the sectors of the bed of the entire bed
• the sector load of the forced sectors of the grate being 20 to 100% higher than the sector load of the reduced sectors of the grate (reduced grate sectors) lies
• sector area ratios are equipped, and that the sector area ratios differ from each other in at least two sectors, so that different amounts of raw gas are deducted from the shaft bed sectors according to the sector area ratios, the Ratio of maximum to minimum sector area ratio> 1, 1 and the bed area ratio as
• the first part of the invention relates to the rotary grate.
• the rotary grate is in accordance with the
• Rust-dumping sectors in the lower part of the bed is made.
• the defined sector loads of the rotary grate sectors point to each Grate filling sector to a defined proportion of supplied gasification agent, which is temporarily variable due to the rotation of the rotary grate. This allows a) permanent, systematic gas flow imbalances, such as the preferred ones
• the rotary grate sectors are set in the position 1-11 o'clock as a reduced rotary grate sector and in the position 11-1 o'clock as a forced rotary grate sector. It is understood that other sectoring such as e.g. 10 o'clock 30 min -1 o'clock 30 min, to be selected.
• Cross sectional area of the rotary grate sector (specific outlet area) is larger than in the reduced rotary grate sector.
• the cross-sectional area of the rotary grate sector is the projection surface in the axial direction.
• For an increase of 20% is the specific outlet area of the forced rotary grate sector 20% higher than that of the reduced rotary grate sector. This is considered constructively in new rotary grates without additional equipment overhead by the outlet surfaces are made correspondingly larger.
• existing grate designs can be changed by very simple adjustments, such as closing every fifth gasification agent outlet in the reduced rotary grate sector or expanding the gasification agent outlets in the forced rotary grate sector by 20%.
• the stepped promotion and reduction of one rotary grate sector described here is referred to as stepped one-sector forcing. Mixed and non-graded, continuous or sliding expansions and reductions in the areas of the gasification agent outlets are also easily possible.
• the fixed bed gasifier is operated so that alternately at least one rotary grate sector with uniformly high and low or with rising and falling
• Sector loads are arranged and the gasification agent supply takes place at a uniformly high and low or at an increasing and decreasing level.
• single-sector forcing represents the non-stepped and sliding symmetrical forcing in one rotary grate sector and the non-stepped and sliding symmetrical reduction in the other rotary grate sector, e.g. by increasing 0 to 20% forcing along the 0-3 o'clock angular position and decreasing 20 to 0% forcing along the 3-6 o'clock angular position, and increasing 0 to 20 percent reduction along the 6-9 o'clock angular position and decreasing 20 to 0 percent reduction along the angular positions 9-12 o'clock.
• the grate filling sector associated with the gas outlet in the position 1 1-1 clock on average only in 1/6 of the operating time applied to the accelerated Vergasungsffenmenge However, 5/6 of the time, the non-gas-related grate filling sector 1-1 1 clock with a locally increased sector load on
• the dynamic rotary grate forcing opens in combination with the stepwise (interrupted) and variable speed rotation of the rotary grate (step operation and stage operation) a further time dimension of the dynamic forcing of the flow through the grate-filling sectors, so that for the first time a controlled, dynamic uniform distribution of the flow over the cross-section of the lower
• Turning grate with one-sector forcing (11-1 o'clock forcing) is rotated stepwise (stepping) so that it is stopped after every 1/3 turn, the grate filling sectors are 1-3 o'clock, 5-7 o'clock and 9- 11 clock forced in the downtime of the rotary grate applied, ie the forced flow is allocated step by step and at sectoral intervals to the grate bed sectors.
• step mode a sectoral slower and faster rotation of the rotary grate (step mode), as well as a combination of both modes, can be done.
• step mode a sectoral slower and faster rotation of the rotary grate
• the rotary grate forcing is indicated by multiple grate bed sectors, for example, by a 50% three sector forcing with the forced sectors in the
• one and two-sector Forcierungen are preferably used when a fixed grate operation is provided for fixed-bed gasifier, in which the rotary grate rotates at several revolutions per hour, for example, greater than 5 h 1 . This is the case when coal with increased ash contents of eg> 10 wt .-% are gasified. Then the rust-bed sectors are forced in sufficiently short intervals.
