CN114893950A - 一种天然气液化工艺运行参数优化方法 - Google Patents
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Abstract
Description
技术领域
本发明涉及能源利用技术领域,具体涉及一种天然气液化工艺运行参数优化方法。
背景技术
液化天然气LNG凭借能量密度高、便于储存、运输灵活等特点,越来越受到市场欢迎。LNG整个产业链由天然气净化、液化、储存、运输、接收环节构成,其中天然气液化环节所使用的技术和资金最为密集。目前,我国的天然气液化工厂主要有两方面的挑战,一是国外天然气气源价格更具优势;二是国外普及的天然气液化工艺规模更大。因此,有必要对已建成的天然气液化工厂进行优化,开发工艺潜力,提升市场竞争力。为此,需研究天然气液化工艺的能效评价和经济评价,提出天然气液化工艺运行参数优化方法。
天然气液化工艺作为一个复杂的能量转化系统,影响其能效和经济性的因素众多。为使工艺达最佳运行工况,研究人员对工艺主要操作运行参数的优化进行研究。通过分析关于天然气液化工艺的评价和运行参数优化研究的研究,发现目前,研究人员多以天然气液化工艺的LNG比功耗为优化目标。优化天然气液化工艺的压缩机出口压力、混合冷剂配比等参数。但是这些研究未综合考虑系统能效性、经济性,以提高工艺能效和经济为目标的运行参数优化研究较少。在双碳目标和能源价格上涨的情况下,急需一种能同时保证天然气液化工艺的能效性、经济性,寻求天然气液化工艺最佳运行参数的方法。
发明内容
本发明针对现有技术存在的问题提供一种可以提高工艺的能效性、经济性的天然气液化工艺运行参数优化方法。
本发明采用的技术方案是:
一种天然气液化工艺运行参数优化方法,包括以下步骤:
步骤1:建立天然气液化工艺流程;
步骤3:将系统最终产品的LNG热经济学成本作为步骤1得到的工艺流程的经济指标;
进一步的,所述步骤3中经济指标确定过程如下:
S2:根据天然气液化工艺流程各设备的燃料-产品定义建立各设备的热经济学成本平衡方程和补充方程;
S3:通过逆矩阵法求解建立的方程组,得每股物流的热经济学成本,将其中的LNG热经济学成本作为系统经济指标。
进一步的,所述步骤4中优化过程目标函数如下:
mindouble(X)=min(f1(x),f2(x))
f1(x)=CLNG
进一步的,所述步骤4中优化过程约束条件如下:
以板式换热器最小传热温差大于3℃为约束条件,采用罚函数将不满足热约束条件的种群及目标函数值淘汰:
JP=f(X)·e5h(t)
h(t)=Max(0,3-Δtmin,H-1)+Max(0,3-Δtmin,H-2)
式中:JP为惩罚后的目标函数值,f(X)为目标函数值,h(x)为惩罚系数变量,Max为区间内的最大值的函数,Δtmin,H-1为换热器H-1的最小传热温差,Δtmin,H-2为换热器H-2的最小传热温差。
进一步的,所述步骤4中优化过程中通过非支配遗传算法对天然气液化工艺流程的运行参数进行优化,得到该优化问题的非劣解集;通过优劣解距离法评价非劣解集的各解,选择最优解;评价得到Ui最高的则为最优解;
式中:为第i个评价对象与最大值的距离,为第i个评价对象与最小值的距离,Ui为第i个评价对象的归一化得分,Bij为第i个评价对象的第j目标的值,为评价对象的第j目标的理想值,为评价对象的第j目标的不理想值,m为目标个数。
本发明的有益效果是:
本发明方法避免了目标函数与运行参数拟合过程产生的误差,优化结果与实际更为接近;建立的优化模型具有较高灵活性,可任意改变目标函数、优化变量。
附图说明
