JP6459718B2 - Method and apparatus for producing solid fuel for cement firing - Google Patents
Method and apparatus for producing solid fuel for cement firing Download PDFInfo
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- JP6459718B2 JP6459718B2 JP2015071732A JP2015071732A JP6459718B2 JP 6459718 B2 JP6459718 B2 JP 6459718B2 JP 2015071732 A JP2015071732 A JP 2015071732A JP 2015071732 A JP2015071732 A JP 2015071732A JP 6459718 B2 JP6459718 B2 JP 6459718B2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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Description
本発明は、セメント焼成用固体燃料の製造方法及び製造装置に関し、特に詳細には引火性揮発性物質を含有する処理対象可燃物を乾燥し、セメント焼成用固体燃料を製造するにあたり、発生する引火性の揮発性物質への引火防止対策と処理対象可燃物の火災発生のリスクを低減しながら乾燥させ、セメント焼成設備の燃費を低下させないセメント焼成用固体燃料の製造方法及び製造装置に関する。 TECHNICAL FIELD The present invention relates to a method and an apparatus for producing a solid fuel for cement firing, and in particular, flammability generated when a combustible to be treated containing a flammable volatile substance is dried to produce a solid fuel for cement firing. TECHNICAL FIELD The present invention relates to a method and an apparatus for producing a solid fuel for cement firing which is dried while reducing the risk of fire of combustible materials to be treated and reducing the risk of fire occurrence of combustible materials to be treated and does not reduce the fuel consumption of cement firing facilities.
セメント焼成設備において、建設廃材、間伐材、廃白土、含油汚泥等の含油物質、下水汚泥、製紙スラッジなどの高含水率の有機系汚泥等を石炭や重油の代替燃料として利用することが行われている。 In cement burning facilities, oil-containing materials such as construction waste, thinned wood, waste white clay, oil-containing sludge, and high water content organic sludge such as sewage sludge and paper sludge are used as alternative fuels for coal and heavy oil. ing.
特開２００４−５００７７号公報（特許文献１）には、木材由来燃料の製造方法が開示され、特開２００６−１７５３５５号公報（特許文献２）には、有機系汚泥の処理方法が開示されている。両者は共に、クリンカクーラーの排ガスなどのセメント焼成設備の余剰熱を利用して、廃棄物などの処理対象可燃物を乾燥させ、セメント焼成用の燃料とするものであるが、従来のこのようなセメント焼成用の燃料の製造方法においては、乾燥により発生する引火性の揮発性物質への引火防止対策や、含水率の下げ過ぎ、静電気、及び自己発熱による火災発生リスクの低減対策については、全く考慮されていなかった。 Japanese Unexamined Patent Application Publication No. 2004-50077 (Patent Document 1) discloses a method for producing wood-derived fuel, and Japanese Unexamined Patent Application Publication No. 2006-175355 (Patent Document 2) discloses a method for treating organic sludge. Yes. In both cases, surplus heat from the cement firing equipment such as exhaust gas from the clinker cooler is used to dry the combustibles to be treated, such as waste, and used as fuel for cement firing. In the method of manufacturing cement firing fuel, there are no measures to prevent flammability of flammable volatile substances generated by drying, or to reduce the risk of fire occurrence due to excessively low water content, static electricity, and self-heating. It was not considered.
このため、上述した様々な代替燃料は、火災等のリスクを回避するため乾燥せず、直接セメント焼成設備へ投入されており、代替燃料が含有する水分が原因で、セメント焼成において燃費低下を引き起こしていた。 For this reason, the various alternative fuels mentioned above are not dried to avoid risks such as fires, but are directly put into the cement burning equipment, causing moisture reduction in cement burning due to moisture contained in the alternative fuel. It was.
従って、本発明の目的は、上記問題を解決し、引火性揮発性物質を含有する処理対象可燃物を、引火性の揮発性物質への引火防止と火災発生のリスクを低減しながら乾燥させると共に、製造された固体燃料がセメント焼成設備の燃費を低下させないセメント焼成用固体燃料の製造方法及び製造装置を提供することである。 Accordingly, an object of the present invention is to solve the above problems and to dry a combustible material containing a flammable volatile substance while preventing the ignition of the flammable volatile substance and reducing the risk of fire. An object of the present invention is to provide a method and an apparatus for producing a solid fuel for cement firing in which the produced solid fuel does not lower the fuel consumption of the cement firing equipment.
上記の課題を解決するため、本発明のセメント焼成用固体燃料の製造方法及び製造装置は以下のような技術的特徴を備えている。
（１） 引火性揮発性物質を含有する処理対象可燃物を、当該処理対象可燃物の引火点より低い温度であって且つ当該処理対象可燃物の含水率が限界含水率となる温度以下の乾燥温度（ｔ１）に調整した乾燥用流体で乾燥させることを特徴とする、セメント焼成用固体燃料の製造方法である。
In order to solve the above problems, the method and apparatus for producing a solid fuel for cement firing of the present invention have the following technical features.
(1) Drying a combustible material to be treated containing a flammable volatile substance at a temperature lower than the flash point of the combustible material to be treated and having a moisture content equal to or lower than the critical moisture content. A method for producing a solid fuel for cement firing, characterized by drying with a drying fluid adjusted to a temperature (t1).
