JPH0259423A - Control method for calcination modulus of lime - Google Patents
Control method for calcination modulus of limeInfo
- Publication number
- JPH0259423A JPH0259423A JP20925988A JP20925988A JPH0259423A JP H0259423 A JPH0259423 A JP H0259423A JP 20925988 A JP20925988 A JP 20925988A JP 20925988 A JP20925988 A JP 20925988A JP H0259423 A JPH0259423 A JP H0259423A
- Authority
- JP
- Japan
- Prior art keywords
- lime
- fuel
- calcination
- amount
- signal
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 235000008733 Citrus aurantifolia Nutrition 0.000 title claims abstract description 111
- 235000011941 Tilia x europaea Nutrition 0.000 title claims abstract description 111
- 239000004571 lime Substances 0.000 title claims abstract description 111
- 238000001354 calcination Methods 0.000 title claims abstract description 73
- 238000000034 method Methods 0.000 title description 13
- 239000000446 fuel Substances 0.000 claims abstract description 51
- 238000009993 causticizing Methods 0.000 claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 17
- 239000000126 substance Substances 0.000 claims abstract description 13
- 238000011084 recovery Methods 0.000 claims abstract description 12
- 238000004519 manufacturing process Methods 0.000 claims abstract description 9
- 239000002828 fuel tank Substances 0.000 claims abstract description 7
- 238000004364 calculation method Methods 0.000 claims description 22
- 230000001105 regulatory effect Effects 0.000 claims description 10
- 238000002485 combustion reaction Methods 0.000 claims description 3
- 238000005245 sintering Methods 0.000 claims 1
- 239000003513 alkali Substances 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract 1
- 238000010304 firing Methods 0.000 description 17
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 15
- 239000000292 calcium oxide Substances 0.000 description 10
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 10
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 8
- 230000001276 controlling effect Effects 0.000 description 7
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 235000010216 calcium carbonate Nutrition 0.000 description 4
- 229910000019 calcium carbonate Inorganic materials 0.000 description 4
- 239000010802 sludge Substances 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 3
- 238000005070 sampling Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000523 sample Substances 0.000 description 2
- 235000017550 sodium carbonate Nutrition 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 239000000538 analytical sample Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000000691 measurement method Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 229910052979 sodium sulfide Inorganic materials 0.000 description 1
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
Landscapes
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
- Paper (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は石灰焼成度の制御方法であって、さらに詳しく
はアルカリパルプ製造工程の薬品回収工程で使用する石
灰の焼成度の制御方法に関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a method for controlling the degree of calcination of lime, and more particularly, to a method for controlling the degree of calcination of lime used in the chemical recovery process of the alkaline pulp manufacturing process. It is.
アルカリパルプ製造の薬品回収工程における石灰の焼成
度の測定方法は、従来焼成された粉体１粒体混合物をサ
ンプリングし、このサンプルのＣａｂ、 ＣａＣＯ３を
測定して求められている。The degree of calcination of lime in the chemical recovery process of alkaline pulp production is conventionally determined by sampling a mixture of one granule of calcined powder and measuring the Cab and CaCO3 of this sample.
また、近年ロータリーキルンに投入されるマッドの水分
量及びロータリーキルンかう排出される排ガス中のＣＯ
濃度を測定して石灰焼成度を制御する方法が提案されて
いる（紙パルプ技術タイムス昭和５９年６月号）。In recent years, the amount of moisture in the mud fed into the rotary kiln and the amount of CO in the exhaust gas emitted from the rotary kiln have also been investigated.
A method of controlling the degree of lime calcination by measuring the concentration has been proposed (Paper and Pulp Technology Times, June 1980 issue).
従来における焼成物をサンプリングして石灰焼成度を測
定する方法ではサンプルの量が限られておりサンプル誤
差を生ずるばかりか固体のサンプルはＣａＯが偏在した
状態であるため、分析試料としては必らずしも充分では
ない。さらにその分析は熟練者であっても１時間に１回
が限度であり、またオンラインの測定方法ではないため
、十分な操業管理ができないと云う欠点がある。In the conventional method of measuring the degree of lime calcination by sampling the calcined material, the amount of sample is limited, which causes sampling errors, and solid samples contain unevenly distributed CaO, so they cannot be used as analytical samples. It's not enough either. Furthermore, even an expert can only perform the analysis once an hour, and since it is not an online measurement method, there is a drawback that sufficient operational management is not possible.