图1为本发明实施例中天然气液化工艺的流程示意图。
图2为本发明实施例中建立的天然气液化工艺工艺流程模拟示意图。
图3为本发明实施例中优化程序逻辑框架图。
图4为本发明实施例中优化后的非劣解集。
图5为本发明方法流程示意图。
图1中:1,4-20为冷剂循环过程中的各物流编号;30-33,35,36为天然气液化过程中的各物流编号;41-46,48,49为蒸发气再液化过程中的各物流编号;C6为脱离出的重烃;H2为闪蒸脱除的氢气;N2为闪蒸脱除的氮气;LNG为液化天然气产品;BOG为闪蒸气;NG为原料天然气;C为压缩机代号;E为水冷器代号;P为冷剂泵代号;H为板式换热器代号;S为分离器代号;V为节流阀代号;T为分流器代号;M为混合器代号;W为输入的电量;Q为输入的热量。
图2中:1-21为冷剂循环过程中的各物流编号;30-37为天然气液化过程中的各物流编号;40-49为蒸发气再液化过程中的各物流编号;C6为脱离出的重烃;H2为闪蒸脱除的氢气;N2为闪蒸脱除的氮气;LNG为液化天然气产品;BOG为闪蒸气;NG为原料天然气;C为压缩机代号;E为水冷器代号;P为冷剂泵代号;H为板式换热器代号;S为分离器代号;V为节流阀代号;T为分流器代号;M为混合器代号;W为输入的电量;Q为输入的热量。
具体实施方式
下面结合附图和具体实施例对本发明做进一步说明。
一种天然气液化工艺运行参数优化方法,包括以下步骤:
步骤1:建立天然气液化工艺流程;采用流程模拟软件Aspen HYSYS,基于天然气液化工艺的实际生产工艺、设备热力模型和运行参数,建立该工艺的流程模拟。本实施例中天然气液化工艺基本流程如图1所示,Aspen HYSYS所建立的天然气液化工艺流程模拟如图2所示。
式中:ELNG为LNG的值,kW,EC6为重烃C6的值,kW,EN2为脱除的氮气的值,kW,EH2为脱除的氢气的值,kW,ENG为原料天然气的值,kW,E自用为工厂自用的部分BOG,kW。根据上式计算得到该工艺100%负荷时系统效率为31.85%。
步骤3:将系统最终产品的LNG热经济学成本作为步骤1得到的工艺流程的经济指标;
基于会计模式热经济学方法,建立该工艺各设备的燃料-产品,建立系统热经济学成本模型。
经济指标确定过程如下:
S2:根据天然气液化工艺流程各设备的燃料-产品定义建立各设备的热经济学成本平衡方程和补充方程;
各设备的燃料-产品定义如表1所示:
表1.主要设备燃料-产品定义表
本实施例中主要设备燃料-产品定义表如表2所示
表2.本实施例主要设备燃料-产品定义表
根据各设备的燃料-产品定义建立补充方程,其基本原则是设备产品的单位热经济学成本是相等的。各设备的热经济学成本平衡方程和补充方程如表3:
表3.设备热经济平衡方程及辅助方程
其中,C为热经济学成本,元/h,Z为非能量成本,元/h。
按照本实施例上述实例建立的各设备的热经济学平衡方程和补充方程如表4所示。
表4.本实施例设备热经济平衡方程及辅助方程
S3:通过逆矩阵法求解建立的方程组,得每股物流的热经济学成本,将其中的LNG热经济学成本作为系统经济指标。
在表4的方程组中,已知和未知的参数共有59个,将方程组、已知参数等式中的系数转化为59×59的可逆矩阵A,将等式结果记为向量B。在矩阵A中,每一列数字对应各代数在不同等式的系数,每一行的系数乘以对应代数之和等于向量B对应的结果。该工艺在100%负荷运行时的矩阵A和向量B如下所示,通过逆矩阵法求解该方程组,可解得方程组中所有数据X,X=A-1B。
根据上式求解热经济成本平衡方程组,得各物流的热经济学成本,其中LNG热经济学成本为91828.25元/h。