（２） 上記（１）に記載のセメント焼成用固体燃料の製造方法において、乾燥用流体の温度を調整するにあたり、引火性揮発性物質を含有する処理対象可燃物の含水率（質量％）と、変化させる温度ｔ２における乾燥質量基準での処理対象可燃物中の引火性揮発性物質の発生量（ｍｇ/ｋｇ）とを予め測定し、次の式：
Ｃ２（容量％）＝［Ｗ×（１−Ｈ／１００）×Ｖ２×１０−６／Ｍ］×（２２．４／Ｑ）×１００
（上記式中、Ｗは処理対象可燃物の処理対象量（ｋｇ／時）、Ｈは処理対象可燃物の含水率（質量％）、Ｖ２は乾燥質量基準での処理対象可燃物の乾燥温度（ｔ２）における引火性揮発性物質の発生量（ｍｇ／ｋｇ）、Ｍは引火性揮発性物質の分子量（ｋｇ／ｋｍｏｌ）、Ｑは乾燥用流体の流量（ｍ３Ｎ／時）を示す）
により乾燥用流体中の引火性揮発性物質の濃度（Ｃ２：容量％）を演算し、前記演算した引火性揮発性物質の濃度（Ｃ２：容量％）と引火性揮発性物質の燃焼範囲の下限濃度（Ｃ：容量％）とを比較して、Ｃ２＜Ｃとなるように乾燥温度（ｔ１）を温度ｔ２と一致させる温度とするように設定することを特徴とする。
(2) In the method for producing a solid fuel for cement firing as described in (1) above, in adjusting the temperature of the drying fluid, the moisture content (% by mass) of the combustible to be treated containing a flammable volatile substance and The amount of flammable volatile substances (mg / kg) in the combustible to be treated on a dry mass basis at the temperature t2 to be changed is measured in advance, and the following formula:
C2 (volume%) = [W × (1-H / 100) × V2 × 10 −6 /M]×(22.4/Q)×100
(W is the amount to be treated of the combustible material to be treated (kg / hour), H is the moisture content (mass%) of the combustible material to be treated, and V2 is the drying temperature of the combustible material to be treated on a dry mass basis ( The amount of flammable volatile substances generated at t2) (mg / kg), M is the molecular weight of flammable volatile substances (kg / kmol), and Q is the flow rate of the drying fluid (m 3 N / hour))
To calculate the concentration (C2: volume%) of the flammable volatile substance in the drying fluid, and the lower limit of the calculated flammable volatile substance concentration (C2: volume%) and the combustion range of the flammable volatile substance The concentration (C: volume%) is compared, and the drying temperature (t1) is set to a temperature that matches the temperature t2 so that C2 <C.
（３） 上記（１）又は（２）に記載のセメント焼成用固体燃料の製造方法において、処理対象可燃物中に引火性揮発性物質が複数含まれる場合には、各引火性揮発性物質についてＣ２＜Ｃを満たすように乾燥温度（ｔ１）を設定することを特徴とする。 (3) In the method for producing a solid fuel for cement firing according to (1) or (2) above, when a plurality of flammable volatile substances are contained in the combustible material to be treated, each flammable volatile substance The drying temperature (t1) is set so as to satisfy C2 <C.
（４） 上記（１）〜（３）のいずれかに記載のセメント焼成用固体燃料の製造方法において、乾燥用流体はセメント製造設備から排出される排ガスを利用し、乾燥後の固体燃料はセメント製造設備の燃料として利用され、処理対象可燃物を乾燥後の乾燥用流体は、セメント焼成設備中の８００℃以上の温度の装置に導入されるか又は乾燥排気処理装置にて処理されることを特徴とする。 (4) In the method for producing a solid fuel for firing a cement according to any one of (1) to (3), the drying fluid uses exhaust gas discharged from a cement production facility, and the solid fuel after drying is cement. The drying fluid that is used as a fuel for manufacturing equipment and has dried the combustibles to be treated is introduced into a device having a temperature of 800 ° C. or higher in the cement firing facility or processed by a dry exhaust treatment device. Features.
（５） セメント製造設備からの乾燥用流体の温度を、処理対象可燃物の引火点より低い温度であって且つ当該処理対象可燃物の含水率が限界含水率となる温度以下の乾燥温度（ｔ１）に調整する温度調整装置と、乾燥温度（ｔ１）に調整された乾燥用流体を導入して処理対象可燃物を乾燥させる乾燥装置とを備えることを特徴とする、セメント焼成用固体燃料の製造装置である。 (5) The temperature of the drying fluid from the cement production facility is a temperature lower than the flash point of the combustible material to be treated, and a temperature equal to or lower than the temperature at which the moisture content of the combustible material to be treated reaches the limit water content (t1 ) And a drying device that introduces a drying fluid adjusted to the drying temperature (t1) and dries the combustible to be treated. Device.
（６） 上記（５）に記載のセメント焼成用固体燃料の製造装置において、更に、乾燥用流体の温度を乾燥温度（ｔ１）とするために、セメント製造設備から排出される排ガスに空気を流入させて乾燥用流体とするための空気流量調整装置を備えることを特徴とする。 (6) In the manufacturing apparatus for solid fuel for cement firing as described in (5) above, in order to set the drying fluid temperature to the drying temperature (t1), air is introduced into the exhaust gas discharged from the cement manufacturing facility. And an air flow rate adjusting device for making a drying fluid.
（７） 上記（５）又は（６）に記載のセメント焼成用固体燃料の製造装置において、更に、乾燥処理された処理対象可燃物の含水率を測定する含水率測定装置を備えることを特徴とする。 (7) The apparatus for producing a solid fuel for cement firing as described in (5) or (6) above, further comprising a moisture content measuring device for measuring the moisture content of the combustible to be treated that has been dried. To do.
