WO2022141741A1 - 一种氧化铝蒸汽产消联锁方法 - Google Patents
一种氧化铝蒸汽产消联锁方法 Download PDFInfo
- Publication number
- WO2022141741A1 WO2022141741A1 PCT/CN2021/075158 CN2021075158W WO2022141741A1 WO 2022141741 A1 WO2022141741 A1 WO 2022141741A1 CN 2021075158 W CN2021075158 W CN 2021075158W WO 2022141741 A1 WO2022141741 A1 WO 2022141741A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- steam
- boiler
- consumption
- coal
- production
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 181
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title claims abstract description 97
- 239000003245 coal Substances 0.000 claims abstract description 144
- 238000004519 manufacturing process Methods 0.000 claims abstract description 137
- 238000001704 evaporation Methods 0.000 claims abstract description 127
- 230000008020 evaporation Effects 0.000 claims abstract description 127
- 238000002309 gasification Methods 0.000 claims abstract description 92
- 238000002485 combustion reaction Methods 0.000 claims abstract description 87
- 239000000446 fuel Substances 0.000 claims abstract description 63
- 239000012452 mother liquor Substances 0.000 claims abstract description 54
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 43
- 230000023556 desulfurization Effects 0.000 claims abstract description 43
- 238000004090 dissolution Methods 0.000 claims description 122
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 101
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 56
- 239000003546 flue gas Substances 0.000 claims description 56
- 230000007423 decrease Effects 0.000 claims description 34
- 238000009826 distribution Methods 0.000 claims description 26
- 238000012937 correction Methods 0.000 claims description 24
- 230000003044 adaptive effect Effects 0.000 claims description 19
- 238000004458 analytical method Methods 0.000 claims description 12
- 238000004134 energy conservation Methods 0.000 claims description 12
- 230000005611 electricity Effects 0.000 claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 238000004364 calculation method Methods 0.000 claims description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 229910052717 sulfur Inorganic materials 0.000 claims description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 claims description 5
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 4
- 229910052782 aluminium Inorganic materials 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 238000005457 optimization Methods 0.000 claims description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
- 229910001570 bauxite Inorganic materials 0.000 claims description 3
- 230000005540 biological transmission Effects 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 239000003034 coal gas Substances 0.000 claims description 3
- 238000001514 detection method Methods 0.000 claims description 3
- 238000005243 fluidization Methods 0.000 claims description 3
- 239000008236 heating water Substances 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 238000011423 initialization method Methods 0.000 claims description 3
- 238000005259 measurement Methods 0.000 claims description 3
- 239000011593 sulfur Substances 0.000 claims description 3
- 239000007789 gas Substances 0.000 claims description 2
- 230000026676 system process Effects 0.000 claims 1
- 238000004131 Bayer process Methods 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000002699 waste material Substances 0.000 abstract description 3
- 230000002596 correlated effect Effects 0.000 abstract 1
- 238000002386 leaching Methods 0.000 abstract 1
- 238000010586 diagram Methods 0.000 description 10
- 238000013473 artificial intelligence Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000007705 chemical test Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910001388 sodium aluminate Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B35/00—Control systems for steam boilers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B35/00—Control systems for steam boilers
- F22B35/008—Control systems for two or more steam generators
Definitions
- the invention belongs to the technical field of industrial artificial intelligence of metallurgical automation, and in particular relates to a method that can realize the online association between the steam consumption of the process section and the boiler steam output, the online association between the boiler steam production and the raw fuel, and the online association between the raw fuel and the power plant, A alumina steam production and consumption interlocking method that reduces the energy consumption of Bayer process alumina production and improves the level of industrial automation.
- the production of alumina by the Bayer process includes the preparation of raw pulp, high-pressure dissolution, dilution of pressure-cooked pulp, separation and washing of red mud, decomposition of seeds, classification and washing of aluminum hydroxide, roasting of aluminum hydroxide, evaporation of mother liquor, and soda causticization. .
- the control center, centralized control department or automation department will have the data of the entire steam generation (which can go to a single boiler), as well as the steam consumption data of each process, but the data of steam generation and consumption are not available. There is no correlation at all, and there is no mutual interlocking. There is no interlock between the steam generation of the boiler and the steam consumption of the process.
- the present invention is aimed at the above problems, and provides a method that can realize the online correlation between the steam consumption of the process section and the boiler steam output, the online correlation between the boiler steam production and the raw fuel, and the online correlation between the raw fuel and the power plant, so as to reduce the production of Bayer process alumina.
- Alumina steam production and consumption interlocking method to improve the level of industrial automation.
- the alumina steam production and consumption interlocking method comprises the following steps:
- Step 1 The interlock between the steam consumption of the alumina process and the steam generation of the boiler; the steam demand of each process depends on the steam demand of each pipeline, and the steam demand of each pipeline comes from the steam online measurement at the meter end of each pipeline data; and online calibration measures are taken in all steam meter links, so that the data can meet the precise requirements;
- Step 2 through the process steam consumption of alumina pre-desilication, high-pressure dissolution, mother liquor evaporation, desulfurization and coal gasification, it can be known that the steam consumption of the alumina production process is:
- Step 3 The steam generated by the boiler is only used for alumina production, and the operation of connecting the excess steam to the steam turbine for power generation is not considered; from the perspective of energy saving and consumption reduction, the amount of steam generated by the boiler will be determined by the amount of steam consumed in the alumina production process ; However, since the steam production of the boiler cannot be completely equal to the steam consumption of the alumina production process, in order to ensure the stability and safety of the production, a margin is added to the steam production of the boiler; therefore, the interlocking of the steam production of the boiler and the steam consumption of the alumina production process The relation is:
- Step 4 The interlocking of boiler steam production and raw fuel;
- the raw fuel refers to the main water supply, primary air, secondary air, and coal combustion required for boiler steam generation.
- Composition, low calorific value of coal-fired, coal-fired consumption; interlocking of boiler steam and raw fuel includes interlocking of coal-fired and air volume, and interlocking of main feed water and main steam;
- Step 5 Interlocking of the raw fuel and the corresponding power plant; the interlocking of the raw fuel and the power plant is achieved through an adaptive process. Through the interlocking of the boiler steam production and the raw fuel in Step 4, it can be clearly obtained. In the aluminum production process, the primary air volume, secondary air volume, main feed water volume, coal consumption, and excess air coefficient required by the boiler, and the amount of various raw fuels and their corresponding power units are driven by the motor of the power unit.
- the second step is to calibrate and determine the steam consumption of pre-desilication;
- the steam used in the pre-desilication includes the steam consumption of each pipeline;
- Pre-desilication steam calibration system by which the data is accurately processed to obtain the steam consumption of the pre-desilication link;
- the pre-desilication steam calibration system is to perform on-line calibration and analysis of the steam flow for the steam table 1 of the pre-desilication pipeline 1 to the steam table M of the pre-desilication pipeline M corresponding to the pre-desilication process; the online calibration corresponding to the steam table M
- the algorithm is as follows:
- K M f M ( ⁇ P M ,T M ,P M )
- M the number of pipes for steam consumed in the pre-desilication process and the number of the M-th pipe
- T M the steam temperature corresponding to the pre-desilication pipeline M, read by the temperature transmitter;
- Q′ pre-desilication the total amount of steam consumed in the pre-desilication process
- the high-pressure dissolution is used to raise the temperature of the pulp from a low temperature to a high temperature, and to remove the impurity components in the pulp;
- the calculation method of the steam demand of the high-pressure dissolution process is similar to that of the pre-desilication process , and also processed by the vapor online calibration system corresponding to high-pressure dissolution;
- the high-pressure stripping steam online calibration system is to perform online calibration and analysis of the steam flow rate from the steam table 1 of the dissolution pipeline 1 to the steam table N of the dissolution pipeline N corresponding to the high-pressure dissolution process; the online calibration algorithm corresponding to the steam table N is as follows:
- K dissolution N f dissolution N ( ⁇ P dissolution N , T dissolution N , P dissolution N )
- N the number of pipes for steam consumed in the high-pressure dissolution process and the number of the Nth pipe
- dissolution N ( ⁇ P dissolution N , T dissolution N , P dissolution N )—the specific algorithm of the steam flow correction number of the dissolution process;
- ⁇ P Dissolution N The differential pressure value of the steam gauge corresponding to the high-pressure dissolution pipeline N, read by the differential pressure transmitter;
- T- dissolution N the steam temperature corresponding to the high-pressure dissolution pipeline N, read by the temperature transmitter;
- P Dissolution N the vapor pressure corresponding to the high-pressure dissolution pipeline N, read by the pressure transmitter;
- the steam consumption of the high pressure dissolution process is:
- Q′ dissolution the total amount of steam consumed by the high-pressure dissolution process
- step 2 the calibration of the steam consumption of mother liquor evaporation is determined; the purpose of mother liquor evaporation is to ensure the concentration in the alumina production process, so that the circulating mother liquor reaches the requirement of dissolving bauxite;
- the mother liquor online calibration system is used to calibrate the steam data;
- the mother liquor evaporation steam online calibration system is to carry out the online calibration analysis of the steam flow rate for the steam table 1 of the evaporation pipe 1 corresponding to the mother liquor evaporation process to the steam table K of the evaporation pipe K; the online calibration algorithm corresponding to the steam table K is as follows:
- K evaporation K f evaporation K ( ⁇ P evaporation K , T evaporation K , P evaporation K )
- K the number of pipelines of steam consumed in the mother liquor evaporation process and the number of the K-th pipeline
- T evaporation K the steam temperature corresponding to the mother liquor evaporation pipeline K, read by the temperature transmitter;
- P evaporation K the vapor pressure corresponding to the mother liquor evaporation pipeline K, read by the pressure transmitter
- the steam consumption of the mother liquor evaporation process is:
- the second step is to determine the steam consumption of desulfurization; since the steam consumption in the desulfurization process is very small, and most of the desulfurization is carried out intermittently, the steam meter signal in the desulfurization process is directly used to determine the desulfurization steam consumption. ;
- the steam consumption for desulfurization is as follows:
- R the number of pipelines of steam consumed in the desulfurization process and the number of the R-th pipeline
- the coal gasifier is responsible for providing coal gas for the roasting process of the alumina production process; its function is to gasify the coal through the coal gasifier and supply it to the roasting workshop, and the roasting process will Aluminum hydroxide is roasted into alumina;
- Coal gasifier steam online calibration system is to perform online calibration and analysis of steam flow for steam table 1 of gasifier pipeline 1 to steam table S of gasification pipeline S corresponding to the coal gasification process; the online calibration algorithm corresponding to steam table S as follows:
- K vaporized S f vaporized S ( ⁇ P vaporized S , T vaporized S , P vaporized S )
- S the number of pipelines for steam consumed in the coal gasification process and the number of the S pipeline
- K gasification S steam flow correction number corresponding to the online calibration gasification process
- T gasification S the steam temperature corresponding to the coal gasification pipeline S, read by the temperature transmitter;
- the steam consumption of the coal gasification process is:
- the principle of steam distribution by the steam adaptive distributor is as follows: it is necessary to ensure the operation process of the boilers. The efficiency of the boiler is within a reasonable range, and it can ensure the coordination between the boilers during operation; the number of boilers is replaced by E, and the distribution algorithm of the steam adaptive distributor is explained by taking the E boiler as an example:
- the distribution of the load coefficient of each boiler adopts the initialization method. Given an initial value of 0.75 for each boiler, the system starts to calculate. If the result meets the requirements of the above formula, the calculation ends; 0.78, &, 0.90 to calculate the above links until the requirements of the above formula are met.
- the step 4 the interlocking of coal combustion and air volume, is for the reasonable matching of coal combustion and air volume, so that the coal combustion can be fully burned; at the same time, it is necessary to satisfy the interlocking of primary air and secondary air itself according to the requirements of the circulating fluidized bed boiler. lock to achieve the optimization of the entire combustion process;
- V 0 0.0889(C ar +0.375S ar )+0.265H ar -0.0333O ar (Nm 3 /kg)
- V 0 the theoretical air volume required for complete combustion of unit fuel
- H ar the percentage of hydrogen element in the received base, %
- N ar the percentage of nitrogen element in the received base, %
- V ⁇ V 0
- V the actual amount of air required for complete combustion of unit fuel
- ⁇ excess air coefficient, which can be detected and calculated in real time by oxygen analyzer
- the coal consumption used on site can be actually detected by the coal supply system. In order to focus on the interlocking, it is not too entangled in the accuracy of the coal consumption detection device itself, and only the coal consumption detected by the coal supply system can be used; Then the total air volume required for the actual combustion of the entire boiler is:
- the air supply system of the circulating fluidized bed boiler can divide the air volume into primary air and secondary air; the primary air is mainly used for the fluidization of pulverized coal, and the secondary air is mainly used to provide oxygen; the matching relationship between the primary air and the secondary air Mainly depends on the type of burner of the circulating fluidized bed boiler;
- V primary ⁇ 1 ⁇ V total air
- V secondary ⁇ 2 ⁇ V total air
- ⁇ 2 The distribution coefficient of the secondary air of the circulating fluidized bed boiler.
