JP2000303079A - System for monitoring operation of gasifier - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a system for controlling the operation of a gasifier wherein the gasifier can be maintained in the optimal state by instantaneously grasping the reaction state in the gasifier and quantitatively and reasonably controlling the amount of the feedstock supplied, the amount of oxygen supplied, and the amount of steam supplied. SOLUTION: Provided is a system for monitoring the operation of a gasifier 1 provided with a feedstock supply section 2, an oxygen supply section, and a steam supply section, which system consists of a first means 11 for determining an elementary analysis value per unit weight of coal being the feedstock; a second means 12 for determining the composition of the formed gas; a third means for determining an index representing the utilization rate of oxygen in the gasifier according to the data determined by the means 11 and 12; a fourth means 14 for determining the amount of decomposed steam, representing the decomposition or formation of steam in the gasifier; and fifth means 15 for determining the future progress of the reaction in the gasifier and for controlling the operating conditions in the sections 2, 3 and 4 according to the determined progress.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a gasification furnace operation monitoring system for controlling the operation of a raw material supply section, an oxygen supply section and a steam supply section so that the state of the gasification furnace can be maintained optimally.

[0002]

2. Description of the Related Art Conventionally, the operation of a gasifier is performed based on the measurement results of temperature, pressure, and differential pressure in or around the furnace, and the measurement results such as generated gas amount, composition, and calorific value. The operating conditions (raw material supply amount, oxygen supply amount, steam supply amount) have been adjusted. Up to now, priority has been given to ensuring stable operation of the furnace, and maintaining the engineered steady state of the gasifier has been emphasized.

[0003] However, recognition of the importance of maintaining the global environment today has led to the aim of improving the thermal efficiency of gasifiers. Improving thermal efficiency requires engineering energy conservation efforts as well as chemical adjustments to optimize the reaction conditions in the gasifier.

Heretofore, the chemical state in the gasifier has been estimated by analyzing the composition of the generated gas, the amount of generated gas, the calorific value, and the like. However, these measurements fluctuate considerably during operation. Many causes of the fluctuations are assumed, and their mutual relationships are also inferred in various ways.
The outline of the situation inside the furnace has been determined using the time average of the measured values.

However, in the recent pressurized spouted bed gasification method and the like, the residence time of the raw material and the gasifying agent such as O ₂ and H ₂ O in the furnace has been reduced to several seconds. Therefore, the operation control according to the reaction situation is delayed.

[0006]

SUMMARY OF THE INVENTION The present invention solves the above-mentioned problems of the prior art, immediately grasps the reaction state in the gasification furnace, and quantitatively determines the raw material supply amount, oxygen supply amount and water vapor supply amount. An object of the present invention is to provide a gasification furnace operation control system that can adjust the rational ratio and maintain the state of the gasification furnace optimally.

[0007]

Means for Solving the Problems The inventors of the present invention have conducted intensive studies to solve the above problems, and as a result, have completed the present invention. That is, according to the present invention, there is provided a gasification furnace operation monitoring system including a raw material supply unit, an oxygen supply unit, and a steam supply unit, wherein a first elemental analysis value per unit amount of coal as a raw material is obtained. Means, a second means for obtaining a product gas composition, and a third means for obtaining an index value indicating an oxygen utilization rate in the gasification reaction based on the data obtained by the first means and the second means. A fourth means for obtaining a steam decomposition amount indicating the decomposition or generation of steam in the gasification reaction based on the data obtained by the first means and the second means; and A fifth means for obtaining the trend of the reaction in the gasification furnace based on the data obtained by the means of the fourth means, and controlling the operations of the raw material supply part, the oxygen supply part and the steam supply part accordingly. Characterized gasifier operation monitoring system provided That.