（８） 上記（５）〜（７）のいずれかに記載のセメント焼成用固体燃料の製造装置において、乾燥装置から排出された乾燥用流体を処理するための乾燥排気処理装置を備えることを特徴とする。 (8) The cement firing solid fuel manufacturing apparatus according to any one of (5) to (7), further including a dry exhaust treatment device for treating the drying fluid discharged from the drying device. And
本発明のセメント焼成用固体燃料の製造方法及び製造装置では、引火性揮発性物質を含有する処理対象可燃物を、処理対象可燃物の引火点より低い温度であって且つ当該処理対象可燃物の含水率が限界含水率となる温度以下の乾燥温度（ｔ１）に調整した乾燥用流体で乾燥させるため、発生する引火性の揮発性物質への引火防止と火災発生のリスクを低減しながら処理対象可燃物を乾燥でき、さらには、製造された固体燃料は限界含水率に近い状態まで乾燥されているため、セメント焼成設備の燃費低下を抑制できる。 In the method and apparatus for producing a solid fuel for cement firing according to the present invention, the combustible material to be treated containing a flammable volatile substance is at a temperature lower than the flash point of the combustible material to be treated and Because it is dried with a drying fluid adjusted to a drying temperature (t1) that is equal to or lower than the temperature at which the moisture content becomes the critical moisture content, it is a target to be treated while preventing the occurrence of flammable volatile substances and reducing the risk of fire. The combustible material can be dried. Further, since the produced solid fuel is dried to a state close to the limit moisture content, it is possible to suppress a reduction in fuel consumption of the cement firing facility.
さらに、乾燥用流体中の引火性揮発性物質の濃度（Ｃ２）＜引火性揮発性物質の燃焼範囲の下限濃度（Ｃ）を満たすように乾燥用流体の温度を設定することで、発生する引火性の揮発性物質への引火をより確実に防止することが可能となる。 Further, by setting the temperature of the drying fluid to satisfy the concentration of the flammable volatile substance in the drying fluid (C2) <the lower limit concentration (C) of the combustion range of the flammable volatile substance, It is possible to more reliably prevent ignition of volatile substances.
本発明を、以下の実施形態により説明する。
本発明のセメント焼成用固体燃料の製造方法は、引火性揮発性物質を含有する処理対象可燃物を、当該処理対象可燃物の引火点より低い温度であって且つ、乾燥用流体中の引火性揮発性物質の濃度（Ｃ２）＜引火性揮発性物質の燃焼範囲の下限濃度（Ｃ）を満たす温度で、加えて当該処理対象可燃物の含水率が限界含水率となる温度以下の乾燥温度（ｔ１）に調整した乾燥用流体で乾燥させることを特徴とする、セメント焼成用固体燃料の製造方法である。
The present invention will be described by the following embodiments.
In the method for producing a solid fuel for cement firing according to the present invention, a combustible material to be treated containing a flammable volatile substance is at a temperature lower than the flash point of the combustible material to be treated and is flammable in a drying fluid. Volatile substance concentration (C2) <temperature satisfying the lower limit concentration (C) of the flammable volatile substance combustion range, and in addition, a drying temperature that is equal to or lower than the temperature at which the moisture content of the combustible to be treated becomes the critical moisture content ( A method for producing a solid fuel for cement firing, characterized by drying with a drying fluid adjusted to t1).
処理対象可燃物とは、本発明のセメント焼成用固体燃料を製造するための処理が行われる対象物のことであり、具体的には、建設廃材、及び間伐材、並びに剪定枝等の破砕物、燃料用木質チップ、畳、布、紙類、食品残渣、農業残渣、廃プラスチック、廃白土、含油汚泥等の含油物質、下水汚泥、製紙スラッジなどの高含水率の有機系汚泥、前記の２つ以上を含む混合物などの各種の可燃物が該当する。そのような可燃物の中でも、特に、含水率が高く、そのままセメント焼成設備に投入すると設備の燃費低下の原因となるようなものであり、かつ、有機溶剤など乾燥処理工程で引火性揮発物質の発生を伴うものは、本発明を適用することが好ましい。 The combustible material to be treated is an object to be treated for producing the solid fuel for cement burning according to the present invention. Specifically, construction waste materials, thinned materials, and crushed materials such as pruned branches , Wood chips for fuel, tatami mat, cloth, paper, food residue, agricultural residue, waste plastic, waste white clay, oil-containing substances such as oil-containing sludge, organic sludge with high water content such as sewage sludge and paper sludge, 2 Applicable to various combustible materials such as a mixture containing two or more. Among such combustible materials, in particular, the moisture content is high, and if it is directly put into cement burning equipment, it may cause a reduction in fuel consumption of the equipment, and flammable volatile substances such as organic solvents may be used in the drying process. It is preferable to apply the present invention to those accompanied by generation.
引火性揮発物質としては、処理対象可燃物の種類によって様々であり、例えば、パラフィン系炭化水素、オレフィン系炭化水素、ナフテン系炭化水素、芳香族炭化水素、有機酸、アルコール、エーテル、ケトン、アルデヒドなどが例示される。特に、本発明では、クリンカクーラーなどのセメント焼成設備の余剰熱を利用して乾燥するため、１００〜４００℃程度の排ガスを温度調整して８０〜２００℃の乾燥用流体（気体）にして乾燥に使用する。このため、このような温度範囲で揮発性のある物質を含有する場合は、本発明を適用することが好ましい。 Flammable volatile substances vary depending on the type of combustible material to be treated. For example, paraffinic hydrocarbons, olefinic hydrocarbons, naphthenic hydrocarbons, aromatic hydrocarbons, organic acids, alcohols, ethers, ketones, aldehydes Etc. are exemplified. In particular, in the present invention, since the drying is performed by using surplus heat of cement baking equipment such as a clinker cooler, the temperature of exhaust gas at about 100 to 400 ° C. is adjusted to a drying fluid (gas) at 80 to 200 ° C. for drying. Used for. For this reason, it is preferable to apply this invention, when a volatile substance is contained in such a temperature range.
