CN102452803B - Waste treatment equipment - Google Patents
Waste treatment equipment Download PDFInfo
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- CN102452803B CN102452803B CN201010514607.3A CN201010514607A CN102452803B CN 102452803 B CN102452803 B CN 102452803B CN 201010514607 A CN201010514607 A CN 201010514607A CN 102452803 B CN102452803 B CN 102452803B
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Abstract
The present invention relates to waste treatment equipment. The purpose of the present invention is to solve the following technical problem that: under the following conditions, the operating safety of cement manufacturing equipment (200) is ensured, wherein the conditions comprise: thermal decomposition gas generated by a gasifier (1) is conveyed to a decomposition furnace (20) of the cement manufacturing equipment (200) under the condition of maintenance of the constant carbon content and the constant ash content in the thermal decomposition gas, and the like. The technical scheme of the present invention is that: waste treatment equipment (100) is arranged close to the cement manufacturing equipment (200). The waste treatment equipment comprises: the gasifier (1) and a gas conveying pipeline (6), wherein the gasifier is provided for carrying out the gasification reaction for the waste to generate the thermal decomposition gas, and the gas conveying pipeline is provided for conveying the generated thermal decomposition gas to the decomposition furnace (20) under the condition of the constant carbon content and the constant ash content in the thermal decomposition gas. According to the present invention, a flow ratio of the thermal decomposition gas from the gasifier (1) to the discharged waste gas from the decomposition furnace (20) is limited below the specified flow ratio, such that the temperature change of the decomposition furnace (20) can be inhibited so as to ensure the stability of the cement manufacturing equipment during the operating process.
Description
Technical field
The present invention relates to adjacent cement making equipment to arrange, utilize cement decomposing furnace wholesomely waste to be carried out to the waste treating device processed.
Background technology
In recent years, even in such as developing country, also along with growth in the living standard, also more and more need to carry out sanitary measure to rubbish, its burning disposal amount is increasing also among prediction, but also exist and build the very large expense of general incinerator needs, need the problem of the duration grown very much.And needs assessment incinerator is on the impact of surrounding environment, to neighbouring resident's public information, therefore need long time before check to prepare.And the problem of burying Treatment stations deficiency of burying the ashes that incinerator occurs also is there is in China, when setting up new disposal site, the establishment etc. of the setting of grey melting furnace and the reuse method of ash is prerequisite.
On the other hand, cement industry is always in order to reduce cement manufacturing cost, have the trend utilized as the part of fuel by combustible waste, as disclosed in Patent Document 1, the document proposes effectively to utilize existing cement making equipment to carry out sanitary measure to waste.In this example embodiment, decomposed by castoff heat in vapourizing furnace, separation of carbon and ash content from the thermolysis gas occurred, be then supplied to cement kiln (firing furnace) by thermolysis gas, carbon and ash content be supplied to preheater.
That is, in above-mentioned prior art example, the thermolysis gas that vapourizing furnace can be occurred utilizes as a part for fuel gas, simultaneously using carbon and ash content as cement material utilization, but both must be separated, be supplied to cement making equipment by other system, therefore there is the difficulty that system is numerous and diverse.
Again, the thermal value of usual rubbish is about 1000 ~ 3000 kcal/kg, than normally used fuel in cement kiln (when using matchmaker, the thermal value of inferior grade matchmaker is 5000 ~ 7000 kcal/kg) low, therefore when the thermolysis gas from rubbish being mixed use, temperature in kiln is on the low side, thus the possibility also having fuel consumption undesirable.
And may detrimentally affect be had from the water vapour comprised in the thermolysis gas of rubbish to the proterties of cement clinker, when thermolysis gas burns in cement kiln, have and the possibility that focus generates dirt settling occurs.
To this, present inventor develops the thermolysis gas that occurred by vapourizing furnace and carbon is supplied to the decomposing furnace of cement making equipment or the technology of firing furnace (kiln) and has first applied for patent (patent documentation 2) together with ash content.Because the temperature of decomposing furnace is lower than kiln, be approximately about 900 DEG C, so the thermolysis gas here provided and carbon are utilized effectively as fuel, ash content also becomes a part for cement raw material.
Again, pass into from the high-temp waste gas in kiln, blown up by cement raw material as jet-stream wind in decomposing furnace, the thermolysis gas therefore here provided also burns to blowing up, is transported to preheater together with water vapour etc.Therefore, the problem that the deterioration of cement clinker proterties and dirt settling occur in kiln is not worried.
Patent documentation 1: specially permit No. 3838951 publication.
Patent documentation 2: the open CN101434461A of Chinese patent application.
Summary of the invention
But, even picture is described above thermolysis gas is supplied to decomposing furnace, if it was measured at most unfavorable condition as described below can occur.Such as due to certain fault, when gasifier operation stops, the supply of the thermolysis gas from this to decomposing furnace also can stop, even if the usage quantity therefore increasing coal etc. in decomposing furnace also can produce the problem of undercharge, may cause operation troubles.
Again, waste also has very big-difference because of the different heat amount of its kind, and the thermal value fluctuation of its thermolysis gas is also very large, and the kind of the waste concentrated in variant time-triggered protocol field is different, and its thermal value also has very large variation.Therefore, if the amount being supplied to the thermolysis gas of decomposing furnace is many, then the thermal value variation produced because of its burning also can cause the variation of calciner temperature.
That is, if amount decomposing furnace being provided as to the thermolysis gas of fuel increases, the steady running of cement making equipment is likely hindered.
In view of above-mentioned Problems existing, the object of the invention is to, at the thermolysis gas occurred by vapourizing furnace when keeping being transported in cement making equipment in its carbon contained and the intact situation of ash content, guaranteeing the stability that this cement making equipment runs.
To achieve these goals, the waste treating device that contiguous cement making equipment of the present invention is arranged, possesses the gas delivery channels making the vapourizing furnace of waste gasification generation thermolysis gas and the thermolysis gas occurred at described vapourizing furnace is transported under its carbon contained of maintenance and the intact situation of ash content the cement decomposing furnace of described cement making equipment; Flow from the thermolysis gas of described vapourizing furnace is restricted to below the throughput ratio of regulation with the ratio of the flow of the waste gas of discharging from described decomposing furnace.