- the step 4 is the interlocking of the main feed water and the main steam; since the output of the main steam depends on the consumption of the steam at the consumption end of the alumina process, the main feed water needs to be passively interlocked with the main steam, that is: the main feed water needs to be fed back with the steam. Quantitatively establish an interlocking relationship;
- the interlocking model of the main feed water and the main steam consists of two parts , which are the two parts of mass conservation and energy conservation, respectively;
- the above formula is mainly used to describe the interlocking relationship between the main feed water of the boiler and the amount of main steam produced.
- the main steam is the criterion
- the amount of the main steam must be used as the criterion to feed back to the main feed water, and then the main steam is the criterion.
- the specific supply amount of feed water is determined according to the current steam production rate; however, the steam production rate of the boiler is not fixed, it changes with the operation and load of the boiler, so energy conservation is also required to further determine the difference between the main feed water and the boiler.
- the interlock between the air volume of the primary air and the secondary air and the fan can be expressed by the following formula:
- P e wind the effective power of the primary air fan and the secondary air fan
- the air volume of the primary air is taken as the known quantity; and the total pressure of the fan is an inherent characteristic, when the fan is determined, the total pressure is determined;
- ⁇ the density of the main feed water of the boiler
- H the head of the pump corresponding to the main water supply
- the known quantity in the above formula is the flow rate of the main water supply, which can be obtained by the steam quantity and energy conservation; for the specific application site, the pump head is also determined;
- the volume of SO 2 produced by the complete combustion of unit fuel is:
- the volume of CO2 produced by the complete combustion of unit fuel is:
- V g the actual volume of flue gas produced by the complete combustion of unit fuel
- the flue gas flow is a known quantity, and the flue gas induced draft fan is determined on site, so the corresponding full pressure of the induced draft fan is also known, and the power of the induced draft fan can be adjusted according to the change of flue gas flow.
- the beneficial effects of the present invention are as follows: 1. Real-time online correlation between the steam consumption of each process and the steam generation at the boiler end can be realized, so as to achieve the purpose of reducing steam consumption. 2. Realize the online correlation between boiler steam output and main water supply, primary air volume, secondary air volume, and coal consumption, so as to improve and optimize the boiler operation efficiency and achieve the purpose of energy saving. 3. Realize online real-time correlation between the matching relationship between primary air and secondary air inside the boiler, the matching relationship between air volume and coal combustion, and the relationship between coal combustion components and complete combustion, reducing the power consumption of fans and pumps, thereby reducing oxidation per ton Aluminum comprehensive energy consumption. Moreover, through the above technical means, on the basis of energy saving and consumption reduction, the automation level and data accuracy level of the Bayer process alumina industry can be greatly improved, laying a solid foundation for the intelligence of the alumina industry.
- Figure 1 is a diagram of the current state of the alumina production process.
- Figure 2 is a block diagram of the relationship between the steam generation and consumption ends of the existing alumina plant.
- FIG. 3 is a simplified flow chart of the production and consumption end of alumina steam of the present invention.
- FIG. 4 is a schematic diagram of the steam consumption of the simplified pre-desilication process of the present invention.
- FIG. 5 is an interlocking operation diagram of alumina steam consumption and boiler steam production according to the present invention.
- FIG. 6 is an interlocking operation diagram of a plurality of boilers and a steam consuming end according to the present invention.
- FIG. 7 is a schematic diagram of the interlocking of the main steam and the main water supply of the present invention.
- FIG. 8 is a schematic diagram of the raw fuel and the corresponding power plant of the present invention.
- Fig. 9 is a logic diagram of energy saving and consumption reduction from the alumina process end to the raw fuel corresponding power plant of the present invention.
- the method adopts the interlocking of steam consumption and boiler steam output in process sections such as high-pressure dissolution, pre-desilication, mother liquor evaporation, desulfurization, boiler self-use, coal gasification, etc. in the alumina production process, the interlocking of boiler steam production and raw fuel, and the interlocking of raw fuel. Interlocking with the power unit, establishing an online production-consumption interlocking relationship for alumina production, realizing energy saving and consumption reduction in Bayer process alumina production, and improving the automation level in this field.
- the alumina steam production and consumption interlocking method includes:
- Step 1 Interlock between the steam consumption of the alumina process and the steam generation of the boiler.
- the alumina steam consumption end involved in the present invention is a general model of the alumina steam consumption end of the Bayer process. Therefore, in the method description process, all pipelines are replaced by virtual data, and it is not necessary to be entangled in the number of pipelines itself. In the subsequent description This method is adopted in all cases, and there will be no further explanation of this dummy data method.
- the present invention only relates to the steam production and consumption end, so only the steam-related process links are reserved in the method description, and the other links are simplified (as shown in FIG. 3 ).
- the steam-related process links are reserved in the method description, and the other links are simplified (as shown in FIG. 3 ).
- different letters are used to replace the virtual data to indicate the difference in the number of pipelines.
- the steam demand of each process depends on the steam demand of each pipeline, and the steam demand of each pipeline comes from the steam online measurement data of the meter end of each pipeline.
- the steam demand of each pipeline comes from the steam online measurement data of the meter end of each pipeline.
- its flow signal can be directly collected and provided to the corresponding system of the present invention. If the installation conditions of the steam meter do not meet the requirements of the meter or the algorithm does not meet the requirements of the working conditions, data accuracy processing is required.
- online calibration measures are taken in all steam meter links, so that the data can meet the precise requirements.
- Step 2 through the process steam consumption of alumina pre-desilication, high-pressure dissolution, mother liquor evaporation, desulfurization and coal gasification, it can be known that the steam consumption of the alumina production process is:
- the steam used in the pre-desilication process includes the steam consumption of pipeline 1, pipeline 2, ... and pipeline M.
- the data of each pipeline enters the pre-desilication steam calibration system through the original pressure, differential pressure, temperature and other signals, and the system performs data accuracy processing to obtain the steam consumption of the pre-desilication link.
- the connection diagram of each signal is shown in Figure 4. Because the present invention does not analyze the accuracy of data, the pressure, temperature and differential pressure are simplified and displayed in the figure by one meter in the signal access link.
- the pre-desilication steam calibration system is to perform on-line calibration and analysis of steam flow on the steam table 1 of the pre-desilication pipeline 1 to the steam table M of the pre-desilication pipeline M corresponding to the pre-desilication process.
- the online calibration algorithm corresponding to the steam meter M is as follows:
- K M f M ( ⁇ P M ,T M ,P M )
- M the number of pipes for steam consumed in the pre-desilication process and the number of the M-th pipe
- T M the steam temperature corresponding to the pre-desilication pipeline M, read by the temperature transmitter;
- Q′ pre-desilication the total amount of steam consumed in the pre-desilication process
- High-pressure dissolution is an important part of the entire Bayer alumina production process. It is mainly used to increase the temperature of the pulp from low temperature to 280°C or 290°C to remove impurities in the pulp, so as to achieve the purpose of pipeline dissolution, and finally obtain sodium aluminate. The solution was used for the next step.
- the calculation method of the steam demand of the high-pressure dissolution process is similar to that of the pre-desilication process, and it also needs to be processed by the steam online calibration system corresponding to the high-pressure dissolution process before the data can be further applied.
- the high-pressure stripping steam online calibration system is to perform online calibration and analysis of the steam flow rate from the steam table 1 of the dissolution pipeline 1 to the steam table N of the dissolution pipeline N corresponding to the high-pressure dissolution process; the online calibration algorithm corresponding to the steam table N is as follows:
- K dissolution N f dissolution N ( ⁇ P dissolution N , T dissolution N , P dissolution N )
- N the number of pipes for steam consumed in the high-pressure dissolution process and the number of the Nth pipe
- dissolution N ( ⁇ P dissolution N , T dissolution N , P dissolution N )—the specific algorithm of the steam flow correction number of the dissolution process;
- ⁇ P Dissolution N The differential pressure value of the steam gauge corresponding to the high-pressure dissolution pipeline N, read by the differential pressure transmitter;
- T- dissolution N the steam temperature corresponding to the high-pressure dissolution pipeline N, read by the temperature transmitter;
- P Dissolution N The vapor pressure corresponding to the high-pressure dissolution pipeline N, read by the pressure transmitter.
- the steam consumption of the high pressure dissolution process is:
- Q′ dissolution the total amount of steam consumed by the high-pressure dissolution process
- mother liquor evaporation The purpose of mother liquor evaporation is to ensure the concentration in the alumina production process, so that the circulating mother liquor can meet the requirements of dissolving bauxite. Applications.
- the mother liquor evaporation steam online calibration system is to carry out the online calibration analysis of the steam flow rate for the steam table 1 of the evaporation pipe 1 corresponding to the mother liquor evaporation process to the steam table K of the evaporation pipe K; the online calibration algorithm corresponding to the steam table K is as follows:
- K evaporation K f evaporation K ( ⁇ P evaporation K , T evaporation K , P evaporation K )
- K the number of pipelines of steam consumed in the mother liquor evaporation process and the number of the K-th pipeline
- T evaporation K the steam temperature corresponding to the mother liquor evaporation pipeline K, read by the temperature transmitter;
- the steam consumption of the mother liquor evaporation process is:
- R the number of pipelines of steam consumed in the desulfurization process and the number of the R-th pipeline
- the coal gasifier is responsible for providing coal gas for the roasting process of the alumina production process; its function is to gasify the coal through the coal gasifier and supply it to the roasting workshop, and the roasting process roasts the aluminum hydroxide into alumina.
- Coal gasifier steam online calibration system is to perform online calibration and analysis of steam flow for steam table 1 of gasifier pipeline 1 to steam table S of gasification pipeline S corresponding to the coal gasification process; the online calibration algorithm corresponding to steam table S as follows:
- K vaporized S f vaporized S ( ⁇ P vaporized S , T vaporized S , P vaporized S )
- S the number of pipelines for steam consumed in the coal gasification process and the number of the S pipeline
- K gasification S steam flow correction number corresponding to the online calibration gasification process
- T gasification S the steam temperature corresponding to the coal gasification pipeline S, read by the temperature transmitter;
- the steam consumption of the coal gasification process is:
- Step 3 The steam generated by the boiler is only used for alumina production, and the operation of connecting the excess steam to the steam turbine for power generation is not considered; from the perspective of energy saving and consumption reduction, the amount of steam generated by the boiler will be determined by the amount of steam consumed in the alumina production process ; However, since the steam production of the boiler cannot be completely equal to the steam consumption of the alumina production process, in order to ensure the stability and safety of the production, a margin is added to the steam production of the boiler; therefore, the interlocking of the steam production of the boiler and the steam consumption of the alumina production process The relation is:
- FIG. 6 omits the structure of the steam consumption end, and only shows the structure of the steam generation end.
- the principle of the steam self-adaptive distributor for steam distribution is: to ensure that the efficiency of the boiler during operation is within a reasonable range, but also to ensure the coordination between the boilers during operation; to replace multiple boilers with the number E, Taking the E boiler as an example to illustrate the distribution algorithm of the steam adaptive distributor:
- the distribution of the load coefficient of each boiler adopts the initialization method. Given an initial value of 0.75 for each boiler, the system starts to calculate. If the result meets the requirements of the above formula, the calculation ends; 0.78, &, 0.90 to calculate the above links until the requirements of the above formula are met.
- E-1 boilers are used to carry out the above cycle calculation process until the allocation meets the conditions of the above formula. Furthermore, the interlocking process of alumina steam consumption and steam generated by the boiler can be realized, so as to meet the real-time online interlocking matching of steam production and consumption, and reduce the large waste of steam.
- Step 4 The interlocking of boiler steam and raw fuel.
- the raw fuel in the present invention refers to the main feed water, primary air, secondary air, coal combustion, etc. required for boiler steam generation, wherein the coal combustion includes the coal type, the composition of the coal, and the low-level heat generated by the coal. value, coal consumption, etc.
- V 0 0.0889(C ar +0.375S ar )+0.265H ar -0.0333O ar (Nm 3 /kg)
- V 0 the theoretical air volume required for complete combustion of unit fuel
- H ar the percentage of hydrogen element in the received base, %
- N ar the percentage of nitrogen element in the received base, %
- V ⁇ V 0
- V the actual amount of air required for complete combustion of unit fuel
- ⁇ excess air coefficient, which can be detected and calculated in real time by oxygen analyzer.
