CN113072978A - Method for controlling reaction temperature of pulverized coal gasification furnace by using heat load - Google Patents
Method for controlling reaction temperature of pulverized coal gasification furnace by using heat load Download PDFInfo
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- CN113072978A CN113072978A CN202110430838.4A CN202110430838A CN113072978A CN 113072978 A CN113072978 A CN 113072978A CN 202110430838 A CN202110430838 A CN 202110430838A CN 113072978 A CN113072978 A CN 113072978A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/723—Controlling or regulating the gasification process
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/74—Construction of shells or jackets
- C10J3/76—Water jackets; Steam boiler-jackets
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
Abstract
The invention relates to the technical field of gasification furnaces, in particular to a method for controlling the reaction temperature of a pulverized coal gasification furnace by using a thermal load. A method for controlling a reaction temperature of a pulverized coal gasifier by a heat load, the method comprising the steps of: firstly, using a pulverized coal gasification furnace, then measuring various data, finally calculating the steam production heat of the gasification furnace, the pollution discharge heat of the gasification furnace and the heat value of E1309 in turn according to a formula, and then calculating the heat load of the gasification furnace. The invention can compensate the changes of the boiler feed water temperature and the working condition of the oxygen preheater, and the heat load of the gasification furnace uses the other two variables, thereby being more beneficial to the operation of the gasification furnace, being capable of truly reflecting the operation state of the gasification furnace, being capable of guiding the operation according to the heat load even if the boiler feed water temperature fluctuates or the working condition of the oxygen preheater fluctuates, and for the running factory, an operator needs to be used to control the reaction temperature of the gasification furnace according to the indication of the heat load, thereby being capable of ensuring the safer and more stable operation of the system.
Description
Technical Field
The invention relates to a method for controlling the reaction temperature of a pulverized coal gasification furnace, in particular to a method for controlling the reaction temperature of the pulverized coal gasification furnace by using heat load, belonging to the technical field of gasification furnaces.
Background
The gasification process of the pulverized coal is carried out under the conditions of high temperature of 1600 ℃ and pressurization of 41bar, the pulverized coal, oxygen and a small amount of steam flow into the gasification furnace in parallel under the pressurization condition, and a series of physical and chemical processes such as temperature rise, volatile component removal, cracking, combustion, conversion and the like are completed in a very short time. Because the temperature in the gasifier is very high, carbon, volatile matters and partial reaction products (H2, CO and the like) are mainly subjected to combustion reaction in the presence of oxygen; after the oxygen is depleted, various carbon conversion reactions occur, i.e., the process enters a gasification reaction stage, and finally, a gas mainly composed of CO and H2 is formed and leaves the gasifier. The control of the reaction temperature in the gasification hearth is vital to the safe and stable operation of the gasification furnace, the water-cooled wall of the reaction chamber loses the protection of a slag layer due to overhigh temperature control, a refractory lining and pins are damaged, and the water-cooled wall is burnt out even if the heat load is overlarge. If the reaction temperature is too low, the slag fluidity is poor, bottom cone slag blockage is easily formed, stopping is caused, the cleaning is very difficult, and the longer production time is delayed.
At present, because high-temperature, gas, solid and liquid multi-state turbulent flow materials exist in a hearth, the environment is very severe, a pulverized coal gasification furnace is not provided with a detection instrument directly used for measuring the reaction temperature, and an operator generally carries out comprehensive judgment according to factors such as the oxygen-carbon ratio of input materials, the yield of reaction steam, the appearance of slag, the composition ratio of synthesis gas and the like so as to control the temperature of gasification reaction. Because the lag time of gasifier steam production with changes in gasification reaction temperature is minimal, controlling gasifier reaction temperature based on gasifier steam production is being adopted by more and more gasifier users. However, the steam yield is affected by various factors such as the change of the feed water temperature of the boiler, the change of the oxygen load and the like, and the temperature of the hearth of the gasification furnace cannot be accurately judged in time.