In the waste treating device with this spline structure, when in vapourizing furnace, castoff heat decomposes generation thermolysis gas, utilize gas delivery channels that this thermolysis gas is transported to cement decomposing furnace under its carbon contained of maintenance and the intact situation of ash content, burn in decomposing furnace.At this moment the heat that the burning of thermolysis gas and carbon occurs has larger variation because of the relation of the kind etc. of waste, if but the ratio of the flow of the waste gas of being discharged with decomposing furnace by the flow of thermolysis gas is limited to below the throughput ratio of regulation, then can suppress the temperature variation of decomposing furnace.
Again, if cause gasifier operation to stop due to certain fault, the supply of thermolysis gas and carbon also stops, if its amount is little, also can be maintained the running status of decomposing furnace by the supply increasing coal etc.That is, the ratio of the exhaust gas flow come with decomposing furnace by the flow of the thermolysis gas carried to decomposing furnace by vapourizing furnace is limited to below regulation throughput ratio, can realize the steady running of cement making equipment.
Specifically, the flow of the thermolysis gas by described gas delivery channels is defined as the throughput ratio of such as less than 0.3 relative to the ratio of the flow of the waste gas of discharging from described decomposing furnace, if adjustment drops into the waste input amount of vapourizing furnace like this, and vapourizing furnace is the vapourizing furnace of flowing laminar, then also can adjust the flow of fluidization air, suppress the generating capacity of thermolysis gas.Such as drop into the waste input amount of vapourizing furnace and the flow of fluidization air adjusts according to the size of the negative pressure of this vapourizing furnace Sum decomposition stove, below above-mentioned throughput ratio can be maintained at.
Usually in the decomposing furnace of cement making equipment, bring out the waste gas in kiln etc. and form negative pressure state, here, if thermolysis gas flows into, then corresponding to this flow, negative pressure diminishes.Thus, if bring out the size of the negative pressure of the vapourizing furnace of thermolysis gas according to the negative pressure of this decomposing furnace, the adjustment input amount of waste and the flow of fluidization air, then can control the generating capacity of thermolysis gas, and the flow flowing into this decomposing furnace is maintained at below prescribed value.
Again, if utilize the negative pressure of decomposing furnace to bring out thermolysis gas from vapourizing furnace like this, in gas delivery channels and vapourizing furnace, also can keep negative pressure state, then thermolysis gas does not externally leak is ideal situation.In order to carry thermolysis gas like this, and be maintained at negative pressure using in the vapourizing furnace as conveying source, often fan is set in the midway of gas delivery channels, but when comprising carbon and ash content in from the thermolysis gas of waste, its part can be piled up on the impeller etc. of fan in attachment, cause the abrasion of impeller itself, likely break down.
In order to prevent such trouble, also considering to remove carbon and ash content from thermolysis gas, but needing removal device for this reason, and due to the carbon removed and the temperature of ash content low, be unsuitable for utilizing once again in the operation below.Again, the outlet of fan is likely in malleation in local, just in case there is such situation, thermolysis gas likely sprays outside pipeline.
If this point is also considered, then by the flow of the thermolysis gas of gas delivery channels, with the ratio of the flow of the waste gas of discharging from decomposing furnace preferably such as less than 0.2, so far, if make throughput ratio be smaller value, this compares the flows such as the kiln waste gas originally flowing through decomposing furnace, the flow of the thermolysis gas added is quite few, therefore, it is possible to the negative pressure in decomposing furnace is maintained enough large state, can utilize this negative pressure inducing thermolysis gas, and vapourizing furnace also can maintain negative pressure state.
Thus, also can not fan be set in the midway of gas delivery channels, worry that carbon in thermolysis gas and ash content adhere to, pile up thereon, cause fan fault.Do not worry that thermolysis gas sprays just in case fan outlet becomes malleation yet.
Here, as vapourizing furnace, there are the flowing laminar type and kiln formula of taking low temperature gasification mode, have shaft type as high-temperature gasification mode, but if adopt low temperature gasification mode, then have the advantage that the iron in waste, aluminium etc. can be reclaimed not oxidizedly.Again, the method for flowing laminar is higher than kiln formula reaction efficiency (gasification efficiency), also has the advantage of facility compact, therefore preferably adopts the vapourizing furnace of this flowing laminar.
If vapourizing furnace adopts the structure that can supply auxiliary fuel, even when then low to thermal value waste processes, also the layer temperature of vapourizing furnace can be maintained at necessary level.As such auxiliary fuel, specifically, can adopt micro fine carbon dust, this can drop into fluidised bed from top.In this case, if the particle of micro fine carbon dust is meticulous, then thermolysis gas stream can be followed to discharge from vapourizing furnace, on the other hand, as fruit granule is excessive, then assemble to sink in fluidised bed, likely can not fully make contributions to burning.Due to this situation, median size preferably about the 0.1 ~ 3mm of micro fine carbon dust.
Further, auxiliary fuel is not limited to micro fine carbon dust, can also adopt such as damaged tire, plastics, wood chip, carbon, ulmification compound etc. in addition, as long as can at the object of fluidised bed combustion, no matter its kind how.
Jet apparatus can be arranged to be blown into pressurized air again in the midway of described gas delivery channels.If done like this, attachment on the wall also can removing gas delivery channels, the carbon piled up and ash content.Again, for being communicated with gas introduction port thermolysis gas being introduced decomposing furnace with gas delivery channels, also in order to suppress attachment, the accumulation of carbon and ash content, make the with respect to the horizontal plane downward-sloping setting of this gas introduction port.
And, even there is no decomposing furnace in cement making equipment, from the high-temp waste gas inflow cement preheater that firing furnace comes, as mentioned above, the ratio of the flow of waste gas that in the future flow of the thermolysis gas of autopneumatolysis stove is discharged relative to preheater is limited to below the throughput ratio of regulation, negative pressure in preheater can be maintained at fully large state with this, by means of this negative pressure-induced thermolysis gas, and vapourizing furnace can be made to be held in negative pressure state.
As previously discussed, if adopt the present invention, make waste gasification with vapourizing furnace, the thermolysis gas of generation to be kept in the carbon that contains and the intact situation of ash content, to conveyings such as the decomposing furnaces of cement making equipment, fuel can being it can be used as to use.At this moment, make the flow of thermolysis gas be limited in below the throughput ratio of regulation with the ratio of the exhaust gas flow come from decomposing furnace etc., the temperature variation of decomposing furnace can be suppressed with this, stability when cement making equipment runs can be guaranteed.And utilize the negative pressure transportation thermolysis gas of decomposing furnace etc., also can keep negative pressure state by vapourizing furnace.
Accompanying drawing explanation
Fig. 1 is the waste treating device of the present invention the 1st example and the system diagram of cement making equipment.