次に、処理対象可燃物を乾燥させる乾燥用流体の温度の設定方法について説明する。
本発明では、以下の２つの条件を満足するよう温度設定している。
（１）処理対象可燃物の引火点より低い温度であること
（２）処理対象可燃物の含水率が限界含水率となる温度以下であること
さらに、本発明では、次の条件を備えることで、より安全に乾燥処理を行うことができる。
（３）乾燥用流体中の引火性揮発性物質の濃度を、当該引火性揮発性物質の燃焼範囲の下限濃度未満とすること
Next, a method for setting the temperature of the drying fluid for drying the combustible to be treated will be described.
In the present invention, the temperature is set so as to satisfy the following two conditions.
(1) The temperature is lower than the flash point of the combustible material to be treated. (2) The water content of the combustible material to be treated is equal to or lower than the temperature at which the moisture content becomes the limit water content. Therefore, the drying process can be performed more safely.
(3) The concentration of the flammable volatile substance in the drying fluid should be less than the lower limit concentration of the combustion range of the flammable volatile substance.
このような条件を判断するためには、乾燥装置に投入する処理対象可燃物の受入れロット毎に、以下の数値を予め測定する。
（ａ）処理する前の処理対象可燃物の含水率
（ｂ）処理対象可燃物を乾燥させた際の限界含水率
（ｃ）乾燥質量基準の処理対象可燃物中の引火性揮発性物質の発生量
（ｄ）処理対象可燃物の引火点（乾燥処理を行う前の処理対象可燃物に関する引火点）
（ｅ）引火性揮発性物質の燃焼範囲の下限濃度（Ｃ）
In order to judge such conditions, the following numerical values are measured in advance for each lot of receiving combustibles to be processed that are put into the drying apparatus.
(A) Moisture content of the combustible material to be treated before processing (b) Limiting water content when the combustible material to be treated is dried (c) Generation of flammable volatile substances in the combustible material to be treated based on dry mass Amount (d) Flash point of the combustible material to be treated (Flash point of the combustible material to be treated before drying)
(E) Lower limit concentration of flammable volatile substances in the combustion range (C)
図１は、処理対象可燃物を乾燥させる乾燥用流体の設定温度の決定方法を説明するフロー図である。ステップＡでは、乾燥用流体（気体）の温度を、処理対象可燃物の引火点以下に設定する。これにより、乾燥中に処理対象可燃物に引火するリスクを避けることができる。 FIG. 1 is a flowchart illustrating a method for determining a set temperature of a drying fluid for drying a combustible to be processed. In step A, the temperature of the drying fluid (gas) is set below the flash point of the combustible material to be treated. Thereby, the risk of igniting the combustible to be treated during drying can be avoided.
次に、ステップＢでは、乾燥用流体中の引火性揮発性物質の濃度を、当該引火性揮発性物質の燃焼範囲の下限濃度未満に設定する。これにより、乾燥中に発生する引火性揮発性物質に引火するリスクを避けることができる。そして、ステップＡで設定した温度が、ステップＢの条件を満足する場合には、温度設定を変更せず、次のステップＣに移る。ステップＢの条件を満足しない場合は、ステップＢの条件を満足する温度に再設定が行われる。 Next, in step B, the concentration of the flammable volatile substance in the drying fluid is set to be less than the lower limit concentration of the combustion range of the flammable volatile substance. This avoids the risk of igniting flammable volatiles that occur during drying. When the temperature set in step A satisfies the condition in step B, the temperature setting is not changed and the process proceeds to the next step C. If the condition of Step B is not satisfied, the temperature is reset to a temperature that satisfies the condition of Step B.
設定温度（ｔ２）における引火性揮発性物質の濃度（Ｃ２：容量％）は、次式により算出することができる。これは、設定温度における引火性揮発性物質の濃度の最大値でもある。
Ｃ２（容量％）＝［Ｗ×（１−Ｈ／１００）×Ｖ２×１０−６／Ｍ］×（２２．４／Ｑ）×１００
上記式中、Ｗは処理対象可燃物の処理対象量（ｋｇ／時）、Ｈは処理対象可燃物の含水率（質量％）、Ｖ２は乾燥質量基準での処理対象可燃物の乾燥温度（ｔ２）における引火性揮発性物質の発生量（ｍｇ／ｋｇ）、Ｍは引火性揮発性物質の分子量（ｋｇ／ｋｍｏｌ）、Ｑは乾燥用流体の流量（ｍ３Ｎ／時）を示す。
The concentration (C2: volume%) of the flammable volatile substance at the set temperature (t2) can be calculated by the following equation. This is also the maximum concentration of flammable volatile material at the set temperature.
C2 (volume%) = [W × (1-H / 100) × V2 × 10 −6 /M]×(22.4/Q)×100
In the above formula, W is the amount to be treated of the combustible material to be treated (kg / hour), H is the moisture content (mass%) of the combustible material to be treated, and V2 is the drying temperature (t2) of the combustible material to be treated on a dry mass basis. ), The amount of flammable volatile substances generated (mg / kg), M is the molecular weight of flammable volatile substances (kg / kmol), and Q is the flow rate of the drying fluid (m3N / hour).
処理対象可燃物の処理対象量（Ｗ：ｋｇ／時）は、処理対象可燃物をどの程度のスピードで処理するかによって決まり、Ｑは乾燥用流体の流量（Ｑ：ｍ３Ｎ／時）は、使用するセメント焼成設備において、乾燥装置に供給可能な乾燥用流体の流量の範囲から、設定される。 The amount of combustible material to be treated (W: kg / hour) depends on how fast the combustible material to be treated is treated, and Q is the flow rate of the drying fluid (Q: m 3 N / hour). In the cement firing facility to be used, the range is set from the range of the flow rate of the drying fluid that can be supplied to the drying device.