• fixed-bed gasifiers with slow-moving rotary grates which are also temporarily stopped, are recommended from the aforementioned
• sectoring of the rotary grate can also be carried out differently in the individual stages.
• the inner, middle and outer sections are each supplied with gasifying agent through the upper, middle and lower stages, respectively.
• the grate filling sectors are applied in different areas with different gasification agent.
• the rotary grate sectoring can be made so that the supply with
• the pressure loss at the outlet openings of the lowest-stage gasification means should be at least equal to twice the pressure loss of the ash bed between the lowest and upper stages.
• the annular space is interrupted at intervals, the length of the interruptions being at least 30 mm and the intervals from interruption to interruption being less than 1 m, and the interruptions being arranged such that between forced and reduced rotary grate sectors there is no approximation of the entry velocities the bedding can be done.
• the solution according to the invention can bring its advantages to even greater advantage when the sectored rotary grate is combined with a customized, sectored coal distributor.
• the second part of the invention relates to the use of a static coal distributor in the form of a Ein whschachtes for the process for fixed bed pressure gasification for static equalization of the flow and increase the specific
• each shaft landfill sector has a ratio of the horizontal projection of the gas exit surface to the upper limit of the bed to the gas collection room in associated with each shaft-bedding sector to the cross-sectional area of the manhole bed sector, which is referred to as sector area ratio, and
• Coal bed is allocated, which is referred to as bed area ratio.
• the cylinder sectors of the limited by the carburetor inner wall carburetor interior are equipped by the design and arrangement of the Ein rehabilitationschachtes with defined sector-area ratios, wherein the sector area ratios differ from each other at least two manhole discharge sectors, so according to the sector area ratios different amounts of raw gas are deducted from the manhole fields, the ratio of maximum to minimum sector area ratio> 1, 1 and preferably> 1, 5 and the bed area ratio as a ratio of the horizontal projection of the total
• Gas outlet area to the bed cross-sectional area > 0.25, preferably> 0.33.
• the values of the ratio of maximum to minimum sector area ratio and the bed area ratio shall be discussed. From the ratio size of the sector-area ratios of> 1, 1, the withdrawn raw gas quantities already differ significantly in the sense of a static forcing and reduction. Small values of> 1, 1 are used when only a small forcing or reduction is required; larger values of> 1, 5 up to 1 and even up to 5 are to be used for a massively disturbed, uneven flow.
• the bed area ratio is at least 0.25, but preferably> 0.33. At these values, the exit velocities of the raw gas withdrawn at the upper limit of the bed to the gas collection room increase
• Raw gas in the bed which is usually 0.2 to 0.3 m / s.
• exit velocities are respectively ⁇ 0.8 to ⁇ 1.2 m / s and ⁇ 0.6 to ⁇ 0.9 m / s.
• Speeds are of the order of vortex point velocities. They should not be exceeded, so that no large-scale fluidization of dust above the upper limit of the bed to the gas collection chamber takes place. Accordingly, low bed area ratios of 0.25 are used for fixed deposit carburetors with higher dust removal propensity and higher of 0.33 for fixed bed gasifiers with less tendency to dust discharge and high specific performances.
• the shaft filling sectors look like tall cake pieces.
• the discharge of the raw gas to the gas collection chamber is favored.
• Raw gas discharge due to fine-grained deposits or of melt composites in baking coals be compensated by an increased sector area ratio. This is called sectoral forcing of the raw gas flow.
• the sector-area ratios and the arrangement of the Ein rehabilitationschacht sectors can thus be achieved that the raw gas from the bed below and within the Ein facultyschachtes in normal operation sectorally forced and thus evenly over the circumference of the Gassammeiraumes distributed dissipated in the Gassammeiraum and thus a one-sided flow and formation of the reaction zones is avoided.
• the sector-area ratio of the forced shaft-bedding sectors can be up to 100% higher than that of the reduced manhole-bed sectors.