また、従来におけるロータリーキルンに投入するマッド
の水分量と、ロータリーキルンからの排ガス中のＣＯ濃
度を測定する方法は、オンラインで行われるものである
が、マッドの水分量と排ガス中のＣＯ濃度は間接的なも
ので、石灰焼成度の測定としては十分でないばがりでな
く、ロータリーキルン排ガス中のｃｏ濃度はロータリー
キルンの燃料の燃焼においても発生すること及び燃焼時
にキルンに流入する空気量の把握が難しい等の欠点があ
り、石灰焼成度を充分に制御し難い。In addition, the conventional method of measuring the moisture content of the mud fed into the rotary kiln and the CO concentration in the exhaust gas from the rotary kiln is done online, but the moisture content of the mud and the CO concentration in the exhaust gas are measured indirectly. This is not only insufficient for measuring the degree of lime calcination, but also because the CO concentration in the rotary kiln exhaust gas is also generated during the combustion of fuel in the rotary kiln, and it is difficult to grasp the amount of air flowing into the kiln during combustion. The drawback is that it is difficult to control the degree of lime calcination sufficiently.
本出願人は、先にバルブ製造の薬品回収工程オンライン
で石灰焼成度を連続的に測定できる方法を提案した（特
願昭６２−２３６４９２号。以下先行技術と云う）。The present applicant previously proposed a method for continuously measuring the degree of lime calcination in the online chemical recovery process of valve manufacturing (Japanese Patent Application No. 62-236492, hereinafter referred to as the prior art).
該先行技術に記載されている発明は、スレーカーにおけ
る苛性化率反応に供せられる石灰の量と緑液の量との割
合の２変数又は前記苛性化率と苛性化反応に供せられる
石灰の量と緑液の量との３変数から石灰焼成度を演算に
よって求めるものである。The invention described in the prior art is based on two variables: the ratio between the amount of lime to be subjected to the causticizing rate reaction in the slaker and the amount of green liquor, or the ratio between the causticizing rate and the amount of lime to be subjected to the causticizing reaction. The degree of lime calcination is determined by calculation from three variables: the amount of lime and the amount of green liquor.
前記先行技術は、オンラインに於て連続的に、かつ高い
精度で石灰焼成度を測定することができると云う効果が
ある。The above-mentioned prior art has the advantage that the degree of lime calcination can be measured continuously and with high precision online.
本発明は前記先行技術をさらに改善し、操業時の石灰焼
成度を予じめ設定した石灰焼成度の適正値と比較して石
灰焼成時の燃料を制御し、常時安定した石灰焼成度に維
持できる石灰焼成度の制御方法を提供することにある。The present invention further improves the prior art, and controls the fuel during lime calcination by comparing the lime calcination degree during operation with a preset appropriate value of the lime calcination degree, and maintains a stable lime calcination degree at all times. The object of the present invention is to provide a method for controlling the degree of lime calcination.
本発明は、アルカリパルプ製造工場の薬品回収工程にお
いて、スレーカーにおける苛性化反応に供せられる石灰
量及び緑液量並びに苛性化率の信号が演算回路に入力さ
れており、他方該演算回路には石灰焼成度の適正値が予
じめ設定されており、該演算回路で前記入力されている
石灰量、緑液量及び苛性化率の信号の値から石灰焼成度
を演算すると共に、予じめ設定されている石灰焼成度の
適正値との差を演算し、該差の信号を出力して燃料演算
回路に入力し、他方該燃料演算回路には、焼成キルンに
投入する石灰量の信号が入力され、この信号から石灰焼
成に必要な燃料量が演算されており、該演算によって求
められた燃料量が前記差の信号によって補正され、この
補正された燃料量の信号を燃料タンクの調整弁に入力し
て調整弁の開度を調整して焼成キルンに燃料を供給し、
石灰焼成度を適正値に維持する石灰焼成度の制御方法で
ある。In the chemical recovery process of an alkali pulp manufacturing factory, the signals of the amount of lime and green liquor used in the causticizing reaction in a slaker and the causticizing rate are input to an arithmetic circuit, and the arithmetic circuit is An appropriate value for the degree of lime calcination is set in advance, and the calculation circuit calculates the degree of lime calcination from the input signal values of the amount of lime, the amount of green liquor, and the causticization rate. The difference between the set lime calcination degree and the appropriate value is calculated, and a signal representing the difference is output and input to a fuel calculation circuit, and the fuel calculation circuit also receives a signal indicating the amount of lime to be fed into the calcination kiln. The amount of fuel required for lime calcination is calculated from this signal, the amount of fuel determined by the calculation is corrected by the difference signal, and the signal of the corrected amount of fuel is sent to the regulating valve of the fuel tank. input to adjust the opening of the regulating valve to supply fuel to the firing kiln,
This is a method for controlling the degree of lime calcination to maintain the degree of lime calcination at an appropriate value.