Fig. 2 A is the enlarged view of the decomposing furnace from the above-mentioned cement making equipment of rotary kiln unilateral observation.
Fig. 2 B is the figure suitable with Fig. 2 A of the decomposing furnace of variation.
Fig. 3 A is the graphic representation of an example of the variation representing the gas volume occurred in vapourizing furnace.
Fig. 3 B is the graphic representation of an example of the pressure variation represented in decomposing furnace.
Fig. 3 C is the graphic representation of the analog result of the pressure variation represented in vapourizing furnace.
Fig. 4 is the graphic representation of the analog result of the relation represented between the pressure in the ratio of thermolysis gas flow and kiln exhaust gas flow and vapourizing furnace.
Fig. 5 A is the graphic representation of the mutual relationship represented between the throughput ratio of thermolysis gas and the total exhaust gas flow ratio from decomposing furnace.
Fig. 5 B is the graphic representation of the mutual relationship represented between the calorific value of coal ratio in the throughput ratio of thermolysis gas and decomposing furnace.
Fig. 6 is the figure suitable with Fig. 1 that water cooler waste gas flows into the 2nd example of decomposing furnace.
Fig. 7 is the figure suitable with Fig. 1 of the variation possessing the decomposing furnace with rotating decomposition room and mixing section.
Fig. 8 has the eel-like figure portion of ring-type in the midway of perisporium, nearby introduce the figure suitable with Fig. 1 of the variation of the air burnt again to it.
Fig. 9 is the figure suitable with Fig. 1 of the variation without decomposing furnace.
Nomenclature:
100 waste treating devices;
1 vapourizing furnace;
6 gas feed line (gas delivery channels);
6a jet apparatus;
The feedway of 7 micro fine carbon dusts;
200 cement making equipments;
10 suspension preheaters;
20 decomposing furnaces;
27 gas introduction ports;
40 air quenching water coolers (clinker cooler).
Embodiment
With reference to the accompanying drawings desirable example of the present invention is described.Fig. 1 is the waste treating device 100 of the 1st example and is adjacent the overall system diagram of cement making equipment 200 of setting.The waste treating device 100 that in figure, left side represents makes castoff heat decompose in vapourizing furnace 1, and the gas (thermolysis gas) occurred is used in mixed firing in the firing process of cement.The amount of this thermolysis gas is such as 2 ~ 30,000 Nm
3about/h, than exhausted air quantity (such as 300,000 Nm of the cement making equipment 200 shown in figure
3/ h) much less, therefore waste treating device 100 can be arranged near it existing cement mill with adding amendment hardly.
-waste treating device-
In waste treating device 100, collect general waste that such as family comes, the trade waste etc. comprising plastic waste and comprise the waste of flammable objects.These wastes are shipped by land conveying etc., are put into the hopper 2a in groove 2, utilize not shown crusher to carry out fragmentation.The waste utilization crane 3 that such fragmentation is crossed is transported to the e Foerderanlage 4 be made up of input hopper and travelling belt etc., and vapourizing furnace 1 is delivered in the action by means of this e Foerderanlage 4.
The conveying belt of e Foerderanlage 4 is such as spiral conveyers, by changing its working speed, can adjust the waste input amount that time per unit drops into vapourizing furnace 1.By means of this, the state of temperature of vapourizing furnace 1 and the generating capacity of thermolysis gas can be suppressed together with the adjustment of fluidization air flow quantity described below.
That is, as an example, vapourizing furnace 1 is the vapourizing furnace of flowing laminar, and the layer (fluidised bed) of the flowing sand (flow media) that the bottom in stove is formed is by means of airflow automation.The fluidization air being sent to fluidised bed utilizes electric blowing machine 5 from groove 2 sucking-off of waste in legend, is provided to vapourizing furnace 1.Be held in negative pressure in the groove 2 of therefore waste, abnormal stink is not easy to leak into outside.Again, in the midway of the air feed path 5a from fan 5 to vapourizing furnace 1, the adjustable damper of aperture (not shown) is set, by means of this, can controls air feed rate with good response characteristic.
And the rotating speed of above-mentioned fan 5 and the aperture of adjustment damper can be changed, the flow of fluidization air is adjusted with this.Such as, if increase the flow of fluidization air, the input amount of described waste is increased, then the layer temperature of vapourizing furnace 1 keeps certain and the increase of the generating capacity of thermolysis gas.The fluidised bed temperature of vapourizing furnace 1 is generally about 500 ~ 600 DEG C (minimum also have more than 450 DEG C).In the fluidised bed of this high temperature, waste disperses under the effect of flowing sand, thermolysis on one side, and the part burning of waste also promotes thermolysis.
About general waste thermal value is approximately 1000 ~ 3000 kcal/kg, therefore the temperature of fluidised bed can be maintained at proper temperature by one partial combustion, but, because of the relation of waste kind, if (such as lower than 1000 kcal/kg) so-called low-grade waste that its thermal value is little, then the temperature of fluidised bed is low.Therefore, the vapourizing furnace 1(concrete structure of this example is not shown) near e Foerderanlage 4, micro fine carbon dust feedway 7 is set, to drop into the such as micro fine carbon dust as auxiliary fuel in vapourizing furnace 1 from waste input port.
The median size of the micro fine carbon dust utilizing this feedway 7 to drop into from upper direction fluidised bed is about 0.1 ~ 3mm.When the particle diameter of micro fine carbon dust is 0.1mm, according to calculating, its final velocity is about 0.9m/s, slightly lower than the flow velocity (the void tower flow velocity of gas reference) of the thermolysis gas risen in vapourizing furnace 1 and air, therefore its major part is dispersed, and does not contribute the burning of fluidised bed.
On the other hand, if micro fine carbon dust particle diameter is excessive, then sink in fluidised bed soon, probably do not have contribution to burning very much.The time of micro fine carbon dust required for the fluidised bed combustion of about 500 DEG C of particle diameter 3.0mm is about the decades of times of the particle of particle diameter 0.1mm, in order to have contribution to the burning in layer, must guarantee the residence time of particle in layer.Here, the minimum stream automation speed of the micro fine carbon dust of particle diameter 3.0mm, according to calculating, is about 1.8m/s, identical with the void tower flow velocity of the air reference of fluidised bed, if therefore median size is at below 3.0mm, no problem.