- the coal consumption used on site can be actually detected by the coal supply system. In order to focus on the interlocking, it is not too entangled in the accuracy of the coal consumption detection device itself, and only the coal consumption detected by the coal supply system can be used; Then the total air volume required for the actual combustion of the entire boiler is:
- the air supply system of the circulating fluidized bed boiler can divide the air volume into primary air and secondary air; the primary air is mainly used for the fluidization of pulverized coal, and the secondary air is mainly used to provide oxygen; the matching relationship between the primary air and the secondary air Mainly depends on the type of burner of the circulating fluidized bed boiler;
- V primary ⁇ 1 ⁇ V total air
- V secondary ⁇ 2 ⁇ V total air
- ⁇ 1 the distribution coefficient of the primary air of the circulating fluidized bed boiler, which is related to the burner type
- Pulverized coal burners are divided into once-through burners and swirl burners.
- there are two forms of air distribution for the DC burner one is 1:1 air distribution (that is, the ratio of primary air and secondary air is equal), and the other is graded air distribution, and the air distribution should ensure that the primary air flow rate is between 20 and 20 25m/s, and the secondary air flow rate is 40-55m/s, depending on the boiler load.
- the air distribution of the swirl burner should ensure that the primary air outlet speed is 14 ⁇ 24m/s, the secondary air inner ring wind speed is 13 ⁇ 26m/s, and the outer ring wind speed is 26 ⁇ 40m/s.
- the interlocking model of the main feed water and the main steam consists of two parts , which are the two parts of mass conservation and energy conservation, respectively.
- the above formula is mainly used to describe the interlocking relationship between the main feed water of the boiler and the amount of main steam produced.
- the main steam is the criterion
- the amount of the main steam must be used as the criterion to feed back to the main feed water, and then the main steam is the criterion.
- the specific supply of water is determined according to the current steam production rate.
- the steam production rate of the boiler is not fixed, it changes with the operation and load of the boiler, so energy conservation is also required to further determine the interlock between the main feed water and the main steam.
- the above steps mainly solve the interlocking relationship between boiler coal combustion and air volume, main feed water and main steam.
- the realization of this part can achieve the optimization of the internal combustion process of the boiler and reduce the coal consumption per ton of steam.
- Step 5 Interlocking the raw fuel and the corresponding power plant.
- the raw fuel and its corresponding power device are: the main water supply water pump, the primary air corresponding to the primary fan, the secondary air corresponding to the secondary fan, the flue gas corresponding to the flue gas induced draft fan, the coal composition and the low calorific value corresponding to the coal type
- the physical and chemical tests and the amount of coal burning correspond to the coal supply system (as shown in Figure 8).
- the interlocking of the raw fuel and the power plant is achieved through the adaptive process.
- the primary air volume and secondary air volume required by the boiler in the alumina production process can be clearly obtained. Air volume, main water supply volume, coal consumption, excess air coefficient, and the amount of various raw fuels and their corresponding power units are driven by the motor of the power unit.
- P e wind the effective power of the primary air fan and the secondary air fan
- p the full pressure corresponding to the primary fan and the secondary fan.
- the air volume of the primary air is taken as the known quantity; and the total pressure of the fan is an inherent characteristic, when the fan is determined, the total pressure is determined;
- ⁇ the density of the main feed water of the boiler
- the known quantity in the above formula is the flow rate of the main water supply, which can be obtained by the steam quantity and energy conservation; for a specific application site, the pump head is determined, and the pump head is also determined.
- the volume of SO 2 produced by the complete combustion of unit fuel is:
- the volume of CO2 produced by the complete combustion of unit fuel is:
- V g the actual volume of flue gas produced by the complete combustion of unit fuel
- Q g the volume flow of flue gas in the actual combustion process.
- the flue gas flow is a known quantity, and the flue gas induced draft fan is determined on site, so the corresponding full pressure of the induced draft fan is also known, and the power of the induced draft fan can be adjusted according to the change of flue gas flow.
- the pump and fan will also have the total efficiency and the prime mover efficiency, it is necessary to consider the impact of the above two efficiencies on the entire control system.
- J 1 the economic benefit from the reduction of coal consumption per ton of steam, 10,000 yuan per ton of steam;
- D tce the price of ton of standard coal, ten thousand yuan/tce.
- the invention realizes automatic interlocking of the main water supply, air volume and coal consumption of the boiler system of the alumina plant, thereby improving the operation efficiency of the boiler water supply pump system, the primary fan system and the secondary fan system.