• the regular operation is characterized with respect to the coal feed by the fact that at any time a sufficiently high coal bed in the fixed-bed gasifier is present, which projects beyond the lower edge of the Einschachtes in height.
• the coal stock in the manhole ensures, among other things, that for the
• the hanger has either a positive, more or less gas-tight, connection to the upper carburetor inner wall, as in DE102012009265B4 the welded construction of a cooled shaft, or the hanger is fastened with detachable connections to the carburetor inner wall, that the width of the annular gap between the Ein yogaschacht and the upper carburetor inner wall is as small as possible, preferably less than 1 cm. This ensures that the sectoral forcing of the raw gas flow, even with a small overlap of the lower edge of the Ein vonschachtes fully occurs.
• a sufficiently large bed area ratio of> 0.25, preferably> 0.33, is required, which guarantees that the Empty tube velocities on entry into the gas collection chamber at less than 1 m / s below the fluidization point of the fine grain introduced with the gasification substances and of the secondary fine grain discharged from the bed, which remains deposited on the bed surface.
• the fixed-bed gasifier can advantageously also be operated such that shaft-bed sectors with high and low sector area ratios with respect to the gas outlet are alternately arranged in such a way that below the gas outlet, a shaft landfill sector with a low sector area ratio and diametrically a shaft Bulk sector with high sector area ratio.
• Fine grain deposits and melt composites are to be expected especially in the areas of the annular Gassammeiraumes, which are opposite to the gas outlet. There, therefore, the higher sector-area ratios are to be realized.
• the upper limit of the bed to Gassammeiraum be set to at least two altitudes in the individual manhole bed sectors, wherein at least one of the altitudes are higher than the altitude of the manhole bed sector below the gas outlet.
• the heights in manhole bulk sectors with high sector-area ratios are higher than the heights in manhole bed sectors with lower sector-area ratios and vice versa.
• the discharge of the raw gas into the annular gas collection chamber can be further equalized by the fact that the altitude of the bed for
• Gas collection chamber with respect to the direction of the gas outlet is different.
• a simple embodiment according to the invention of the hook-in shaft consists in that the cylindrical hook-in shaft to the gas outlet along the extended symmetry axis of the gas outlet is shifted (asymmetrically arranged Ein mentalschacht).
• Sector area ratio of the manhole bulk sector facing the gas outlet is increased by approximately 10-30% compared to the manhole area associated with the gas outlet, the ratio of maximum to minimum sector area ratio always> 1, 1 should be.
• the lower edge of the horizontally offset Ein rehabilitationschachtes is designed in this case beveled so that it drops in the direction of the gas outlet.
• the angle of inclination of the lower edge against the horizontal is smaller than the angle of repose of the gasification substance.
• manhole bulk sectors having an increased sector area ratio can also be achieved, according to the invention, by means of a circular cross-section hanging bay, in that the sectors of the
• the shaft-bed sectors are alternately equipped with a low and a high sector area ratio. But it is also a multiple grading between high and low value possible.
• the high value is at least 50% to 100% above the low value.
• three, four or five forcing and correspondingly three, four or five reductions are applied, wherein the gas discharge associated with the shaft discharge sector is preferably carried out reduced. But there are also more than five forcing possible.
• the forced and the reduced shaft-bed sectors are
• An exception may be the manhole associated with the gas outlet, whose sector angle may be larger and up to twice that of the other manhole sector.
• Another embodiment uses the sector-wise reduction of the diameter of the Ein rehabilitationschachtes or a different kind of sectoral narrowing of the
• the promotion can be temporarily or permanently lifted by the dumping height of the coal bed is temporarily or permanently lowered below the lower edge of the Einitatischachtes.
• the combination consists in the coordinated, sectoral forcing and reduction of the grate filling sectors and the shaft filling sectors as well as a coordinated rotary grate method.
• Rotary grate sectors match (example: a two-sided 3-sector forcing with the positions 0-3 o'clock, 3-6 o'clock, etc.). If, for example, a wider in comparison to the other Ein vonschacht sectors hangman sector selected at the gas outlet, this sectoring can also be beneficial in the same way on the rotary grate be made.