Disclosure of Invention
The present invention is directed to solving the above problems by providing a method for controlling the reaction temperature of a pulverized coal gasification furnace using a thermal load.
The invention achieves the aim through the following technical scheme, and a method for controlling the reaction temperature of a pulverized coal gasification furnace by using heat load comprises the following steps:
s1, heating the pulverized coal gasification furnace for a period of time by using the pulverized coal gasification furnace until the thicknesses of a fixed slag layer and a flowing slag layer on the water-cooled wall reach dynamic balance;
s2, calculating the heat of the steam generated by the gasification furnace, measuring the mass flow of the steam generated by the gasification furnace and the feed water temperature of the gasification furnace by using corresponding instruments, and substituting the measured data into a formula 1 to obtain the heat value of the steam generated by the gasification furnace:
s3, calculating the heat of the gasification furnace blowdown, measuring the mass flow and the temperature of the sewage discharged by the gasification furnace by using a corresponding instrument, and calculating the heat of the gasification furnace blowdown according to a formula 2;
s4, calculating the calorific value of E1309, measuring the mass flow of oxygen contacting with the oxygen of the oxygen preheater E1309, the temperatures of oxygen at the inlet and the outlet of the oxygen preheater E1309 and the mass flow of the total steam quantity of the gasification furnace by using corresponding instruments, and calculating the calorific value of the oxygen heated by the oxygen preheater E1309 according to a formula 3;
s5, calculating the heat load of the gasification furnace according to a formula 4: and (3) calculating the thermal load of the gasification furnace, namely the calorific value of steam produced by the gasification furnace, the calorific value of pollution discharge and the calorific value of E1309.
Preferably, the normal temperature of the gasification reaction of the gasification furnace in the S1 is controlled to be 1500-1600 ℃.
Preferably, in S2, before calculating the heat value of the steam generated by the gasification furnace, the enthalpy table is consulted to obtain the enthalpy values of the steam and the feed water of the gasification furnace.
Preferably, formula 1 in S2 is: the steam-generating heat value of the gasification furnace is equal to the mass flow rate of the steam generated by the gasification furnace (steam enthalpy value-feed water enthalpy value).
Preferably, in S3, before calculating the calorific value of the gasifier blowdown, the enthalpy value of the gasifier blowdown needs to be obtained by referring to the corresponding enthalpy value table.
Preferably, formula 2 in S3 is: the gasification furnace blowdown calorific value is equal to the gasification furnace blowdown mass flow rate (blowdown enthalpy value-feed water enthalpy value) x 1/3.
Preferably, in S4, the calorific value of E1309 is equal to the mass flow rate of oxygen × specific heat capacity of oxygen (E1309 outlet oxygen temperature-E1309 inlet oxygen temperature) × (mass flow rate of steam generated by the gasification furnace/total steam amount).
Preferably, the gasifier heat load in S7 is the total heat conducted from the gasifier hearth to the water wall.
The invention has the beneficial effects that: the heat load of the gasification furnace adopted by the invention is the same as the steam yield, the working condition of the gasification furnace can be quickly reflected, the heat load of the gasification furnace can compensate the changes of the boiler feed water temperature and the working condition of the oxygen preheater, and the heat load of the gasification furnace uses the other two variables, so that the gasification furnace is more beneficial to the operation of the gasification furnace, the operation state of the gasification furnace can be really reflected, the operation can still be guided according to the heat load even if the boiler feed water temperature fluctuates or the working condition of the oxygen preheater fluctuates, and for a running factory, an operator needs to be used to control the reaction temperature of the gasification furnace according to the indication of the heat load, so that the system can be ensured.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without inventive exercise.
FIG. 1 is a schematic diagram of the process steps of the present invention;
FIG. 2 is a schematic view of the gasifier thermal load of the present invention;
FIG. 3 is a heat balance flow diagram of a gasifier according to the present invention.