[0008]

Embodiments of the present invention will be described below in detail. FIG. 1 is a block diagram showing a configuration example of a gasification furnace operation system according to the present invention. In the figure, reference numeral 1 denotes a gasification furnace, which includes a raw material supply unit 2, an oxygen supply unit 3, and a steam supply unit 4. Numeral 11 denotes an elemental analysis value calculation means (first element) for obtaining an elemental analysis value per unit amount of 1 mol of coal as a raw material.
Means, 12 is a product gas composition calculation means (second means) for obtaining the product gas composition, and 13 is an index value indicating the utilization rate of oxygen in the gasification reaction based on the data obtained by the means of 11 and 12. Index value calculating means (third means) to be obtained;
Reference numeral 14 denotes a steam decomposition amount calculating means (fourth means) for obtaining a steam decomposition amount indicating the decomposition or generation of steam in the gasification reaction based on the data obtained by the means 11 and 12.
5 is a control means (fifth type) for obtaining the trend of the reaction in the gasification furnace based on the data obtained by the means of 13 and 14, and for controlling the operations of the raw material supply unit, the oxygen supply unit and the steam supply unit accordingly. Means).

First, the principle of the present system will be described. The present system is based on an elemental analysis value of coal and data on a product gas composition, and from an ideal partial oxidation reaction C + (1/2) O ₂ → CO, How much gasification reaction is on the combustion reaction side (oxygen excess side), CO + (１ ／) O ₂ → CO ₂ H ₂ + (１ ／) O ₂ → H ₂ O or water gasification reaction side ( An index value indicating whether C + H ₂ O → CO + H _{2 has} progressed on the oxygen-deficient side (hereinafter also referred to as oxygen excess).
And the amount of steam decomposition, which indicates the decomposition or generation of steam in the gasification reaction, are calculated by a uniquely derived theoretical formula, and the obtained data is analyzed according to a unique theory. Reaction and shift reaction The trend of CO + H ₂ O → CO + H ₂ is grasped in real time, and the raw material supply amount, oxygen supply amount and steam supply amount are appropriately controlled so that the state of the gasification furnace can be maintained optimally.

First, a theoretical formula used for control of the present system will be described. The gasification reaction is represented by the following general formula. During _{CH m O n + αO 2 +} βH 2 O → γCO + δH 2 + εCO 2 + ζH 2 O + ηCH 4 (1) above formula, _CH m _{O n} represents coal 1 mol of gasified, alpha, beta respectively feedstock per mole Shows the amount of oxygen and water vapor supplied to. Γ to η are the amounts of each generated gas per mole of the raw material. The element balance of (1) is as follows: C: 1 = α + ε + η (2) H: m + 2β = 2δ + 2ζ + 4η (3) O: n + 2α + β = γ + 2ε + ζ (4) By subtracting equation (2) from equation (4), the following is obtained. (N-1) + 2α + β = ε + ζ−η By modifying this equation, the following equation is obtained. α-0.5 (1-n) = Δ = 0.5 {ε-η- (β-ζ)} (5) theoretical amount of oxygen when generating CO 1 mol starting material _CH m _{O n} 1 mole 0.5 (1-n) mol. Therefore, △, which is the difference between the supplied oxygen amount and the theoretical oxygen amount, is an index value indicating the utilization rate of oxygen in gasification. Also, (β-
ζ) indicates the amount of steam decomposition. (5) Rewriting the formula gives C
The amount of O ₂ generated can be expressed by equation (6). ε = (β−ζ) + 2Δ + η (6) By substituting ε in equation (6) into equation (2), the amount of generated CO is expressed by equation (7). γ = 1− (β−ζ) −2Δ−2η (7) The H ₂ generation amount is expressed by Expression (8) by modifying Expression (3). δ = 0.5 m + (β−ζ) −2η (8) From the equations (6), (7), (8) and η, the generated gas amount is expressed by the following equation. γ + δ + ε + η = 1 + 0.5 m + (β−ζ) −2η (9) Here, the concentrations of CO ₂ and CO ₂ in the generated gas are represented by X, respectively.
And Y, the following relational expression is obtained. CO ₂ : ε / (γ + δ + ε + η) = X = {(β−ζ) + 2Δ + n} / {1 + 0.5m + (β−ζ) −2η} (10) CO: γ / (γ + δ + ε + η) = Y = ｛1− ( β-ζ) -2Δ-2η｝ / ｛1 + 0.5m + (β-ζ) -2η｝ (11) From the equations (10) and (11), the excess oxygen amount △ and the steam decomposition amount (β-ζ) The value can be expressed by the following equation using the CO ₂ concentration X, the CO concentration Y, and the conversion rate η to methane. Δ = 0.5 (1 + 0.5m−3η) − (1-X) (1−η) / (X + Y) (12) (β−ζ) = (1−η) / (X + Y) − (1 + 0.5m) −2η) (13) When the CH ₂ concentration is Z, η is expressed as η = Z / (X + Y + Z).