• the potential imbalance of the raw gas flow is statically suppressed, while the gas outlet remote cylinder sectors of the bed are maximally dynamically uniformed. The amount of forcing depends on the requirements of the dynamic equalization according to the specific application, in particular with regard to the flowability of the bed and with regard to the ash content and the type of gasification.
• An advantageous, simple embodiment relates to the combination of non-stepped and sliding, symmetrical one-sector forcing the rotary grate and the asymmetric Einitatischachtes.
• Rotary grate sector (specific outlet area) is increased or decreased and / or in which the Ein rehabilitationschacht has a lower edge with a constant height at which the gasification material quenches and thus outlines the upper limit of the bed to Gassammeiraum, and that the contour and the position the lower edge of the cylinder sectors of the bed assigns different sector area ratios such that the raw gas amounts at the upper limit of the bed to
• Gases are deducted in the ratio of the sector-area ratios by the sector area ratios differ from each other in at least two manhole hoppers and the ratio of maximum to minimum sector area ratio> 1, 1, and preferably> 1.5, the lower edge being designed to be below the shaft fill sector below the
• rotary grate sectors of the rotary grate are delimited from one another in that one of the solids-free annular space, which adjoins the gasification agent outlet openings, at intervals
• interruptions are interrupted, the length of the interruptions being at least 30 mm and the intervals from interrupt to interruption being less than 1 m.
• the suspension shaft is designed with a different cross section (eg circular or oval) and along the extended axis of symmetry of the gas outlet horizontally in the direction of the gas outlet
• Hook-in shaft in the lower part is sectorally cylindrical or conically tapered alternately, wherein below the gas outlet a hook-in sector without rejuvenation and to diametrically a sector with taper is located.
• the suspension shaft with a circular cross section may also be designed sector by sector with different diameters, wherein below the
• Gas outlet be inclined to the horizontal. Is the bottom of the
• Forming surface of the bed to Gassammeiraum formed serrated or wavy is a surface of the bed at the border to Gassammeiraum achieved with radially oriented elevations and depressions in the form of ridges and valleys.
• the gasification substance is discharged to the valleys.
• the slopes thus formed are approximately below the slope angle ⁇ of the
• Gasification inclined to the horizontal This formed from ridges, valleys and connecting slopes surface of the bed is inventively created by the fact that the lower edge of the static coal distribution, on which the gasification substance quenched, is serrated or wave-shaped.
• the spikes can be designed as isosceles triangles or trapezoids.
• Gas collection chamber passes, which can form fluidized beds in the form of jet layers in the area of the combs.
• Fine grain deposits in the valleys are formed at higher levels of fine grain formation
• Fusion networks primarily in the area below the valleys. In addition to the deposition of fine grain have the height of the bed to be flowed through and
• melt composites preferably form below the combs.
• the ridges and valleys are therefore according to the invention with respect to the gas outlet to be arranged so that below the gas outlet a valley and diametrically a comb is located.
• Such a bulk material surface can be produced according to the invention in that the lower edge of the static coal distributor, at which the gasification substance quenches, at an angle which is smaller than the slope angle ⁇ of the
• Gasification substance is inclined downwards towards the horizontal in the direction of the gas outlet.
• such an asymmetrical coal distributor is arranged in the lower area such that the deepest valley forms below the gas outlet, the height of the ridges and valleys decreases in the direction of the gas outlet. This favors the fine grain transport in the direction of gas outlet.
• the maximum amount of fine grain deposits depends on the altitude of the gas outlet on the carburettor. The greater the height difference between the The upper limit of the bed to the gas collection chamber and the gas outlet, the higher the fine grain layer, and thus their influence can be. At high
• Fine grain deposits can form jet layers in the area of the combs, via which the fine grain transport to the gas outlet must take place. Due to the number and shape of the realized combs and valleys and the altitude of the gas outlet can thus be made to adapt to the properties of the gasification substance.