Detailed Description
In order to make the objects, features and advantages of the present invention more obvious and understandable, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the embodiments described below are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The first embodiment is as follows:
referring to fig. 1 to 3, a method for controlling a reaction temperature of a pulverized coal gasification furnace by using a heat load includes the steps of:
s1, heating the pulverized coal gasification furnace for a period of time by using the pulverized coal gasification furnace until the thicknesses of a fixed slag layer and a flowing slag layer on the water-cooled wall reach dynamic balance;
s2, calculating the heat of the steam generated by the gasification furnace, measuring the mass flow of the steam generated by the gasification furnace and the feed water temperature of the gasification furnace by using corresponding instruments, and substituting the measured data into a formula 1 to obtain the heat value of the steam generated by the gasification furnace:
s3, calculating the heat of the gasification furnace blowdown, measuring the mass flow and the temperature of the sewage discharged by the gasification furnace by using a corresponding instrument, and calculating the heat of the gasification furnace blowdown according to a formula 2;
s4, calculating the calorific value of E1309, measuring the mass flow of oxygen contacting with the oxygen of the oxygen preheater E1309, the temperatures of oxygen at the inlet and the outlet of the oxygen preheater E1309 and the mass flow of the total steam quantity of the gasification furnace by using corresponding instruments, and calculating the calorific value of the oxygen heated by the oxygen preheater E1309 according to a formula 3;
s5, calculating the heat load of the gasification furnace according to a formula 4: and (3) calculating the thermal load of the gasification furnace, namely the calorific value of steam produced by the gasification furnace, the calorific value of pollution discharge and the calorific value of E1309.
Specifically, the normal temperature of the gasification reaction of the gasification furnace in S1 is controlled to be 1500-1600 ℃.
Specifically, in S2, before calculating the steam generation heat value of the gasification furnace, the enthalpy value table needs to be consulted to obtain the enthalpy values of the steam and the feed water of the gasification furnace.
Specifically, formula 1 in S2 is: the steam-generating heat value of the gasification furnace is equal to the mass flow rate of the steam generated by the gasification furnace (steam enthalpy value-feed water enthalpy value).
Specifically, in S3, before calculating the calorific value of the gasifier blowdown, a corresponding enthalpy table needs to be consulted to obtain the enthalpy value of the gasifier blowdown.
Specifically, formula 2 in S3 is: the gasification furnace blowdown calorific value is equal to the gasification furnace blowdown mass flow rate (blowdown enthalpy value-feed water enthalpy value) x 1/3.
Specifically, in S4, the calorific value of E1309 is equal to the mass flow rate of oxygen × the specific heat capacity of oxygen (E1309 outlet oxygen temperature-E1309 inlet oxygen temperature) × (mass flow rate of steam generated by the gasification furnace/total steam amount).
Specifically, the gasifier heat load in S7 is the total heat conducted from the gasifier hearth to the water wall.
Example two:
referring to fig. 1 to 3, a method for controlling a reaction temperature of a pulverized coal gasification furnace by using a heat load includes the steps of:
s1, heating the pulverized coal gasification furnace for a period of time by using the pulverized coal gasification furnace until the thicknesses of a fixed slag layer and a flowing slag layer on the water-cooled wall reach dynamic balance;
s2, calculating the heat of the steam generated by the gasification furnace, measuring the mass flow of the steam generated by the gasification furnace and the feed water temperature of the gasification furnace by using corresponding instruments, and substituting the measured data into a formula 1 to obtain the heat value of the steam generated by the gasification furnace:
s3, calculating the heat of the gasification furnace blowdown, measuring the mass flow and the temperature of the sewage discharged by the gasification furnace by using a corresponding instrument, and calculating the heat of the gasification furnace blowdown according to a formula 2;
s4, calculating the calorific value of E1309, measuring the mass flow of oxygen contacting with the oxygen of the oxygen preheater E1309, the temperatures of oxygen at the inlet and the outlet of the oxygen preheater E1309 and the mass flow of the total steam quantity of the gasification furnace by using corresponding instruments, and calculating the calorific value of the oxygen heated by the oxygen preheater E1309 according to a formula 3;
s5, calculating the heat load of the gasification furnace according to a formula 4: and (3) calculating the thermal load of the gasification furnace, namely the calorific value of steam produced by the gasification furnace, the calorific value of pollution discharge and the calorific value of E1309.
