CN105080335A - Denitration equipment and replacing method of catalyst - Google Patents
Denitration equipment and replacing method of catalyst Download PDFInfo
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- CN105080335A CN105080335A CN201410553897.0A CN201410553897A CN105080335A CN 105080335 A CN105080335 A CN 105080335A CN 201410553897 A CN201410553897 A CN 201410553897A CN 105080335 A CN105080335 A CN 105080335A
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Abstract
The utility model provides denitration equipment which can remove nitrogen oxides efficiently in longer period or a replacing method of a catalyst. The denitration equipment comprises a waste gas channel (40f) allowing waste gas to flow, a rectifying and denitration catalyst layer (80) arranged on the waste gas channel (40f) and at least one denitration catalyst layer (82, 84, 86) arranged in the position, close to the downstream side of the rectifying and denitration catalyst layer (80) in the waste gas flowing direction, of the waste gas channel (40f). The length of the rectifying and denitration catalyst layer (80) in the waste gas flowing direction is shorter than the length of the denitration catalyst layers (82, 84, 86) in the waste gas flowing direction.
Description
Technical field
The replacing options of the catalyst of the denitration device that the present invention relates to the nitrogen oxide removed contained by waste gas and the catalyst changing denitration device.
Background technology
As being the burner that fuel makes it burn with coal, having and fuel pulverized and carries out as fine coal the boiler that burns.In existing fine coal incinerator, supply the gaseous mixture of fine coal (fuel) and carrying air (primary air) of being pulverized by coal, and supply the auxiliary air of high temperature, this gaseous mixture and auxiliary air are blown in stove, thus formation flame, can burning gases be generated.Further, this stove is linked with flue on top, being provided with the superheater, reheater, economizer etc. of the heat for reclaiming waste gas, the waste gas produced because of burning can be utilized to carry out heating water and generating steam in this flue.In addition, this flue and exhaust passageway link, and be provided with denitration device, electric precipitation machine, desulfurizer etc., and be provided with chimney at downstream end in this exhaust passageway.
The stacked denitrating catalyst (with reference to patent document 1) being configured with the reduction reaction promoting nitrogen oxide in denitration device.As denitrating catalyst, there are the tabular catalyst that is laminated along the direction orthogonal with the direction that waste gas passes through by plate and the honeycomb type catalyst in cellular perforate.In addition, as the denitrating catalyst used in denitration device, the end face of the side that catalyst gas flows into is provided with coating (with reference to patent document 2).
At first technical literature
Patent document
Patent document 1: Japanese Unexamined Patent Publication 2008-126148 publication
Patent document 2: Japanese Unexamined Patent Publication 2000-237600 publication
At this, when burning as fuel using coal, in waste gas, being mixed into combustion ash, not firing composition, be also mixed into combustion ash, do not fire the explosion ash content of composition bonding (block ash).If explosion ash content arrives denitration device, on the denitrating catalyst being deposited in denitration device sometimes with the state being contained in waste gas.If explosion ash content is piled up on denitrating catalyst, then reduce at the waste gas of this partial-flow or do not exist, the removal capacity of nitrogen oxide reduces, and needs to carry out the maintenances such as replacing.
In addition, if containing various solid contents such as dusts in waste gas, make denitrating catalyst wear and tear sometimes.On the other hand, mar proof can be improved by a part for protection inflow side as described in Patent Document 2, but denitration performance reduces.
Summary of the invention
The problem that invention will solve
The invention solves above-mentioned problem, its object is to provide in longer-term, denitration device and catalyst-replacing method that nitrogen oxide can be removed efficiently.
Solution
In order to realize described object, the feature of denitration device of the present invention is, described denitration device has: exhaust passageway, and it is for exhaust-gas flow; Rectification is held concurrently denitration catalyst oxidant layer, and it is arranged at described exhaust passageway; And the denitration catalyst oxidant layer of at least one deck, rectification described in its ratio being configured at described exhaust passageway is held concurrently the position of denitration catalyst oxidant layer by the flow direction downstream of waste gas, described rectification hold concurrently denitration catalyst oxidant layer described waste gas flow direction on length shorter than the length on the flow direction of the described waste gas of described denitration catalyst oxidant layer.
Preferably be configured to, the hold concurrently hydraulic diameter of catalyst opening portion of denitration catalyst oxidant layer of described rectification is larger than the hydraulic diameter of the catalyst opening portion of described denitration catalyst oxidant layer.
In addition, be preferably configured to, the hold concurrently hydraulic diameter of catalyst opening portion of denitration catalyst oxidant layer of described rectification is more than 8mm.
In addition, be preferably configured to, described rectification denitration catalyst oxidant layer of holding concurrently is tabular catalyst, and described denitration catalyst oxidant layer is honeycombed catalyst.
In order to realize described object, the feature of denitration device of the present invention is, described denitration device has: exhaust passageway, and it is for exhaust-gas flow; Rectification layer, it is arranged at described exhaust passageway; And at least two-layer denitration catalyst oxidant layer, described in its ratio being configured at described exhaust passageway, rectification layer is by the position in the flow direction downstream of waste gas, the flow direction of the described waste gas of described at least two-layer denitration catalyst oxidant layer be tabular catalyst by the denitration catalyst oxidant layer of upstream side, the denitration catalyst oxidant layer of swimming side most on the lower of the flow direction of described waste gas is honeycombed catalyst, and the denitration catalyst oxidant layer of all described tabular catalyst is configured in the position leaning on the upstream side of the flow direction of described waste gas than the denitration catalyst oxidant layer of described honeycombed catalyst.
In order to realize described object, the feature of denitrification apparatus of the present invention is, described denitration device has: exhaust passageway, and it is for exhaust-gas flow; Rectification layer, it is arranged at described exhaust passageway; And the denitration catalyst oxidant layer of at least one deck, described in its ratio being configured at described exhaust passageway, rectification layer is by the position in the flow direction downstream of waste gas, with flow in described denitration catalyst oxidant layer waste gas mean flow rate compared with the relatively slow area configurations of flow velocity have tabular catalyst, the area configurations relatively fast at flow velocity compared with described mean flow rate has honeycombed catalyst.
In addition, from the view point of the increase of the pressure loss suppressing catalyst abrasion and foreign matter to cause, be preferably configured to, described exhaust passageway makes described waste gas flow towards downside on the upside of vertical.
In order to realize described object, the replacing options of catalyst of the present invention is the replacing options of the catalyst of denitration device, this denitration device has rectification layer and is configured in the direction of flow of the exhaust gases than the denitration catalyst oxidant layer of the position of described rectification layer downstream, it is characterized in that, the replacing options of this catalyst comprises the following steps: judge whether described rectification layer possesses catalyst function; And when described rectification layer does not possess catalyst function, denitration catalyst oxidant layer that the rectification that described rectification layer is replaced by the function possessing denitrating catalyst is held concurrently.
In addition, be preferably configured to, the hold concurrently hydraulic diameter of catalyst opening portion of denitration catalyst oxidant layer of described rectification is more than 8mm.
In addition, be preferably configured to, described rectification denitration catalyst oxidant layer of holding concurrently is tabular catalyst.
In order to realize described object, the replacing options of catalyst of the present invention is the replacing options of the catalyst of denitration device, this denitration device has rectification layer and is configured in the direction of flow of the exhaust gases than at least two-layer denitration catalyst oxidant layer of the position of described rectification layer downstream, it is characterized in that, the replacing options of this catalyst comprises the following steps: find out the denitration catalyst oxidant layer that will change; And when the described denitration catalyst oxidant layer that will change does not have honeycombed catalyst at the upstream side of the flow direction of described waste gas, be replaced by tabular catalyst.