• the heating rate in the area close to the bulk material surface which is crucial for the formation of melt bonds, can also be influenced by the height of the bulk material surface. Will the bottom of the static
• a further advantageous embodiment of the fixed-bed gasifier is also that the lower edge of the Einticianschachtes at which the gasification substance quöscht and thus forms the surface of the bed to Gassammeiraum, serrated or wavy, the teeth have the shape of isosceles triangles or trapezoids , whose legs are inclined approximately at the angle of slope of the gasification substance ⁇ to the horizontal, or wherein the wavy line in the upper and lower region of the periphery of circle segments which are interconnected by common tangents which approximately at the angle of slope of the gasification substance ⁇ against the Horizontal are inclined.
• a further advantageous embodiment of the fixed-bed gasifier according to the invention also consists in the fact that the lower edge of the hook-in shaft is shortened in height in shaft-bed sectors with higher sector-area ratios or vice versa.
• FIG. 1b sectional view in section A-A to Fig. 1a
• Fig. 1d Plan view of the lower part of the fixed-bed gasifier with rotary grate
• Fig. 2a upper part of a fixed bed gasifier with asymmetrically arranged
• FIG. 2b sectional view in section A-A to Fig. 2a
• FIG. 2c top view of the lower part of the fixed bed gasifier with rotary grate
• FIG. 3b sectional view in section A-A to Fig. 3a
• Fig. 5 hanger with a sector-wise extension
• Embodiment 1 shown in Fig. 1, describes an advantageous solution for uniform distribution of the flow in the bed cross section of the entire coal bed of fixed bed gasifier by means of a targeted local Forctechnik the flow through both the execution of the Ein Strukturschachtes and the special
• Inner diameter of 3.9 m is used for the gasification of slightly baking, lumped hard coal 3 with a grain size of about 3 to 50 mm.
• the longitudinal section of the upper part of the fixed bed gasifier 1 is shown in Fig. 1a.
• the hard coal 3 is in Fig. 1a from the above the fixed bed gasifier 1 arranged coal lock (not shown) via the feed shaft 4 in the
• Feeder shaft 4 of the 2 m long Einitatischacht 6 is arranged.
• Top edge 7 of the Ein rehabilitationschachtes 6 is with detachable connections 8, with a very small gap of a few mm ( ⁇ 1cm), not conclusive with the
• the suspension shaft 6 is used, inter alia, as a storage space for the coal 3, so that the upper limit 10 of the Kohleschu 11 11 between two acceleration operations not below the lower edge 12 of the
• Hook-in shaft 6 (outer diameter 3.1 m) is conically tapered in the lower half 13 sectorwise (except for the diameter 2.5 m) and the lower edge 12 is formed horizontally flat.
• the side gas outlet 14 In the amount of the upper half of the Ein rehabilitationschachtes 6 is the side gas outlet 14. The Ein rehabilitationschacht 6 lies in the
• Fig. 1a thus shows, as well as Fig. 1b and 1c, the static forcing the flow in the upper part of the bed 11 by the special configuration of the Ein vonschachtes. 6
• Fig. 1b shows a sectional view in section A-A to Fig. 1a.
• the cylindrical bed 11 in the limited by the carburetor inner wall 9 interior 5 of the
• Carburettor 1 is conceptually subdivided into geometric cylinder sectors, which are referred to in the vicinity of the hang-in shaft 6 as shaft-bulkhead sectors.
• the six shaft filling sectors are based on a mental subdivision according to times 11-1 clock (11 00 -1 00 ), 1-3 clock (1 00 - 3 00 ), 3- 5 o'clock (3 00 -5 00 ), 5-7 o'clock (5 00 -7 00 ), 7-9 o'clock (7 00 -9 00 ) and 9-11 o'clock (9 00 -11 00 ) drawn.
• the shaft filling sectors 1-3 o'clock, 5-7 o'clock and 9-11 o'clock are flow-forced by the rejuvenation of the Ein rehabilitationschachtes 6 in these ranges and the shaft filling sectors 11-1 o'clock, 3-5 o'clock and 7-9 o'clock are flow-reduced.