処理対象可燃物の含水率（Ｈ：質量％）、乾燥質量基準での処理対象可燃物の乾燥温度（ｔ２）における引火性揮発性物質の発生量（Ｖ２：ｍｇ／ｋｇ）、引火性揮発性物質の分子量（Ｍ：ｋｇ／ｋｍｏｌ）は、処理対象可燃物の性状を調べることにより、特定される。 Moisture content of the combustible material to be treated (H: mass%), amount of flammable volatile substances generated at the drying temperature (t2) of the combustible material to be treated on a dry mass basis (V2: mg / kg), flammable volatility The molecular weight (M: kg / kmol) of the substance is specified by examining the properties of the combustible material to be treated.
ステップＢでは、上記式により演算した、乾燥用流体中の引火性揮発性物質の濃度（Ｃ２：容量％）と、引火性揮発性物質の燃焼範囲の下限濃度（Ｃ：容量％）とを比較して、Ｃ２＜Ｃとなるように乾燥温度（ｔ１）を温度ｔ２と一致させる温度とするように設定する。 In Step B, the concentration of the flammable volatile substance in the drying fluid (C2: volume%) calculated by the above formula is compared with the lower limit concentration (C: volume%) of the combustion range of the flammable volatile substance. Then, the drying temperature (t1) is set to a temperature that matches the temperature t2 so that C2 <C.
ステップＣでは、乾燥装置の出口から排出される、乾燥処理された処理対象可燃物（「固体燃料」ともいう。）の含水率を適時測定し、固体燃料の含水率が、上記（ｂ）で測定した処理対象可燃物の限界含水率となる温度以下となるように設定される。つまり、固体燃料の含水率が、上記（ｂ）で測定した処理対象可燃物の限界含水率より高い場合は、乾燥用流体の温度調整は行わず、上記（ｂ）で測定した処理対象可燃物の限界含水率より低い場合には、乾燥用流体の温度を下げ、製造される固体燃料の含水率を前記限界含水率よりも高くなるように調整する。これにより、乾燥装置から排出される固体燃料の含水率が前記限界含水率より大きくなるため、含水率の下げ過ぎ、静電気、及び自己発熱による火災の発生を抑制することが可能となる。 In Step C, the moisture content of the treated combustible material (also referred to as “solid fuel”) discharged from the outlet of the drying device is measured in a timely manner, and the moisture content of the solid fuel is determined by (b) above. The temperature is set to be equal to or lower than the temperature at which the measured moisture content of the treatment target combustible material becomes the limit moisture content. That is, when the moisture content of the solid fuel is higher than the limit moisture content of the combustible material to be treated measured in the above (b), the temperature of the drying fluid is not adjusted and the combustible material to be treated measured in the above (b). If the moisture content is lower than the critical moisture content, the temperature of the drying fluid is lowered, and the moisture content of the produced solid fuel is adjusted to be higher than the critical moisture content. Thereby, since the moisture content of the solid fuel discharged from the drying device becomes larger than the limit moisture content, it becomes possible to suppress the occurrence of fire due to excessive reduction of moisture content, static electricity, and self-heating.
ステップＣにもあるように、本発明の固体燃料の製造方法は、乾燥処理された処理対象可燃物の性状（含水率）を適時測定し、乾燥用流体の設定温度を調整することが、より好ましい。乾燥処理された処理対象可燃物の含水率は、乾燥装置の出口で、処理対象可燃物の含水率を測定し、上記（ｂ）で測定した処理対象可燃物の限界含水率と比較される。 As also in Step C, the solid fuel production method of the present invention can measure the property (moisture content) of the combustible material that has been dried and adjust the set temperature of the drying fluid in a timely manner. preferable. The moisture content of the combustible material to be treated that has been dried is measured at the outlet of the drying device, and the moisture content of the combustible material to be treated is measured and compared with the critical moisture content of the combustible material to be treated measured in (b) above.
また、処理対象可燃物中に引火性揮発性物質が複数含まれる場合には、各引火性揮発性物質毎について濃度（Ｃ２）を演算し、各引火性揮発物質の燃焼範囲の下限濃度（Ｃ）と比較し、Ｃ２＜Ｃの条件を満足するように乾燥温度（ｔ１）を設定する。ただし、異なる引火性揮発性物質であっても引火性においては発生する濃度を足し合わせて考慮する必要がある種類については、それらの総和の濃度を基に判断する。 If the combustible material to be treated contains a plurality of flammable volatile substances, the concentration (C2) is calculated for each flammable volatile substance, and the lower limit concentration (C2) of the combustion range of each flammable volatile substance is calculated. ) And the drying temperature (t1) is set so as to satisfy the condition of C2 <C. However, even for different flammable volatile substances, the types that need to be considered in addition to the concentration generated in flammability are determined based on the total concentration.
乾燥に使用される乾燥用流体（気体）は、セメント焼成設備の余剰熱を利用したものであるなら、特に限定されないが、例えば、クリンカクーラーの排ガス、仮焼成炉出口から煙突にいた排ガス経路の排ガスなどを利用することが可能である。 The drying fluid (gas) used for drying is not particularly limited as long as it uses surplus heat of the cement firing equipment. For example, the exhaust gas from the clinker cooler and the exhaust gas path from the calciner exit to the chimney It is possible to use exhaust gas.
また、乾燥で使用された乾燥用流体は、専用の乾燥排気処理装置で粉塵、臭気成分等を除去した後外部に放出させることも可能であるが、セメント焼成設備に再度戻し、処理することも可能である。特に、キルンから仮焼成炉の出口までの間のように温度が８００℃以上ある場所に戻すことで、乾燥工程で発生した揮発性物質を燃料として利活用できるとともに、臭気成分等を分解処理することが可能となる。 In addition, the drying fluid used for drying can be released to the outside after removing dust, odor components, etc. with a dedicated dry exhaust treatment device, but it can also be returned to the cement firing facility and processed again. Is possible. In particular, by returning to a place where the temperature is 800 ° C. or more, such as between the kiln and the exit of the pre-baking furnace, the volatile substances generated in the drying process can be used as fuel, and the odor components are decomposed. It becomes possible.