In order to realize described object, the replacing options of catalyst of the present invention is the replacing options of the catalyst of denitration device, this denitration device has rectification layer and is configured in the direction of flow of the exhaust gases than the denitration catalyst oxidant layer of at least one deck of the position of described rectification layer downstream, it is characterized in that, the replacing options of described catalyst comprises the following steps: find out the denitration catalyst oxidant layer that will change; And the described denitration catalyst oxidant layer that will change is replaced by has tabular catalyst in the area configurations that flow velocity is relatively slow and the denitration catalyst oxidant layer having honeycombed catalyst in the area configurations that flow velocity is relatively fast.
Invention effect
According to denitration device of the present invention and catalyst-replacing method, in longer-term, nitrogen oxide can be removed efficiently.
Accompanying drawing explanation
Fig. 1 is the brief configuration figure of the fine coal incinerator representing the denitration device applying the first embodiment.
Fig. 2 is the brief configuration figure of the denitration device that the first embodiment is shown.
Fig. 3 is that rectification is held concurrently the top view of denitration catalyst oxidant layer.
Fig. 4 amplifies to illustrate that rectification is held concurrently the amplification plan view of tabular catalyst of denitration catalyst oxidant layer.
Fig. 5 amplifies the amplification plan view that the honeycombed catalyst of denitration catalyst oxidant layer is shown.
Fig. 6 is the curve map of an example of the conversion that the duration of runs and denitration performance are shown.
Fig. 7 is the curve map of the relation illustrated between catalyst length and conversion coefficient.
Fig. 8 is the flow chart of an example of the replacing options of the catalyst that denitration device is shown.
Fig. 9 is the brief configuration figure of the denitration device that the second embodiment is shown.
Figure 10 is the flow chart of an example of the replacing options of the catalyst that denitration device is shown.
Figure 11 is the brief configuration figure of the denitration device that the 3rd embodiment is shown.
Figure 12 is the top view of denitration catalyst oxidant layer.
Figure 13 is the curve map of the relation illustrated between denitrating catalyst and the pressure loss.
Figure 14 is the flow chart of an example of the replacing options of the catalyst that denitration device is shown.
Figure 15 is the top view of other examples of the denitrating catalyst that the 4th embodiment is shown.
Description of reference numerals is as follows:
10: fine coal incinerator
11: stove
21: burner
40: flue (exhaust passageway)
41,42: superheater (heat recovery section)
43,44: reheater (heat recovery section)
45,46,47: economizer (heat recovery section)
50,50a, 50b: denitration device
61,62: hopper
70: reducer feeding device
80: rectification is held concurrently denitration catalyst oxidant layer
82,82a, 182: the first denitration catalyst oxidant layer
84,184: the second denitration catalyst oxidant layer
86,186: the three denitration catalyst oxidant layer
100,110a, 250,260,270,310: tabular catalyst
102,112,112a, 122,132,162,212,222,232: supporting device
110,120,130,252,262,272,312: honeycombed catalyst
150: control device
152: reporting unit
160: rectification layer
Detailed description of the invention
Below, with reference to accompanying drawing, the preferred embodiment of the present invention is described in detail.It should be noted that, and can't help this embodiment to limit the present invention, in addition, when there is multiple embodiment, combining each embodiment and the scheme formed also is contained in the present invention.
[the first embodiment]
Fig. 1 is the brief configuration figure of the fine coal incinerator representing the denitration device applying the first embodiment.The fine coal incinerator applying the denitration device of the first embodiment can use the fine coal pulverized by coal as solid fuel, utilizes burner to make this pulverized coal friring, and reclaims the heat produced because of this burning.It should be noted that, at this, though apply fine coal incinerator and be described, the present invention is not limited to the boiler of this form.Denitration device can be used as the equipment removing nitrogen oxide from the waste gas making to generate containing the fuel combustion of coal.Therefore, the burner of fuel combustion is made to be not limited to boiler.In addition, do not limit yet only make fuel be pulverize after coal burning.Denitration device also can be used as the treatment facility of the waste gas of discharging from the burner of mixed combustion type, and coal and liquid fuel, gaseous fuel mix as fuel and make it burn by the burner of mixed combustion type.
As shown in Figure 1, the fine coal incinerator 10 of this first embodiment is conventional oven, has stove 11 and burner 12.Stove 11 is the hollow shape of square tube and arranges along vertical, is provided with burner 12 in the bottom of the stove wall forming this stove 11.
Burner 12 has multiple burner 21 being assemblied in stove wall.In the present embodiment, with circumferentially using this burner 21 arranged all at equal intervals as one group, configure five groups along vertical, in other words, be configured with five layers.
Further, each burner 21 links with fine coal feedway 30.Fine coal feedway 30 has fine coal supply pipe, coal pulverizer (flour mill), from coal pulverizer via fine coal supply pipe to burner 21 feeding pulverized coal.Fine coal feedway 30 utilizes carrying air (primary air) to sieve, and the fine coal sieved out and carrying air is supplied to burner 21.
In addition, stove 11 is provided with bellows 36 at the rigging position of each burner 21, these bellows 36 is linked with an end of air hose 37, is equipped with pressure fan 38 in the other end of this air hose 37.Therefore, it is possible to the combustion air utilizing pressure fan 38 to carry (auxiliary air, tertiary air) is supplied from air hose 37 to bellows 36, and supply from these bellows 36 to each burner 21.
Therefore, the fine powder fuel mixture (fuel gas) that each burner 21 can utilize burner 12 fine coal and primary air to be mixed is blown in stove 11, and auxiliary air can be blown in stove 11, by utilizing not shown igniter to light a fire to fine powder fuel mixture, flame can be formed thus.It should be noted that, generally when the starting of boiler, oil fuel sprays and forms flame by each burner 21 in stove 11.
Flue 40 is linked with on the top of stove 11, be provided with in this flue 40 as convective heat transfer portion (heat recovery section) superheater (superheater) 41 of the heat reclaiming waste gas, 42, reheater (reheater) 43,44 and economizer (economizer) 45,46,47, carry out heat exchange at the waste gas produced because of the burning in stove 11 with between convective heat transfer portion (heat recovery section) middle water of flowing or steam.
The flue gas leading (exhaust passageway) 48 supplying the waste gas after carrying out heat exchange to discharge is linked with in the downstream of flue 40.Air preheater 49 is set between this flue gas leading 48 and air hose 37, carries out heat exchange flowing through between the air of air hose 37 and the waste gas flowing through flue gas leading 48, the combustion air being supplied to burner 21 can be made to heat up.
In addition, in flue gas leading 48, be provided with denitration device 50 in the position of the upstream side of air preheater 49, be provided with coal dust treating apparatus (electric precipitation machine, desulfurizer) 51 in the position in the downstream of air preheater 49, guide pressure fan 52, and be provided with chimney 53 at downstream end.Denitration device 50 and coal dust treating apparatus 51 play function as harmful substance removal unit.About denitration device 50, be described later.
In flue gas leading 48, denitration device 50 is utilized to remove NO by the waste gas G after the economizer 45,46,47 of flue 40
xetc. harmful substance, utilize coal dust treating apparatus 51 remove particulate material and remove sulfur component, discharge to air from chimney 53 afterwards.