• According to the invention are located at the gas outlet 14 at 12 o'clock position with the sector 11-1 clock a flow-reduced sector (hatched sector 19) and diametrically opposite the gas outlet 14 a flow-reinforced sector
• Each cylinder sector is a ratio of the horizontal projection of the
• the sector area ratio of the flow-forced manhole land sectors is 60% higher than the sector area ratio of the reduced-flow manhole land sectors.
• the total bed 11 as the buzzer of all cylinder sectors is associated with a ratio of the horizontal projection of the entire gas outlet surface at the upper limit 10 of the bed 11 to the gas collection chamber to the cross-sectional area of the entire bed 11, which is referred to as bed area ratio.
• the bed area ratio in the first embodiment is 0.48.
• the hook-in shaft 6 with sector-wise conical taper is illustrated in FIG. 1c in a non-scale spatial representation.
• Gas collection room which serves as a calming room, can settle before the raw gas leaves the carburetor 1 via the gas outlet 14.
• the gas velocity of the raw gas increases at the outlet of bed 11 as in the embodiment 1 only conditionally (from an empty tube speed between 0.25-0.3 m / s to about 0.5-0.6 m / s). This ensures that no
• Grate filling sectors 11-1 o'clock, 1-3 o'clock, 3-5 o'clock, 5-7 o'clock, 7-9 o'clock and 9-11 o'clock are drawn.
• the gas outlet 14 (not shown) is in the 12 o'clock position.
• the rotary grate 15 is equipped with a 30% three-sector forcing, wherein in Fig.ld the flow-reinforced grate-bed sectors are at 1-3 o'clock, 5-7 o'clock and 9-11 o'clock and the flow-reduced grate-bed sectors
• Positions 11-1 o'clock, 3-5 o'clock and 7-9 o'clock are assigned. According to the invention is located in the position of the gas outlet 14 at 12 o'clock with the sector 11-1 clock a flow-reduced grate filling sector 22 (hatched) and diametrically thereto a flow-forced grate-bed sector, which acts by the rotary grate sector 23 (hatched) with gasification agent is.
• the rotary grate 15 is rotated at 10 revolutions per hour, i. 1 turn per
• Embodiment 2 shown in Fig. 2, describes a simple advantageous solution for suppressing imbalances of the gas flow to the gas outlet 14 in fixed bed gasifier 1 by means of a targeted local Forctechnik the flow through both the execution of the Einticianschachtes 6 and the special
• the fixed bed gasifier 1 in Fig. 2a with the pressure-bearing outer shell 2 and an inner diameter of 3.9 m is used for the gasification of lumped hard coal 3 with a grain size of about 3 to 50 mm.
• the longitudinal section of the upper part of the fixed-bed gasifier 1 is shown in FIG. 2 a and, like FIG. 2 b, shows the static forcing of the flow in the upper part of the bed due to the special configuration of the hook-in shaft 6.
• the hard coal 3 is shown in Fig. 2a from the above the fixed bed gasifier 1 arranged coal lock (not shown) via the feed shaft 4 in the
• Feeder shaft 4 is a 2 m long Ein knowledgeschacht 6 is arranged.
• Top edge 7 of the hook-in shaft 6 is not connected in a form-fitting manner to the carburetor inner wall 9 with detachable connections 8. Which is between the
• Insertion shaft 6 and the upper carburetor inner wall 9 forming gap is smaller than 1 cm.
• the hook-in shaft 6 serves, inter alia, as a storage space for the coal 3, so that the upper limit 10 of the bed 11 between two acceleration operations does not fall below the lower edge 12 of the Ein rehabilitationschachtes 6 and thus ensures a constant bed height of the bed 11 during operation.