- the amount of steam y 3 produced per ton of alumina is saved, and the boiler system realizes automatic interlocking before and after saving electricity consumption and realizes the economy as follows:
- J feed pump - the electricity saving economy of the feed pump system, yuan/ton of alumina
- y 3 the amount of steam saved in the production of ton of alumina, ton/ton of alumina
- E pump, i the average power consumption of the feed pump corresponding to the rated load of the boiler for i hour, Yuan/hour;
- Mpump,i the main feed water volume of the feed pump i hour corresponding to the rated load of the boiler, ton/hour;
- y 3 the amount of steam saved in the production of ton of alumina, ton/ton of alumina
- M wind/s primary air volume corresponding to ton of steam, t/t;
- M primary fan, i the rated load of the boiler corresponds to the primary air volume of the primary fan i hour, ton/hour;
- y 3 the amount of steam saved in the production of ton of alumina, ton/ton of alumina
- M secondary fan, i secondary air volume of secondary fan i hour corresponding to rated load of boiler, ton/hour;
- the steam consumption per ton of alumina can be reduced by 2 tons, and the economic benefit that can be produced is calculated as:
- G Q total steam production ⁇ J 1 +10000 ⁇ A ⁇ (J 2 +J feed water pump + J primary fan + J secondary fan )
- G the annual economic benefit of an alumina plant
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Regulation And Control Of Combustion (AREA)
Abstract
一种氧化铝蒸汽产消联锁方法,解决现有氧化铝生产过程中各工序的蒸汽产生和消耗数据缺乏关联性,造成大量的蒸汽浪费,煤粉燃烧效率低,吨氧化铝生产成本高的问题。该氧化铝蒸汽产消联锁方法,通过氧化铝生产过程中高压溶出、预脱硅、母液蒸发、脱硫、锅炉自用、煤气化等工艺段蒸汽用量与锅炉蒸汽产量的联锁,锅炉产汽与原燃料的联锁,以及原燃料与动力装置的联锁,建立氧化铝生产的在线产消联锁关系,进而使锅炉燃烧过程的煤耗以及运行过程中的蒸汽需求量下降,降低拜耳法氧化铝生产的能耗,提升氧化铝生产领域的自动化水平。
Description
本发明属于冶金自动化的工业人工智能技术领域,具体涉及一种可实现工艺段蒸汽用量与锅炉蒸汽产量的在线关联、锅炉产汽与原燃料的在线关联,以及原燃料与动力装置的在线关联,降低拜耳法氧化铝生产的能耗,提升工业自动化水平的氧化铝蒸汽产消联锁方法。
目前,我国工业人工智能进程十分缓慢,重点在于两方面的原因,一是由于大量的工业基础数据缺乏精准性,导致了整个产业链无法有效地利用这些数据做联锁、预测及优化调度等;二是由于大量的工业基础数据背后缺少在能源端的关联性,导致大量数据在集控中心或者能源管理中心只是数据简单的罗列和显示,并没有对能源系统起到有效的节能降耗作用。现阶段工业数据只是用于基础的生产和环保监测,保证生产不出事故、保证环保排放达标。然而,数据之间的精准性联锁对能源系统的意义,在接下来数十年的中国工业中,将会起到巨大的作用。
拜耳法生产氧化铝有原矿浆制备、高压溶出、压煮矿浆稀释及赤泥分离和洗涤、晶种分解、氢氧化铝分级和洗涤、氢氧化铝焙烧、母液蒸发及苏打苛化等主要生产工序。在现有氧化铝生产过程中,控制中心、集控部门或自动化部门会有整个蒸汽产生的数据(可以到单台锅炉),也有每个工序消耗的蒸汽数据,但蒸汽产生和消耗的数据没有丝毫关联性,也不存在相互联锁。锅炉端蒸汽产生量和工序的蒸汽消耗量没有联锁,一旦生产过程所需蒸汽量减少,例如:产量调整下降,检修过程或者故障状态时,锅炉产汽端不能及时掌握情况,会持续按照正常状态为消耗端提供蒸汽,这样就造成了大量的蒸汽浪费。
蒸汽浪费的背后,是主给水量的增加、一次风和二次风量的增加、燃煤量的增加,主给水量增加会加剧主给水的水泵电耗,一次风和二次风量的增加则会加剧对应风机的电耗,燃煤量的增加则直接增加了吨氧化铝的生产成本。另外,锅炉内部的风量和燃煤消耗也没有形成在线的关联,导致经常出现锅炉的一次风、二次风不匹配,锅炉的风量与煤耗不匹配,从而引起了煤粉燃烧不充分,煤粉燃烧效率降低等问题。故有必要对现有的氧化铝生产工艺中 蒸汽产生端和消耗端的关联方式进行改进。
发明内容
本发明就是针对上述问题,提供一种可实现工艺段蒸汽用量与锅炉蒸汽产量的在线关联、锅炉产汽与原燃料的在线关联,以及原燃料与动力装置的在线关联,降低拜耳法氧化铝生产的能耗,提升工业自动化水平的氧化铝蒸汽产消联锁方法。
本发明所采用的技术方案是:该氧化铝蒸汽产消联锁方法包括如下步骤:
步骤一、氧化铝工序蒸汽消耗与锅炉蒸汽产生的联锁;各工序的蒸汽需求量取决于各条管线的蒸汽需求量,而各管线的蒸汽需求量来源于各管线的表计端的蒸汽在线计量数据;并在所有蒸汽表环节都采取在线的校准措施,进而使数据达到精准要求;
步骤二、通过氧化铝的预脱硅、高压溶出、母液蒸发、脱硫及煤气化环节的工序蒸汽消耗量,可知氧化铝生产工艺所消耗的蒸汽量为:
Q
消耗总量=Q′
预脱硅+Q′
溶出+Q′
蒸发+Q
脱硫+Q′
气化
式中:Q
消耗总量—氧化铝工艺蒸汽消耗总量;
Q′
预脱硅—预脱硅工序所消耗的蒸汽总量;
Q′
溶出—高压溶出工序所消耗的蒸汽总量;
Q′
蒸发—母液蒸发工序所消耗的蒸汽总量;
Q
脱硫—脱硫管道所消耗的蒸汽总量;
Q′
气化—煤气化工序所消耗的蒸汽总量;
步骤三、锅炉产生的蒸汽只用于氧化铝生产,不考虑多余蒸汽用来连接汽轮机进行发电的操作;从节能降耗的角度,锅炉产生的蒸汽量将由氧化铝生产过程所消耗的蒸汽量决定;但由于锅炉产汽量不能完全等于氧化铝工序的蒸汽消耗量,为了保证生产稳定安全,对锅炉产汽量增加裕量;因此,锅炉蒸汽产生量与氧化铝生产工序蒸汽消耗量的联锁关系式为:
Q
产汽总量-Q
锅自用=α×Q
消耗总量
式中:Q
产汽总量—锅炉产生的蒸汽总量;
Q
锅自用—锅炉自身消耗的蒸汽量;
α—保证蒸汽消耗总量的安全裕量系数,取1.1~1.15;
步骤四、锅炉产汽与原燃料的联锁;原燃料指的是锅炉蒸汽产生所需要的主给水、一次风、二次风、燃煤,燃煤包含了燃煤的煤种、燃煤的成分、燃煤的低位发热值、燃煤的消耗量;锅炉产汽与原燃料的联锁包括燃煤与风量的联锁、以及主给水与主蒸汽的联锁;
步骤五、原燃料与对应动力装置的联锁;原燃料与动力装置建立的联锁是通过自适应过程实现的,通过步骤四中锅炉产汽与原燃料的联锁,已经可以明确获得在氧化铝生产过程中锅炉所需要的一次风量、二次风量、主给水量、燃煤消耗量、过量空气系数,而各种原燃料的量与其对应的动力装置是通过动力装置的电机驱动来实现的;当工艺端所需要的蒸汽量下降时,则对应锅炉的主蒸汽量会根据反馈相应下降,对应产生主蒸汽的锅炉中的风量、主给水、燃煤量也会下降;同时,风量下降会反馈给风机,风机电耗下降;主给水量下降会反馈给水泵,水泵电耗下降;煤耗下降会反馈给供煤系统,供煤系统的传输电耗下降;由于风量减少,则锅炉对应的烟气量下降,则烟气对应的引风机的电耗也随之下降。
所述步骤二、预脱硅的蒸汽消耗量的校准确定;预脱硅环节用到的蒸汽包含了各条管道的蒸汽消耗量;各管道的数据经过原始压力、差压、温度等信号进入到预脱硅蒸汽校准系统,由该系统进行数据精准性处理,以得到预脱硅环节的蒸汽消耗量;
预脱硅蒸汽校准系统是对预脱硅工序所对应的预脱硅管道1的蒸汽表1~预脱硅管道M的蒸汽表M,进行蒸汽流量的在线校准分析;蒸汽表M对应的在线校准算法如下:
Q′
预脱硅M=K
M×Q
预脱硅M
K
M=f
M(ΔP
M,T
M,P
M)
式中:M—预脱硅工序所消耗蒸汽的管道数量及第M条管道的编号;
Q′
预脱硅M—在线校准后预脱硅管道M对应的蒸汽流量;
Q
预脱硅M—在线校准前预脱硅管道M对应的蒸汽表显示的流量;
K
M—在线校准过程对应的蒸汽流量修正数;
f
M(ΔP
M,T
M,P
M)—蒸汽流量修正数的具体算法;
ΔP
M—预脱硅管道M对应的蒸汽表差压值,由差压变送器读取;
T
M—预脱硅管道M对应的蒸汽温度,由温度变送器读取;
P
M—预脱硅管道M对应的蒸汽压力,由压力变送器读取;
由于在预脱硅工序中,所有管道是平行结构,互不影响,因此,预脱硅工序的蒸汽消耗量为:
式中:Q′
预脱硅—预脱硅工序所消耗的蒸汽总量;
Q′
预脱硅i—在线校准后预脱硅第i条管道对应的蒸汽流量。
所述步骤二、高压溶出的蒸汽消耗量的校准确定;高压溶出用于将矿浆的温度从低温提升到高温,去除矿浆内杂质成分;高压溶出工序蒸汽的需求量计算方法与预脱硅工序类似,也要经过高压溶出对应的蒸汽在线校准系统处理;
高压溶出蒸汽在线校准系统是对高压溶出工序所对应的溶出管道1的蒸汽表1~溶出管道N的蒸汽表N,进行蒸汽流量的在线校准分析;蒸汽表N对应的在线校准算法如下:
Q′
溶出N=K
溶出N×Q
溶出N
K
溶出N=f
溶出N(ΔP
溶出N,T
溶出N,P
溶出N)
式中:N—高压溶出工序所消耗蒸汽的管道数量及第N条管道编号;
Q′
溶出N—在线校准后高压溶出管道N对应的蒸汽流量;
Q
溶出N—在线校准前高压溶出管道N对应的蒸汽表显示的流量;
K
溶出N—在线校准溶出过程对应的蒸汽流量修正数;
f
溶出N(ΔP
溶出N,T
溶出N,P
溶出N)—溶出工序蒸汽流量修正数的具体算法;
ΔP
溶出N—高压溶出管道N对应的蒸汽表差压值,由差压变送器读取;
T
溶出N—高压溶出管道N对应的蒸汽温度,由温度变送器读取;
P
溶出N—高压溶出管道N对应的蒸汽压力,由压力变送器读取;
高压溶出工序的蒸汽消耗量为:
式中:Q′
溶出—高压溶出工序所消耗的蒸汽总量;
Q′
溶出i—在线校准后高压溶出第i条管道对应的蒸汽流量。
所述步骤二、母液蒸发的蒸汽消耗量的校准确定;母液蒸发的目的是为了保证氧化铝生产过程中的浓度,使得循环母液达到溶出铝土矿的要求;母液蒸发工序所需的蒸汽量经过母液在线校准系统进行蒸汽数据的校准;
母液蒸发蒸汽在线校准系统是对母液蒸发工序所对应的蒸发管道1的蒸汽表1~蒸发管道K的蒸汽表K,进行蒸汽流量的在线校准分析;蒸汽表K对应的在线校准算法如下:
Q′
蒸发K=K
蒸发K×Q
蒸发K
K
蒸发K=f
蒸发K(ΔP
蒸发K,T
蒸发K,P
蒸发K)
式中:K—母液蒸发工序所消耗蒸汽的管道数量及第K条管道编号;
Q′
蒸发K—在线校准后母液蒸发管道K对应的蒸汽流量;
Q
蒸发K—在线校准前母液蒸发管道K对应的蒸汽表显示的流量;
K
蒸发K—在线校准蒸发过程对应的蒸汽流量修正数;
f
蒸发K(ΔP
蒸发K,T
蒸发K,P
蒸发K)—蒸发工序蒸汽流量修正数的具体算法;
ΔP
蒸发K—母液蒸发管道K对应的蒸汽表差压值,由差压变送器读取;
T
蒸发K—母液蒸发管道K对应的蒸汽温度,由温度变送器读取;
P
蒸发K—母液蒸发管道K对应的蒸汽压力,由压力变送器读取;
母液蒸发工序的蒸汽消耗量为:
式中:Q′
蒸发—母液蒸发工序所消耗的蒸汽总量;
Q′
蒸发i—在线校准后母液蒸发第i条管道对应的蒸汽流量。