In the fine coal incinerator 10 so formed, the part in the downstream (flue 40) of stove 11 as the first embodiment blast pipe and play function.Further, this flue 40 is by arranging the first horizontal flue portion 40a, the first vertical gas pass portion 40b, the second horizontal flue portion 40c, the second vertical gas pass portion 40d, the 3rd horizontal flue portion 40e, the 3rd vertical gas pass portion 40f and the 4th horizontal flue portion 40g continuously and forming.3rd horizontal flue portion 40e becomes the fold back portion of the flow direction linked in vertical the second different vertical gas pass portion 40d and the 3rd vertical gas pass portion 40f.In addition, the second vertical gas pass portion 40d makes waste gas G flow on the upside of vertical.3rd vertical gas pass portion 40f makes waste gas G flow on the downside of vertical.
Further, the first horizontal flue portion 40a of flue 40 and the first vertical gas pass portion 40b be configured with superheater 41,42, reheater 43,44 and economizer 45,46,47.In addition, in flue 40, be provided with hopper 61 in the bottom of the first vertical gas pass portion 40b of the waste gas G flowing for the velocity component had down, be provided with hopper 62 in the bottom of the second vertical gas pass portion 40d of the waste gas G flowing for the velocity component had upward.Hopper 61,62 reclaims and stockpiles the PA (solid particle) the waste gas G fallen from the first vertical gas pass portion 40b, the second vertical gas pass portion 40d etc.In addition, a part for denitration device 50 is provided with at the 3rd vertical gas pass portion 40f supplying waste gas G to flow downward of flue 40.A part for denitration device 50 is configured with at the second vertical gas pass portion 40d of flue 40.
Next, on the basis of Fig. 1, use Fig. 2 ~ Fig. 5 to be described denitration device 50.Fig. 2 is the brief configuration figure of the denitration device that the first embodiment is shown.Fig. 3 is that rectification is held concurrently the top view of denitration catalyst oxidant layer.Fig. 4 amplifies to illustrate that rectification is held concurrently the amplification plan view of tabular catalyst of denitration catalyst oxidant layer.Fig. 5 amplifies the amplification plan view that the honeycombed catalyst of denitration catalyst oxidant layer is shown.
Ammonia, urea water etc. have and supply in flue 40 reducing agent of the effect that nitrogen oxide reduces by denitration device 50, making the waste gas G after supply reducing agent by promoting the selective reduction type catalyst of the reaction of nitrogen oxide and reducing agent, removing thus, the nitrogen oxide reduced in waste gas G.As shown in Figure 1 and Figure 2, denitration device 50 has reducer feeding device 70, denitration catalyst oxidant layer 80, first denitration catalyst oxidant layer 82, second denitration catalyst oxidant layer 84 is held concurrently in rectification, the 3rd denitration catalyst oxidant layer 86, pressure gauge 140,146, nitrous oxides concentration meter 148, control device 150, ammoniameter 149 and reporting unit 152.
Reducer feeding device 70 is the devices supplying reducing agent in flue 40.Reducing agent can use ammoniacal liquor, ammonia, urea water etc.In reducer feeding device 70, supply port reducing agent being supplied to the inside of flue 40 is configured at the second vertical gas pass portion 40d of flue 40, supplies reducing agent by discharging (ejection) reducing agent from supply port in the second vertical gas pass portion 40d.The reducing agent supplied from reducer feeding device 70, while move together with waste gas G, spreads in the path that confession waste gas G flows.
Rectification denitration catalyst oxidant layer 80 of holding concurrently is configured at the 3rd vertical gas pass portion 40f of flue 40.Rectification is held concurrently, and to flowing into from the 3rd horizontal flue portion 40e to the 3rd vertical gas pass portion 40f, the waste gas G stream of flow direction change carries out rectification to denitration catalyst oxidant layer 80, and promotes the reaction of nitrogen oxide and reducing agent.Rectification denitration catalyst oxidant layer 80 of holding concurrently has tabular catalyst 100 and tabular catalyst 100 is fixed on the supporting device 102 of the 3rd vertical gas pass portion 40f.As long as supporting device 102 can support the mechanism of tabular catalyst 100, structure does not limit especially.
As shown in Figure 3, multiple catalyst assemblies 106 of tabular catalyst 100 are configured as line column-shaped.Tabular catalyst 100 configures in the mode of whole of the horizontal plane of multiple catalyst assembly 106 shutoff the 3rd vertical gas pass portion 40f.Thus, the waste gas G flowed in the 3rd vertical gas pass portion 40f is by catalyst assembly 106.In the catalyst assembly 106 of tabular catalyst 100, as shown in Figure 4, multiple plates (such as metallic plate) 108 with catalyst function configure along the direction (direction orthogonal with the flow direction of waste gas become the thickness direction of plate towards) of waste gas.Multiple plates 108 of catalyst assembly 106 configure side by side.In addition, in catalyst assembly 106, the hydraulic diameter of the catalyst opening portion 107 between the plate 108 of configured in parallel and plate 108 is more than 8mm.The hydraulic diameter of the catalyst opening portion 107 of tabular catalyst 100 can be represented by (4 × A)/L.A is the area of section of opening portion, and L is perimeter length (cross-sectional length).In addition, multiple plate 108 is being partially formed protuberance 109 to keep the interval between adjacent plate 108, and protuberance 109 contacts with adjacent plate 108.Between the plate 108 that waste gas G passes through catalyst assembly 106 and plate 108.In addition, as shown in Figure 4, when fine coal incinerator 10 operates, the catalyst assembly 106 of tabular catalyst 100 to grade foreign matter 90 at surface sediment explosion ash.
First denitration catalyst oxidant layer 82 is configured in rectification and holds concurrently the downstream of denitration catalyst oxidant layer 80 on the flow direction of waste gas G.First denitration catalyst oxidant layer 82 has honeycombed catalyst 110 and honeycombed catalyst 110 is fixed on the supporting device 112 of the 3rd vertical gas pass portion 40f.As long as supporting device 112 can support the mechanism of honeycombed catalyst 110, structure does not limit especially.
Honeycombed catalyst 110 has multiple catalyst assembly in the same manner as tabular catalyst 100.Honeycombed catalyst 110 also configures in the mode of whole of the horizontal plane of multiple catalyst assembly shutoff the 3rd vertical gas pass portion 40f.Thus, the waste gas G flowed in the 3rd vertical gas pass portion 40f is by the catalyst assembly of honeycombed catalyst 110.As shown in Figure 5, the partial configuration with catalyst function of honeycombed catalyst 110 becomes clathrate.Waste gas G is by the opening with the grid of catalyst function of honeycombed catalyst 110.At this, hydraulic diameter (4 × A)/L of the opening (catalyst opening portion) 117 supplying waste gas G to pass through of honeycombed catalyst 110 is less than 8mm.
At this, the honeycombed catalyst 110 of the first denitration catalyst oxidant layer 82 is thicker than tabular catalyst 100.In other words, if the length of the flow direction of the waste gas G of tabular catalyst 100 is set to W1, the length of the flow direction of the waste gas of honeycombed catalyst 110 is set to W2, then W1 < W2.
