双回流变压吸附高效分离CO/H2制备高纯H2和CO

doi:10.11949/0438-1157.20240535

摘要/Abstract

摘要：

双回流（DR）变压吸附（PSA）工艺具有不受压力比影响的优势，有望突破传统变压吸附（PSA）的热力学限制同时获得两种高纯气体。本工作基于两塔四步DR PSA工艺，分别考察了活性炭（AC）、13X和5A分子筛复合吸附剂以及Cu（I）/AC单吸附剂的分离效果，实现了同时制备高纯H₂和CO产品。利用Aspen Adsorption模拟平台开发了一个由质量、动量和能量平衡方程组成的非等温吸附模型，并通过固定床吸附实验验证了模型的可靠性。结果表明，AC、13X和5A分子筛复合吸附剂的DR PSA工艺分离效率欠佳，但表现出更强的CO解吸能力；而单独以Cu（I）/AC为吸附剂，可以显著提升分离效率，即以CO/H₂=0.5/0.5（体积比）合成气为原料，获得纯度>99.999%的H₂产品，其中CO含量<0.20 mL/m³，收率达96.69%；同时CO产品纯度>97.00%，收率达99.16%。增大轻、重组分回流比可以进一步提高H₂和CO产品气的纯度。

关键词: 双回流, 变压吸附, 一氧化碳, Cu（I）/AC, 数值模拟

Abstract:

The dual-reflux pressure swing adsorption (DR PSA) process has the advantage of without being affected by pressure ratio, and is expected to break through the thermodynamic limitations of traditional PSA while obtaining two types of high-purity gases. In this work, based on the two-bed four-step DR PSA process, we investigated the separation effects of activated carbon (AC), 13X and 5A molecular sieve composite adsorbents, and Cu(I)/AC single adsorbent, achieving the simultaneous preparation of high-purity H₂ and CO products. A non-isothermal adsorption model consisting of mass, momentum and energy balance equations was developed using the Aspen Adsorption simulation platform, and its reliability was verified through fixed-bed adsorption experiments. The results demonstrated that the DR PSA process with AC, 13X, and 5A molecular sieve composite adsorbents exhibited unsatisfactory separation efficiency, but exhibited stronger CO desorption ability; using Cu(I)/AC alone as the adsorbent can significantly enhance the separation efficiency, that is, using CO/H₂=0.5/0.5 (volume ratio) synthesis gas as the raw material, H₂ product with a purity of>99.999% could be obtained, the CO content is<0.20 mL/m³, and the yield is 96.69%. At the same time, the purity of CO product attains >97.00%, and the yield reaches 99.16%. Increasing the reflux ratio of light and heavy components could further improve the purity of H₂ and CO product gases, respectively.

Key words: dual-reflux, pressure swing adsorption, carbon monoxide, Cu(I)/AC, numerical simulation

中图分类号:

TQ028.1

郭强, 肇启东, 肖永厚. 双回流变压吸附高效分离CO/H₂制备高纯H₂和CO[J]. 化工学报, DOI: 10.11949/0438-1157.20240535.

Qiang GUO, Qidong ZHAO, Yonghou XIAO. Preparation of high-purity H₂ and CO by efficient separation of CO/H₂ using dual-reflux pressure swing adsorption process[J]. CIESC Journal, DOI: 10.11949/0438-1157.20240535.

图/表 17

图1 CO中试穿透实验装置示意图

Fig.1 Schematic diagram of pilot CO adsorption breakthrough experimental device

表1 吸附床的性质和操作条件

Table 1 Properties of the adsorption bed and operating conditions

Parameters	AC/13X/5A	Cu(I)/AC	Units
Height of adsorbent layer	0.50/0.50/0.80	2.0	m
Diameter of adsorbent layer	0.13	0.20	m
Thickness of bed wall	0.0050	0.0020	/
Inter-particle voidage	0.43/0.35/0.35	0.35	/
Intra-particle voidage	0.61/0.65/0.65	0.33	/
Bulk solid density of adsorbent	708.00/851.29/715.70	625.00	kg/m³
Adsorbent particle radius	2.0	1.4	mm
Feed gas pressure	5.0	5.0	bar
Feed flow rate	33.33	33.33	SLPM

