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摘要: 針對鋼鐵空分企業氧氣放散率高、綜合能耗高的問題，建立了以減小轉爐用氧總量波動和降低系統能耗為目標的轉爐用氧調度模型。綜合考慮了吹煉區間時長不變、各吹煉區間起始時刻滿足工藝要求、鋼水溫度大于1250 °C、轉爐用氧調度前后變動最小等約束，以基于整數空間的粒子群（Particle swarm optimization, PSO）算法進行求解。同時，以國內某大型鋼鐵企業空分廠為案例，采用Pipeline Studio軟件建立該廠區氧氣管網輸配系統模型，對轉爐用氧調度的節能優化效果進行了驗證。結果表明，本文提出的轉爐用氧節能優化調度在研究時間段盡可能安排單臺轉爐生產，有效降低多臺轉爐吹氧重疊時間，在生產時間內錯峰用氧，減小轉爐用氧總量波動，緩解氧氣供求不平衡的矛盾。在120 min研究時長內，調度前后系統氧氣放散量由1242.1 m3降低至0，相應的空分系統的電耗節約了1192.42 kW·h，氧壓機的壓縮能耗增大了41 kW·h，氧氣管網輸配系統節約總能耗為1151.42 kW·h。綜合計算來看，轉爐用氧調度應用到全年，預計減少氧氣放散總量5.44×106 m3，節約氧氣管網輸配系統總能耗5.22×106 kW·h。Abstract: The air separation plants of iron and steel enterprises are characterized by a high oxygen-emission rate and high comprehensive energy consumption. To solve this problem, a converter oxygen scheduling model was established based on particle swarm optimization (PSO) with the goal of reducing the fluctuation of the total oxygen consumption and saving system energy consumption in the converter. With the full consideration of constraints, such as the constant duration of blowing intervals, compliant starting time of each blowing interval, molten steel temperature above 1250 °C, and minimal variation before and after converter scheduling, PSO based on integer space was used to solve the hypothesis. With the air separation plant of a large domestic iron and steel enterprise as a case study, Pipeline Studio software was used to establish the oxygen transmission and distribution model, and the energy-saving performance of the converter oxygen scheduling was verified. The results show that the optimal scheduling of converter oxygen based on PSO can arrange oxygen for a single converter as much as possible during the study period; moreover, the optimal scheduling can effectively reduce the overlapping time of oxygen blowing in multiple converters, reduce the fluctuation of the total oxygen amount, and alleviate the contradiction between oxygen supply and demand. The oxygen emission of the pipeline transmission and distribution system before and after the dispatch is reduced from 1242.1 m3 to 0 within the 120 min simulation period; the corresponding air separation system oxygen production energy consumption saves 1192.42 kW·h; the compression energy consumption of the oxygen compressor increases by 41 kW·h; and the total energy saving of the system is 1151.42 kW·h. Based on comprehensive calculations, optimal scheduling of converter oxygen based on PSO is applied throughout the year. The oxygen transmission and distribution pipeline system is expected to reduce the total amount of oxygen emission by 5.44×106 m3 and save the total energy consumption by 5.22×106 kW·h.
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圖 1 國內某大型空分鋼鐵企業中壓氧氣管網輸配系統示意圖
Figure 1. Schematic of a medium-pressure oxygen transmission and distribution network system for a large domestic air separation steel plant
圖 2 各轉爐的生產周期排列示意
Figure 2. Schematic arrangement of the production cycle of each converter
圖 4 不同設備氧氣流量隨時間的變化圖
Figure 4. Change in oxygen flow rate over time for different equipment types
圖 5 調度前后5臺轉爐的吹氧情況對比。（a）調度前（b）調度后
Figure 5. Comparison of oxygen blowing situations of five converters before (a) and after (b) dispatching
圖 6 調度前后轉爐的總用氧量隨時間的變化
Figure 6. Changes in total oxygen consumption of converter before and after scheduling
圖 7 調度前后轉爐的工作用氧情況
Figure 7. Working oxygen conditions of converter before and after scheduling
圖 8 中壓氧氣管網輸配系統模型示意圖
Figure 8. Schematic model of medium-pressure oxygen pipeline network system
圖 9 采用調度的氧壓機出口壓力對比
Figure 9. Outlet pressure comparison of oxygen compressor using scheduling
圖 10 采用調度的中壓管道壓力對比
Figure 10. Medium-pressure pipeline pressure comparison using scheduling
圖 11 采用放散的氧壓機出口壓力變化曲線
Figure 11. Oxygen compressor outlet pressure change curve using medium pressure release
圖 13 中壓放散閥氧氣流量時間變化曲線
Figure 13. Time-varying curve of oxygen flow of medium-pressure relief valve
圖 14 氧壓機的壓縮能耗對比
Figure 14. Compression energy consumption of oxygen compressor comparison
表 1 PSO算法基本參數
Table 1. Basic parameters of PSO algorithm
k1 k2 R M tmax c1 c2 wmax wmin 0.9999 0.0001 600 11 200 0.8 0.8 0.95 0.05 
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表 2 工序氧氣流量表
Table 2. Process oxygen flow meter
Time Total instantaneous oxygen demand for ironmaking/
(m3?h?1)Total instantaneous oxygen demand for steelmaking/
(m3?h?1)Total instantaneous oxygen production/
(m3?h?1)Network pressure/MPa 0 80733.348 60875.992 135690.117 1.962 2 79554.535 60516.899 136006.664 1.962 4 79819.277 48000.639 136118.836 1.965 6 80312.504 23078.353 136107.457 1.986 8 78686.025 35453.71116 135280.527 2.022 … … … … …
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表 3 氧壓機能耗和效率的計算步驟
Table 3. Calculation steps of oxygen compressor energy consumption and efficiency
Procedure Specific operation STEP1 Use Matlab R2014a software to calculate the inlet guide vane opening k according to the intake flow Qn and exhaust pressure pd. STEP2 Calculate the shaft power Nz from the inlet guide vane opening k and the intake air flow Qn. STEP3 Calculate the isothermal efficiency ηT combined with the isothermal efficiency calculation formula of centrifugal oxygen compressor. STEP4 Use the trapz function in Matlab R2014a software to calculate the integral of the shaft power Nz during the study period to obtain the value of the total energy consumption E.
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