蕊に、石灰の焼成度は、焼成キルンから取出される原料
中のＣａＯの重量構成比で、下記１式で定義されるもの
である。In other words, the degree of calcination of lime is the weight composition ratio of CaO in the raw material taken out from the calcination kiln, and is defined by the following equation.
但しＡ：原料単位定量中のＣａＯ重量
Ｂ ： ＣａＣｏａ重量石灰焼成度
が高い程消和反応の効率は高くなると共に、白液セトラ
ーでのスラッジの量も減少するが、反面高い焼成度を得
るために石灰焼成のためのエネルギーコストが増加し、
両者はトレードオフの関係にあり、７５〜８０％の焼成
度が好適であると云われている。However, A: Weight of CaO in raw material unit determination B: Weight of CaCoa The higher the degree of lime calcination, the higher the efficiency of the slaked reaction and the less the amount of sludge in the white liquor settler, but on the other hand, in order to obtain a high degree of calcination. The energy cost for lime calcination increases,
There is a trade-off relationship between the two, and it is said that a firing degree of 75 to 80% is suitable.
つまり、８０％を越えるような焼成度に達したものにさ
らにこれ以上の熱エネルギーを与えても石灰焼成度はそ
れ程向上せず、過剰な燃料の使用は省エネルギーの観点
から好ましくない。In other words, even if more thermal energy is applied to lime that has reached a degree of calcination of more than 80%, the degree of lime calcination will not improve significantly, and the use of excessive fuel is not preferable from the viewpoint of energy conservation.
また、石灰焼成度の変動は、直ちに消和反応及び苛性化
反応の変動につながり、苛性化工程の大きな外乱要因と
なるため、石灰焼成度は可能な限り定値制御されること
が望ましい。Further, since fluctuations in the degree of lime calcination immediately lead to fluctuations in the slaked reaction and causticizing reaction and become a major disturbance factor in the causticizing process, it is desirable that the degree of lime calcination be controlled to a constant value as much as possible.
本発明は薬品回収工程における石灰焼成度を制御するに
当り、焼成キルンに供給する燃料を制御するものである
。The present invention controls the fuel supplied to the calcination kiln in controlling the degree of lime calcination in the chemical recovery process.
蕊に苛性化率Ｘは下記２式で定義される。The causticization rate X is defined by the following two equations.
但しＣ：単位体積当りのＮａｌの重量
Ｄ ： ＃ Ｎａ２ＣＯ３の重量薬品回収
工程は安定的に循環する工程であるから、前記２式中Ｃ
＋Ｄの量はほぼ一定の値を示すために、苛性化率ＸはＣ
の量（ＮａＯＨの重量）と高い相関関係がある。However, C: Weight of Nal per unit volume D: # Weight of Na2CO3 Since the chemical recovery process is a process of stable circulation, C in the above two equations
Since the amount of +D is approximately constant, the causticization rate X is C
There is a high correlation with the amount of NaOH (weight of NaOH).
苛性化反応は下記式、
Ｎａ２ＣＯ３＋ ＣａＯ＋ Ｈ２Ｏ−＋ ２ＮａＯＨ＋
ＣａＣＯ３に示す通りであって、焼成度の高い石灰を
投入し続けるとＣａ（ＯＨ）２の量が増加し、前記反応
式の正反応が進み、従って苛性化率が高くなる。The causticization reaction is expressed by the following formula, Na2CO3+ CaO+ H2O-+ 2NaOH+
As shown in CaCO3, if lime with a high degree of calcination is continued to be added, the amount of Ca(OH)2 will increase, the forward reaction of the above reaction formula will proceed, and the causticization rate will therefore increase.
しかし、一定の苛性化率にコントロールする場合には、
焼成度の高い石灰の投入量を減らし、反応に供せられる
石灰の量と緑液の量との比率を減少させることによって
反応に供せられる酸化カルシウムの量と緑液の量とを一
定に保つようにすればよい。However, when controlling the causticization rate to a certain level,
By reducing the input amount of highly calcined lime and decreasing the ratio between the amount of lime and the amount of green liquor used for the reaction, the amount of calcium oxide and the amount of green liquor used for the reaction are kept constant. Just try to keep it.