Second denitration catalyst oxidant layer 84 is configured in the downstream of the first denitration catalyst oxidant layer 82 on the flow direction of waste gas G.Second denitration catalyst oxidant layer 84 has honeycombed catalyst 120 and honeycombed catalyst 120 is fixed on the supporting device 122 of the 3rd vertical gas pass portion 40f.Second denitration catalyst oxidant layer 84 is except allocation position difference, and all the other are identical with the first denitration catalyst oxidant layer 82.3rd denitration catalyst oxidant layer 86 is configured in the downstream of the second denitration catalyst oxidant layer 84 on the flow direction of waste gas G.3rd denitration catalyst oxidant layer 86 has honeycombed catalyst 130 and honeycombed catalyst 130 is fixed on the supporting device 132 of the 3rd vertical gas pass portion 40f.3rd denitration catalyst oxidant layer 86 is except allocation position difference, and all the other are identical with the first denitration catalyst oxidant layer 82, second denitration catalyst oxidant layer 84.In other words, denitration device 50 is laminated with three denitration catalyst oxidant layer in the hold concurrently downstream of denitration catalyst oxidant layer 80 of rectification.
The rectification that pressure gauge 140 is configured in the 3rd vertical gas pass portion 40f is held concurrently the upstream side of denitration catalyst oxidant layer 80.The pressure of the waste gas G before holding concurrently denitration catalyst oxidant layer 80 inflow to rectification measured by pressure gauge 140.The result of measurement is sent to control device 150 by pressure gauge 140.
Pressure gauge 146 is configured in the downstream of the 3rd denitration catalyst oxidant layer 86 of the 3rd vertical gas pass portion 40f.The pressure of the waste gas G after by the 3rd denitration catalyst oxidant layer 86 measured by pressure gauge 146.The result of measurement is sent to control device 150 by pressure gauge 146.
Nitrous oxides concentration meter 148 is configured in the downstream of the 3rd denitration catalyst oxidant layer 86 of the 3rd vertical gas pass portion 40f.The nitrous oxides concentration of the waste gas G after by the 3rd denitration catalyst oxidant layer 86 measured by nitrous oxides concentration meter 148.Nitrous oxides concentration meter 148 can use various methods as described below: the laser of irradiation absorption wavelength is also measured its uptake thus measures the method for concentration; Obtain sample gas from waste gas G and by the continuous analyzer of chemiluminescence mode, infrared ray absorbing mode etc., chemical analysis composition analyzed thus measure the method etc. of concentration.The result of measurement is sent to control device 150 by nitrous oxides concentration meter 148.
Ammoniameter 149 is configured in the downstream of the 3rd denitration catalyst oxidant layer 86 of the 3rd vertical gas pass portion 40f.Ammoniameter 149 measures the nitrous oxides concentration of the waste gas G after by the 3rd denitration catalyst oxidant layer 86.Ammoniameter 149 can use various methods as described below: the laser of irradiation absorption wavelength is also measured its uptake thus measures the method for concentration; Obtain sample gas from waste gas G and utilize and based on the continuous analyzer of Fourier transform infrared measure, chemical analysis composition to be analyzed thus to measure the method etc. of concentration.The result of measurement is sent to control device 150 by ammoniameter 149.
Control device 150 is the arithmetic units such as personal computer, performs various process by performing various control program.Control device 150 judges the exception of denitration device 50 according to the result utilizing pressure gauge 140,146 to measure.In addition, control device 150 judges the state of denitration device 50 according to the result utilizing nitrous oxides concentration meter 148, ammoniameter 149 measures, and judges whether the maintenance carrying out comprising more catalyst changeout.
Reporting unit 152 is to manager's report information of the denitration devices such as operating personnel 50.Reporting unit 152 can use the various equipment of output information, such as, can use the display of display image, export the loudspeaker of sound, by the communication equipment etc. carrying out exporting that communicates.
Denitration device 50 is configured in the upstream side of the first denitration catalyst oxidant layer 82 by denitration catalyst oxidant layer 80 of the rectification possessing rectification function and denitration function being held concurrently, rectification can be carried out to the waste gas G of inflow first denitration catalyst oxidant layer 82 thus, and carry out the removal of nitrogen oxide.Thereby, it is possible to improve the denitration performance (removing the performance of nitrogen oxide) of denitration device 50.In addition, to hold concurrently denitration catalyst oxidant layer 80 by arranging the rectification possessing rectification function and denitration function, not needing to configure the rectification layer only possessing rectification function, thus can miniaturization of the apparatus.
Fig. 6 is the curve map of an example of the change that the duration of runs and denitration performance are shown.The longitudinal axis of Fig. 6 is denitration performance characteristic, and transverse axis is the duration of runs.In figure 6, the basis that the result of the denitration device in present embodiment is shown as comparative example replace rectification to hold concurrently denitration catalyst oxidant layer 80 and be provided with the result of the situation of the rectification layer not possessing catalyst function.As shown in Figure 6, to hold concurrently denitration catalyst oxidant layer 80 by arranging rectification, denitration performance characteristic can be improved, the duration of runs of satisfied necessary performance can be extended further.
In addition, for denitration device 50, rectification denitration catalyst oxidant layer 80 of holding concurrently uses tabular catalyst 100, can improve the resistance to ag(e)ing of the situation as rectification layer thus.Specifically, when carrying out rectification to the waste gas G stream of movement disorder, although probably with the abnormal contact such as dust, the generation of the wearing and tearing caused because of this contact etc. can be reduced, can long term maintenance denitration performance.In addition, for denitration device 50, rectification denitration catalyst oxidant layer 80 of holding concurrently uses tabular catalyst 100, can reduce thus when the ash that bursts grade foreign matter stacked the increase of the pressure loss that produces, can within the longer time maintenance high-performance.
Although the rectification of present embodiment is held concurrently, denitration catalyst oxidant layer 80 is configured with tabular catalyst 100, is not limited to this.As long as rectification is held concurrently region, in other words the catalyst opening portion for waste gas G flowing of denitration catalyst oxidant layer 80 hydraulic diameter than be configured in downstream denitration catalyst oxidant layer honeycombed catalyst catalyst opening portion hydraulic diameter greatly.In addition, preferred rectification holds concurrently the hydraulic diameter of catalyst opening portion of denitration catalyst oxidant layer 80 at more than 8mm.As mentioned above, the hydraulic diameter of catalyst opening portion can be represented by (4 × A)/L.The shape of catalyst opening portion forms different shapes because of the kind of catalyst.Rectification denitration catalyst oxidant layer 80 of holding concurrently such as also can use the hydraulic diameter of catalyst opening portion at the large honeycombed catalyst (Large space honeycombed catalyst) of the configuration space of more than 8mm.
At this, the length W1 on the flow direction of the waste gas G of preferred tabular catalyst 100 is set to more than 50mmL and below 300mmL.Fig. 7 is the curve map of the relation illustrated between catalyst length and material conversion coefficient.As shown in Figure 7, by the length on the flow direction of waste gas G is set to 50mmL, the conversion coefficient of material can be reduced.In other words, waste gas G can be adjusted flow.In addition, by the length on the flow direction of waste gas G is set to 300mmL, rectification denitration catalyst oxidant layer 80 of holding concurrently can be suppressed excessively to increase.
In addition, the denitration device 50 of present embodiment is configured with the first denitration catalyst oxidant layer 82, second denitration catalyst oxidant layer 84 and these three denitration catalyst oxidant layer of the 3rd denitration catalyst oxidant layer 86 in the hold concurrently downstream of denitration catalyst oxidant layer 80 of rectification, but the quantity of denitration catalyst oxidant layer is not defined as three.Denitration catalyst oxidant layer configures more than one, also can configure two denitration catalyst oxidant layer, also can configure more than four denitration catalyst oxidant layer.