• the cylindrical hook-in shaft 6 (outer diameter 3.1 m) is evenly conically tapered in the lower half 13 (except for the diameter 2.5 m) and the lower edge 12 is formed horizontally flat. At the height of the upper half of the
• the suspension shaft 6 is displaced from the symmetry axis 16 of the fixed bed gasifier 1 to the gas outlet 14 along the extended axis of symmetry 17 of the gas outlet 14 by 0.2 m, so that the axis of symmetry 18 of the Ein rehabilitationschachtes 6 by 0.2 m from the symmetry axis 16 of the fixed bed gasifier. 1 differs. From the lower edge 12 of the Ein rehabilitationschachtes 6, the bed 11 böscht evenly in the interior 5 of the carburetor 1 from. By the cone-shaped
• Fig. 2b shows a sectional view in section A-A to Fig. 2a.
• the cylindrical bed 11 in the limited by the carburetor inner wall 9 interior 5 of the
• Carburettor 1 is conceptually subdivided into geometric cylinder sectors, which are referred to in the vicinity of the hang-in shaft 6 as shaft-bulkhead sectors.
• Fig. 2b, section A-A the simple sectoring of the Ein vonschachtes 6 is shown.
• the flow-reduced shaft filling sector 19 hatchched in the position 10: 30-1: 30 o'clock faces the gas outlet 14 (position 12 o'clock) and the flow-forced shaft filling sector 20 in the position 1: 30-10.30 o'clock from the gas outlet 14.
• the sector area ratio of the flow-forced manhole bulk sector at 1: 30-10: 30 hours is 95% higher than the sector area ratio of the
• Fixed bed gasifier 1 with the outer casing 2 and the rotary grate 15 shown.
• the rotary grate 15 is indicated by the outer edge 21.
• the rotary grate 15 is equipped with a 40% one-sector forcing in the position 5-7 clock, wherein in Fig. 2c of the gas outlet 14 close to reduced area of the grate-dumping sector 22 (hatched) according to the invention straight in position 11- 1 clock and the forced rotary grate sector 23 (hatched) is currently in position 1-11 clock.
• the gas outlet 14 (not shown) is in the 12 o'clock position.
• the rotary grate 15 is at 10 revolutions per hour, ie 1 revolution per
• Fig. 3a shows a solution for suppressing imbalances of the gas flow to the gas outlet in the upper part of the fixed-bed gasifier 1.
• the fixed-bed gasifier 1 in Fig. 3a with the pressure-bearing outer shell 2 and an inner diameter of 3.9 m is used for gasification of non-baking, lumpy hard coal 3 with a grain size of about 3 to 50 mm used.
• the hard coal 3 is introduced from the coal sluice (not shown) arranged above the fixed-bed gasifier 1 via the feed chute 4 into the carburetor interior 5 of the fixed-bed gasifier 1. Below the
• Feeder shaft 4 is an average of 2 m long Ein theoryschacht 6 is arranged.
• the upper edge 7 of the Einticianschachtes 6 is not connected with releasable connections 8 form fit with the carburetor inner wall 9. Which is between the
• Insertion shaft 6 and the upper carburetor inner wall 9 forming gap is smaller than 1 cm.
• the hook-in shaft 6 serves, inter alia, as a storage space for the coal 3, so that the upper limit 10 of the bed 11 between two acceleration operations does not fall below the lower edge 12 of the Ein rehabilitationschachtes 6 and thus ensures a constant bed height of the bed 11 during operation.
• the cylindrical attachment shaft 6 (outer diameter 3.1 m) is conically tapered in the lower half 13 (except for the diameter of 2.5 m) and the lower
• Edge 12 formed inclined by 8 °.
• Edge 12th formed inclined by 8 °.
• the suspension shaft 6 is from the symmetry axis 16 of the fixed-bed gasifier 1 to the gas outlet 14 along the extended axis of symmetry 17 of the gas outlet 14th shifted by 0.2 m, so that the axis of symmetry 18 of the Ein rehabilitationschachtes 6 deviates by 0.2 m from the axis of symmetry 16 of the fixed-bed gasifier 1.
• Fig. 3b shows a sectional view in section A-A to Fig. 1a.
• the cylindrical bed 11 in the limited by the carburetor inner wall 9 interior 5 of the
• Carburettor 1 is conceptually subdivided into geometric cylinder sectors, which are referred to as manhole land sectors near hanger shaft 6.