即ち、苛性化率制御を行っている苛性化工程にあっては
、石灰焼成度と苛性化率の相関は正であり、石灰の量と
緑液の量との比率との相関は負であるので、これらの変
数から石灰焼成度を演算することができる。That is, in the causticizing process where the causticizing rate is controlled, the correlation between the degree of lime calcination and the causticizing rate is positive, and the correlation between the ratio between the amount of lime and the amount of green liquor is negative. Therefore, the degree of lime calcination can be calculated from these variables.
また、苛性化率Ｘは、ＮａＯＨが水中で高い導電率を示
すため、（２）式中のＣの量（ＮａＯＨの重量）は電導
度肝で測定できる。Further, since NaOH exhibits high conductivity in water, the amount of C (weight of NaOH) in formula (2) can be measured by the degree of conductivity.
他方、スレーカーにおいて苛性化反応に供せられる石灰
の量は、ゲージミル、コンベアスケール等を用いて直接
にその重量を求めることもできるが、この場合スクリュ
ーフィーダー等によって石灰をスレーカーに投入する場
合には、該スクリューフィーダーの回転数と石灰の重量
との相関関係を利用し、スクリューフィーダーの回転数
をパラメーターとして石灰の重量を求めることができる
。On the other hand, the amount of lime to be subjected to the causticizing reaction in the slaker can be determined by its weight directly using a gauge mill, conveyor scale, etc.; By using the correlation between the rotation speed of the screw feeder and the weight of lime, the weight of lime can be determined using the rotation speed of the screw feeder as a parameter.
また緑液の量は超音波流量計又は電磁流量計などの公知
の体積流量計により測定可能である。この場合、重量に
換算した値を求めるためには比重の値が必要になるが、
スレーカーに送られる緑液は通常は比重制御されており
、体積流量は重量（質量流量）に比例するのでこれら公
知の体積流量計の指示値をそのまままた緑液の量として
使用することができる。尚、前記超音波流量計又は電磁
流量計による測定はオンラインで測定することができる
。Further, the amount of green liquor can be measured using a known volumetric flowmeter such as an ultrasonic flowmeter or an electromagnetic flowmeter. In this case, the value of specific gravity is required to calculate the value converted to weight,
The specific gravity of the green liquor sent to the slaker is usually controlled, and the volumetric flow rate is proportional to the weight (mass flow rate), so the readings of these known volumetric flowmeters can be used as they are as the amount of green liquor. Note that the measurement using the ultrasonic flowmeter or electromagnetic flowmeter can be performed online.
上に述べた方法により測定された石灰の量及び緑液の量
は、各々独立の変数として石灰焼成度を演算するための
演算式に用いることができるが、その場合には、苛性化
液の苛性化率が緑液の処理量に依存しない変数であるの
に対し、石灰の量及び緑液の量はマクロ的にみればパル
プ生産量に比例的に依存する変景であり、１〜３回／日
変動することがある。たんに緑液の処理量変更を行ない
、これに応じて石灰の量を変えた場合にも同じ比率で変
らないと、石灰焼成度の演算値に影響を与えてしまう。The amount of lime and the amount of green liquor measured by the method described above can be used as independent variables in the formula for calculating the degree of lime calcination. While the causticization rate is a variable that does not depend on the amount of green liquor processed, the amount of lime and the amount of green liquor are variables that depend proportionally on the pulp production amount from a macroscopic perspective. Times/day may vary. Even if the amount of green liquor processed is simply changed and the amount of lime is changed accordingly, unless the ratio remains the same, the calculated value of the degree of lime calcination will be affected.
従って、石灰の量と緑液の量は両者の比率とし、緑液の
処理量に依存し、ない変量として用いることにより緑液
の処理量変更の影響を除去して用いることが好ましい。Therefore, it is preferable to use the amount of lime and the amount of green liquor as a ratio between the two, and to use them as variables that are independent of and depend on the amount of green liquor treated, thereby eliminating the influence of changes in the amount of green liquor treated.
この石灰の量と緑液の量との比率としては、重量比を用
いてもよいが、上記したような重量と比例関係を持つ回
転数や体積流量の間の比率の値を用いてもよい。As the ratio between the amount of lime and the amount of green liquor, a weight ratio may be used, but it is also possible to use a value of the ratio between the rotation speed and volumetric flow rate, which have a proportional relationship with weight as described above. .