In addition, for denitration device 50, preferred waste gas flows towards downside as in the present embodiment in exhaust passageway on the upside of vertical.In other words, preferred disposition has the flue in the region of denitration catalyst oxidant layer to extend along vertical, and waste gas flows towards downside in this flue on the upside of vertical.Thus, foreign matter easily falls, and foreign matter can be suppressed to be layered in denitration catalyst oxidant layer.Thereby, it is possible to suppression catalyst abrasion, the increase of the pressure loss that foreign matter can be suppressed to cause.Because denitration device 50 can obtain above-mentioned effect, therefore preferably adopt waste gas exhaust passageway towards downside flowing on the upside of vertical, but be not limited thereto.Denitration device 50 also can adopt waste gas along the exhaust passageway of the direction flowing of tilting relative to vertical.In other words, the flue being configured with the waste gas in the region of denitration catalyst oxidant layer also can tilt relative to vertical.
Next, the example of Fig. 8 to the replacing options of the catalyst of denitration device 50 is used to be described.Fig. 8 is the flow chart of an example of the replacing options of the catalyst that denitration device is shown.Can utilize the processing control apparatus 150 shown in Fig. 8 carry out the need of safeguard judgement.In addition, the replacing of catalyst is performed by operating personnel.In addition, even if the rectification of denitration device 50 is held concurrently, denitration catalyst oxidant layer 80 also can perform the process shown in Fig. 8 under the state of rectification layer not possessing catalyst function.
Control device 150 measures ammonia density and nitrous oxides concentration (step S12).Control device 150 detects the nitrous oxides concentration of the waste gas G after by the 3rd denitration catalyst oxidant layer 86 according to the testing result of nitrous oxides concentration meter 148.In addition, control device 150 detects the ammonia density of the waste gas G after by the 3rd denitration catalyst oxidant layer 86 according to the testing result of ammoniameter 149.
Control device 150 judges whether to need to safeguard (step S14) according to the ammonia density detected and nitrous oxides concentration.Control device 150 judges the denitration performance of the entirety of the layer possessing denitration function according to the concentration of ammonia density and nitrogen oxide.In addition, also judged result can be exported to reporting unit by control device 150, the part that operator takes out each catalyst layer according to information checks, obtains its result, and judges whether to need to safeguard.
When control device 150 is judged as not needing to safeguard (step S14 is no), returns step S12, carry out the process of step S12.When control device 14 is judged as needing to safeguard (step S14 is yes), judge whether to change rectification layer (step S16).Control device 150 when rectification layer does not have denitration function, denitration function reduce when, be judged as changing.
Rectification layer, when being judged as changing rectification layer (step S16 is yes), being replaced by rectification and holding concurrently denitration catalyst oxidant layer (step S18) by control device 150.Control device 150, when being judged as changing rectification layer (step S16 is no), changes denitration catalyst oxidant layer (the first denitration catalyst oxidant layer 82, second denitration catalyst oxidant layer 84, the 3rd denitration catalyst oxidant layer 86) (step S20).Though be change denitration catalyst oxidant layer in the present embodiment, new denitration catalyst oxidant layer also can be added.
As shown in Figure 8, to hold concurrently denitration catalyst oxidant layer by rectification layer being replaced by rectification, can the maximization of restraining device, and can denitration performance be improved.In addition, as mentioned above, the hydraulic diameter of the opening supplying waste gas G to pass through of denitration catalyst oxidant layer of rectification being held concurrently is set to more than 8mm, preferably adopts tabular catalyst, thus can improve resistance to ag(e)ing.
In the process shown in Fig. 8, though judge whether to safeguard according to ammonia density, nitrous oxides concentration, be not limited thereto.Control device 150 also can judge whether to safeguard according between the duration of runs, operating period.
[the second embodiment]
Fig. 9 is the brief configuration figure of the denitration device that the second embodiment is shown.It should be noted that, identical Reference numeral is marked and detailed to the component had with above-mentioned embodiment identical function.
Denitration device 50a shown in Fig. 9 have reducer feeding device 70, rectification layer 160, first denitration catalyst oxidant layer 82a, the second denitration catalyst oxidant layer 84, the 3rd denitration catalyst oxidant layer 86, pressure gauge 140,146, nitrous oxides concentration meter 148, ammoniameter 149, control device 150, reporting unit 152.Due to reducer feeding device 70, the second denitration catalyst oxidant layer 84 of denitration device 50a, the 3rd denitration catalyst oxidant layer 86, pressure gauge 140,146, nitrous oxides concentration meter 148, control device 150, ammoniameter 149, reporting unit 152 function identical with denitration device 50, therefore omit the description.
Rectification layer 160 is configured at the 3rd vertical gas pass portion 40f of flue 40.Rectification layer 160 is configured in the identical position of denitration catalyst oxidant layer 80 of holding concurrently with rectification.The rectification layer 160 waste gas G stream that flow direction changes to flowing into from the 3rd horizontal flue portion 40e to the 3rd vertical gas pass portion 40f carries out rectification.In rectification layer 160, the plate that the bearing of trend along the 3rd vertical gas pass portion 40f extends is configured to column-shaped on the direction orthogonal with bearing of trend.
First denitration catalyst oxidant layer 82a has tabular catalyst 110a and tabular catalyst 110a is fixed on the supporting device 112a of the 3rd vertical gas pass portion 40f.As long as supporting device 112a can support the mechanism of tabular catalyst 110a, structure does not limit especially.Tabular catalyst 110a is the structure identical with tabular catalyst 100.The honeycombed catalyst 120 of the length of the tabular catalyst 110a on the flow direction of waste gas G and the second denitration catalyst oxidant layer 84, denitration catalyst oxidant layer 86,130 identical.
Lean on most denitrating catalyst, the i.e. first denitration catalyst oxidant layer 82a of upstream side of the flow direction of waste gas G are set to tabular catalyst 110a by denitration device 50a, the reduction of denitration performance can be suppressed thus, and the pressure loss at multiple denitration catalyst oxidant layer place can be suppressed.Specifically, by adopting tabular catalyst 110a, compared with the situation of configuration honeycombed catalyst, also can suppress the increase of the pressure loss at denitration catalyst oxidant layer place when identical foreign matter (explosion ash grades) is sudden.The denitrating catalyst in the downstream of the flow direction of waste gas G is set to honeycombed catalyst by denitration device 50a, can increase the surface area of catalyst thus further, thus can improve denitration performance.
The denitration device 50a of described embodiment is not limited to the first denitration catalyst oxidant layer 82a is set to tabular catalyst, the second denitration catalyst oxidant layer 84 and the 3rd denitration catalyst oxidant layer 86 are set to honeycombed catalyst.As long as denitration device 50a possesses the denitration catalyst oxidant layer of honeycombed catalyst and both denitration catalyst oxidant layer of tabular catalyst, and the denitration catalyst oxidant layer of tabular catalyst is configured in the upstream side of the denitration catalyst oxidant layer of honeycombed catalyst on the flow direction of waste gas G.In other words, denitration device 50a only otherwise at the upstream side configuration honeycombed catalyst of tabular catalyst, in other words, only configure tabular catalyst at the upstream side of tabular catalyst.