所述步骤二、脱硫的蒸汽消耗量的确定;由于脱硫过程中的蒸汽消耗量很小,且脱硫大多数是间歇式进行,所以直接采用脱硫过程中的蒸汽表信号来确定脱硫的蒸汽消耗量;脱硫的蒸汽消耗量如下:
式中:R—脱硫工序所消耗蒸汽的管道数量及第R条管道编号;
Q
脱硫—脱硫管道所消耗的蒸汽总量;
Q
脱硫i—第i条脱硫管道对应的蒸汽表流量。
所述步骤二、煤气化炉蒸汽消耗量的校准确定;煤气化炉负责给氧化铝生产工艺环节的焙烧工序提供煤气;其作用是将煤通过煤气化炉气化,供给焙烧车间,焙烧工序将氢氧化铝焙烧成氧化铝;
煤气化炉蒸汽在线校准系统是对煤气化工序所对应的气化炉管道1的蒸汽表1~气化管道S的蒸汽表S,进行蒸汽流量的在线校准分析;蒸汽表S对应的在线校准算法如下:
Q′
气化S=K
气化S×Q
气化S
K
气化S=f
气化S(ΔP
气化S,T
气化S,P
气化S)
式中:S—煤气化工序所消耗蒸汽的管道数量及第S条管道编号;
Q′
气化S—在线校准后气化炉管道S对应的蒸汽流量;
Q
气化S—在线校准前气化炉管道S对应的蒸汽表显示的流量;
K
气化S—在线校准气化过程对应的蒸汽流量修正数;
f
气化S(ΔP
气化S,T
气化S,P
气化S)—煤气化工序蒸汽流量修正数的具体算法;
ΔP
气化S—煤气化管道S对应的蒸汽表差压值,由差压变送器读取;
T
气化S—煤气化管道S对应的蒸汽温度,由温度变送器读取;
P
气化S—煤气化管道S对应的蒸汽压力,由压力变送器读取;
煤气化工序的蒸汽消耗量为:
式中:Q′
气化—煤气化工序所消耗的蒸汽总量;
Q′
气化i—在线校准后煤气化第i条管道对应的蒸汽流量。
所述步骤三、在实际生产过程中,一般会有多台锅炉参与蒸汽的生产;在多台锅炉同时 运行的条件下,蒸汽自适应分配器进行蒸汽分配的原则为:既要保证锅炉运行过程中的效率在合理范围,又能保证在运行过程中各台锅炉之间的协同;将多台锅炉以数量E进行替代,以E锅炉为例对蒸汽自适应分配器的分配算法进行说明:
χ
1·Q
1满负荷+χ
2·Q
2满负荷+…+χ
E·Q
E满负荷=Q
产汽总量
0.75≤χ
1,χ
2,…,χ
E≤0.9
式中:Q
1满负荷—锅炉1在满负荷条件下的蒸汽产量;
Q
2满负荷—锅炉2在满负荷条件下的蒸汽产量;
Q
E满负荷—锅炉E在满负荷条件下的蒸汽产量;
χ
1—锅炉自适应分配器分配给锅炉1的负荷系数;
χ
2—锅炉自适应分配器分配给锅炉2的负荷系数;
χ
E—锅炉自适应分配器分配给锅炉E的负荷系数;
蒸汽自适应分配器分配要同时满足上式的要求;每台锅炉的实际产汽量最终可由下式进行计算:
Q
E实际产汽量=χ
E·Q
E满负荷
式中:Q
E实际产汽量—分配后锅炉E的实际蒸汽产生量;
每台锅炉负荷系数的分配采用初始化方法,给定每台锅炉一个初始值0.75,则系统开始计算,如结果满足上述公式要求,则计算结束;如不满足要求,则依次给定0.76,0.77,0.78,……,0.90进行上述环节计算,直到满足上述公式要求为止。
所述步骤四、燃煤与风量的联锁,是为了燃煤与风量匹配合理,使得燃煤燃烧充分;同时,需要根据循环流化床锅炉的要求,满足一次风、二次风本身的联锁,以达到整个燃烧过程的最优化;
1kg燃料完全燃烧所需理论空气量计算如下式所示:
V
0=0.0889(C
ar+0.375S
ar)+0.265H
ar-0.0333O
ar(Nm
3/kg)
式中:V
0—单位燃料完全燃烧所需的理论空气量;
C
ar—收到基中碳元素成分百分比,%;
S
ar—收到基中硫元素成分百分比,%;
H
ar—收到基中氢元素成分百分比,%;
O
ar—收到基中氧元素成分百分比,%;
N
ar—收到基中氮元素成分百分比,%;
M
ar—收到基中水分百分比,%;
考虑到燃烧过程中必须有过量空气以保证燃烧的顺利进行,则实际燃烧过程中所需要的风量应为:
V=αV
0
式中:V—单位燃料完全燃烧所需的实际空气量;
α—过量空气系数,通过氧量分析仪可实时检测并计算出;
现场使用的燃煤量可以通过供煤系统进行实际的检测,为了侧重联锁,不过分纠结于燃煤量检测装置本身的精度,只对供煤系统检测到的燃煤量进行使用即可;则整个锅炉实际燃烧所需要的总空气量为:
V
总空气=m×V
式中:V
总空气—锅炉实际燃烧过程所需的总空气流量;
m—对应的锅炉煤耗,通过供煤系统可实时检测;
循环流化床锅炉的供风系统可以将风量分为一次风和二次风;一次风主要用于煤粉的流化,二次风主要用于提供氧;一次风和二次风的匹配关系主要取决于循环流化床锅炉的燃烧器型式;
V
一次=κ
1·V
总空气
V
二次=κ
2·V
总空气
κ
1+κ
2=1
式中:V
一次—循环流化床锅炉一次风的风量;
V
二次—循环流化床锅炉二次风的风量;
κ
1—循环流化床锅炉一次风的分配系数;
κ
2—循环流化床锅炉二次风的分配系数。
所述步骤四、主给水与主蒸汽的联锁;由于主蒸汽的产量取决于氧化铝工艺消耗端蒸汽的用量,所以主给水需要被动与主蒸汽联锁,即:主给水需要与蒸汽反馈的量建立联锁关系;
另外,从能量守恒的角度,还要考虑到主给水变成主蒸汽所需的热量与燃煤燃烧所产生的热量之间的关系;所以,主给水与主蒸汽的联锁模型由两部分构成,分别是质量守恒和能量守恒两部分;
Q
E主给水·η
E=Q
E实际产汽量
式中:Q
E主给水—锅炉E对应的主给水流量;
η
E—锅炉E对应的产汽率;
上式主要用来描述锅炉主给水与主蒸汽产生量之间的联锁关系,但由于以主蒸汽为准,所以在实现环节一定是以主蒸汽的量为准来反馈给主给水,然后主给水依据当前的产汽率来决定具体的供应量;但锅炉的产汽率并不是固定不变的,是随着锅炉的运行和负荷在变化的,因此还需要能量守恒来进一步确定主给水与主蒸汽之间的联锁;
Q
E主给水·γ=m·q
低位-θ
式中:γ—单位质量主给水变成主蒸汽所需要的热量;
q
低位—锅炉所用燃煤的低位发热值;
θ—锅炉除加热水变成蒸汽以外的其它热损失。
所述步骤五、对于一次风、二次风的风量与风机之间的联锁,可用下式表示:
式中:P
e风—一次风风机、二次风风机的有效功率;
p—一次风机、二次风机对应的全压;
在上式中,以一次风的风量为已知量;且风机全压为固有特性,当风机确定时,全压是确定的;
对于主给水的流量与水泵之间的联锁,可用下式表示:
式中:P
e水—主给水对应水泵的有效功率;
ρ—锅炉主给水的密度;
H—主给水对应水泵的扬程;
上式中已知量为主给水的流量,可采用蒸汽量及能量守恒得到;对于具体的应用现场,水泵是确定的,则水泵的扬程也是确定的;
对于烟气系统的烟气量和引风机,首先需要根据一次风、二次风量、煤耗、过量空气系数等进行烟气的计算;单位燃料在理论所需空气量下、完全燃烧所产生的烟气量计算公式如下:
单位燃料完全燃烧生成的SO
2容积为:
单位燃料完全燃烧生成的CO
2容积为:
故可知:
理论N
2容积为:
理论水蒸气容积为:
由于循环流化床锅炉实际燃烧过程是在过量空气系数条件下进行的,此时的烟气容积除了理论烟气容积外,还增加了过量空气及过量空气中携带的水蒸气容积,实际烟气流量为:
则实际产生的烟气流量可用下式表示为:
Q
g=m·V
g
式中:V
g—单位燃料完全燃烧产生的实际烟气体积;
Q
g—实际燃烧过程中烟气的体积流量;
因此,可建立烟气流量及其对应引风机的联锁关系为:
式中:P
eg—烟气对应引风机的有效功率;
p
g—烟气对应引风机的全压;
在上述关系式中,烟气的流量为已知量,烟气引风机在现场是确定的,故引风机对应的全压也是已知,可根据烟气流量变化调整引风机的功率。
本发明的有益效果:1、可以实现各工序蒸汽用量和锅炉端蒸汽产生量的实时在线关联,达到减少蒸汽消耗量的目的。2、实现锅炉蒸汽产量与主给水量、一次风量、二次风量、燃煤消耗量的在线关联,进而使锅炉运行效率得到提升和优化,达到节能的目的。3、将锅炉内部的一次风与二次风的匹配关系、风量与燃煤的匹配关系、燃煤成分与完全燃烧的关系等实现在线实时关联,降低风机、水泵的电耗,从而降低吨氧化铝综合能耗。并且,通过上述技术手段,在节能降耗的基础上,能够大幅度提升拜耳法氧化铝行业的自动化水平和数据精准性水平,为氧化铝行业的智能化奠定坚实的基础。
图1是氧化铝生产工艺现状图。
图2是现有氧化铝厂蒸汽产生和消耗端的关系框图。
图3是本发明的简化后的氧化铝蒸汽产耗端流程图。
图4是本发明的简化后的预脱硅工序蒸汽消耗量示意图。
图5是本发明的氧化铝蒸汽消耗与锅炉蒸汽产量的联锁运行图。
图6是本发明的多台锅炉与蒸汽消耗端的联锁运行图。
图7是本发明的主蒸汽与主给水的联锁示意图。
图8是本发明的原燃料及对应的动力装置示意图。
图9是本发明的氧化铝工艺端到原燃料对应动力装置的节能降耗逻辑图。
该方法通过氧化铝生产过程中高压溶出、预脱硅、母液蒸发、脱硫、锅炉自用、煤气化等工艺段蒸汽用量与锅炉蒸汽产量的联锁,锅炉产汽与原燃料的联锁,原燃料与动力装置的联锁,建立氧化铝生产的在线产消联锁关系,实现拜耳法氧化铝生产的节能降耗,提升该领域自动化水平。
详细说明本发明的具体步骤。该氧化铝蒸汽产消联锁方法包括:
步骤一、氧化铝工序蒸汽消耗与锅炉蒸汽产生的联锁。
本发明涉及到的氧化铝蒸汽消耗端为拜耳法氧化铝蒸汽消耗端的通用模型,因此在方法描述过程中,将所有的管线以虚拟数据代替,而不必纠结于管线的条数本身,后续描述中均采用此法,不再对此虚拟数据法做过多说明。
本发明只涉及到蒸汽产耗端,故在方法描述中仅保留与蒸汽有关的工序环节,其它环节做简化处理(如图3所示)。在蒸汽消耗的各工序段中,由于每个工序的管道数量不同,所以采用虚拟数据时用不同的字母替代,以表示管道数量的不同,但由于高压溶出属于核心工序段,且高压溶出管线条数较多,所以在图中会以较多的管线条数与其它管道进行示意区分。
各工序的蒸汽需求量取决于各条管线的蒸汽需求量,而各管线的蒸汽需求量来源于各管线的表计端的蒸汽在线计量数据。对于各管线段仪表满足安装条件且流量算法准确的蒸汽表,此处可直接采集其流量信号提供给本发明对应的系统。如果蒸汽表的安装条件不满足仪表要求或算法不符合工况要求,则需进行数据精准性处理。并且,为了方法的通用性,在所有蒸汽表环节都采取在线的校准措施,进而使数据达到精准要求。
步骤二、通过氧化铝的预脱硅、高压溶出、母液蒸发、脱硫及煤气化环节的工序蒸汽消耗量,可知氧化铝生产工艺所消耗的蒸汽量为:
Q
消耗总量=Q′
预脱硅+Q′
溶出+Q′
蒸发+Q
脱硫+Q′
气化
式中:Q
消耗总量—氧化铝工艺蒸汽消耗总量;
Q′
预脱硅—预脱硅工序所消耗的蒸汽总量;
Q′
溶出—高压溶出工序所消耗的蒸汽总量;
Q′
蒸发—母液蒸发工序所消耗的蒸汽总量;
Q
脱硫—脱硫管道所消耗的蒸汽总量;
Q′
气化—煤气化工序所消耗的蒸汽总量。
(1)预脱硅的蒸汽消耗量。预脱硅环节用到的蒸汽包含了管道1、管道2、……、管道M的蒸汽消耗量。各管道的数据经过原始压力、差压、温度等信号进入到预脱硅蒸汽校准系统,由该系统进行数据精准性处理,以得到预脱硅环节的蒸汽消耗量。各信号的连接示意图如图4所示。因本发明并不是做数据精准性分析,所以在信号接入环节将压力、温度、差压采用一个仪表在图中进行简化显示。
预脱硅蒸汽校准系统是对预脱硅工序所对应的预脱硅管道1的蒸汽表1~预脱硅管道M的蒸汽表M,进行蒸汽流量的在线校准分析。蒸汽表M对应的在线校准算法如下:
Q′
预脱硅M=K
M×Q
预脱硅M
K
M=f
M(ΔP
M,T
M,P
M)
式中:M—预脱硅工序所消耗蒸汽的管道数量及第M条管道的编号;
Q′
预脱硅M—在线校准后预脱硅管道M对应的蒸汽流量;
Q
预脱硅M—在线校准前预脱硅管道M对应的蒸汽表显示的流量;
K
M—在线校准过程对应的蒸汽流量修正数;
f
M(ΔP
M,T
M,P
M)—蒸汽流量修正数的具体算法;
ΔP
M—预脱硅管道M对应的蒸汽表差压值,由差压变送器读取;
T
M—预脱硅管道M对应的蒸汽温度,由温度变送器读取;
P
M—预脱硅管道M对应的蒸汽压力,由压力变送器读取。
由于在预脱硅工序中,所有管道是平行结构,互不影响,因此,预脱硅工序的蒸汽消耗量为:
式中:Q′
预脱硅—预脱硅工序所消耗的蒸汽总量;
Q′
预脱硅i—在线校准后预脱硅第i条管道对应的蒸汽流量。
(2)高压溶出的蒸汽消耗量。高压溶出属于整个拜耳法氧化铝生产工艺的重要环节,主要用于将矿浆的温度从低温提升到280℃或290℃,去除矿浆内杂质成分,以达到管道化溶出的目的,最终得到铝酸钠溶液用于下一工序使用。
高压溶出工序蒸汽的需求量计算方法与预脱硅工序类似,也要经过高压溶出对应的蒸汽在线校准系统处理,然后才能对数据进行进一步的应用。
高压溶出蒸汽在线校准系统是对高压溶出工序所对应的溶出管道1的蒸汽表1~溶出管道N的蒸汽表N,进行蒸汽流量的在线校准分析;蒸汽表N对应的在线校准算法如下:
Q′
溶出N=K
溶出N×Q
溶出N
K
溶出N=f
溶出N(ΔP
溶出N,T
溶出N,P
溶出N)
式中:N—高压溶出工序所消耗蒸汽的管道数量及第N条管道编号;
Q′
溶出N—在线校准后高压溶出管道N对应的蒸汽流量;
Q
溶出N—在线校准前高压溶出管道N对应的蒸汽表显示的流量;