また、前記の６値は何れも電気信号への変換が容易であ
る。Furthermore, all of the six values mentioned above can be easily converted into electrical signals.
本発明は、前述の手段によって得られた苛性化率と石灰
の量及び緑液の量（この場合石灰の量と緑液の量は両者
の比としてもよい）の値を演算回路で石灰焼成度を演算
する。In the present invention, the values of the causticization rate, the amount of lime, and the amount of green liquor (in this case, the amount of lime and the amount of green liquor may be a ratio of the two) obtained by the above-mentioned means are used in a calculation circuit to perform lime calcination. Calculate degrees.
前記演算回路には予じめ石灰焼成度の適正値が設定され
ており、前記の如く入力された苛性化率並びに石灰の量
と緑液の量又は石灰の量と緑液の量との割合の値の信号
から石灰焼成度を演算し、この演算によって求められた
石灰焼成度と、予じめ設定されている石灰焼成度の適正
値とを比較して差を求め、この差の信号を燃料演算回路
に出力する。An appropriate value for the degree of lime calcination is set in advance in the arithmetic circuit, and the causticization rate and the ratio between the amount of lime and the amount of green liquor or the amount of lime and the amount of green liquor are input as described above. Calculate the degree of lime calcination from the value signal of Output to fuel calculation circuit.
他方、燃料演算回路には、焼成キルンに投入する石灰の
量の信号が入力され、この石灰焼成に必要な燃料の量が
演算によって求められ、この燃料の量の信号が燃料タン
クの調整弁に入力され、該調整弁の開度を調整して燃料
を焼成キルンに供給しているが、この燃料の量が前記差
の信号によって燃料調整弁の開度を修正し、適正な石灰
焼成度の維持に必要な燃料の量に補正する。On the other hand, a signal indicating the amount of lime to be fed into the firing kiln is input to the fuel calculation circuit, the amount of fuel necessary for firing this lime is determined by calculation, and this signal of the amount of fuel is sent to the regulating valve of the fuel tank. The amount of fuel is input and the opening degree of the regulating valve is adjusted to supply fuel to the firing kiln. Correct the amount of fuel required for maintenance.
尚、一般的には焼成キルンで得らｈた石灰は、−旦石灰
ビンに貯蔵された後順次スレーカーに供給されている。Incidentally, lime obtained in a firing kiln is generally stored in a lime bin and then sequentially supplied to a slaker.
かかる場合薬品回収工程オンラインで測定される苛性化
率並びに石灰の量及び緑液の量から得られる石灰焼成度
と、その時点で焼成キルンで焼成されている石灰とでは
、石灰ビンでの貯留に伴う無駄時間に起因する側御上の
・・ンテイングが発生する。In such a case, the causticization rate measured in the chemical recovery process online, the degree of lime calcination obtained from the amount of lime and the amount of green liquor, and the lime being burned in the kiln at that time, the amount of lime stored in the lime bin is Due to the wasted time that comes with this, there is a risk of side-monitoring.
そのため、本発明では前記無駄時間補償が可能なコント
ローラーとして、演算機能を有する調節計やマイクロコ
ンピュータ−等を用いることが好ましい。或いはこの場
合分散計数システム内の演算機能を用いることもできる
。Therefore, in the present invention, it is preferable to use a controller, a microcomputer, or the like having an arithmetic function as the controller capable of compensating for the dead time. Alternatively, calculation functions within the distributed counting system can also be used in this case.
さらに本発明では焼成キルンに投入する石灰量（即ち焼
成キルンの負荷）が変更された場合石灰投入址の変更に
よって石灰焼成度が変動するおそれがあるが、本発明で
は焼成キルンに投入する石灰の焼成に必要な燃料の量が
演算によって求められているため、燃成キルンの負荷が
変更された場合これに必要な燃料の量が燃料演算回路で
直ちに演算できるため、焼成キルンの負荷の変更に起因
する石灰焼成度の変動は殆んどなく、従って焼成キルン
の負荷の変更に関係なく適正な石灰焼成度に制御できる
。Furthermore, in the present invention, if the amount of lime charged into the firing kiln (i.e., the load of the firing kiln) is changed, the degree of lime calcination may change due to a change in the lime charging site. Since the amount of fuel required for firing is determined by calculation, if the load of the firing kiln changes, the amount of fuel required for this can be immediately calculated by the fuel calculation circuit, so it is easy to calculate the amount of fuel required for changing the load of the firing kiln. There is almost no variation in the degree of lime calcination due to this, and therefore the degree of lime calcination can be controlled to an appropriate degree regardless of changes in the load of the firing kiln.