A simplified method of calculating the thermal load of a gasifier is as follows: q gasifier produces steam + Q blowdown + QE1309 ═ Q gasifier
By simplifying the blowdown, drum pressure and oxygen preheater inlet temperature (15 ℃ considerations), the calculation formula for the gasifier heat load can be simplified as:
q gasifier produces steam + Q blowdown + QE1309 ═ Q gasifier
Q gasification furnace for producing steam
Steam production in M gasifier, 13FI-0153(2788.7kJ/kg-H feed water, 13TI-0040)
Q blowdown-M blowdown (H blowdown-H feedwater) x (1/3) -105 kW
QE-1309,. M oxygen, 13 FI-0903X 0.9784kJ/kg X (TE1309, export, 13 TI-0005-15 ℃). times.M gasifier steam production, 13FI-0153/M total steam quantity, 13FI-0044
Wherein Q is heat, H: enthalpy, M: mass flow, T: temperature, CP: heat capacity;
in conclusion, the Q gasifier can produce steam 13FI-0153(2788.7kJ/kg-H feed water, 13TI-0040) +105kW + M gas, 13FI-0903 × 0.9784kJ/kg × (TE-1309, outlet, 13 TI-0005-15 ℃) multiplied by M gasifier, the total steam quantity of 13FI-0153/M and 13FI-0044, and 13FI-0153 is considered for the steam yield 13FI-0047 of the gasifier on the spot with the steam pocket bidirectional flowmeter.
The gasifier heat load is calculated from the material/heat balance at the drum cell end, and the steam production is measured directly by the meter. The gasifier heat load uses some other parameters 13TI-000513FI-0903 for calculating oxygen preheater heat load, drum pressure, discharge capacity, oxygen preheater inlet temperature, etc. parameters can be considered as constants because they have little (< 1%) influence on the gasifier heat load, and the drum steam yield is greatly influenced by the boiler feed water temperature and the oxygen preheater heat load, and the true gasifier operating condition can be more indicated by considering the boiler feed water temperature, the oxygen preheater heat load, discharge capacity, and the gasifier heat load, as shown in the following table:
TABLE 1 comparison of gasifier Heat load and steam production as a function of different parameters
It can be seen from the comparison table of the gasifier heat load and steam production as a function of different parameters: 1. the changes of the boiler feed water temperature and the heat load of the oxygen preheater have no influence on the heat load of the gasification furnace; 2. the steam yield 13FI0047 is greatly influenced by the change of the temperature of the boiler feed water, if the temperature of the boiler feed water is reduced from 190 ℃ to 150 ℃, the steam yield can be reduced by 8 percent, and the indication of the heat load of the gasifier is kept unchanged (the operation state of the gasifier is not changed); 3. the steam production 13FI0047 is greatly influenced by the change of the total oxygen load of the gasifier, if the oxygen load is reduced by 50%, the steam production can be increased by 12%, and the indication of the heat load of the gasifier is kept unchanged (the operation state of the gasifier is not changed); 4. the drum pressure has an impact on both heat load and steam production. Under the steady state of the operation state of the gasification furnace, the change of the thermal load of the gasification furnace is small.
It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments, and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.