Next, the example of Figure 10 to the replacing options of the catalyst of denitration device 50a is used to be described.Figure 10 is the flow chart of an example of the replacing options of the catalyst that denitration device is shown.Can utilize the processing control apparatus 150 shown in Figure 10 carry out the need of safeguard judgement.In addition, the replacing of catalyst is performed by operating personnel.In addition, the process shown in Figure 10 also can perform when the first denitration catalyst oxidant layer 82a of denitration device 50a is honeycombed catalyst.
Control device 150 measures ammonia density and nitrous oxides concentration (step S12).Control device 150 judges whether to need to safeguard (step S14) according to the ammonia density detected and nitrous oxides concentration.
When control device 150 is judged as not needing to safeguard (step S14 is no), returns step S12, carry out the process of step S12.When control device 150 is judged as needing to safeguard (step S14 is yes), operating personnel carries out the inspection of each catalyst layer, finds out the catalyst layer (step S30) that will change.Specifically, the layer that will change in the first denitration catalyst oxidant layer 82a, the second denitration catalyst oxidant layer 84, the 3rd denitration catalyst oxidant layer 86 is judged.It should be noted that, the catalyst layer that change can be one also can be multiple.In addition, also can not carry out checking the catalyst layer waiting and just determine to change.
After finding out the catalyst layer that will change, judge whether the catalyst in downstream is all honeycomb type catalyst (step S32).When control device 150 is judged as that the catalyst in downstream is all honeycomb type catalyst (step S32 is yes), the catalyst layer that will change is replaced by tabular catalyst (step S34).When control device 150 is judged as that the catalyst in downstream is not honeycomb type catalyst (step S32 is no) entirely, the catalyst layer that will change is replaced by honeycomb type catalyst (step S36).
As shown in Figure 10, by carrying out the replacing of the denitration catalyst oxidant layer of denitration device, become waste gas structure by honeycombed catalyst after by tabular catalyst.Such as, when all denitration catalyst oxidant layer are all honeycombed catalysts, the denitration catalyst oxidant layer of upstream side is replaced by tabular catalyst.In addition, when all denitration catalyst oxidant layer are all tabular catalyst, the denitration catalyst oxidant layer in downstream is replaced by honeycombed catalyst.Thereby, it is possible to suppress to produce the pressure loss because of the attachment of foreign matter, high denitration performance can be maintained.Thereby, it is possible to maintain high denitration performance, and can operate for a long time.It should be noted that, in described process, describe process when changing denitration catalyst oxidant layer, but also can be equipped with both honeycombed catalyst and tabular catalyst during fabrication, and with above-mentioned layout configurations.
[the 3rd embodiment]
Figure 11 is the brief configuration figure of the denitration device that the 3rd embodiment is shown.Figure 12 is the top view of denitration catalyst oxidant layer.In addition, identical Reference numeral is marked and detailed to the component had with above-mentioned embodiment identical function.
Denitration device 50b shown in Figure 11 have reducer feeding device 70, rectification layer 160, first denitration catalyst oxidant layer 182, second denitration catalyst oxidant layer 184, the 3rd denitration catalyst oxidant layer 186, pressure gauge 140,146, nitrous oxides concentration meter 148, ammoniameter 149, control device 150 and reporting unit 152.Due to the reducer feeding device 70 of denitration device 50b, pressure gauge 140,146, nitrous oxides concentration meter 148, control device 150, ammoniameter 149, reporting unit 152 function identical with denitration device 50, therefore omit the description.
Rectification layer 160 is configured at the 3rd vertical gas pass portion 40f of flue 40.Rectification layer 160 is configured in the identical position of denitration catalyst oxidant layer 80 of holding concurrently with rectification.The rectification layer 160 waste gas G stream that flow direction changes to flowing into from the 3rd horizontal flue portion 40e to the 3rd vertical gas pass portion 40f carries out rectification.In rectification layer 160, the plate that the bearing of trend along the 3rd vertical gas pass portion 40f extends is configured to column-shaped on the direction orthogonal with bearing of trend.
First denitration catalyst oxidant layer 182 has catalyst elements 210 and catalyst elements 210 is fixed on the supporting device 212 of the 3rd vertical gas pass portion 40f.As long as supporting device 212 can the mechanism of supporting catalyst unit 210, structure does not limit especially.
Catalyst elements 210 has tabular catalyst 250 and honeycombed catalyst 252.Tabular catalyst 250 has multiple catalyst assembly 250a.Honeycombed catalyst 252 has multiple catalyst assembly 252a.In catalyst elements 210, as shown in figure 12, the catalyst assembly 250a of tabular the catalyst 250 and catalyst assembly 252a of honeycombed catalyst 252 is configured as line column-shaped respectively.Catalyst elements 210 configures in the mode of whole of the horizontal plane of multiple catalyst assembly 250a, 252a shutoff the 3rd vertical gas pass portion 40f.Thus, the waste gas G flowed in the 3rd vertical gas pass portion 40f is by tabular catalyst 250 or honeycombed catalyst 252.
At this, catalyst elements 210 in the region being configured with denitration catalyst oxidant layer of exhaust passageway 40 that is the 3rd vertical gas pass portion 40f upstream side and be configured with tabular catalyst 250 as being configured with in the region of the second vertical gas pass portion 40d and the 3rd 40e side, horizontal flue portion of upstream region, in the region of the side contrary with the side being configured with upstream region, be configured with honeycombed catalyst 252.The catalyst elements 210 of present embodiment in the region being configured with denitration catalyst oxidant layer of the exhaust passageway 40 i.e. position of the upstream side of the 3rd vertical gas pass portion 40f and be relative to vertical tilt (being level in the present embodiment) upstream region, be namely configured with the 3rd horizontal flue portion 40e side region in be configured with tabular catalyst 250, in the region of the side contrary with the side being configured with upstream region, be configured with honeycombed catalyst 252.At this, the side being configured with upstream region is the side of the exhaust-gas flow of upstream side.The side being configured with upstream region of present embodiment is the side that upstream region (the 3rd horizontal flue portion 40e) tilts relative to the region (the 3rd vertical gas pass portion 40f) being configured with denitration catalyst oxidant layer.
For waste gas G flows, in the structure of flue 40, the flow velocity in the region of the side that the velocity ratio being configured with the region of the side of upstream region is contrary with the side being configured with upstream region is slow.In addition, the region being configured with the side of upstream region is the region that flow velocity is relatively slow for the mean flow rate of the waste gas flowed in denitration catalyst oxidant layer.Also can think, the region of the side contrary with the side being configured with upstream region is the comparatively faster region of flow velocity for described mean flow rate.
For catalyst elements 210, when observing from the flow direction of waste gas G, tabular catalyst 250 configures with identical area with honeycombed catalyst 252.It should be noted that, tabular catalyst 250 is not defined as 1: 1 with the area ratio of honeycombed catalyst 252.For catalyst elements 210, from the viewpoint of the averaging effect of flow velocity, preferred tabular catalyst 250 is configured to overall more than 1% and less than 50% or cellular 252 is configured to overall more than 1% and less than 50%.
In addition, preferred catalyst unit 210 adjusts configuration tabular catalyst 250 or configuration honeycombed catalyst 252 in units of catalyst assembly.Thereby, it is possible to make the replacing of catalyst assembly become easy.