〔実 施 例〕
図面は本発明の一実施例を示したものであるが、つぎに
図面を参照して本願発明を具体的に説明する。薬品回収
工程は搾成キルン１で焼成された石灰がスレーカー２に
送られ温水を作用させてＣａＯを消和してＣａ（ＯＨ）
２に転化した後、デシルバー（図示省略）からスレーカ
ー２に送られてくる緑液中のＮａ、２ＣＯ３と下記式の
如く反応させてＮａＯＨ＆ ＣａＣＯ３とを得る。[Embodiment] The drawings show one embodiment of the present invention. Next, the present invention will be specifically explained with reference to the drawings. In the chemical recovery process, the lime calcined in the squeezing kiln 1 is sent to the slaker 2, where hot water is applied to slake the CaO and turn it into Ca(OH).
After conversion to 2, Na and 2CO3 in the green liquor sent from DeSilver (not shown) to the slaker 2 are reacted as shown in the following formula to obtain NaOH & CaCO3.
Ｎａ２ＣＯｓ＋ ＣａＯ＋ Ｈ□０→２ＮａＯＨ＋ Ｃ
ａＣＯ３蕊で得られた苛性化液は、１００″Ｃを超える
白濁液で、これを順次苛性化タンク３，４及びセトラー
５等を経て静澄化され、セトラー５の上澄液であるＮａ
ＯＨ及びＮａ２Ｓの混合溶液（これを白液と云う）を回
収しタンク６に貯蔵する。Na2COs+ CaO+ H□0→2NaOH+ C
The causticizing liquid obtained in the aCO3 tank is a white cloudy liquid with a temperature exceeding 100"C, which is sequentially passed through causticizing tanks 3 and 4 and a settler 5, etc., and then clarified.
A mixed solution of OH and Na2S (referred to as white liquor) is collected and stored in tank 6.
他方、ＣａＣＯ３はセトラー５で沈降してスラッジとし
て分離され、スラッジフィルター７で濃縮、脱水された
後、焼成キルン１にフィードバックし、該焼成キルン１
で数百度乃至チエ百度で焼成してＣａＯに変性し、この
ＣａＯは再びスレーカー２に供給され循環して使用され
ている。On the other hand, CaCO3 settles in the settler 5 and is separated as sludge, is concentrated and dehydrated in the sludge filter 7, and then fed back to the firing kiln 1.
It is calcined at a temperature of several hundred degrees to 100 degrees to change into CaO, and this CaO is again supplied to the slaker 2 for circulation and use.
本発明はスレーカー２に供給されるＣａＯ及びデシルバ
ー（図示省略）から供給される緑液の各号の信号８及び
９を夫々マイクロコンピュータ−１０に入力すると共に
、タンク６の苛性化率の値の信号１１がマイクロコンピ
ュータ−１０に入力されている。尚、苛性化率はタンク
６に限定するものではなく、タンク３〜５で測定しても
よい。The present invention inputs each signal 8 and 9 of CaO supplied to the slaker 2 and green liquor supplied from DeSilver (not shown) to the microcomputer 10, and also inputs the values of the causticization rate of the tank 6. A signal 11 is input to the microcomputer 10. Incidentally, the causticization rate is not limited to tank 6, and may be measured in tanks 3 to 5.
マタ、マイクロコンピュータ−１０には、予じめ適正な
石灰焼成度の値１２が設定されており（以下適正値とい
う）、該マイクロコンピュータ−１０では前記入力され
ている石灰の量の信号８、緑液の量の信号９及び苛性化
率の信号とから石灰焼成度を演算すると共に、該演算に
よって求められた石灰焼成度と、石灰焼成度の適正値１
２との差を求め、該差の信号１３を出力し、この信号１
３を燃料演算回路１４へ入力する。In the microcomputer 10, an appropriate lime calcination degree value 12 is set in advance (hereinafter referred to as an appropriate value), and in the microcomputer 10, the input lime amount signal 8, The degree of lime calcination is calculated from the signal 9 of the amount of green liquor and the signal of the causticization rate, and the degree of lime calcination obtained by the calculation and the appropriate value 1 of the degree of lime calcination are calculated.