Therefore, provide micro fine carbon dust as required, the temperature of fluidised bed can be maintained at suitable scope, the waste be put into can effective decomposition gasification.This thermolysis gas is discharged, by means of gas feed line 6(gas delivery channels from the top of vapourizing furnace 1) be transported to cement making equipment 200.In thermolysis gas, form small-particle as the carbon of unburnt ingredient and ash content and swim, be transferred together with thermolysis gas.Flowing laminar vapourizing furnace 1 in, waste pulverize by the flowing of flowing sand, therefore the particle diameter of carbon and ash content easily diminishes, this for prevent its attachment, pile up be favourable.
In this example, from the gas of vapourizing furnace 1 negative pressure transportation utilizing decomposing furnace 20 as described below, therefore also keep negative pressure in vapourizing furnace 1, thermolysis gas can not externally leak.Thermolysis gas due to the negative pressure transportation of decomposing furnace 20 can be utilized, so do not arrange fan in gas feed line 6.Therefore do not worry the upper attachment such as the impeller of fan, pile up carbon in thermolysis gas and ash content causes fault.
But on the inner-walls of duct face of gas feed line 6, As time goes on the situation having attachment, heap carbon distribution and ash to grade occurs, therefore can build-up of pressure loss increase, so in this example, gas feed line 6 to stop at regulation above interval arrange multiple jet apparatus 6a.Utilize this jet apparatus 6a, the pressurized air provided by not shown compressor is intermittently blown in pipeline, the carbon of accumulation and ash content can be blown away.Further, the damper of open and close type is also set in gas feed line 6 midway, when the operation of waste treating device 100 is stopped, damper can cuts out.
Relative to being discharged to gas feed line 6 on the top of the thermolysis gas of waste from vapourizing furnace 1 like this, the not combustionmaterial comprising the tinsel of the residue after as the thermolysis in vapourizing furnace 1 is fallen from the lower end of vapourizing furnace 1 together with flowing sand by the husky lower floor of flowing.That is, the residue of waste utilizes fluidised bed to carry out so-called proportion separation.Like this from vapourizing furnace 1 discharge sand and not combustionmaterial utilize the conveyings such as not shown travelling belt, the sand utilizing the sorting equipment outside figure to be separated returns vapourizing furnace 1.On the other hand, utilize sorting unit never to select metal ingredient in combustionmaterial, remaining not combustionmaterial be used as cement raw material.
-cement making equipment-
Cement making equipment 200 possesses general NSP kiln in legend.Cement raw material after preheating, is heated to about 900 DEG C (calcinings) with decomposing furnace 20, as in the rotary kiln 30 of firing furnace, burns till with the high temperature of about 1500 DEG C in as the suspension preheater 10 of preheater.By burned material quenching in air quenching water cooler 40 of rotary kiln 30, become granular cement clinker, then deliver in the refining step outside figure.
Above-mentioned suspension preheater 10 has the Multi-stage spiral device 11 be arranged side by side at above-below direction.Swirler 11 utilizes eddy flow to carry cement raw material while carry out heat exchange with the high-temp waste gas be blown into from subordinate respectively.This exhaust flow is as described below, from the high-temp waste gas (hereinafter referred to as " kiln waste gas ") of rotary kiln 30 by rising in decomposing furnace 20, is provided to the swirler 11 of most next stage.Kiln waste gas as shown in phantom in FIG., is risen step by step by swirler, arrives the swirler 11 of most upper level, flows out from this to waste line 50.
As shown in the figure, the jumbo induction fan 52 of inducing kiln waste gas it to be sent toward chimney 51 is set at waste line 50, at the upstream side of the more front side of this induction fan 52, i.e. exhaust flow, get involved and gas cooler 53(such as boiler be set) and precipitron 54.Induction fan 52 guides large quantity of exhaust gas by suspension preheater 10 Sum decomposition stove 20 from rotary kiln 30, simultaneously also described above in decomposing furnace 20 formed negative pressure, therefore there is the function of inducing thermolysis gas from vapourizing furnace 1.
On the other hand, in each swirler 11 of suspension preheater 10, after cement raw material described above and high temperature kiln waste gas carry out heat exchange, as shown by the solid line in the drawings, land downwards, move to next stage swirler 11.Time like this from the swirler 11 of most upper level sequentially step by step by multiple swirler 11, cement raw material obtains abundant preheating, and above most next stage, one-level swirler 11 provides to decomposing furnace 20.
Decomposing furnace 20 is arranged at the kiln rear portion of rotary kiln 30 with extending at above-below direction, in the lower pipeline 21 that the connection of its lower end is probably L-shaped, be connected again with between rotary kiln 30, connecting in decomposing furnace 20 upper end is on the other hand probably the upper pipe 22 of L-shaped, then is connected with between the swirler 11 of the most next stage of suspension preheater 10.In Fig. 2 A, can see from rotary kiln 30 side, decomposing furnace 20 bottom arrange respectively the such auxiliary fuel of micro fine carbon dust supplying opening 26, introduce from the gas introduction port 27 of the thermolysis gas of above-mentioned vapourizing furnace 1 and the air induction port 25 introduced from the high temperature cooling waste gas (air) of air quenching water cooler 40 as the air making it burn.
In legend, all with respect to the horizontal plane downward-sloping setting of air induction port 25 and gas introduction port 27, at Fig. 2 A, as black and white arrow represents respectively, air and the thermolysis gas of burning flow into downwards.These thermolysis gases and combustion air utilize the vacuum suction in decomposing furnace 20, change a kind of view, utilize kiln waste gas to also have induction fan 52 to induce exactly simultaneously, also have, as an example, also as shown in Figure 2 B, gas introduction port 27 can be connected to the midway of air induction port 25, while by the air mixed of thermolysis gas with burning, make it flow in decomposing furnace 20.
Kiln waste gas flows into decomposing furnace 20 lower end by lower pipeline 21, as shown in the arrow of grey in Fig. 2 A, 2B, form jet flow, along upper-lower axis 20a to blowing up.Then, when described thermolysis gas and combustion air flow into downwards in this decomposing furnace 20, these thermolysis air and airflow do not pass through decomposing furnace 20 with kiln exhaust flow, and burn with time enough in this decomposing furnace.
On the other hand, the cement raw material dropped into from cement input port 28 follows the jet flow of kiln waste gas as above to blowing up, when by rising in decomposing furnace 20, be heated to about 900 DEG C, and decarbonations reaction occurs 80 ~ 90% of lime composition.Then, be sent to the most next stage swirler 11 of suspension preheater 10 by upper pipe 22 from the topmost of decomposing furnace 20.Here, kiln waste gas is separated with cement raw material, moves to upper level swirler 11, and on the other hand, cement raw material falls the entrance arriving rotary kiln 30 from the lower end of swirler 11.