Second denitration catalyst oxidant layer 184 has catalyst elements 220 and catalyst elements 220 is fixed on the supporting device 222 of the 3rd vertical gas pass portion 40f.As long as supporting device 222 can the mechanism of supporting catalyst unit 220, structure does not limit especially.Catalyst elements 220 has tabular catalyst 260 and honeycombed catalyst 262.Second denitration catalyst oxidant layer 184 is except allocation position difference, and all the other are all identical with the first denitration catalyst oxidant layer 182.
3rd denitration catalyst oxidant layer 186 has catalyst elements 230 and catalyst elements 230 is fixed on the supporting device 232 of the 3rd vertical gas pass portion 40f.As long as supporting device 232 can the mechanism of supporting catalyst unit 230, structure does not limit especially.Catalyst elements 230 has tabular catalyst 270 and honeycombed catalyst 272.3rd denitration catalyst oxidant layer 186 is except allocation position difference, and all the other are all identical with the first denitration catalyst oxidant layer 182.
Denitration device 50b is being configured with the area configurations tabular catalyst 250,260,270 of side of upstream region, at the area configurations honeycombed catalyst 252,262,272 of the side contrary with the side being configured with upstream region, thus can at the fast area configurations honeycombed catalyst 252,262,272 of the flow velocity of waste gas G, at the area configurations tabular catalyst 250,260,270 that the flow velocity of waste gas G is slow.Thereby, it is possible to the slow-footed area configurations tabular catalyst 250,260,270 of the waste gas G easily piled up at foreign matter.Compared with honeycombed catalyst 252,262,272, foreign matter is not easily deposited on tabular catalyst 250,260,270, and the rising having the situation downforce of foreign matter to lose is also less piling up.Thus, by the slow area configurations tabular catalyst 250,260,270 of flow velocity, the accumulation of foreign matter can be suppressed, the rising of the pressure loss can be reduced, therefore, it is possible to long term maintenance denitration performance.In addition, by the area configurations honeycombed catalyst 252,262,272 that the flow velocity not easily piled up at foreign matter is fast, denitration performance can be improved.
Figure 13 is the curve map of the relation illustrated between denitrating catalyst and the pressure loss.As shown in figure 13, for honeycombed catalyst and tabular catalyst, the pressure loss of honeycombed catalyst is larger than the pressure loss of tabular catalyst.In other words, compared with tabular catalyst, waste gas not easily flows in honeycombed catalyst.Denitration device 50b passes through, at the fast area configurations honeycombed catalyst of the flow velocity of waste gas G, at the area configurations tabular catalyst that the flow velocity of waste gas G is slow, flow velocity can be made thus to become even.In addition, due to compared with tabular catalyst, waste gas G not easily flows in honeycombed catalyst, therefore, it is possible to slow down the flow velocity of waste gas G, can suppress the wearing and tearing of catalyst.In addition, because the pressure loss of tabular catalyst is few, therefore, it is possible to suppress the reduction of flow velocity, the accumulation of foreign matter can be suppressed.
In addition, when observing denitration device 50b from the flow direction of waste gas G, the region of tabular catalyst of preferred multiple denitration catalyst oxidant layer is in identical region with the region of honeycombed catalyst.Thereby, it is possible to suppress foreign matter bulk deposition on the honeycombed catalyst in downstream.
Next, the example of Figure 14 to the replacing options of the catalyst of denitration device 50b is used to be described.Figure 14 is the flow chart of an example of the replacing options of the catalyst that denitration device is shown.Can utilize the processing control apparatus 150 shown in Figure 14 carry out the need of safeguard judgement.In addition, the replacing of catalyst is performed by operating personnel.In addition, the process shown in Figure 14 also can perform when each layer of the denitration catalyst oxidant layer of denitration device 50b is only made up of honeycombed catalyst or is only made up of tabular catalyst.
Control device 150 measures ammonia density and nitrous oxides concentration (step S12).Control device 150 judges whether to need to safeguard (step S14) according to the ammonia density detected and nitrous oxides concentration.When control device 150 is judged as not needing to safeguard (step S14 is no), returns step S12, carry out the process of step S12.
When control device 150 is judged as needing to safeguard (step S14 is yes), operating personnel carries out the inspection of each catalyst layer, finds out the catalyst layer (step S40) that will change.Specifically, the layer that will change in the first denitration catalyst oxidant layer 82a, the second denitration catalyst oxidant layer 84, the 3rd denitration catalyst oxidant layer 86 is judged.It should be noted that, the catalyst layer that change both can be one also can be multiple.In addition, also can not carry out checking the catalyst layer waiting and just determine to change.
After finding out the catalyst layer that will change, determine the configuration (step S42) of tabular catalyst and honeycombed catalyst.Control device 150 is to determine configuration at the relatively slow area configurations tabular catalyst of flow velocity in the mode of the relatively fast area configurations honeycombed catalyst of flow velocity.Next, after the configuration determining tabular catalyst and honeycombed catalyst, according to carried out determination, the catalyst layer being configured with tabular catalyst and honeycombed catalyst is replaced by the catalyst layer (step S44) found out.
As shown in figure 14, by making a denitration catalyst oxidant layer, there is both honeycombed catalyst and tabular catalyst, and at the area configurations tabular catalyst that flow velocity is relatively slow, at the area configurations honeycombed catalyst that flow velocity is relatively fast, flow velocity can be made thus to become evenly, improve resistance to ag(e)ing, and improve denitration performance.In other words, by the slow partial configuration tabular catalyst of flow velocity, foreign matter is not easily piled up thus, and, the pressure loss also can be made not easily to increase even if foreign matter is piled up.In addition, increase the pressure loss by the partial configuration honeycombed catalyst fast at flow velocity and reduce flow velocity, increasing the surface area of catalyst in addition, thus can denitration performance be improved.It should be noted that, in described process, describe process when changing denitration catalyst oxidant layer, but also can be equipped with both honeycombed catalyst and tabular catalyst during fabrication, and with above-mentioned layout configurations.
[the 4th embodiment]
Figure 15 is the top view of other examples of the denitrating catalyst that the 4th embodiment is shown.It should be noted that, identical Reference numeral is marked and detailed to the component had with above-mentioned embodiment identical function.4th embodiment only illustrates the denitrating catalyst of denitration device.The denitrating catalyst of preferred present embodiment replaces above-mentioned honeycombed catalyst and configures.
Denitrating catalyst 302 shown in Figure 15 has tabular catalyst 310 and is configured in the honeycombed catalyst 312 in downstream of flow direction of waste gas G of tabular catalyst 310.For denitrating catalyst 302, the face of the flow direction upstream side of the face in the flow direction downstream of the waste gas G of tabular catalyst 310 and the waste gas of honeycombed catalyst 312 is close.Also contacting at least partially of tabular catalyst 310 and honeycombed catalyst 312 can be made.Waste gas G is rear by honeycombed catalyst 312 by tabular catalyst 310.
Denitrating catalyst 302 configures, thereby, it is possible to make the waste gas G after utilizing tabular catalyst 310 to carry out rectification flow into honeycombed catalyst 312 with the flow direction upstream side of the waste gas G at honeycombed catalyst 312 and the close state of tabular catalyst 310.Thus, without the need to strengthening the end face of the upstream side of the flow direction of the waste gas G of honeycombed catalyst 312, the mar proof of the flow direction upstream side of the waste gas G of denitrating catalyst 302 can just be improved.In addition, tabular catalyst 310 can maintain the performance of higher catalyst because not carrying out the coating etc. on surface.In addition, by configuration tabular catalyst 310, the pressure loss also can be suppressed to increase when foreign matter is piled up.