次に、セメント焼成用固体燃料の製造装置について図２を参考に説明する。
セメント焼成設備としては、セメント原料を、予熱器、仮焼成炉、キルンに順次投入し焼成される。焼成されたセメントクリンカは、クリンカクーラーで冷却される。キルンで発生した排ガスは、仮焼成炉、予熱器、排ガス処理設備、煙突を経て外部に放出される。クリンカクーラーでは、空気により冷却が行われ、クリンカクーラーから排出される排ガスは、２００〜４００℃の温度を有している。通常であれば、クリンカクーラーの排ガスは、仮焼成炉などに導入される。
Next, an apparatus for producing a cement firing solid fuel will be described with reference to FIG.
As a cement firing facility, cement raw materials are sequentially put into a preheater, a temporary firing furnace, and a kiln and fired. The fired cement clinker is cooled by a clinker cooler. The exhaust gas generated in the kiln is discharged to the outside through a temporary firing furnace, a preheater, an exhaust gas treatment facility, and a chimney. In the clinker cooler, cooling is performed with air, and the exhaust gas discharged from the clinker cooler has a temperature of 200 to 400 ° C. Normally, the exhaust gas from the clinker cooler is introduced into a temporary firing furnace or the like.
処理対象可燃物は、不図示の貯蔵設備から定量供給設備に供給され、当該定量供給設備により、予め設定された処理対象可燃物の処理量（所定時間当たりの処理量）に応じて、所定速度で所定量の処理対象可燃物を乾燥装置に供給される。 The combustible material to be processed is supplied from a storage facility (not shown) to a fixed amount supply facility, and the fixed amount supply facility supplies a predetermined speed according to a predetermined processing amount of the combustible material to be processed (processing amount per predetermined time). A predetermined amount of combustible material to be treated is supplied to the drying device.
乾燥装置には、乾燥用流体が導入されている。図２では、乾燥用流体として、クリンカクーラーの排ガスの一部を利用しているが、仮焼成炉出口から煙突に至る排ガス経路の排ガスを利用することも可能である。乾燥装置で使用できる乾燥用流体に必要な温度、例えば、８０℃以上が維持できる排ガスを利用することが好ましい。 A drying fluid is introduced into the drying device. In FIG. 2, a part of the exhaust gas from the clinker cooler is used as the drying fluid, but it is also possible to use exhaust gas in the exhaust gas path from the calciner outlet to the chimney. It is preferable to use exhaust gas that can maintain a temperature necessary for a drying fluid that can be used in a drying apparatus, for example, 80 ° C. or higher.
本発明では、乾燥装置に導入される乾燥用流体の温度を、処理対象可燃物の引火点より低い温度であって且つ当該処理対象可燃物の含水率が限界含水率となる温度以下の乾燥温度（ｔ１）に調整する温度調整装置を備えている。 In the present invention, the temperature of the drying fluid introduced into the drying apparatus is a temperature lower than the flash point of the combustible material to be treated, and a drying temperature equal to or lower than the temperature at which the water content of the combustible material to be treated becomes the critical moisture content. A temperature adjusting device for adjusting to (t1) is provided.
温度調整装置により、セメント焼成設備の排ガスの温度を、乾燥装置で必要な温度「乾燥温度（ｔ１）」に設定するには、セメント製造設備から排出される排ガスに空気を混入して、温度を調整する。図２のダンパ（１）のような空気流量調整装置が、この機能を有している。さらに、ダンパ（２）は、乾燥装置に導入する乾燥用流体の流量を調整している。ファンは、乾燥用流体を乾燥装置に送風する送風機である。乾燥用流体の流路に沿って（乾燥装置の入り口付近）に流体の温度を測定する温度計（ＴＩＣ）を設け、温度の測定結果に基づき、所定の温度になるように、前記空気の流量を調節する。 In order to set the temperature of the exhaust gas from the cement firing equipment to the temperature required for the drying equipment, “Drying temperature (t1)”, the air is mixed into the exhaust gas discharged from the cement manufacturing equipment, and the temperature is adjusted. adjust. An air flow rate adjusting device such as the damper (1) of FIG. 2 has this function. Further, the damper (2) adjusts the flow rate of the drying fluid introduced into the drying device. The fan is a blower that blows the drying fluid to the drying device. A thermometer (TIC) for measuring the temperature of the fluid is provided along the flow path of the drying fluid (near the entrance of the drying device), and the flow rate of the air is set to a predetermined temperature based on the temperature measurement result. Adjust.
乾燥装置から排出される排ガスは、乾燥排気処理装置で粉塵、臭気成分等が除去され、外部に排気される。また、キルンから仮焼成炉出口までの間で８００℃以上の高温雰囲気に、乾燥装置の排ガスを導入することも可能である。 The exhaust gas discharged from the drying apparatus is exhausted to the outside after the dust and odor components are removed by the dry exhaust treatment apparatus. It is also possible to introduce the exhaust gas from the drying apparatus into a high temperature atmosphere of 800 ° C. or higher between the kiln and the pre-baking furnace exit.
乾燥装置で乾燥された処理対象可燃物（固体燃料）は、固体燃料貯蔵設備で蓄積され、定量供給装置により、仮焼成炉に燃料として導入したり、キルン出口から仮焼成炉の入り口に至る窯尻部で燃料として燃焼させる方法もある。 The combustible material to be treated (solid fuel) dried by the drying device is accumulated in the solid fuel storage facility and introduced into the calcining furnace as a fuel by the quantitative supply device or from the kiln outlet to the entrance of the calcining furnace There is also a method of burning as fuel at the bottom.