Rotary kiln 30 is formed from entrance to outlet slightly to the configuration that has a down dip by the rotary kiln of oval for the transverse direction of such as 70 ~ 100m tubular.Cement raw material, around its axle center slow circumvolve, is carried to outlet side with this by rotary kiln.Arrange combustion unit 31 at this outlet side, the high-temperature combustion gas that the burning such as coal, Sweet natural gas, heavy oil produces sprays to inlet side.The cement raw material generation chemical reaction (cement burns till reaction) that burned gas surrounds, its part burns till semi-melting state.
This cement burned material is subject to cold wind quenching in air quenching water cooler 40, forms granular cement clinker.And, although diagram and detailed description are omitted, after cement clinker is stored in grog warehouse, adds gypsum etc. and carry out composition adjustment, then through grinding as fine powder (finishing step).On the other hand, obtain the water cooler waste gas that heat is elevated to about 800 DEG C from burned material, as mentioned above, the air as burning is supplied to decomposing furnace 20.That is, reclaim used heat and the combustion air in decomposing furnace 20 is heated up, seek to improve thermo-efficiency with this.
On the basis of basic structure as above, also in the cement making equipment 200 of this example, in order to prevent being concentrated by the chlorine component in suspension preheater 10 Sum decomposition stove 20 circulation time gas and alkali composition, bypass line 60 is set.That is, as this example in cement making equipment during the thermolysis gas of multifuel combustion waste, the original chlorine component that comprises in waste and alkali composition impact under chlorine component in cement clinker and alkali constituent concentration have the tendency uprised, also may have the trouble that attachment occurs.
Therefore, in illustrated cement making equipment 200, utilize the bypass line 60 being connected to the bottom (or lower pipeline 21) of decomposing furnace 20 part for gas to be extracted out, after cooling with water cooler 60, be sent to swirler 62(classifier) by dust classification.Utilize fan 63 pairs of water coolers 61 to send cold wind, by will extract out quenching of gases to the fusing point of muriate etc. below, using extraction gas in chlorine component or alkali composition be separated as solid (dust).
Then in swirler 62, the dust in the gas of extraction is classified as meal and micro mist, the meal comprising chlorine and alkali composition hardly falls from the lower end of swirler 62, omits the reflux pipeline 60a represented return decomposing furnace 20 by means of a part.On the other hand, the high micro mist of chlorine component and alkali constituent concentration with extract out from swirler 62 bleed together be discharged to the downstream side pipeline 60b of bypass line 60, trapped by precipitron 54.
Also have, in FIG, indicate the midway downstream side pipeline 60b of bypass line 60 being connected to waste line 50, share the induction fan 52, gas cooler 53 and the precipitron 54 that kiln waste gas are sent to chimney 51, but the induction fan, gas cooler and the precipitron that are specifically designed to bypass line 60 are set in physical device, make it independent of waste line 50.
-throughput ratio of thermolysis gas-
As mentioned above, in the waste reduction and disposal equipment 100 of this example, utilize the negative pressure of inducing kiln waste gas in cement making equipment 200, from vapourizing furnace 1, be guided out thermolysis gas, utilize gas delivery line 6 to be transported to decomposing furnace 20.That is, in decomposing furnace 20, utilize induction fan 52 to induce kiln waste gas, formed negative pressure state, if the flow of these waste gas is abundant, though then corresponding thereto comparatively small amt thermolysis gas flow into, also can maintain enough large negative pressure.
In this example, the exhausted air quantity of cement making equipment 200 is more than ten times of the amount of the thermolysis gas that vapourizing furnace 1 occurs, therefore the negative pressure state of decomposing furnace 20 is stable, therefore, also this stable negative pressure can be utilized, carry the thermolysis gas from vapourizing furnace 1, air shooter line 6 does not arrange fan.Again, also keep negative pressure in vapourizing furnace 1, thermolysis gas does not leak into outside.
But if the flow of thermolysis gas is many, then, during the change such as generating capacity of the thermolysis gas in the state of combustion of decomposing furnace 20 and vapourizing furnace 1, vapourizing furnace 1 temporarily can not keep negative pressure state, and thermolysis gas also may externally leak again.The present inventor periodically increases the throughput ratio of thermolysis gas relative to kiln exhaust gas flow on one side, the pressure change in the vapourizing furnace 1 utilizing simplation validation to cause thus.
First, Fig. 3 A ~ 3C represents analog result when throughput ratio to be decided to be about 1/10 as this example.Fig. 3 A represents the variation considering to be sent to the air capacity of the fluidised bed of vapourizing furnace 1, the upset condition of the generating capacity of the thermolysis gas of the vapourizing furnace 1 when providing using it as external disturbance.The variation of this gas volume is obtained by means of simulation.On the other hand, by means of using the test of actual cement decomposing furnace, measure the upset condition of its air pressure inside, the curve of Fig. 3 B this amplitude of fluctuation is expanded to the result of 3 times.
When simulating according to the variation of the variation Sum decomposition furnace gases pressure of above-mentioned vapourizing furnace gas generating capacity, shown in Fig. 3 C, obtain the curve of the gaseous tension variation represented in vapourizing furnace 1.Even this gaseous tension known is maximum also below-0.5kPa, throughput ratio is under the state having leeway of 1/10, even if thermolysis gas generating capacity has variation, also can keep suitable negative pressure state in vapourizing furnace 1.
Below, Fig. 4 represents in the throughput ratio of thermolysis gas flow and vapourizing furnace 1 between pressure relation.In relation curve, solid line represents the pressure mean values in a certain throughput ratio gasified stove 1, and what consider variation as mentioned above is the relation curve shown in dotted line.As shown in the left end (throughput ratio=0) of relation curve, decomposing furnace pressure employing-0.9kPa during kiln isolated operation.Along with the increase of throughput ratio, the increase of instant heating decomposition gas generating capacity, the pressure in vapourizing furnace 1 uprises, and becomes close to normal atmosphere.
According to relation curve, if throughput ratio is about 0.1=1/10 as this example, pressure then in vapourizing furnace 1 is-0.5 ~-0.7kPa, when the throughput ratio of thermolysis gas is about 0.2, as representing with the relation curve shown in solid line, in vapourizing furnace, the mean value of pressure is probably normal atmosphere (0).According to this situation, can say, in order to be transported to the decomposing furnace 20 of cement with the thermolysis gas of its negative pressure autopneumatolysis in the future stove 1, the flow of thermolysis gas must be reduced to less than 1/5 of the flow of kiln waste gas.