At this, the length on the flow direction of the waste gas G of preferred tabular catalyst 310 is at more than 50mmL and below 300mmL.Shown in Fig. 7 described above, by the length on the flow direction of waste gas G is set to 50mmL, the conversion coefficient of material can be reduced.In other words, rectification can be carried out to waste gas G stream.In addition, by the length on the flow direction of waste gas G is set to 300mmL, tabular catalyst 310 can be suppressed excessively to increase.
Claims (12)
1. a denitration device, is characterized in that,
Described denitration device has:
Exhaust passageway, it is for exhaust-gas flow;
Rectification is held concurrently denitration catalyst oxidant layer, and it is arranged at described exhaust passageway; And
At least denitration catalyst oxidant layer of one deck, rectification described in its ratio being configured at described exhaust passageway is held concurrently the position of denitration catalyst oxidant layer by the flow direction downstream of waste gas,
Described rectification hold concurrently denitration catalyst oxidant layer described waste gas flow direction on length shorter than the length on the flow direction of the described waste gas of described denitration catalyst oxidant layer.
2. denitration device according to claim 1, is characterized in that,
The hold concurrently hydraulic diameter of catalyst opening portion of denitration catalyst oxidant layer of described rectification is larger than the hydraulic diameter of the catalyst opening portion of described denitration catalyst oxidant layer.
3. denitration device according to claim 1, is characterized in that,
The hold concurrently hydraulic diameter of catalyst opening portion of denitration catalyst oxidant layer of described rectification is more than 8mm.
4. denitration device according to any one of claim 1 to 3, is characterized in that,
Described rectification denitration catalyst oxidant layer of holding concurrently is tabular catalyst,
Described denitration catalyst oxidant layer is honeycombed catalyst.
5. a denitration device, is characterized in that,
Described denitration device has:
Exhaust passageway, it is for exhaust-gas flow;
Rectification layer, it is arranged at described exhaust passageway; And
At least two-layer denitration catalyst oxidant layer, described in its ratio being configured at described exhaust passageway, rectification layer is by the position in the flow direction downstream of waste gas,
Described at least two-layer denitration catalyst oxidant layer comprises:
Tabular catalyst, it is the denitration catalyst oxidant layer leaning on upstream side most of the flow direction of described waste gas; And
Honeycombed catalyst, it is the denitration catalyst oxidant layer of swimming side most on the lower of the flow direction of described waste gas,
The denitration catalyst oxidant layer of all described tabular catalyst is configured in the position leaning on the upstream side of the flow direction of described waste gas than the denitration catalyst oxidant layer of described honeycombed catalyst.
6. a denitration device, is characterized in that,
Described denitration device has:
Exhaust passageway, it is for exhaust-gas flow;
Rectification layer, it is arranged at described exhaust passageway; And
At least denitration catalyst oxidant layer of one deck, described in its ratio being configured at described exhaust passageway, rectification layer is by the position in the flow direction downstream of waste gas,
With flow in described denitration catalyst oxidant layer waste gas mean flow rate compared with the relatively slow area configurations of flow velocity have tabular catalyst, the area configurations relatively fast at flow velocity compared with described mean flow rate has honeycombed catalyst.
7. denitration device according to any one of claim 1 to 6, is characterized in that,
Described exhaust passageway configures towards the mode of downside flowing on the upside of vertical to make described waste gas.
8. the replacing options of a catalyst, the replacing options of this catalyst is the replacing options of the catalyst of denitration device, described denitration device has rectification layer and is configured in the direction of flow of the exhaust gases than the denitration catalyst oxidant layer of the position of described rectification layer downstream
It is characterized in that,
The replacing options of described catalyst comprises the following steps:
Judge whether described rectification layer possesses catalyst function; And
When described rectification layer does not possess catalyst function, denitration catalyst oxidant layer that the rectification that described rectification layer is replaced by the function possessing denitrating catalyst is held concurrently.
9. the replacing options of catalyst according to claim 8, is characterized in that,
Hold concurrently in the step of denitration catalyst oxidant layer being replaced by described rectification, the hydraulic diameter being replaced by catalyst opening portion is that the rectification of more than 8mm is held concurrently denitration catalyst oxidant layer.
10. the replacing options of catalyst according to claim 8 or claim 9, is characterized in that,
Hold concurrently in the step of denitration catalyst oxidant layer being replaced by described rectification, be replaced by tabular catalyst.
The replacing options of 11. 1 kinds of catalyst, the replacing options of this catalyst is the replacing options of the catalyst of denitration device, described denitration device has rectification layer and is configured in the direction of flow of the exhaust gases than at least two-layer denitration catalyst oxidant layer of the position of described rectification layer downstream
It is characterized in that,
The replacing options of described catalyst comprises the following steps:
Find out the denitration catalyst oxidant layer that will change; And
When the described denitration catalyst oxidant layer that will change does not have honeycombed catalyst at the upstream side of the flow direction of described waste gas, be replaced by tabular catalyst.
The replacing options of 12. 1 kinds of catalyst, the replacing options of this catalyst is the replacing options of the catalyst of denitration device, described denitration device has rectification layer and is configured in the direction of flow of the exhaust gases than the denitration catalyst oxidant layer of at least one deck of the position of described rectification layer downstream
It is characterized in that,
The replacing options of described catalyst comprises the following steps:
Find out the denitration catalyst oxidant layer that will change; And
Change denitration catalyst oxidant layer in the manner as described below: with flow in described denitration catalyst oxidant layer waste gas mean flow rate compared with the relatively slow region of flow velocity, the denitration catalyst oxidant layer found out in the described step found out is replaced by tabular catalyst, in the region that flow velocity compared with described mean flow rate is relatively fast, the denitration catalyst oxidant layer found out in the described step found out is replaced by honeycombed catalyst.
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| JP7171164B2 (en) * | 2017-04-14 | 2022-11-15 | 三菱重工業株式会社 | Combustion exhaust gas treatment method, combustion exhaust gas treatment device and maintenance method thereof |
| JP7657071B2 (en) | 2021-02-26 | 2025-04-04 | 三菱重工業株式会社 | Method for determining catalyst arrangement in denitration device, method for maintaining denitration device, and denitration device, boiler, and power plant |
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- 2014-10-17 CN CN201420602898.5U patent/CN204208457U/en not_active Expired - Lifetime
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102553405A (en) * | 2010-12-20 | 2012-07-11 | 邱吉康 | Secondary united flue gas denitration device of oil burning boiler and flue gas denitration method |
| CN202460474U (en) * | 2012-01-19 | 2012-10-03 | 大连贝斯特环境工程设备有限公司 | Integral desulfurization and denitration complete device by catalytic reduction ammonia method for small and medium boilers |
| CN102861511A (en) * | 2012-09-28 | 2013-01-09 | 南京龙源环保有限公司 | SNCR (selective non-catalytic reduction) and SCR (selective catalytic reduction) combined denitration method and SNCR and SCR combined denitration device for flue gas of coal-fired boiler |
| CN203570400U (en) * | 2013-11-20 | 2014-04-30 | 潍柴动力股份有限公司 | SCR box |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2015222163A (en) | 2015-12-10 |
| CN105080335B (en) | 2021-04-06 |
| CN204153805U (en) | 2015-02-11 |
| CN204208457U (en) | 2015-03-18 |
| JP6513341B2 (en) | 2019-05-15 |
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