K
溶出N—在线校准溶出过程对应的蒸汽流量修正数;
f
溶出N(ΔP
溶出N,T
溶出N,P
溶出N)—溶出工序蒸汽流量修正数的具体算法;
ΔP
溶出N—高压溶出管道N对应的蒸汽表差压值,由差压变送器读取;
T
溶出N—高压溶出管道N对应的蒸汽温度,由温度变送器读取;
P
溶出N—高压溶出管道N对应的蒸汽压力,由压力变送器读取。
高压溶出工序的蒸汽消耗量为:
式中:Q′
溶出—高压溶出工序所消耗的蒸汽总量;
Q′
溶出i—在线校准后高压溶出第i条管道对应的蒸汽流量。
(3)母液蒸发的蒸汽消耗量。母液蒸发的目的是为了保证氧化铝生产过程中的浓度,使得循环母液达到溶出铝土矿的要求;母液蒸发工序所需的蒸汽量经过母液在线校准系统进行蒸汽数据的校准,然后才能参与下一步的应用。
母液蒸发蒸汽在线校准系统是对母液蒸发工序所对应的蒸发管道1的蒸汽表1~蒸发管道K的蒸汽表K,进行蒸汽流量的在线校准分析;蒸汽表K对应的在线校准算法如下:
Q′
蒸发K=K
蒸发K×Q
蒸发K
K
蒸发K=f
蒸发K(ΔP
蒸发K,T
蒸发K,P
蒸发K)
式中:K—母液蒸发工序所消耗蒸汽的管道数量及第K条管道编号;
Q′
蒸发K—在线校准后母液蒸发管道K对应的蒸汽流量;
Q
蒸发K—在线校准前母液蒸发管道K对应的蒸汽表显示的流量;
K
蒸发K—在线校准蒸发过程对应的蒸汽流量修正数;
f
蒸发K(ΔP
蒸发K,T
蒸发K,P
蒸发K)—蒸发工序蒸汽流量修正数的具体算法;
ΔP
蒸发K—母液蒸发管道K对应的蒸汽表差压值,由差压变送器读取;
T
蒸发K—母液蒸发管道K对应的蒸汽温度,由温度变送器读取;
P
蒸发K—母液蒸发管道K对应的蒸汽压力,由压力变送器读取。
母液蒸发工序的蒸汽消耗量为:
式中:Q′
蒸发—母液蒸发工序所消耗的蒸汽总量;
Q′
蒸发i—在线校准后母液蒸发第i条管道对应的蒸汽流量。
(4)脱硫的蒸汽消耗量的确定。由于脱硫过程中的蒸汽消耗量很小,且脱硫大多数是间歇式进行,一般间隔1~2天脱硫一次,每次蒸汽用量约为2t/h。因此,本发明中不再对脱硫过程进行数据在线校准处理,直接采用脱硫过程中的蒸汽表信号来确定脱硫的蒸汽消耗量;脱硫的蒸汽消耗量如下:
式中:R—脱硫工序所消耗蒸汽的管道数量及第R条管道编号;
Q
脱硫—脱硫管道所消耗的蒸汽总量;
Q
脱硫i—第i条脱硫管道对应的蒸汽表流量。
(5)煤气化炉蒸汽消耗量。煤气化炉负责给氧化铝生产工艺环节的焙烧工序提供煤气;其作用是将煤通过煤气化炉气化,供给焙烧车间,焙烧工序将氢氧化铝焙烧成氧化铝。
煤气化炉蒸汽在线校准系统是对煤气化工序所对应的气化炉管道1的蒸汽表1~气化管道S的蒸汽表S,进行蒸汽流量的在线校准分析;蒸汽表S对应的在线校准算法如下:
Q′
气化S=K
气化S×Q
气化S
K
气化S=f
气化S(ΔP
气化S,T
气化S,P
气化S)
式中:S—煤气化工序所消耗蒸汽的管道数量及第S条管道编号;
Q′
气化S—在线校准后气化炉管道S对应的蒸汽流量;
Q
气化S—在线校准前气化炉管道S对应的蒸汽表显示的流量;
K
气化S—在线校准气化过程对应的蒸汽流量修正数;
f
气化S(ΔP
气化S,T
气化S,P
气化S)—煤气化工序蒸汽流量修正数的具体算法;
ΔP
气化S—煤气化管道S对应的蒸汽表差压值,由差压变送器读取;
T
气化S—煤气化管道S对应的蒸汽温度,由温度变送器读取;
P
气化S—煤气化管道S对应的蒸汽压力,由压力变送器读取。
煤气化工序的蒸汽消耗量为:
式中:Q′
气化—煤气化工序所消耗的蒸汽总量;
Q′
气化i—在线校准后煤气化第i条管道对应的蒸汽流量。
步骤三、锅炉产生的蒸汽只用于氧化铝生产,不考虑多余蒸汽用来连接汽轮机进行发电的操作;从节能降耗的角度,锅炉产生的蒸汽量将由氧化铝生产过程所消耗的蒸汽量决定;但由于锅炉产汽量不能完全等于氧化铝工序的蒸汽消耗量,为了保证生产稳定安全,对锅炉 产汽量增加裕量;因此,锅炉蒸汽产生量与氧化铝生产工序蒸汽消耗量的联锁关系式为:
Q
产汽总量-Q
锅自用=α×Q
消耗总量
式中:Q
产汽总量—锅炉产生的蒸汽总量;
Q
锅自用—锅炉自身消耗的蒸汽量;
α—保证蒸汽消耗总量的安全裕量系数,取1.1~1.15。
此处需要说明的是,由于锅炉本身运行过程就可额外增加约10%的产汽量,所以本发明中的安全裕量系数取值不必过大。
在实际生产过程中,一般会有多台锅炉参与蒸汽的生产,因此,在多台锅炉同时运行的条件下(如图5所示),会变成如图6所示的联锁运行。并且,为了便于描述,图6省略了蒸汽消耗端的结构,只给出了蒸汽发生端的结构。
蒸汽自适应分配器进行蒸汽分配的原则为:既要保证锅炉运行过程中的效率在合理范围,又能保证在运行过程中各台锅炉之间的协同;将多台锅炉以数量E进行替代,以E锅炉为例对蒸汽自适应分配器的分配算法进行说明:
χ
1·Q
1满负荷+χ
2·Q
2满负荷+…+χ
E·Q
E满负荷=Q
产汽总量
0.75≤χ
1,χ
2,…,χ
E≤0.9
式中:Q
1满负荷—锅炉1在满负荷条件下的蒸汽产量;
Q
2满负荷—锅炉2在满负荷条件下的蒸汽产量;
Q
E满负荷—锅炉E在满负荷条件下的蒸汽产量;
χ
1—锅炉自适应分配器分配给锅炉1的负荷系数;
χ
2—锅炉自适应分配器分配给锅炉2的负荷系数;
χ
E—锅炉自适应分配器分配给锅炉E的负荷系数。
蒸汽自适应分配器分配要同时满足上式的要求;每台锅炉的实际产汽量最终可由下式进行计算:
Q
E实际产汽量=χ
E·Q
E满负荷
式中:Q
E实际产汽量—分配后锅炉E的实际蒸汽产生量。
每台锅炉负荷系数的分配采用初始化方法,给定每台锅炉一个初始值0.75,则系统开始计算,如结果满足上述公式要求,则计算结束;如不满足要求,则依次给定0.76,0.77,0.78,……,0.90进行上述环节计算,直到满足上述公式要求为止。
如通过上述算法后,依然不能得到满足,则说明锅炉数量多余,需要对锅炉数量进行调整,采用E-1台锅炉进行上述循环计算过程,一直到分配满足上述公式条件为止。进而实现氧化铝蒸汽消耗与锅炉产生的蒸汽联锁过程,以满足蒸汽产耗的实时在线联锁匹配,降低蒸汽的大幅度浪费。
步骤四、锅炉产汽与原燃料的联锁。本发明中的原燃料指的是锅炉蒸汽产生所需要的主给水、一次风、二次风、燃煤等,其中燃煤包含了燃煤的煤种、燃煤的成分、燃煤的低位发热值、燃煤的消耗量等。
(1)燃煤与风量的联锁。本发明中燃煤和风量进行联锁,是为了燃煤与风量匹配合理,使得燃煤燃烧充分;同时,需要根据循环流化床锅炉的要求,满足一次风、二次风本身的联锁,以达到整个燃烧过程的最优化。
1kg燃料完全燃烧所需理论空气量计算如下式所示:
V
0=0.0889(C
ar+0.375S
ar)+0.265H
ar-0.0333O
ar(Nm
3/kg)
式中:V
0—单位燃料完全燃烧所需的理论空气量;
C
ar—收到基中碳元素成分百分比,%;
S
ar—收到基中硫元素成分百分比,%;
H
ar—收到基中氢元素成分百分比,%;
O
ar—收到基中氧元素成分百分比,%;
N
ar—收到基中氮元素成分百分比,%;
M
ar—收到基中水分百分比,%。
考虑到燃烧过程中必须有过量空气以保证燃烧的顺利进行,则实际燃烧过程中所需要的风量应为:
V=αV
0
式中:V—单位燃料完全燃烧所需的实际空气量;
α—过量空气系数,通过氧量分析仪可实时检测并计算出。
现场使用的燃煤量可以通过供煤系统进行实际的检测,为了侧重联锁,不过分纠结于燃煤量检测装置本身的精度,只对供煤系统检测到的燃煤量进行使用即可;则整个锅炉实际燃烧所需要的总空气量为:
V
总空气=m×V
式中:V
总空气—锅炉实际燃烧过程所需的总空气流量;
m—对应的锅炉煤耗,通过供煤系统可实时检测。
循环流化床锅炉的供风系统可以将风量分为一次风和二次风;一次风主要用于煤粉的流化,二次风主要用于提供氧;一次风和二次风的匹配关系主要取决于循环流化床锅炉的燃烧器型式;
V
一次=κ
1·V
总空气
V
二次=κ
2·V
总空气
κ
1+κ
2=1
式中:V
一次—循环流化床锅炉一次风的风量;
V
二次—循环流化床锅炉二次风的风量;
κ
1—循环流化床锅炉一次风的分配系数,与燃烧器型式有关;
κ
2—循环流化床锅炉二次风的分配系数,与燃烧器型式有关。
煤粉燃烧器分为直流燃烧器和旋流燃烧器。其中,直流燃烧器配风有两种形式:一种是1:1配风(即一次风和二次风比例相等),一种是分级配风,配风要保证一次风流速在20~25m/s,二次风流速在40~55m/s,具体以锅炉负荷为准。旋流燃烧器配风要保证一次风出口速度14~24m/s,二次风内环风速13~26m/s,外环风速26~40m/s。
(2)主给水与主蒸汽的联锁。由于主蒸汽的产量取决于氧化铝工艺消耗端蒸汽的用量,所以主给水需要被动与主蒸汽联锁,即:主给水需要与蒸汽反馈的量建立联锁关系。主给水与蒸汽反馈的示意如图7所示。
另外,从能量守恒的角度,还要考虑到主给水变成主蒸汽所需的热量与燃煤燃烧所产生 的热量之间的关系;所以,主给水与主蒸汽的联锁模型由两部分构成,分别是质量守恒和能量守恒两部分。
Q
E主给水·η
E=Q
E实际产汽量
式中:Q
E主给水—锅炉E对应的主给水流量;
η
E—锅炉E对应的产汽率。
上式主要用来描述锅炉主给水与主蒸汽产生量之间的联锁关系,但由于以主蒸汽为准,所以在实现环节一定是以主蒸汽的量为准来反馈给主给水,然后主给水依据当前的产汽率来决定具体的供应量。但锅炉的产汽率并不是固定不变的,是随着锅炉的运行和负荷在变化的,因此还需要能量守恒来进一步确定主给水与主蒸汽之间的联锁。
Q
E主给水·γ=m·q
低位-θ
式中:γ—单位质量主给水变成主蒸汽所需要的热量;
q
低位—锅炉所用燃煤的低位发热值;
θ—锅炉除加热水变成蒸汽以外的其它热损失。
上述步骤主要解决了锅炉燃煤与风量、主给水与主蒸汽的联锁关系,该部分的实现可以达到锅炉内部燃烧过程的最优化,降低吨蒸汽的燃煤消耗。
步骤五、原燃料与对应动力装置的联锁。原燃料及其对应的动力装置为:主给水对应水泵、一次风对应一次风机、二次风对应二次风机、烟气对应烟气的引风机、燃煤煤种成分及低位发热值对应煤种理化试验、燃煤量对应供煤系统(如图8所示)。
原燃料与动力装置建立的联锁是通过自适应过程实现的,通过步骤四中锅炉产汽与原燃料的联锁,已经可以明确获得在氧化铝生产过程中锅炉所需要的一次风量、二次风量、主给水量、燃煤消耗量、过量空气系数,而各种原燃料的量与其对应的动力装置是通过动力装置的电机驱动来实现的。当工艺端所需要的蒸汽量下降时,则对应锅炉的主蒸汽量会根据反馈相应下降,对应产生主蒸汽的锅炉中的风量、主给水、燃煤量也会下降;同时,风量下降会反馈给风机,风机电耗下降;主给水量下降会反馈给水泵,水泵电耗下降;煤耗下降会反馈给供煤系统,供煤系统的传输电耗下降;由于风量减少,则锅炉对应的烟气量下降,则烟气 对应的引风机的电耗也随之下降。上述联锁节能过程如图9所示。
对于一次风、二次风的风量与风机之间的联锁,可用下式表示:
式中:P
e风—一次风风机、二次风风机的有效功率;
p—一次风机、二次风机对应的全压。
在上式中,以一次风的风量为已知量;且风机全压为固有特性,当风机确定时,全压是确定的;
对于主给水的流量与水泵之间的联锁,可用下式表示:
式中:P
e水—主给水对应水泵的有效功率;
ρ—锅炉主给水的密度;
H—主给水对应水泵的扬程。
上式中已知量为主给水的流量,可采用蒸汽量及能量守恒得到;对于具体的应用现场,水泵是确定的,则水泵的扬程也是确定的。
对于烟气系统的烟气量和引风机,首先需要根据一次风、二次风量、煤耗、过量空气系数等进行烟气的计算。单位燃料在理论所需空气量下、完全燃烧所产生的烟气量计算公式如下:
单位燃料完全燃烧生成的SO
2容积为:
单位燃料完全燃烧生成的CO
2容积为:
故可知:
理论N
2容积为:
理论水蒸气容积为:
由于循环流化床锅炉实际燃烧过程是在过量空气系数条件下进行的,此时的烟气容积除了理论烟气容积外,还增加了过量空气及过量空气中携带的水蒸气容积,实际烟气流量为:
则实际产生的烟气流量可用下式表示为:
Q
g=m·V
g
式中:V
g—单位燃料完全燃烧产生的实际烟气体积;
Q
g—实际燃烧过程中烟气的体积流量。
因此,可建立烟气流量及其对应引风机的联锁关系为:
式中:P
eg—烟气对应引风机的有效功率;
p
g—烟气对应引风机的全压。
在上述关系式中,烟气的流量为已知量,烟气引风机在现场是确定的,故引风机对应的全压也是已知,可根据烟气流量变化调整引风机的功率。在实际的操作层面,由于泵和风机还会有总效率和原动机效率,所以还需考虑上述两项效率对于整个控制系统的影响。
经济效益预测:
1、锅炉产汽与原燃料、动力装置连锁经济效益
由于本发明中主给水、风量与煤耗实现自动连锁,可实现吨蒸汽煤耗降低y
1吨,产生的 经济效益计算如下:
该部分经济效益=节约原煤效益+动力系统节约电量效益
(1)节约燃煤效益
式中:J
1—吨蒸汽煤耗降低产生的经济效益,万元/吨蒸汽;
y
1—吨蒸汽煤耗降低量,吨/吨蒸汽;
29310—热量与标煤折算系数,MJ/tce;
D