本発明のセメント焼成用固体燃料の製造装置では、更に、乾燥処理された処理対象可燃物の含水率を測定する含水率測定装置（ＸＩＣ）を備えている。当該測定装置は、乾燥装置の出口に備え付けることで、固体燃料の含水率を処理対象可燃物の限界含水率以上に調整する際の生情報として有用となる。 The manufacturing apparatus for solid fuel for cement firing according to the present invention further includes a moisture content measuring device (XIC) for measuring the moisture content of the combustible to be treated that has been dried. By providing the measurement device at the outlet of the drying device, it becomes useful as raw information when adjusting the moisture content of the solid fuel to be higher than the limit moisture content of the combustible to be treated.
以下では、図１の温度設定に係るフロー図に沿って、具体的事例を基に設定方法を説明する。
まず、処理対象可燃物を固体燃料Ａ（引火性揮発性物質を含む。）とする。処理対象可燃物の処理量（Ｗ）は、１０００ｋｇ／時とする。
処理対象可燃物の性状として、処理前の含水率（Ｈ）は４０質量％、引火点は１６０℃、温度（ｔ２）における引火性揮発性物質の発生量（Ｖ２）は、表１の通りである。
Below, the setting method is demonstrated based on the specific example along the flowchart which concerns on the temperature setting of FIG.
First, the combustible material to be treated is solid fuel A (including flammable volatile substances). The processing amount (W) of the combustible material to be processed is 1000 kg / hour.
As the properties of combustible materials to be treated, the moisture content (H) before treatment is 40% by mass, the flash point is 160 ° C., and the amount of flammable volatile substances generated at temperature (t2) (V2) is as shown in Table 1. is there.
固体燃料Ａに含まれる引火性揮発性物質を、揮発性物質Ｂとする。揮発性物質の分子量（Ｍ）は、１０６ｋｇ／ｋｍｏｌであり、燃焼範囲の下限濃度（Ｃ）は、０．９０容量％である。 The flammable volatile substance contained in the solid fuel A is referred to as a volatile substance B. The molecular weight (M) of the volatile substance is 106 kg / kmol, and the lower limit concentration (C) of the combustion range is 0.90% by volume.
乾燥用流体は、クリンカクーラーの排ガスに空気を混合させたものであり、流量（Ｑ）は、３４００ｍ３Ｎ／時とする。 The drying fluid is a mixture of clinker cooler exhaust gas and air, and the flow rate (Q) is 3400 m 3 N / hour.
図１のステップＡで、乾燥用流体の温度（ｔ１）は、処理対象可燃物の引火点（１６０℃）より低く設定する必要があるため、温度ｔ１は、１６０℃未満となる。 In Step A of FIG. 1, the temperature (t1) of the drying fluid needs to be set lower than the flash point (160 ° C.) of the combustible to be processed, and therefore the temperature t1 is less than 160 ° C.
ステップＢで、処理対象可燃物の処理量（Ｗ）、処理前の処理対象可燃物の含水率（Ｈ）、引火性揮発性物質の分子量（Ｍ）、乾燥用流量（Ｑ）及び表１の引火性揮発性物質の発生量（Ｖ２）を基に、各温度（ｔ２）における引火性揮発性物質の濃度（Ｃ２）を算出する。当該濃度を表２に示す。 In Step B, the treatment amount of the combustible material to be treated (W), the moisture content of the combustible material to be treated before treatment (H), the molecular weight of the flammable volatile substance (M), the flow rate for drying (Q) and Based on the generation amount (V2) of the flammable volatile substance, the concentration (C2) of the flammable volatile substance at each temperature (t2) is calculated. The concentration is shown in Table 2.
表２の結果より、引火性揮発性物質Ｂの燃焼範囲の下限濃度０．９０容量％より低い濃度となる温度ｔ２を選択すると、１２０℃の条件が選択される。これにより、設定温度ｔ１は、ｔ１＝ｔ２（１２０℃）となる。 From the results in Table 2, when the temperature t2 at which the lower limit concentration of the flammable volatile substance B is lower than the lower limit concentration of 0.90% by volume is selected, the condition of 120 ° C. is selected. As a result, the set temperature t1 becomes t1 = t2 (120 ° C.).
ステップＣでは、乾燥装置出口での固体燃料の含水率を測定し、限界含水率と比較する。仮に、測定された当該含水率が１０質量％であり、また、１２０℃の乾燥用流体で処理した際の固体燃料の限界含水率が５質量％であった場合には、ステップＢで設定された温度ｔ１＝１２０℃は変更されない。また、限界含水率の方より製造された固体燃料の含水率が低い場合には、限界含水率を実現する温度に温度ｔ１を再設定する。 In Step C, the moisture content of the solid fuel at the outlet of the drying apparatus is measured and compared with the limit moisture content. If the measured moisture content is 10% by mass and the limit moisture content of the solid fuel when treated with a drying fluid at 120 ° C. is 5% by mass, it is set in Step B. The temperature t1 = 120 ° C. is not changed. Further, when the water content of the solid fuel produced is lower than the limit water content, the temperature t1 is reset to a temperature that achieves the limit water content.
図１のフロー図に示された各ステップＡ〜Ｃにより、乾燥用流体の温度（ｔ１）を設定することにより、処理対象可燃物の乾燥中に処理対象可燃物に引火したり、乾燥工程中に発生する引火性揮発性物質に引火したり、さらには、製造された固体燃料の火災発生を抑制することが可能となる。 By setting the temperature (t1) of the drying fluid by the steps A to C shown in the flow chart of FIG. 1, the combustible to be treated is ignited during the drying of the combustible to be treated, or the drying process is being performed. It is possible to ignite the flammable volatile substance generated in the fuel, and to suppress the fire of the produced solid fuel.