But above-mentioned simulation does not almost change to existing cement mill, it is the simulation that the situation arranging waste treating device 100 is in its vicinity carried out.That is, usually in cement mill, the capacity of the induction fan 52 of discharge kiln waste gas is made to have the surplus of about 10%, as mentioned above, the quantitative change of thermolysis gas stream is many, can not be maintained at negative pressure by vapourizing furnace 1, be in the supply by means of thermolysis gas, when making the exhaust gas flow from decomposing furnace 20 increase about 10%.
Here, the thermal value of general waste is 1000 ~ 3000 kcal/kg, lower than coal etc., and therefore the thermal value of unit of fuel gas volume is also little.Therefore, if guarantee premised on necessary thermal value in order to the burning be used in decomposing furnace 20, if add the thermolysis gas that waste that thermal value is low comes, then comprise the waste gas total flux that combustion gases and kiln waste gas from the waste gas of decomposing furnace 20, instant heating decomposition gas and micro fine carbon dust is added together and increase.
Such as, the thermal value of coal is assumed to 5500 kcal/kg tentative calculations, then adds that total exhaust gas flow that thermolysis gas produces changes as shown in the relation curve of Fig. 5 A.The transverse axis of this pipeline curve is the flow of thermolysis gas and the ratio of kiln exhaust gas flow, and the longitudinal axis is total exhaust gas flow ratio, when namely not adding thermolysis gas, be the increase ratio of total exhaust gas flow of the decomposing furnace 20 of benchmark.According to this figure, known thermolysis gas flow ratio is larger, then the total exhaust gas flow from decomposing furnace 20 increases.
And for example solid line in figure, dotted line, long and short dash line, sequentially shown in, the thermal value of waste is lower, even then same traffic ratio, total exhaust gas flow also becomes many.Waste thermal value shown in each relation curve is respectively 2500 kcal/kg, 1400 kcal/kg, 1000 kcal/kg.As shown in the relation curve that dotted line represents, if the thermal value of waste is 1400 kcal/kg, when the throughput ratio of thermolysis gas is 0.2, total exhaust gas flow ratio is 1.1.With reference to Fig. 4, as mentioned above, when ventilation system of this kiln waste gas corresponded in cement factory has a surplus of about 10%, if throughput ratio is 0.2, then corresponding in vapourizing furnace 1 is malleation.
Corresponding thereto, if strengthen the ventilation system of the kiln waste gas in existing cement mill, or when new construction cement mill, the surplus of ventilation system is arranged larger, even then throughput ratio increases further, also negative pressure can be maintained at by vapourizing furnace 1, if there is the surplus of about 20 ~ 25%, then the relation curve according to the long and short dash line of above-mentioned Fig. 5 A, even when the thermal value of waste is 1000 quite low kcal/kg, throughput ratio also can be made to increase to about 0.3.
In the relation curve of Fig. 5 B below, the longitudinal axis is the ratio (calorific value of coal ratio) of the heat that the burning of micro fine carbon dust in the heat of the burning generation of decomposing furnace 20 produces, the correlationship between investigation with the throughput ratio of transverse axis.Throughput ratio is higher, then the ratio in fuel shared by thermolysis gas is higher, and therefore calorific value of coal is than step-down, the thermal value of thermolysis gas is larger, then its degree namely comply with long and short dash line, dotted line, solid line order progressively strengthen.
Can know again, time throughput ratio is high, the change of the calorific value of coal ratio that the difference of thermolysis heat release in gas region causes is larger, and the change of the temperature of combustion caused due to the fluctuation of thermolysis heat release in gas region is large.That is, the throughput ratio of thermolysis gas is higher, then the difference of waste kind etc. and the variation of the thermal value caused is reflected in the temperature of combustion of decomposing furnace 20, the temperature change of decomposing furnace 20 consumingly.
For this point, when watching three relation curves of Fig. 5 B, it is when throughput ratio is 0.3 that the mean value of calorific value of coal ratio is about 0.8, in other words, at that time thermolysis gas and micro fine carbon dust burning produce thermal value in about 80% be micro fine carbon dust burning produce heat.That is, if make the throughput ratio of thermolysis gas be less than 0.3, the burning of micro fine carbon dust then can be made to be top dog for the temperature of decomposing furnace 20, even if can say that the fluctuation of the thermal value of thermolysis gas is large, also can to realize the steady running of cement making equipment 200.
In the present embodiment, by controlling the waste input amount of working speed adjustment to vapourizing furnace 1 of e Foerderanlage 4, make throughput ratio be about 1/10, utilize simultaneously and the rotating speed of fan 5 is controlled and the control of adjustment throttle opening is adjusted, control the generating capacity of thermolysis gas.As an example, the flow that also can measure the thermolysis gas in the negative pressure of vapourizing furnace 1 and gas line of pipes 6 or the negative pressure measuring decomposing furnace 20 and exhaust gas flow etc., control according to this measurement value.
As mentioned above, in the waste treating device 100 of the 1st example, in vapourizing furnace 1, the thermolysis gas occurred by waste is under the carbon contained by keeping and ash content keep intact situation, utilize line of pipes 6 to deliver to cement making equipment 200, be introduced into decomposing furnace 20.At this moment the flow of thermolysis gas is restricted to below prescribed value relative to the throughput ratio of kiln waste gas, therefore, it is possible to suppress the temperature variation of decomposing furnace 20, can guarantee the operating safety of cement making equipment 200.
Again, by means of the negative pressure transportation thermolysis gas of decomposing furnace 20, negative pressure state can be maintained at by air shooter line 6 and vapourizing furnace 1, therefore fan is not set at air shooter line 6 passable yet, do not worry that carbon in thermolysis gas and ash grade attachment, the impeller etc. being piled up in fan causes fault.Also the leakage of the thermolysis gas of vapourizing furnace 1 can be prevented.
If stop because certain fault causes vapourizing furnace 1 to run, stop providing thermolysis gas and carbon to decomposing furnace 20, as long as the supply of the auxiliary fuels such as corresponding increase micro fine carbon dust, also decomposing furnace 20 can be made to run unaffected.
Again, vapourizing furnace 1 adopts the vapourizing furnace of flowing laminar, waste is crushed to very thin degree by the flowing husky by means of flowing, and the carbon therefore in thermolysis gas and the particle diameter of ash content also easily diminish, and is conducive to suppressing the attachment of carbon in air shooter line 6 and ash content, accumulation.And by providing micro fine carbon dust as deposited fuel, even if when processing low-grade waste, the temperature of vapourizing furnace 1 also fully can be improved, this attachment being also conducive to suppressing the carbon in air shooter line 6 and ash to grade, accumulation.