[0011] か ら calculated from the CO ₂ concentration and the CO concentration is x
Assuming that (β-ζ) calculated in the same way is the y-axis, the points on the graph theoretically follow the locus shown in FIG. 2 according to the gasification reaction path. When the excess oxygen amount 正 is positive and carbon or carbon monoxide is selectively consumed in the above-described combustion reaction, the trajectory goes rightward on the △ axis. When H ₂ is selectively combusted, because it generates water vapor in proportion to the excess oxygen content, steam cracking the amount is negative, the trajectory along a straight line the slope -2 runs in the lower right direction. When the excess oxygen amount becomes negative,
Since unreacted carbon reacts with water vapor, its trajectory is inclined
Follow the straight line 2 and go up left. Since the shift reaction is not directly related to a series of partial oxidation reactions, its trajectory is directed upward along the (β-ζ) axis. That is, the outline of the reaction path in which the change in the composition of the generated gas has occurred is shown in (12).
It can be analyzed semi-quantitatively by the equation, the equation (13) and the △-(β-ζ) diagram.

In FIG. 1, elemental analysis value calculating means 11
Determines the elemental analysis value per mole of the raw material. The product gas composition calculation means 12 calculates the product gas composition. The index value calculating means 13 receives the data from the means 11 and 12, and obtains an index value according to the above-mentioned theoretical formula. The steam decomposition amount calculating means 14 receives the data from the means 11 and 12, and calculates the steam decomposition amount according to the above-mentioned theoretical formula. The control means 15 plots the excess oxygen amount and the amount of water vapor decomposition calculated by the means 13 and 14 on a graph centered on each axis with time, analyzes the trajectory according to the theory described above, and performs the control based on the result. Can be done.

FIG. 3 shows the result of applying the theory of the present invention to the operation result of oxygen-blown spouted bed gasification. From the elemental analysis value of the raw material, the theoretical oxygen amount for producing 1 mol of CO from 1 mol of the raw material is 0.431 (mol / mol (coal)). In this operation, since 0.45 to 0.51 mol of oxygen was supplied, 0.02 to 0.08 mol / mol
It is expected that the gasification reaction will proceed by swinging to the (coal) combustion side. However, in the operation result of FIG.
Since 0.157 mol / mol (coal) of excess oxygen was consumed, it can be seen from FIG. 3 that in this operation, unreacted carbon was generated while supplying more than the theoretical amount of oxygen. In fact, this operation resulted in significant unreacted carbon being recovered. In FIG. 3, the case where the amount of steam decomposition (β- 増 減) increases / decreases almost perpendicularly to the △ axis is recognized. This is presumed to be due to the shift reaction, and it is presumed that a shift reaction is likely to occur when the oxygen supply rate or the like is changed.

FIG. 4 shows the result when an almost ideal amount of oxygen was supplied to a furnace of the same type. In this case, too, the excess oxygen amount is a positive value of 0.052 to 0.082 on the gas composition,
It can be seen that the reaction proceeded on the combustion side. In this case, when the excess oxygen amount decreases, the amount of steam decomposition increases, and the ratio has a linear relationship of -2. Therefore, it is considered that the water gasification reaction has occurred. Conversely, when the excess oxygen amount increases, the generation of water vapor occurs, and the relationship is along a straight line with a slope of −2. Therefore, it is determined that the selective combustion of H ₂ has occurred when the oxygen amount becomes excessive.