使用时,以Aspen HYSYS和Matlab数据交互,实现Matlab对Aspen HYSYS中的电子表格的读取数值、赋予数值。
Matlab调用Aspen HYSYS的句柄如下:
HYSYS=actxserver(HYSYS.Application)
Matlab与Aspen HYSYS中的数据表格交互句柄如下:
sheet=op.Item('SPRDSHT-1')
Matlab提取Aspen HYSYS数据表格数据的句柄如下:
hycell=CellNameString.cell
Matlab向Aspen HYSYS数据表格赋值的句柄如下:
hyset=CellObjects.cell
然后构建工艺运行参数的双目标优化模型:
mindouble(X)=min(f1(x),f2(x))
f1(x)=CLNG
以板式换热器最小传热温差大于3℃为约束条件,采用罚函数将不满足热约束条件的种群及目标函数值淘汰,使优化过程在约束条件内进行。罚函数使不满足约束条件情况下得到的目标函数值变大:
JP=f(X)·e5h(t)
h(t)=Max(0,3-Δtmin,H-1)+Max(0,3-Δtmin,H-2)
式中:JP为惩罚后的目标函数值,f(X)为目标函数值,h(x)为惩罚系数变量,Max为区间内的最大值的函数,Δtmin,H-1为换热器H-1的最小传热温差,℃,Δtmin,H-2为换热器H-2的最小传热温差,℃。
以工艺的压缩机出口压力、冷箱出口温度、混合冷剂配比为优化变量。其中压缩机出口压力范围满足各自的特性曲线。混合冷剂中各组分的摩尔流量的变化不超过基础值的±20%,如表5所示。
表5.待优化变量的上限及下限
优化过程中通过非支配遗传算法对天然气液化工艺流程的运行参数进行优化,得到该优化问题的非劣解集;通过优劣解距离法评价非劣解集的各解,选择最优解;评价得到Ui最高的则为最优解;本实施例中优化程序逻辑图如图3所示。
通过非支配遗传算法得到该工艺运行参数的非劣解集,具体结果如表6和图4所示。
表6.该工艺运行参数的非劣解集
式中:为第i个评价对象与最大值的距离,为第i个评价对象与最小值的距离,Ui为第i个评价对象的归一化得分,Bij为第i个评价对象的第j目标的值,为评价对象的第j目标的理想值,为评价对象的第j目标的不理想值,m为目标个数。
根据上述优劣解距离法评价非劣解集的各解,各解的评分如表7所示。
表7.该非劣解集中各解的评分
评分最高的运行参数方案是2号,其详细的运行参数如表8所示。
表8.2号方案的运行参数
优化后的压缩机C-1、压缩机C-2的出口压力下降,接近最低下限。压缩机C-3的出口压力略有提升;混合冷剂的流量增大、冷箱出口温度变低。作为优化目标的系统效率和LNG热经济学成本得到了改善。系统效率由31.85%升高到35.81%,提高了3.96%。LNG热经济学成本由91828.25元/h降低到91374.13元/h,降低了454.12元/h。
Claims (6)
5.根据权利要求4所述的一种天然气液化工艺运行参数优化方法,其特征在于,所述步骤4中优化过程约束条件如下:
以板式换热器最小传热温差大于3℃为约束条件,采用罚函数将不满足热约束条件的种群及目标函数值淘汰:
JP=f(X)·e5h(t)
h(t)=Max(0,3-Δtmin,H-1)+Max(0,3-Δtmin,H-2)
式中:JP为惩罚后的目标函数值,f(X)为目标函数值,h(x)为惩罚系数变量,Max为区间内的最大值的函数,Δtmin,H-1为换热器H-1的最小传热温差,Δtmin,H-2为换热器H-2的最小传热温差。
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