And, arrange multiple jet apparatus 6a in the midway of air shooter line 6, intermittently spray into pressurized air, by means of this, also can remove carbon and the ash content of the inside being deposited in air shooter line 6.And for thermolysis gas being imported the gas introduction port 27 of decomposing furnace 20, by making it downward-sloping, the attachment of carbon and dust, accumulation can be suppressed.
-2 example-
Referring to Fig. 6, the waste treating device of the present invention the 2nd example and cement making equipment are described.This figure is equivalent to Fig. 1 of above-mentioned 1st example.Further, in this example, the structure of the suspension preheater 10 Sum decomposition stove 20 of cement making equipment 200 is different from the 1st example, but for decomposing furnace 20, except there is no air induction port 25, identical with the 1st example, be therefore marked with identical symbol 20.The component of identical formation in addition, is also marked with identical symbol and the description thereof will be omitted.
Again, in the figure, the part of the air shooter line 6 formula preheater 10 that is draped covered, therefore the diagram arranging device 6a is omitted, equally, conveniently also omit the diagram of bypass line 60, but the same with the 1st example, arrange multiple jet apparatus 6a at air shooter line 6, possess again bypass line 60, water cooler 61, swirler 62 etc.
And in the cement making equipment 200 of this 2nd example, suspension preheater 10 is divided into two systems, and each system possesses such as 5 grades of swirlers 11.In the system in figure left side, be blown into kiln waste gas from subordinate, except decomposing furnace 20 is not set, identical with the 1st example.On the other hand, in the system on figure right side, be provided with decomposing furnace 20, but what flow into not kiln waste gas here, but from the high temperature cooling waste gas of air quenching water cooler 40.
Cooling exhaust is the same with the kiln waste gas of the 1st example flows into decomposing furnace 20 lower end, blows upward (shown in figure chain lines) as jet flow.This cooling exhaust be introduced into thermolysis gas and vapor permeation in decomposing furnace 20, make it burn by cement raw material to blowing up, from upper pipe 22 to the swirler of most next stage.And risen by swirler 11 step by step, flow out from the swirler 11 of most upper level to waste line 50.
To decomposing furnace 20 bottom (illustrating omission in detail), equally with the 1st example provide cement raw material from swirler 11, again, the gas introduction port 27 introducing thermolysis gas from vapourizing furnace 1 is set, but the introducing port 25 of the air making it burn is not set.Because as described above, be different from kiln waste gas, containing a large amount of oxygen by decomposing furnace 20 to the cooling exhaust of blowing up.
Except this point, the structure of decomposing furnace 20 is identical with the 1st example, and thermolysis gas is drawn towards in decomposing furnace 20 from the gas introduction port 27 of with respect to the horizontal plane downward-sloping setting, Thorough combustion after mixing with by the cooling exhaust blown up.Utilize this burning to make the temperature of cooling exhaust bring up to more than 900 DEG C, by means of this, promote by the calcining of the cement raw material blown up (decarbonation reaction).
And in the 2nd example, be also about 1/10 of the suppressed flow in cooling exhaust of flow of thermolysis gas, even if therefore its thermal value because of waste kind etc. and change, the temperature variation of decomposing furnace 20 is also not too large.Again, thermolysis gas utilizes the negative pressure generated in decomposing furnace 20 to carry.
Thus, as as described in this 2nd example, even when making cooling exhaust inflow decomposing furnace 20 such, by being that cement making equipment 200 carries out safe operation below the throughput ratio that the thermolysis gas of vapourizing furnace 1 is limited to regulation relative to the throughput ratio of the waste gas of this decomposing furnace 20, only can utilize the negative pressure transportation thermolysis gas of decomposing furnace 20 simultaneously.Therefore air shooter line 6 do not arrange fan also can, therefore need not worry its fault.
-variation-
Fig. 7 with Fig. 8 represents the variation of the 1st example that the formation of the decomposing furnace of cement making equipment 200 is different respectively.Again, Fig. 9 represents the situation not having decomposing furnace.These variation except about all identical with above-mentioned 1st example except the structure of decomposing furnace, are therefore marked with identical symbol for identical component and the description thereof will be omitted.
First, the decomposing furnace 70 of the variation shown in Fig. 7 is the same with the decomposing furnace of the 1st example, has the mixing section 71 at the kiln rear portion being arranged at rotary kiln 30.And the rotating decomposition room 72 to be communicated with its underpart, arrange combustion unit 73 in this rotating decomposition room 72.The high-temperature fuel gas that the burnings such as ejection coal, Sweet natural gas, heavy oil produce.In rotating decomposition room 72 shown in the figure, import from the high-temperature cooler waste gas (air) of air quenching water cooler 40 as rotating fluid, the cement raw material of preheating is provided from one-level swirler 11 above most next stage simultaneously.
This cement raw material accepts the calcining from the combustion gas of combustion unit 73 while move to mixing section 71, here, by means of the jet flow of the kiln waste gas come from below by cement raw material to blowing up.That is, mix with kiln exhaust flow at mixing section 71, the gas-flow that comprises cement raw material, both mix and rise.Along with upstream by blowing up time, cement raw material obtains fully calcined, is carried from the outlet of the topmost of mixing section 71 by the swirler 11 of pipeline to most next stage.Further, as long as the thermolysis gas of the stove of autopneumatolysis in the future 1 is introduced the outlet from the entrance of rotary kiln 30 to mixing section 71, or between rotating decomposition stove 72 and mixing section 71.
On the other hand, the decomposing furnace 75 of the variation shown in Fig. 8 has general identical with the 1st example structure, the structure vertically extended is set at the kiln rear portion of rotary kiln 30, form the eel-like figure portion 75a of ring-type at the substantial middle position of this above-below direction, being formed in this eel-like figure portion 75a also can to the structure of introducing air in decomposing furnace 75.
That is, the same with above-mentioned 1st example, the high temperature cooling waste gas from air quenching water cooler 40 as rotating fluid can be imported to decomposing furnace 75 bottom, but by means of point cross road that the supply road bifurcated from this water cooler waste gas goes out, a part for water cooler waste gas is introduced above-mentioned eel-like figure portion 75a, imported in decomposing furnace 75 from the introducing port formed at this.A part for the water cooler waste gas of such importing is provided in the jet flow of the kiln waste gas by rising in decomposing furnace 75 by as the air burnt again.Also be that the thermolysis gas of vapourizing furnace 1 is introduced the outlet from the entrance of rotary kiln 30 to decomposing furnace 75 in this variation.