The features of the present invention are as follows. 1) Since the trend of the reaction in the gasification furnace is analyzed based on the universal theory, it can be widely applied regardless of the gasification method.
In order to operate the gasifier at the highest thermal efficiency, it is necessary to adjust the coal feed rate and the supply rates of oxygen and steam to optimize the combination of chemical reactions occurring in the gasifier. 2. Description of the Related Art Conventionally, it is common practice to empirically analyze measurement results such as temperature, pressure, gas generation amount, and the like shown during operation of a specific plant to establish an operation method unique to that plant. However, such a method cannot be applied to different plants and processes. The gasification reaction was analyzed using the equilibrium constant and rate of the reaction between carbon and the gasifying agent or product gas in order to understand the operation of the gasifier chemically. These are generally performed as a part of the performance analysis of the gasifier after the end of the operation, and the progress of the reaction in the gasifier during the operation is rarely analyzed dynamically. One of the reasons is that in the analysis of the conventional gasification reaction, the theory was constructed based on the feedstock.
That is, (1) when considering the overall reaction equation of such gasification as formula, CH _m O _n is to take the feed 1 mol been customary. In order to clarify the reaction process per mole of the raw material, it is essential to analyze the raw material supply amount. In recent spouted bed gasification, the gasification temperature is high and the residence time of the raw material in the furnace is several seconds. It is almost impossible to stabilize the supply rate in several seconds with the current dry feed system for raw materials, and fluctuations in raw material supply are inevitable, and gasification reactions are likely to continue to change mainly due to this fluctuation. .
Analyzing the resulting change in gas composition along the gasification reaction equation per mole of feedstock was inconsistent in principle and often resulted in confusion in interpretation of the results.
The present invention performs an analysis based on the theory of the reaction per mole of the reacted material instead of the amount of the feed material. Therefore, the reaction caused by the fluctuation of the supply amount of the raw material can be handled without theoretical confusion, and a highly reliable analysis can be performed even when the generated gas composition changes over time. In addition, since any process or approximation of numerical values is not used at all in the derivation process of the theory, the theoretical formula holds universally for the general gasification phenomenon represented by the formula (1). Can be widely used.

2) The excess amount of oxygen and the amount of decomposition of steam, which indicate the utilization of oxygen and steam in the gasifying agent, can be displayed simultaneously with the analysis result of the concentration of the produced gas. The product gas composition is important information for knowing the reaction state in the gasification furnace, but the progress of the gasification reaction cannot be grasped only by the absolute value of the concentration of each gas. It is necessary to perform some analysis to clarify the reaction process that led to the gas analysis values. Regarding the generation and decomposition of CO, H ₂ , CO ₂ , H ₂ O, and CH ₄ , which are typical product gases, more than 10 elementary reactions are assumed. It is necessary to analyze the element balance relationship between the feed amount of the raw material or gasifying agent and the yield of the product, and it is not easy to obtain the necessary information during operation and perform the analysis. Absent. In the present invention, a new method for estimating the consumption form of oxygen and water vapor by the amount of excess oxygen and the amount of decomposition of water vapor was proposed, and a calculation formula capable of theoretically estimating the excess oxygen was derived. Since the equations have been derived excluding any arbitrary assumptions, they can generally be used for analysis of product gas composition, and the required oxygen excess and steam cracking are reliable values. In addition, since the formula consists of simple four arithmetic operations, the calculation of oxygen excess and water vapor decomposition can be achieved in a very short time, and these index values should be displayed on the instrument at the same time as the gas analysis result is displayed. And the tendency of the gasification reaction can be interpreted more quantitatively.

3) The calculation results of the excess amount of oxygen and the amount of decomposition of steam are shown on a graph every moment, and the trajectory thereof can be analyzed to dynamically analyze the time course of the reaction. Since the conventional reaction analysis has always pursued the reaction between the gasification raw material supplied to the furnace and the gasifying agent, the instantaneous state of the gasification furnace could not be clarified. Since the present invention analyzes the reaction per mole of the reacted raw material instead of the amount of the raw material, it can also theoretically handle the reaction caused by the fluctuation of the raw material supply amount. Can analyze the situation dynamically. Taking advantage of the characteristics of such dynamic analysis, in the present invention, the trajectory drawn by the excess oxygen amount and the steam decomposition amount obtained from the product gas composition is obtained and compared with the theoretically estimated trajectory to obtain the dynamic characteristics of the reaction. Analyze and display in real time. As a result, the contribution of the water gasification reaction and the shift reaction, which could not be clarified, can be clearly and quantitatively separately examined, and the supply amount of steam can be quantitatively and rationally adjusted.