tce—吨标煤的价格,万元/tce。
(2)动力系统节约电量效益
本发明实现氧化铝厂锅炉系统的主给水、风量与煤耗实现自动连锁,从而使锅炉给水泵系统、一次风机系统、二次风机系统运行效率得到提高。产生吨氧化铝节约蒸汽量y
3,锅炉系统实现自动连锁前后节约电耗实现经济性如下:
式中:J
给水泵—给水泵系统节约电量经济性,元/吨氧化铝;
y
3—生产吨氧化铝节约蒸汽量,吨/吨氧化铝;
M
w/s—吨蒸汽对应的主给水量,t/t;
E
泵,i—锅炉额定负荷对应给水泵i小时电耗平均值,元/小时;
M
泵,i—锅炉额定负荷对应给水泵i小时主给水量,吨/小时;
D
J—电价平均值。
式中:J
一次风机—一次风机系统节约电量经济性,元/吨氧化铝;
y
3—生产吨氧化铝节约蒸汽量,吨/吨氧化铝;
M
wind/s—吨蒸汽对应的一次风量,t/t;
E
一次风机,i—锅炉额定负荷对应一次风机i小时电耗平均值,元/小时;
M
一次风机,i—锅炉额定负荷对应一次风机i小时一次风量,吨/小时;
DJ—电价平均值。
式中:J
二次风机—二次风机系统节约电量经济性,元/吨氧化铝;
y
3—生产吨氧化铝节约蒸汽量,吨/吨氧化铝;
M
wind/s—吨蒸汽对应的二次风量,t/t;
E
二次风机,i—锅炉额定负荷对应二次风机i小时电耗平均值,元/小时;
M
二次风机,i—锅炉额定负荷对应二次风机i小时二次风量,吨/小时;
DJ—电价平均值。
2、锅炉与工艺消耗端联锁经济效益
通过本发明的实施,可实现吨氧化铝的蒸汽消耗量下降y
2吨,则可产生的经济效益计算为:
J
2=y
2·D
吨蒸汽
式中:J
2—吨氧化铝蒸汽下降产生的经济效益;
D
吨蒸汽—氧化铝生产过程中吨蒸汽的价格。
某厂的氧化铝年产量按照A万吨计算,则通过本发明的联锁方法,全年可产生的经济效益如下式所示:
G=Q
产汽总量·J
1+10000·A·(J
2+J
给水泵+J
一次风机+J
二次风机)
式中:G—某氧化铝厂全年产生的经济效益;
A—某铝厂年氧化铝产量。
Claims (10)
- 一种氧化铝蒸汽产消联锁方法,其特征在于,包括如下步骤:步骤一、氧化铝工序蒸汽消耗与锅炉蒸汽产生的联锁;各工序的蒸汽需求量取决于各条管线的蒸汽需求量,而各管线的蒸汽需求量来源于各管线的表计端的蒸汽在线计量数据;并在所有蒸汽表环节都采取在线的校准措施,进而使数据达到精准要求;步骤二、通过氧化铝的预脱硅、高压溶出、母液蒸发、脱硫及煤气化环节的工序蒸汽消耗量,可知氧化铝生产工艺所消耗的蒸汽量为:Q 消耗总量=Q′ 预脱硅+Q′ 溶出+Q′ 蒸发+Q 脱硫+Q′ 气化式中:Q 消耗总量—氧化铝工艺蒸汽消耗总量;Q′ 预脱硅—预脱硅工序所消耗的蒸汽总量;Q′ 溶出—高压溶出工序所消耗的蒸汽总量;Q′ 蒸发—母液蒸发工序所消耗的蒸汽总量;Q 脱硫—脱硫管道所消耗的蒸汽总量;Q′ 气化—煤气化工序所消耗的蒸汽总量;步骤三、锅炉产生的蒸汽只用于氧化铝生产,不考虑多余蒸汽用来连接汽轮机进行发电的操作;从节能降耗的角度,锅炉产生的蒸汽量将由氧化铝生产过程所消耗的蒸汽量决定;但由于锅炉产汽量不能完全等于氧化铝工序的蒸汽消耗量,为了保证生产稳定安全,对锅炉产汽量增加裕量;因此,锅炉蒸汽产生量与氧化铝生产工序蒸汽消耗量的联锁关系式为:Q 产汽总量-Q 锅自用=α×Q 消耗总量式中:Q 产汽总量—锅炉产生的蒸汽总量;Q 锅自用—锅炉自身消耗的蒸汽量;α—保证蒸汽消耗总量的安全裕量系数,取1.1~1.15;步骤四、锅炉产汽与原燃料的联锁;原燃料指的是锅炉蒸汽产生所需要的主给水、一次风、二次风、燃煤,燃煤包含了燃煤的煤种、燃煤的成分、燃煤的低位发热值、燃煤的消耗量;锅炉产汽与原燃料的联锁包括燃煤与风量的联锁、以及主给水与主蒸汽的联锁;步骤五、原燃料与对应动力装置的联锁;原燃料与动力装置建立的联锁是通过自适应过程实现的,通过步骤四中锅炉产汽与原燃料的联锁,已经可以明确获得在氧化铝生产过程中锅炉所需要的一次风量、二次风量、主给水量、燃煤消耗量、过量空气系数,而各种原燃料的量与其对应的动力装置是通过动力装置的电机驱动来实现的;当工艺端所需要的蒸汽量下降时,则对应锅炉的主蒸汽量会根据反馈相应下降,对应产生主蒸汽的锅炉中的风量、主给水、燃煤量也会下降;同时,风量下降会反馈给风机,风机电耗下降;主给水量下降会反馈给水泵,水泵电耗下降;煤耗下降会反馈给供煤系统,供煤系统的传输电耗下降;由于风量减少,则锅炉对应的烟气量下降,则烟气对应的引风机的电耗也随之下降。
- 根据权利要求1所述的氧化铝蒸汽产消联锁方法,其特征在于:所述步骤二、预脱硅的蒸汽消耗量的校准确定;预脱硅环节用到的蒸汽包含了各条管道的蒸汽消耗量;各管道的数据经过原始压力、差压、温度等信号进入到预脱硅蒸汽校准系统,由该系统进行数据精准性处理,以得到预脱硅环节的蒸汽消耗量;预脱硅蒸汽校准系统是对预脱硅工序所对应的预脱硅管道1的蒸汽表1~预脱硅管道M的蒸汽表M,进行蒸汽流量的在线校准分析;蒸汽表M对应的在线校准算法如下:Q′ 预脱硅M=K M×Q 预脱硅MK M=f M(ΔP M,T M,P M)式中:M—预脱硅工序所消耗蒸汽的管道数量及第M条管道的编号;Q′ 预脱硅M—在线校准后预脱硅管道M对应的蒸汽流量;Q 预脱硅M—在线校准前预脱硅管道M对应的蒸汽表显示的流量;K M—在线校准过程对应的蒸汽流量修正数;f M(ΔP M,T M,P M)—蒸汽流量修正数的具体算法;ΔP M—预脱硅管道M对应的蒸汽表差压值,由差压变送器读取;T M—预脱硅管道M对应的蒸汽温度,由温度变送器读取;P M—预脱硅管道M对应的蒸汽压力,由压力变送器读取;由于在预脱硅工序中,所有管道是平行结构,互不影响,因此,预脱硅工序的蒸汽消耗量为:式中:Q′ 预脱硅—预脱硅工序所消耗的蒸汽总量;Q′ 预脱硅i—在线校准后预脱硅第i条管道对应的蒸汽流量。
- 根据权利要求1所述的氧化铝蒸汽产消联锁方法,其特征在于:所述步骤二、高压溶出的蒸汽消耗量的校准确定;高压溶出用于将矿浆的温度从低温提升到高温,去除矿浆内杂质成分;高压溶出工序蒸汽的需求量计算方法与预脱硅工序类似,也要经过高压溶出对应的蒸汽在线校准系统处理;高压溶出蒸汽在线校准系统是对高压溶出工序所对应的溶出管道1的蒸汽表1~溶出管道N的蒸汽表N,进行蒸汽流量的在线校准分析;蒸汽表N对应的在线校准算法如下:Q′ 溶出N=K 溶出N×Q 溶出NK 溶出N=f 溶出N(ΔP 溶出N,T 溶出N,P 溶出N)式中:N—高压溶出工序所消耗蒸汽的管道数量及第N条管道编号;Q′ 溶出N—在线校准后高压溶出管道N对应的蒸汽流量;Q 溶出N—在线校准前高压溶出管道N对应的蒸汽表显示的流量;K 溶出N—在线校准溶出过程对应的蒸汽流量修正数;f 溶出N(ΔP 溶出N,T 溶出N,P 溶出N)—溶出工序蒸汽流量修正数的具体算法;ΔP 溶出N—高压溶出管道N对应的蒸汽表差压值,由差压变送器读取;T 溶出N—高压溶出管道N对应的蒸汽温度,由温度变送器读取;P 溶出N—高压溶出管道N对应的蒸汽压力,由压力变送器读取;高压溶出工序的蒸汽消耗量为:式中:Q′ 溶出—高压溶出工序所消耗的蒸汽总量;Q′ 溶出i—在线校准后高压溶出第i条管道对应的蒸汽流量。
- 根据权利要求1所述的氧化铝蒸汽产消联锁方法,其特征在于:所述步骤二、母液蒸发的蒸汽消耗量的校准确定;母液蒸发的目的是为了保证氧化铝生产过程中的浓度,使得循环母液达到溶出铝土矿的要求;母液蒸发工序所需的蒸汽量经过母液在线校准系统进行蒸汽数据的校准;母液蒸发蒸汽在线校准系统是对母液蒸发工序所对应的蒸发管道1的蒸汽表1~蒸发管道K的蒸汽表K,进行蒸汽流量的在线校准分析;蒸汽表K对应的在线校准算法如下:Q′ 蒸发K=K 蒸发K×Q 蒸发KK 蒸发K=f 蒸发K(ΔP 蒸发K,T 蒸发K,P 蒸发K)式中:K—母液蒸发工序所消耗蒸汽的管道数量及第K条管道编号;Q′ 蒸发K—在线校准后母液蒸发管道K对应的蒸汽流量;Q 蒸发K—在线校准前母液蒸发管道K对应的蒸汽表显示的流量;K 蒸发K—在线校准蒸发过程对应的蒸汽流量修正数;f 蒸发K(ΔP 蒸发K,T 蒸发K,P 蒸发K)—蒸发工序蒸汽流量修正数的具体算法;ΔP 蒸发K—母液蒸发管道K对应的蒸汽表差压值,由差压变送器读取;T 蒸发K—母液蒸发管道K对应的蒸汽温度,由温度变送器读取;P 蒸发K—母液蒸发管道K对应的蒸汽压力,由压力变送器读取;母液蒸发工序的蒸汽消耗量为:式中:Q′ 蒸发—母液蒸发工序所消耗的蒸汽总量;Q′ 蒸发i—在线校准后母液蒸发第i条管道对应的蒸汽流量。
- 根据权利要求1所述的氧化铝蒸汽产消联锁方法,其特征在于:所述步骤二、煤气化炉蒸汽消耗量的校准确定;煤气化炉负责给氧化铝生产工艺环节的焙烧工序提供煤气;其作用是将煤通过煤气化炉气化,供给焙烧车间,焙烧工序将氢氧化铝焙烧成氧化铝;煤气化炉蒸汽在线校准系统是对煤气化工序所对应的气化炉管道1的蒸汽表1~气化管道S的蒸汽表S,进行蒸汽流量的在线校准分析;蒸汽表S对应的在线校准算法如下:Q′ 气化S=K 气化S×Q 气化SK 气化S=f 气化S(ΔP 气化S,T 气化S,P 气化S)式中:S—煤气化工序所消耗蒸汽的管道数量及第S条管道编号;Q′ 气化S—在线校准后气化炉管道S对应的蒸汽流量;Q 气化S—在线校准前气化炉管道S对应的蒸汽表显示的流量;K 气化S—在线校准气化过程对应的蒸汽流量修正数;f 气化S(ΔP 气化S,T 气化S,P 气化S)—煤气化工序蒸汽流量修正数的具体算法;ΔP 气化S—煤气化管道S对应的蒸汽表差压值,由差压变送器读取;T 气化S—煤气化管道S对应的蒸汽温度,由温度变送器读取;P 气化S—煤气化管道S对应的蒸汽压力,由压力变送器读取;煤气化工序的蒸汽消耗量为:式中:Q′ 气化—煤气化工序所消耗的蒸汽总量;Q′ 气化i—在线校准后煤气化第i条管道对应的蒸汽流量。
- 根据权利要求1所述的氧化铝蒸汽产消联锁方法,其特征在于:所述步骤三、在实际生产过程中,一般会有多台锅炉参与蒸汽的生产;在多台锅炉同时运行的条件下,蒸汽自适应分配器进行蒸汽分配的原则为:既要保证锅炉运行过程中的效率在合理范围,又能保证在运行过程中各台锅炉之间的协同;将多台锅炉以数量E进行替代,以E锅炉为例对蒸汽自适应分配器的分配算法进行说明:χ 1·Q 1满负荷+χ 2·Q 2满负荷+…+χ E·Q E满负荷=Q 产汽总量0.75≤χ 1,χ 2,…,χ E≤0.9式中:Q 1满负荷—锅炉1在满负荷条件下的蒸汽产量;Q 2满负荷—锅炉2在满负荷条件下的蒸汽产量;Q E满负荷—锅炉E在满负荷条件下的蒸汽产量;χ 1—锅炉自适应分配器分配给锅炉1的负荷系数;χ 2—锅炉自适应分配器分配给锅炉2的负荷系数;χ E—锅炉自适应分配器分配给锅炉E的负荷系数;蒸汽自适应分配器分配要同时满足上式的要求;每台锅炉的实际产汽量最终可由下式进行计算:Q E实际产汽量=χ E·Q E满负荷式中:Q E实际产汽量—分配后锅炉E的实际蒸汽产生量;每台锅炉负荷系数的分配采用初始化方法,给定每台锅炉一个初始值0.75,则系统开始计算,如结果满足上述公式要求,则计算结束;如不满足要求,则依次给定0.76,0.77,0.78,……,0.90进行上述环节计算,直到满足上述公式要求为止。
- 根据权利要求1所述的氧化铝蒸汽产消联锁方法,其特征在于:所述步骤四、燃煤与风量的联锁,是为了燃煤与风量匹配合理,使得燃煤燃烧充分;同时,需要根据循环流化床锅炉的要求,满足一次风、二次风本身的联锁,以达到整个燃烧过程的最优化;1kg燃料完全燃烧所需理论空气量计算如下式所示:V 0=0.0889(C ar+0.375S ar)+0.265H ar-0.0333O ar(Nm 3/kg)式中:V 0—单位燃料完全燃烧所需的理论空气量;C ar—收到基中碳元素成分百分比,%;S ar—收到基中硫元素成分百分比,%;H ar—收到基中氢元素成分百分比,%;O ar—收到基中氧元素成分百分比,%;N ar—收到基中氮元素成分百分比,%;M ar—收到基中水分百分比,%;考虑到燃烧过程中必须有过量空气以保证燃烧的顺利进行,则实际燃烧过程中所需要的风量应为:V=αV 0式中:V—单位燃料完全燃烧所需的实际空气量;α—过量空气系数,通过氧量分析仪可实时检测并计算出;现场使用的燃煤量可以通过供煤系统进行实际的检测,为了侧重联锁,不过分纠结于燃煤量检测装置本身的精度,只对供煤系统检测到的燃煤量进行使用即可;则整个锅炉实际燃烧所需要的总空气量为:V 总空气=m×V式中:V 总空气—锅炉实际燃烧过程所需的总空气流量;m—对应的锅炉煤耗,通过供煤系统可实时检测;循环流化床锅炉的供风系统可以将风量分为一次风和二次风;一次风主要用于煤粉的流化,二次风主要用于提供氧;一次风和二次风的匹配关系主要取决于循环流化床锅炉的燃烧器型式;V 一次=κ 1·V 总空气V 二次=κ 2·V 总空气κ 1+κ 2=1式中:V 一次—循环流化床锅炉一次风的风量;V 二次—循环流化床锅炉二次风的风量;κ 1—循环流化床锅炉一次风的分配系数;κ 2—循环流化床锅炉二次风的分配系数。