2 and outputs the signal 13 of the difference, and this signal 1
3 is input to the fuel calculation circuit 14.
燃料演算回路１４には、焼成キルン１に投入する石灰量
の信号１８が入力されると共に、該石灰の焼成に必要な
燃料の量が予じめ演算され、さらに前記差の信号１３か
ら燃料の量を補正し、この燃料の量の信号１５が燃料タ
ンク１６の調整弁１７に入力して調整弁１７の開度を調
整し、焼成キルン１に燃料を供給する。A signal 18 representing the amount of lime to be fed into the kiln 1 is input to the fuel calculation circuit 14, and the amount of fuel required for firing the lime is calculated in advance, and the amount of fuel is calculated from the difference signal 13. The amount of fuel is corrected, and a signal 15 indicating the amount of fuel is input to the regulating valve 17 of the fuel tank 16 to adjust the opening degree of the regulating valve 17, thereby supplying fuel to the firing kiln 1.
また、焼成キルン１の負荷が変更されたときは、石灰の
量の信号１８が燃料演算回路１４に入力し、該石灰の量
に必要な燃料の量を演算するため、焼成キルン１の負荷
の変更による石灰焼成度の影響を防止できる。Further, when the load of the firing kiln 1 is changed, the lime amount signal 18 is input to the fuel calculation circuit 14, and the amount of fuel required for the amount of lime is calculated. It is possible to prevent the influence of lime calcination degree due to changes.
尚、マイクロコンピュータ−１０は焼成された石灰が石
灰ビン１９に貯蔵されている無駄時間を予じめ求め、無
駄時間を補償しているため、無駄時間に起因する制御上
のハンティングが防止できる。Note that the microcomputer 10 determines in advance the wasted time during which calcined lime is stored in the lime bin 19 and compensates for the wasted time, so that control hunting caused by the wasted time can be prevented.
即ち、本発明はマイクロコンピュータ−１０に予じめ設
定されている石灰焼成度の適正値１２とオンラインで得
られた値から演算によって求められた石灰焼成度とを比
較し、その差に相当する燃料の量を求めて燃焼する燃料
を制御し、石灰焼成度を適正値に維持するものであるか
ら、石灰焼成度の変動は極めて小さく、また焼成キルン
で燃焼する燃料の量が規正できるため、従来の如き過剰
な燃料を使用しないため省エネルギーに資することがで
きる。That is, the present invention compares the appropriate value 12 of the degree of lime calcination preset in the microcomputer 10 with the degree of lime calcination calculated by calculation from the value obtained online, and calculates the value corresponding to the difference. Since the amount of fuel is determined and the fuel to be burned is controlled to maintain the degree of lime calcination at an appropriate value, fluctuations in the degree of lime calcination are extremely small, and the amount of fuel burned in the kiln can be regulated. Since excessive fuel is not used as in the conventional method, it can contribute to energy saving.
また、従来石灰焼成度が１日に１回管理値（適正値）を
外れる場合があり、そのため苛性化工程の変動をひき起
していたが、本発明では管理値を外れる頻度が１／１０
以下に減少しており、その間焼成度の変更又はオペレー
ターの手動操作による自動制御への介入は皆無である。In addition, conventionally, the degree of lime calcination may deviate from the control value (appropriate value) once a day, causing fluctuations in the causticizing process, but with the present invention, the frequency of deviation from the control value is reduced to 1/10.
During this period, there is no need to change the degree of firing or intervene in automatic control by manual operation by the operator.
その結果、石灰焼成度の標準偏差は、従来の５．０％程
度であったものが約２．５％と半減しており、工程の安
定化に寄与しているのが認められる。As a result, the standard deviation of the degree of lime calcination has been halved from the conventional 5.0% to approximately 2.5%, which is recognized to have contributed to the stabilization of the process.
以上の如く本発明はアルカリパルプ製造時の薬品回収工
程オンラインで石灰焼成度を求め、これを予じめ設定し
た石灰焼成度の適正値と比較し、その差から焼成キルン
の燃料を調整して石灰焼成度を適正値に維持できるから
、薬品口取工程における苛性化反応、消和反応の変動が
なく安定した操業が達成できる。As described above, the present invention determines the degree of lime calcination online in the chemical recovery process during alkali pulp production, compares this with a preset appropriate value for the degree of lime calcination, and adjusts the fuel for the calcination kiln based on the difference. Since the degree of lime calcination can be maintained at an appropriate value, stable operation can be achieved without fluctuations in the causticizing reaction and slaked reaction in the chemical extraction process.