• the six shaft-bedding sectors are based on a mental subdivision according to times 11-1 clock (11 00 -1 00 ), 1-3 clock (1 00 - 3 00 ), 3- 5 o'clock (3 00 -5 00 ), 5-7 o'clock (5 00 -7 00 ), 7-9 o'clock (7 00 -9 00 ) and 9-11 o'clock (9 00 -11 00 ) drawn.
• Each manhole bed sector is assigned a ratio of the horizontal projection of the gas outlet surface at the upper limit 10 of the bed 11 to the gas collection chamber in the respective cylinder sector to the cross-sectional area of the cylinder sector, which is referred to as sector area ratio.
• the manhole sector 11-1 o'clock is near the gas outlet 14 at 12 o'clock position (hatched tray filling sector 19) and the sector 5-7 o'clock opposite the gas outlet 14 (hatched tray filling sector 20).
• the sector area ratios increase from pit-land sector 19 (minimum sector area ratio) to pit-land sector 20 (maximum sector area ratio). In the present example, the maximum sector area ratio is 24% higher than the minimum sector area ratio.
• the total bed 11 as buzzer of all cylinder sectors is a ratio of the horizontal projection of the entire gas outlet surface at the upper limit 10 of the bed of coal 11 to the gas collection chamber to the cross-sectional area of the entire Kohlesch üttung assigned 11, which is referred to as bed area ratio.
• the bed area ratio in the first embodiment is 0.59.
• Gas outlet 14 sloping bottom edge 12 is formed during the gasification, upwardly rising crude gas preferably from the gas outlet 14th
• Fig. 4 shows a simplified form of the Ein Strukturschachtes 6 according to
• Embodiment 1 in a schematic spatial representation.
• the simplification concerns the formation of two rather than six manhole sectors.
• the low-flow shaft filling sector 19 in the position 10-2 o'clock is located at the gas outlet 14 (position 12 o'clock) and the flow-forced manhole sector 20 in the position 2-10 o'clock opposite the gas outlet 14.
• Fig. 5 shows in a simplified form, the sector-by-section enlargement of the diameter of the Einticianschachtes 6, wherein the flow-reduced manhole bulk sector 19 in the position 10-2 o'clock at the gas outlet 14 (12 o'clock position) and the flow-forced shaft-bed sector 20 in position -10 o'clock opposite the gas outlet 14 is located.
• the magnification is carried out in the lower third of the Ein vonschachtes 6.
• FIGS. 6 to 8 show examples of different configurations of the lower one
• the serrations have the shape of isosceles triangles with the height hi.
• formed on the surface of the bed primarily pointed ridges and valleys.
• the legs of the triangles are approximately below the slope angle ⁇ of the
• the tines are designed as isosceles trapezoids with the height h2.
• the ridges have a flat top and the valleys a flat sole.
• the legs of the trapezoids are analogous to FIG. 2 approximately below the
• the lower edge 12 of the Ein rehabilitationschachtes 6 is designed so that form dome-shaped ridges and trough-shaped valleys. This is achieved by a wave-shaped design of the lower edge 12 of the Ein von hereachtes 6. These waves consist in the region of the ridges or valleys from the periphery of circle segments, which are interconnected by common tangents. The inclination of these tangents with respect to the horizontal should approximately correspond to the angle of repose ⁇ of the gasification substance. The height of the waves is equal to the vertical distance h3 between the highest and the lowest point of the wavy line.
• the hook-in shaft 6 is arranged with the lower serrated or wave-shaped edge in such a way that it extends below the lower edge
• Gates 14 a valley and forms a ridge diametrically to this valley.
• Such an arrangement which is achievable with the same design of the ridges and valleys only with an odd number of spikes or bulges, favors the fine grain transport to the gas outlet via spout layers.

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• 2015
  • 2015-07-28 CN CN201580040790.9A patent/CN106574194B/zh active Active
  • 2015-07-28 WO PCT/DE2015/000384 patent/WO2016015705A1/de active Application Filing

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