[0018]

According to the present invention, since the above-mentioned configuration is employed, the following remarkable effects can be obtained as compared with the prior art. Conventionally, the operation of a coal gasifier has been monitored mainly by the values of the temperature pressure and the differential pressure of each part of the plant.
Driving is first required to be stable for a long time,
The process system was set up and the plant structure was tested. The cold gas efficiency is one numerical value that indicates the performance of the process, and is usually calculated based on the mass balance between the raw material, the gasifying agent, and the generated gas after the operation is completed. Recently, it has been recognized that the suppression of CO ₂ emission and the restriction of resources have made it important to improve the efficiency and improve the carbon conversion rate. Improvements in cold gas efficiency are limited only by engineering techniques, and require chemical treatments to optimize the configuration of numerous gasification reactions and bring carbon conversion closer to unity. But,
A method for monitoring the operation of the gasifier that does this reliably has not been established. In recent years, in a spouted bed gasification system whose development is competing, the furnace is operated at ７7 MPa and 1300 to 1600 ° C.
It is important to know the gasification temperature in order to ensure the safety of operation related to the heat resistance of furnace materials, but there are few thermometers that can measure this temperature range stably for a long time. In the gasification method, which has a good mixture of raw material and gas in the furnace and has a relatively uniform temperature distribution, a method of estimating the furnace temperature from the temperature dependence of the equilibrium concentration of methane instead of directly measuring the temperature Is used. However, a development that actively configures a high-temperature part mainly for the partial oxidation reaction and a relatively low-temperature part mainly for the thermal decomposition reaction in the gasification furnace and uses the sensible heat of the generated gas chemically. In the middle method, the temperature estimation method cannot be used because the contribution of methane generation by thermal decomposition is large and the methane concentration greatly deviates from the chemical equilibrium relationship. Therefore, a method of determining the contribution of the combustion reaction of the partial oxidation reaction section from the excess oxygen amount obtained in the present invention and estimating the temperature thereof can be an effective means. Water vapor is consumed by a water gasification reaction that reacts with carbon to produce carbon monoxide and hydrogen, and a shift reaction that reacts with carbon monoxide to produce carbon dioxide and hydrogen, and is generated by combustion of hydrogen. Since the hydrogenation gasification reaction enhances the cold gas efficiency by the endothermic reaction, the steam decomposition rate has been used as an index value for evaluating the performance and operation status of the gasification furnace. On the other hand, the shift reaction does not affect the cold gas efficiency even if the composition of the product gas is changed. Since the hydrogenation gasification reaction and the shift reaction cannot be quantitatively separated by the product gas composition alone, the steam decomposition rate could not be directly related to the cold gas efficiency.However, using the present invention, the contribution of both reactions can be roughly estimated. In addition, it is possible to easily understand the operating conditions for improving the cold gas efficiency. Water vapor, in addition to the above chemical actions,
It is often used as a cooling medium for suppressing overheating of a gasifier. In order to accurately separate the chemical action of water vapor and the function as a cooling medium and to realize the use of steam without waste, it is necessary to know the amount of chemical decomposition of water vapor.
The steam cracking rate was calculated from the average hydrogen balance, oxygen balance, and the material balance of the whole process during a certain operation period after the end of the experiment. In this method, the amount of steam decomposition can be obtained only after the end of the operation. In order to optimize the operation of the furnace, it is desirable to know the steam cracking behavior during operation and immediately adjust the operation conditions, but there is no appropriate method. For this reason, excess steam is sometimes added by overestimating the contribution of the water gasification reaction, and as a result, excessive oxygen is supplied to maintain the furnace temperature without noticing that the furnace is cooling. In some cases, the efficiency was not improved because the gasification reactivity of the raw material was low, even if the operating results deteriorated. The conventional operation monitoring technology merely outputs the raw material supply rate, oxygen / steam supply rate, product gas composition, product gas amount, and temperature / pressure of each part. The raw material supply rate, the supply rate of oxygen and steam, or the rapid rate today can be adjusted while accurately grasping in real time the usage of oxygen and the amount of steam decomposition that directly governs It is possible to make a quick and quantitative determination, avoid erroneous operations performed in the past, and ensure safe operation in an emergency.

[Brief description of the drawings]

FIG. 1 is a block diagram showing a configuration of a gasification furnace operation monitoring system according to the present invention.

FIG. 2 is a view showing a trend of a theoretical gasification reaction when Δ is taken on an x-axis and (β−ζ) is taken on a y-axis.

FIG. 3 is a diagram showing the result of applying the theory of the present invention to the operation result of oxygen-blown spouted bed gasification.