- 根据权利要求1所述的氧化铝蒸汽产消联锁方法,其特征在于:所述步骤四、主给水与主蒸汽的联锁;由于主蒸汽的产量取决于氧化铝工艺消耗端蒸汽的用量,所以主给水需要被动与主蒸汽联锁,即:主给水需要与蒸汽反馈的量建立联锁关系;另外,从能量守恒的角度,还要考虑到主给水变成主蒸汽所需的热量与燃煤燃烧所产生的热量之间的关系;所以,主给水与主蒸汽的联锁模型由两部分构成,分别是质量守恒和能量守恒两部分;Q E主给水·η E=Q E实际产汽量式中:Q E主给水—锅炉E对应的主给水流量;η E—锅炉E对应的产汽率;上式主要用来描述锅炉主给水与主蒸汽产生量之间的联锁关系,但由于以主蒸汽为准,所以在实现环节一定是以主蒸汽的量为准来反馈给主给水,然后主给水依据当前的产汽率来决定具体的供应量;但锅炉的产汽率并不是固定不变的,是随着锅炉的运行和负荷在变化的,因此还需要能量守恒来进一步确定主给水与主蒸汽之间的联锁;Q E主给水·γ=m·q 低位-θ式中:γ—单位质量主给水变成主蒸汽所需要的热量;q 低位—锅炉所用燃煤的低位发热值;θ—锅炉除加热水变成蒸汽以外的其它热损失。
- 根据权利要求1所述的氧化铝蒸汽产消联锁方法,其特征在于:所述步骤五、对于一次风、二次风的风量与风机之间的联锁,可用下式表示:式中:P e风—一次风风机、二次风风机的有效功率;p—一次风机、二次风机对应的全压;在上式中,以一次风的风量为已知量;且风机全压为固有特性,当风机确定时,全压是 确定的;对于主给水的流量与水泵之间的联锁,可用下式表示:式中:P e水—主给水对应水泵的有效功率;ρ—锅炉主给水的密度;H—主给水对应水泵的扬程;上式中已知量为主给水的流量,可采用蒸汽量及能量守恒得到;对于具体的应用现场,水泵是确定的,则水泵的扬程也是确定的;对于烟气系统的烟气量和引风机,首先需要根据一次风、二次风量、煤耗、过量空气系数等进行烟气的计算;单位燃料在理论所需空气量下、完全燃烧所产生的烟气量计算公式如下:单位燃料完全燃烧生成的SO 2容积为:单位燃料完全燃烧生成的CO 2容积为:故可知:理论N 2容积为:理论水蒸气容积为:由于循环流化床锅炉实际燃烧过程是在过量空气系数条件下进行的,此时的烟气容积除了理论烟气容积外,还增加了过量空气及过量空气中携带的水蒸气容积,实际烟气流量为:则实际产生的烟气流量可用下式表示为:Q g=m·V g式中:V g—单位燃料完全燃烧产生的实际烟气体积;Q g—实际燃烧过程中烟气的体积流量;因此,可建立烟气流量及其对应引风机的联锁关系为:式中:P eg—烟气对应引风机的有效功率;p g—烟气对应引风机的全压;在上述关系式中,烟气的流量为已知量,烟气引风机在现场是确定的,故引风机对应的全压也是已知,可根据烟气流量变化调整引风机的功率。
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN202011581464.8 | 2020-12-28 | ||
CN202011581464.8A CN112696658B (zh) | 2020-12-28 | 2020-12-28 | 一种氧化铝蒸汽产消联锁方法 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2022141741A1 true WO2022141741A1 (zh) | 2022-07-07 |
Family
ID=75512859
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/CN2021/075158 WO2022141741A1 (zh) | 2020-12-28 | 2021-02-04 | 一种氧化铝蒸汽产消联锁方法 |
Country Status (2)
Country | Link |
---|---|
CN (1) | CN112696658B (zh) |
WO (1) | WO2022141741A1 (zh) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN115490252A (zh) * | 2022-09-29 | 2022-12-20 | 东方希望晋中铝业有限公司 | 一种氧化铝厂铝电联动开车方法 |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5483797A (en) * | 1988-12-02 | 1996-01-16 | Ormat Industries Ltd. | Method of and apparatus for controlling the operation of a valve that regulates the flow of geothermal fluid |
CN103134570A (zh) * | 2011-11-29 | 2013-06-05 | 中国科学院沈阳自动化研究所 | 一种钢铁企业蒸汽产生量与消耗量认证的方法 |
CN104915728A (zh) * | 2015-05-22 | 2015-09-16 | 中冶南方工程技术有限公司 | 一种确定钢铁企业蒸汽系统优化调度可行解的方法 |
CN106529710A (zh) * | 2016-11-02 | 2017-03-22 | 广州优华过程技术有限公司 | 一种基于边际成本核算的蒸汽动力系统优化方法 |
CN108487955A (zh) * | 2018-01-31 | 2018-09-04 | 中冶华天南京工程技术有限公司 | 基于蒸汽参数提升的煤气增效利用系统及方法 |
CN111475913A (zh) * | 2020-03-04 | 2020-07-31 | 曹雁青 | 一种蒸汽动力系统的运行操作优化方法及系统 |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101551103B (zh) * | 2009-04-30 | 2010-11-10 | 东莞德永佳纺织制衣有限公司 | 循环流化床锅炉燃烧自动控制系统 |
CN103423740B (zh) * | 2013-08-05 | 2015-10-28 | 浙江大学 | 循环流化床锅炉燃烧过程自动控制系统及方法 |
CN109084291B (zh) * | 2018-08-21 | 2023-11-03 | 北京富士特锅炉有限公司 | 贯流式蒸汽锅炉应用于啤酒生产过程预判反馈群控系统 |
-
2020
- 2020-12-28 CN CN202011581464.8A patent/CN112696658B/zh active Active
-
2021
- 2021-02-04 WO PCT/CN2021/075158 patent/WO2022141741A1/zh unknown
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5483797A (en) * | 1988-12-02 | 1996-01-16 | Ormat Industries Ltd. | Method of and apparatus for controlling the operation of a valve that regulates the flow of geothermal fluid |
CN103134570A (zh) * | 2011-11-29 | 2013-06-05 | 中国科学院沈阳自动化研究所 | 一种钢铁企业蒸汽产生量与消耗量认证的方法 |
CN104915728A (zh) * | 2015-05-22 | 2015-09-16 | 中冶南方工程技术有限公司 | 一种确定钢铁企业蒸汽系统优化调度可行解的方法 |
CN106529710A (zh) * | 2016-11-02 | 2017-03-22 | 广州优华过程技术有限公司 | 一种基于边际成本核算的蒸汽动力系统优化方法 |
CN108487955A (zh) * | 2018-01-31 | 2018-09-04 | 中冶华天南京工程技术有限公司 | 基于蒸汽参数提升的煤气增效利用系统及方法 |
CN111475913A (zh) * | 2020-03-04 | 2020-07-31 | 曹雁青 | 一种蒸汽动力系统的运行操作优化方法及系统 |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN115490252A (zh) * | 2022-09-29 | 2022-12-20 | 东方希望晋中铝业有限公司 | 一种氧化铝厂铝电联动开车方法 |
Also Published As
Publication number | Publication date |
---|---|
CN112696658A (zh) | 2021-04-23 |
CN112696658B (zh) | 2022-06-17 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
Wang et al. | Model establishment and performance evaluation of a modified regenerative system for a 660 MW supercritical unit running at the IPT-setting mode | |
CN110096817B (zh) | 低热值煤发电入炉燃料收到基热值的在线估算系统及方法 | |
CN111881405B (zh) | 一种燃煤锅炉飞灰可燃物含量的实时计算方法 | |
CN205717147U (zh) | 一种全负荷脱硝与烟气余热利用及空预器防腐防堵耦合系统 | |
WO2022141741A1 (zh) | 一种氧化铝蒸汽产消联锁方法 | |
CN201387242Y (zh) | 隧道窑余热发电装置 | |
CN102966941A (zh) | 一种相变换热器与低压省煤器联合的余热回收系统 | |
CN112964492B (zh) | 一种适用于高背压梯级供热机组的供热耗煤在线测定方法 | |
CN112965386A (zh) | 水煤浆气化与燃煤锅炉超低NOx排放一体化协同控制方法 | |
CN113468732A (zh) | 一种抽汽供热机组供热用生产成本的确定系统及方法 | |
CN111336493B (zh) | 一种电站锅炉炉内低温低压蒸汽生产装置及工艺方法 | |
CN202693508U (zh) | 火电机组管道效率测试系统 | |
CN111536806A (zh) | 一种具有酸露点在线监控的水媒式烟气余热利用系统 | |
CN106765035A (zh) | 提高scr反应器温度系统装置及方法 | |
CN215892366U (zh) | 焚烧炉炉排的烟气循环加热装置 | |
CN110273715A (zh) | 一种基于0号高压加热器疏水方式的汽轮发电机组改造方法 | |
CN109140492B (zh) | 锅炉烟风耦合余热回收系统 | |
CN110822458B (zh) | 一种余热阶梯利用的低浓度瓦斯稳态催化氧化装置 | |
CN204097079U (zh) | 一种co变换系统水气比调节装置 | |
CN114154103A (zh) | 一种燃煤锅炉烟气余热深度利用系统节能效果的计算方法 | |
CN207080980U (zh) | 一种大型汽水两用型锅炉 | |
CN206019368U (zh) | 冶炼炉余热锅炉 | |
CN106288831B (zh) | 一种双取风单通道烧结环冷机余热锅炉取风流量软测量方法 | |
CN106323019B (zh) | 双取风单通道烧结环冷机余热锅炉取风流量软测量方法 | |
CN104614197A (zh) | 煤粉与高炉煤气混烧锅炉热效率的在线监测方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 21912519 Country of ref document: EP Kind code of ref document: A1 |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
32PN | Ep: public notification in the ep bulletin as address of the adressee cannot be established |
Free format text: NOTING OF LOSS OF RIGHTS PURSUANT TO RULE 112(1) EPC (EPO FORM 1205A DATED 16/11/2023) |