また、焼成キルンの負荷に応じて必要とする燃料を制御
できるため、焼成キルンの負荷変更に伴なう石灰焼成度
の変動も防止できると共に、焼成キルンに供給する燃料
を常に適正な４゜
量に調整できるため過剰の燃料を使用しないため省エネ
ルギーに資することができるという効果もある。In addition, since the required fuel can be controlled according to the load of the kiln, it is possible to prevent fluctuations in the degree of lime calcination due to changes in the load of the kiln, and to ensure that the amount of fuel supplied to the kiln is always at an appropriate amount. It also has the effect of contributing to energy conservation because it can be adjusted to avoid using excess fuel.
図面は本発明の一実施例の説明図である。
１：焼成キルン、２：スレーカー、３，４゜６：タンク
、５：セトラ−７：スラッジフィルター、８ 、９ 、
１１．１３．１５．１８：信号、１０：マイクロコンピ
ュータ−，１２：適正（Ｌｉ４：燃料演算回路、１６：
燃料タンク、１７：調整弁、１９：石灰ビン。The drawings are explanatory diagrams of one embodiment of the present invention. 1: Baking kiln, 2: Slaker, 3,4゜6: Tank, 5: Settler - 7: Sludge filter, 8, 9,
11.13.15.18: Signal, 10: Microcomputer, 12: Proper (Li4: Fuel calculation circuit, 16:
Fuel tank, 17: Regulating valve, 19: Lime bottle.
Claims (1)
ーカーにおける苛性化反応に供せられる石灰の量及び緑
液の量並びに苛性化率の信号が演算回路に入力されてお
り、他方該演算回路には石灰焼成度の適正値が予じめ設
定されており、該演算回路で前記入力されている石灰の
量、緑液の量及び苛性化率の信号の値から石灰焼成度を
演算すると共に、予じめ設定されている石灰焼成度の適
正値との差を演算し、該差の信号を出力して燃料演算回
路に入力し、他方該燃料演算回路には、燃成キルンに投
入する石灰量の信号が入力され、この信号から石灰焼成
に必要な燃料の量が演算されており、該演算によって求
められた燃料の量が、前記差の信号によって補正され、
この補正された燃料の量の信号を燃料タンクの調整弁に
入力して調整弁の開度を調整して焼成キルンに燃料を供
給し、石灰焼成度を適正値に維持することを特徴とする
石灰焼成度の制御方法。In the chemical recovery process of an alkaline pulp manufacturing factory, signals of the amount of lime and green liquor used in the causticizing reaction in the slaker and the causticizing rate are input to an arithmetic circuit. An appropriate value for the degree of calcination is set in advance, and the calculation circuit calculates the degree of lime calcination from the input signal values of the amount of lime, the amount of green liquor, and the causticization rate. The difference between the set lime calcination degree and the appropriate value is calculated, and a signal representing the difference is output and input to the fuel calculation circuit, and the fuel calculation circuit also receives a signal indicating the amount of lime to be fed into the combustion kiln. is input, the amount of fuel required for lime calcination is calculated from this signal, and the amount of fuel determined by the calculation is corrected by the signal of the difference,
This corrected fuel amount signal is input to the regulating valve of the fuel tank and the opening degree of the regulating valve is adjusted to supply fuel to the sintering kiln and maintain the degree of lime calcination at an appropriate value. How to control the degree of lime calcination.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP20925988A JPH0647461B2 (en) | 1988-08-23 | 1988-08-23 | Control method of calcination degree of lime |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP20925988A JPH0647461B2 (en) | 1988-08-23 | 1988-08-23 | Control method of calcination degree of lime |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0259423A true JPH0259423A (en) | 1990-02-28 |
| JPH0647461B2 JPH0647461B2 (en) | 1994-06-22 |
Family
ID=16569990
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP20925988A Expired - Lifetime JPH0647461B2 (en) | 1988-08-23 | 1988-08-23 | Control method of calcination degree of lime |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0647461B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04119186A (en) * | 1990-09-03 | 1992-04-20 | Sumitomo Heavy Ind Ltd | Method for controlling operation of caustification process |
-
1988
- 1988-08-23 JP JP20925988A patent/JPH0647461B2/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04119186A (en) * | 1990-09-03 | 1992-04-20 | Sumitomo Heavy Ind Ltd | Method for controlling operation of caustification process |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0647461B2 (en) | 1994-06-22 |
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