The above-mentioned embodiments are only used for illustrating the technical solutions of the present invention, and not for limiting the same; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (8)
1. A method for controlling the reaction temperature of a pulverized coal gasification furnace by using heat load is characterized in that: the method comprises the following steps:
s1, heating the pulverized coal gasification furnace for a period of time by using the pulverized coal gasification furnace until the thicknesses of a fixed slag layer and a flowing slag layer on the water-cooled wall reach dynamic balance;
s2, calculating the heat of the steam generated by the gasification furnace, measuring the mass flow of the steam generated by the gasification furnace and the feed water temperature of the gasification furnace by using corresponding instruments, and substituting the measured data into a formula 1 to obtain the heat value of the steam generated by the gasification furnace:
s3, calculating the heat of the gasification furnace blowdown, measuring the mass flow and the temperature of the sewage discharged by the gasification furnace by using a corresponding instrument, and calculating the heat of the gasification furnace blowdown according to a formula 2;
s4, calculating the calorific value of E1309, measuring the mass flow of oxygen contacting with the oxygen of the oxygen preheater E1309, the temperatures of oxygen at the inlet and the outlet of the oxygen preheater E1309 and the mass flow of the total steam quantity of the gasification furnace by using corresponding instruments, and calculating the calorific value of the oxygen heated by the oxygen preheater E1309 according to a formula 3;
s5, calculating the heat load of the gasification furnace according to a formula 4: and (3) calculating the thermal load of the gasification furnace, namely the calorific value of steam produced by the gasification furnace, the calorific value of pollution discharge and the calorific value of E1309.
2. The method of claim 1, wherein the method comprises the following steps: and the normal temperature of the gasification reaction of the gasification furnace in the S1 is controlled to be 1500-1600 ℃.
3. The method of claim 1, wherein the method comprises the following steps: in S2, before calculating the steam heat value of the gasification furnace, the enthalpy value table is consulted to obtain the enthalpy values of the steam and the feed water of the gasification furnace.
4. The method of claim 1, wherein the method comprises the following steps: in S2, formula 1 is: the steam-generating heat value of the gasification furnace is equal to the mass flow rate of the steam generated by the gasification furnace (steam enthalpy value-feed water enthalpy value).
5. The method of claim 1, wherein the method comprises the following steps: in the step S3, before calculating the calorific value of the gasifier blowdown, a corresponding enthalpy table needs to be consulted to obtain the enthalpy value of the gasifier blowdown.
6. The method of claim 1, wherein the method comprises the following steps: in S3, formula 2 is: the gasification furnace blowdown calorific value is equal to the gasification furnace blowdown mass flow rate (blowdown enthalpy value-feed water enthalpy value) x 1/3.
7. The method of claim 1, wherein the method comprises the following steps: in S4, the calorific value of E1309 is equal to the mass flow rate of oxygen × the specific heat capacity of oxygen (E1309 outlet oxygen temperature-E1309 inlet oxygen temperature) × (mass flow rate of steam production/total steam quantity of the gasification furnace).
8. The method of claim 1, wherein the method comprises the following steps: the gasifier heat load in the S7 refers to the total heat conducted from the gasifier hearth to the water-cooled wall.
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2021
- 2021-04-21 CN CN202110430838.4A patent/CN113072978A/en active Pending
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| EP0273656B1 (en) * | 1986-12-30 | 1990-11-07 | G.G.C. Inc | Pyrolysis and combustion apparatus |
| CN101486928A (en) * | 2009-02-18 | 2009-07-22 | 刘宏建 | Temperature control method for fixed bed gasification furnace oxidation zone and gasification furnace |
| CN105018718A (en) * | 2014-04-24 | 2015-11-04 | 宝山钢铁股份有限公司 | Heating furnace process furnace temperature control method based on thermal load distribution |
| US10571195B2 (en) * | 2016-03-31 | 2020-02-25 | Mitsubishi Heavy Industries, Ltd. | Furnace monitoring device and gasification unit provided with same |
| KR20190034813A (en) * | 2017-09-25 | 2019-04-03 | 한국서부발전 주식회사 | Integrated Coal Gasification Heat Duty Auto Control System |
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| 李亚东等: "壳牌气化炉热负荷用于控制反应温度的论析", 《化肥设计》 * |
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