本発明により、引火性揮発性物質を含有する処理対象可燃物を、引火性の揮発性物質への引火防止と火災発生のリスクを低減しながら乾燥させると共に、製造された固体燃料がセメント焼成設備の燃費を低下させないセメント焼成用固体燃料の製造方法及び製造装置を提供することができる。 According to the present invention, a combustible material to be treated containing a flammable volatile substance is dried while preventing ignition of the flammable volatile substance and reducing the risk of fire occurrence, and the manufactured solid fuel is converted into a cement burning facility. It is possible to provide a method and apparatus for producing a solid fuel for cement firing that does not reduce the fuel consumption of the cement.
Claims (7)
Ｃ２（容量％）＝［Ｗ×（１−Ｈ／１００）×Ｖ２×１０ −６ ／Ｍ］×（２２．４／Ｑ）×１００
（上記式中、Ｗは処理対象可燃物の処理対象量（ｋｇ／時）、Ｈは処理対象可燃物の含水率（質量％）、Ｖ２は乾燥質量基準での処理対象可燃物の乾燥温度（ｔ２）における引火性揮発性物質の発生量（ｍｇ／ｋｇ）、Ｍは引火性揮発性物質の分子量（ｋｇ／ｋｍｏｌ）、Ｑは乾燥用流体の流量（ｍ ３ Ｎ／時）を示す）
により乾燥用流体中の引火性揮発性物質の濃度（Ｃ２：容量％）を演算し、前記演算した引火性揮発性物質の濃度（Ｃ２：容量％）と引火性揮発性物質の燃焼範囲の下限濃度（Ｃ：容量％）とを比較して、Ｃ２＜Ｃとなるように乾燥温度（ｔ１）を温度ｔ２と一致させる温度とするように設定することを特徴とする、セメント焼成用固体燃料の製造方法。 A drying temperature (t1) of a combustible material containing a flammable volatile substance that is at a temperature lower than the flash point of the combustible material to be treated and at which the water content of the combustible material to be treated is a critical water content. When adjusting the temperature of the drying fluid, the moisture content (% by mass) of the combustible to be treated containing flammable volatile substances and the dry mass at the temperature t2 to be changed are adjusted. Pre-measure the amount of flammable volatile substances (mg / kg) in the combustibles subject to treatment, and use the following formula:
C2 (volume%) = [W × (1-H / 100) × V2 × 10 −6 /M]×(22.4/Q)×100
(W is the amount to be treated of the combustible material to be treated (kg / hour), H is the moisture content (mass%) of the combustible material to be treated, and V2 is the drying temperature of the combustible material to be treated on a dry mass basis ( The amount of flammable volatile substances generated at t2) (mg / kg), M is the molecular weight of flammable volatile substances (kg / kmol), and Q is the flow rate of the drying fluid (m 3 N / hour))
To calculate the concentration (C2: volume%) of the flammable volatile substance in the drying fluid, and the lower limit of the calculated flammable volatile substance concentration (C2: volume%) and the combustion range of the flammable volatile substance concentration: compared to (C% by volume) and, C2 <characterized to settings which cause the temperature to match the temperature t2 of the drying temperature (t1) such that C, the cement firing solid fuel Manufacturing method.
Ｃ２（容量％）＝［Ｗ×（１−Ｈ／１００）×Ｖ２×１０ −６ ／Ｍ］×（２２．４／Ｑ）×１００
（上記式中、Ｗは処理対象可燃物の処理対象量（ｋｇ／時）、Ｈは処理対象可燃物の含水率（質量％）、Ｖ２は乾燥質量基準での処理対象可燃物の乾燥温度（ｔ２）における引火性揮発性物質の発生量（ｍｇ／ｋｇ）、Ｍは引火性揮発性物質の分子量（ｋｇ／ｋｍｏｌ）、Ｑは乾燥用流体の流量（ｍ ３ Ｎ／時）を示す）
により乾燥用流体中の引火性揮発性物質の濃度（Ｃ２：容量％）を演算し、前記演算した引火性揮発性物質の濃度（Ｃ２：容量％）と引火性揮発性物質の燃焼範囲の下限濃度（Ｃ：容量％）とを比較して、Ｃ２＜Ｃとなるように乾燥温度（ｔ１）を温度ｔ２と一致させる温度とするように調整する温度調整装置と、乾燥温度（ｔ１）に調整された乾燥用流体を導入して処理対象可燃物を乾燥させる乾燥装置とを備えることを特徴とする、セメント焼成用固体燃料の製造装置。 The temperature of the drying fluid from the cement manufacturing facility, to be processed inflammable material a lower temperature flash point and being processed combustibles water content of the critical moisture content temperature below the drying temperature (t1) As described above, the moisture content (% by mass) of the combustible material to be treated containing the flammable volatile material and the amount of flammable volatile material generated in the combustible material to be treated on the basis of the dry mass at the temperature t2 to be changed (mg / kg) in advance and the following formula:
C2 (volume%) = [W × (1-H / 100) × V2 × 10 −6 /M]×(22.4/Q)×100
(W is the amount to be treated of the combustible material to be treated (kg / hour), H is the moisture content (mass%) of the combustible material to be treated, and V2 is the drying temperature of the combustible material to be treated on a dry mass basis ( The amount of flammable volatile substances generated at t2) (mg / kg), M is the molecular weight of flammable volatile substances (kg / kmol), and Q is the flow rate of the drying fluid (m 3 N / hour))
To calculate the concentration (C2: volume%) of the flammable volatile substance in the drying fluid, and the lower limit of the calculated flammable volatile substance concentration (C2: volume%) and the combustion range of the flammable volatile substance Compared with the concentration (C: volume%), a temperature adjusting device that adjusts the drying temperature (t1) to a temperature that matches the temperature t2 so that C2 <C, and the drying temperature (t1) is adjusted. And a drying device for drying the combustible material to be treated by introducing the dried drying fluid.
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