FIG. 4 is a view showing a result when an almost ideal amount of oxygen is supplied to a furnace of the same type as that of FIG. 3;

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 1 Gasifier 2 Raw material supply part 3 Oxygen supply part 4 Steam supply part 11 Elemental analysis value calculation means (first means) 12 Product gas composition calculation means (second means) 13 Index value calculation means (third means) 14) Steam decomposition amount calculation means (fourth means) 15 Control means for controlling (fifth means)

[Procedure amendment]

[Submission date] February 16, 2000 (2000.2.1
6)

[Procedure amendment 1]

[Document name to be amended] Statement

[Correction target item name] 0010

[Correction method] Change

[Correction contents]

First, a theoretical formula used for control of the present system will be described. The gasification reaction is represented by the following general formula. During _{CH m O n + αO 2 +} βH 2 O → γCO + δH 2 + εCO 2 + ζH 2 O + ηCH 4 (1) above formula, _CH m _{O n} represents coal 1 mol of gasified, alpha, beta respectively feedstock per mole Shows the amount of oxygen and water vapor supplied to. Γ to η are the amounts of each generated gas per mole of the raw material. The element balance of (1) is as follows: C: 1 = γ + ε + η (2) H: m + 2β = 2δ + 2ζ + 4η (3) O: n + 2α + β = γ + 2ε + ζ (4) By subtracting equation (2) from equation (4), the following is obtained. (N-1) + 2α + β = ε + ζ−η By modifying this equation, the following equation is obtained. α-0.5 (1-n) = Δ = 0.5 {ε-η- (β-ζ)} (5) theoretical amount of oxygen when generating CO 1 mol starting material _CH m _{O n} 1 mole 0.5 (1-n) mol. Therefore, △, which is the difference between the supplied oxygen amount and the theoretical oxygen amount, is an index value indicating the utilization rate of oxygen in gasification. Also, (β-
ζ) indicates the amount of steam decomposition. (5) Rewriting the formula gives C
The amount of O ₂ generated can be expressed by equation (6). ε = (β−ζ) + 2Δ + η (6) By substituting ε in equation (6) into equation (2), the amount of generated CO is expressed by equation (7). γ = 1− (β−ζ) −2Δ−2η (7) The H ₂ generation amount is expressed by Expression (8) by modifying Expression (3). δ = 0.5 m + (β−ζ) −2η (8) From the equations (6), (7), (8) and η, the generated gas amount is expressed by the following equation. γ + δ + ε + η = 1 + 0.5 m + (β−ζ) −2η (9) Here, the concentrations of CO ₂ and CO ₂ in the generated gas are represented by X, respectively.
And Y, the following relational expression is obtained. CO ₂ : ε / (γ + δ + ε + η) = X = {(β−ζ) + 2Δ + n} / {1 + 0.5m + (β−ζ) −2η} (10) CO: γ / (γ + δ + ε + η) = Y = ｛1− ( β-ζ) -2Δ-2η｝ / ｛1 + 0.5m + (β-ζ) -2η｝ (11) From the equations (10) and (11), the excess oxygen amount △ and the steam decomposition amount (β-ζ) The value can be expressed by the following equation using the CO ₂ concentration X, the CO concentration Y, and the conversion rate η to methane. Δ = 0.5 (1 + 0.5m−3η) − (1-X) (1−η) / (X + Y) (12) (β−ζ) = (1−η) / (X + Y) − (1 + 0.5m) −2η) (13) Here, assuming that the CH ₂ concentration is Z, η is represented by η = Z / (X + Y + Z).

Claims (1)

[Claims] 1. A gasification furnace operation monitoring system including a raw material supply unit, an oxygen supply unit, and a steam supply unit, comprising: first means for obtaining an elemental analysis value per unit amount of coal as a raw material; A second means for obtaining a product gas composition; a third means for obtaining an index value indicating an oxygen utilization rate in a gasification reaction based on the data obtained by the first means and the second means; A fourth means for obtaining a steam decomposition amount representing the decomposition or generation of steam in the gasification reaction based on the data obtained by the first means and the second means; a third means and the fourth means A fifth means for obtaining a reaction trend in the gasification furnace based on the data obtained in the step, and controlling the operations of the raw material supply unit, the oxygen supply unit and the steam supply unit in accordance with the trend. Gasification furnace operation monitoring system.