And in the variation shown in Fig. 9, do not arrange decomposing furnace, the lower pipeline 21 being connected to the entrance of rotary kiln 30 utilizes increase in pipeline 29 to be connected with between the upper pipe 22 of the swirler 11 of the most next stage being connected to suspension preheater 10.This increase in pipeline 29 is provided respectively to the thermolysis gas of cement raw material and vapourizing furnace 1, utilize the jet flow of kiln waste gas by it to blowing up.The oxygen comprised in thermolysis gas and kiln waste gas reacts and to burn in upcast 29 and suspension preheater 10.
-other examples-
Further, the explanation of the above-mentioned 1st and the 2nd example and its variation is only illustrate, and the present invention is not intended to limit its applicable object or its purposes.Such as, in above-mentioned each example etc., only utilize the negative pressure transportation thermolysis gas of cement decomposing furnace 20, but be not limited to this.Utilize this part thing of negative pressure transportation thermolysis gas of decomposing furnace not mean that and get rid of complementary additional fan, and mean and do not establish fan that negative pressure also can be utilized thermolysis gas to be transported to decomposing furnace 20, negative pressure state can be maintained at by vapourizing furnace 1.
Again, as long as if process thermal value is the general waste of more than such as 1000 kcal/kg, by burning, the fluidised bed of vapourizing furnace 1 just can be maintained at suitable temperature by its part, therefore need not provide auxiliary fuel as above-mentioned each example, also can save for this reason and the micro fine carbon dust feedway 7 arranged.Equally, if only process chloride and contain the fewer waste of alkali, then also bypass line 60 can be saved in above-mentioned each example.
Again, in above-mentioned each example etc., arranging jet apparatus 6a from vapourizing furnace 1 to the air shooter line 6 of decomposing furnace 20, blowing away the carbon of accumulation and ash can be graded, but also can omitted.
Further, for the structure of the vapourizing furnace 1 of waste treating device 100 and the kiln (firing furnace) of cement making equipment 200 etc., above-mentioned each example is also not limited to.Vapourizing furnace 1 is not limited to the laminar that flows, and equally also can adopt the kiln formula of low temperature gasification mode, also can adopt high-temperature gasification mode.Again, firing furnace is also not limited to rotary kiln 30.Such as also can formula fluidised bed kiln.
Again, in above-mentioned each example, as the waste being supplied to vapourizing furnace 1 be envisioned for from family general waste and comprise the trade waste etc. of plastic waste, but be not limited to this, other animals and plants fuel wastes that also can the fecaluria of the wood wastes such as thinning timber (Thinned wood), wood chip or domestic animal, sewage sludge be provided such to vapourizing furnace 1.
Industrial applicability
If employing the present invention, the thermolysis gas of the waste that then vapourizing furnace can be occurred, under the carbon contained by keeping and the intact situation of ash content, carry to cement decomposing furnace, make it burn, therefore, it is possible to effectively utilize existing cement making equipment, realize the sanitary measure of waste with low cost, industrial application value is very high.
Claims (3)
1. the refuse processing method carried out in the waste treating device of contiguous cement making equipment setting, make the thermolysis in the vapourizing furnace of this waste treating device of the waste in described waste treating device, and make the method for thermolysis gas mixed firing in cement making equipment of generation, it is characterized in that
By e Foerderanlage, described waste is delivered to described vapourizing furnace;
Make the described waste be transferred gasify in described vapourizing furnace occur thermolysis gas and
Utilize the negative pressure-induced described thermolysis gas occurred at described vapourizing furnace of the cement decomposing furnace of cement making equipment, and under the carbon contained by keeping and the intact situation of ash content by gas delivery channels by described thermolysis gas induced to the cement decomposing furnace of described cement making equipment;
Wherein, the flow from the thermolysis gas of described vapourizing furnace is made to be restricted to less than 0.3 with the ratio of the flow of the waste gas of discharging from described cement decomposing furnace.
2. refuse processing method according to claim 1, is characterized in that,
Described cement decomposing furnace has mixing section and rotating decomposition room;
From the entrance of the rotary kiln as firing furnace be arranged in described cement making equipment between the outlet of described mixing section or import described thermolysis gas between described rotating decomposition room and described mixing section.
3. refuse processing method according to claim 1, is characterized in that,
Increase in pipeline is set and replaces described cement decomposing furnace;
Described thermolysis gas is imported to described increase in pipeline.
Priority Applications (9)
| Application Number | Priority Date | Filing Date | Title |
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| CN201010514607.3A CN102452803B (en) | 2010-10-21 | 2010-10-21 | Waste treatment equipment |
| PCT/CN2011/081081 WO2012051958A1 (en) | 2010-10-21 | 2011-10-20 | Waste-processing apparatus |
| DK11833864.9T DK2631222T3 (en) | 2010-10-21 | 2011-10-20 | WASTE TREATMENT DEVICES |
| KR1020137005987A KR101497847B1 (en) | 2010-10-21 | 2011-10-20 | Waste-processing apparatus |
| JP2013532043A JP5753585B2 (en) | 2010-10-21 | 2011-10-20 | Waste treatment facility |
| TW100138049A TWI532701B (en) | 2010-10-21 | 2011-10-20 | Waste disposal equipment |
| BR112013009116A BR112013009116B8 (en) | 2010-10-21 | 2011-10-20 | installation and waste treatment method |
| MYPI2013700637A MY163099A (en) | 2010-10-21 | 2011-10-20 | Waste treatment facility |
| EP11833864.9A EP2631222B2 (en) | 2010-10-21 | 2011-10-20 | Waste-processing apparatus |
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| TWI516302B (en) | 2013-12-11 | 2016-01-11 | 財團法人工業技術研究院 | Loop tower co2 capture system, carbonator, calciner and operating method thereof |
| CN112303630B (en) * | 2020-09-30 | 2024-02-09 | 汕尾市广物环保科技有限公司 | Biomass gasification and medical waste incineration co-production system and method |
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| CN101434461A (en) * | 2007-11-13 | 2009-05-20 | 川崎成套设备股份有限公司 | Apparatus and method for processing wastes |
| CN202030667U (en) * | 2010-10-21 | 2011-11-09 | 川崎重工业株式会社 | Waste treatment equipment |
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| CN202030667U (en) * | 2010-10-21 | 2011-11-09 | 川崎重工业株式会社 | Waste treatment equipment |
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