图2 各组分在AC、13X、5A和Cu(I)/AC上的吸附等温线拟合曲线

Fig.2 Fitting curves of adsorption isotherms for each component over AC, 13X, 5A and Cu(I)/AC

表2 DR PSA模型中使用的方程

Table 2 The equations employed in DR PSA model

Model equation	Expression	Equation
Mass balance	$- ε b D a x, i ∂ 2 c i ∂ z 2 + ε b ∂ v g c i ∂ z + ε b + 1 - ε b ε p ∂ c i ∂ t + ρ s 1 - ε b ∂ q i ∂ t = 0$	(1)
Energy balance	Gas phase $- ε b k g ∂ 2 T g ∂ z 2 + C v g v g ρ g ∂ T g ∂ z + ε b C v g ρ g ∂ T g ∂ t + P ∂ v g ∂ z + h f a p T g - T s + 4 h w T g - T 0 D b = 0$	(2)
	Solid phase $- k s ∂ 2 T s ∂ z 2 + C p s ρ s ∂ T s ∂ t + ρ s ∑ i = 1 n C p a, i q i ∂ T s ∂ t + ρ s ∑ i = 1 n (∆ H i ∂ q i ∂ t) - h f a p T g - T s = 0$	(3)
	Bed wall $k w ∂ 2 T w ∂ z 2 + C p w ρ w ∂ T w ∂ t - h w 4 D b D b + W t 2 - D b 2 T g - T w + h a m b 4 D b + W t 2 D b + W t 2 - D b 2 T w - T a m b = 0$	(4)
	$N u f = 2 + 1.1 P r 1 / 3 R e 0.6$	(5)
	$N u w = 12.5 + 0.048 R e$	(6)
	$N u 0 = 0.1 R a 1 / 3$	(7)
Momentum balance	$- ∂ P ∂ z = 150 μ 1 - ε b 2 ε b 3 2 r p ψ 2 v g + 1.75 1 - ε b 2 r p ψ ε b 3 ρ g v g v g$	(8)
LDF	$∂ q i ∂ t = k L D F, i (q i * - q i)$	(9)
LDF	$k L D F, i = 15 D p, i R p 2$	(10)
Ideal gas law	$P V i = n i R T$	(11)

表2 DR PSA模型中使用的方程

Table 2 The equations employed in DR PSA model

Model equation	Expression	Equation
Mass balance	$- ε b D a x, i ∂ 2 c i ∂ z 2 + ε b ∂ v g c i ∂ z + ε b + 1 - ε b ε p ∂ c i ∂ t + ρ s 1 - ε b ∂ q i ∂ t = 0$	(1)
Energy balance	Gas phase $- ε b k g ∂ 2 T g ∂ z 2 + C v g v g ρ g ∂ T g ∂ z + ε b C v g ρ g ∂ T g ∂ t + P ∂ v g ∂ z + h f a p T g - T s + 4 h w T g - T 0 D b = 0$	(2)
	Solid phase $- k s ∂ 2 T s ∂ z 2 + C p s ρ s ∂ T s ∂ t + ρ s ∑ i = 1 n C p a, i q i ∂ T s ∂ t + ρ s ∑ i = 1 n (∆ H i ∂ q i ∂ t) - h f a p T g - T s = 0$	(3)
	Bed wall $k w ∂ 2 T w ∂ z 2 + C p w ρ w ∂ T w ∂ t - h w 4 D b D b + W t 2 - D b 2 T g - T w + h a m b 4 D b + W t 2 D b + W t 2 - D b 2 T w - T a m b = 0$	(4)
	$N u f = 2 + 1.1 P r 1 / 3 R e 0.6$	(5)
	$N u w = 12.5 + 0.048 R e$	(6)
	$N u 0 = 0.1 R a 1 / 3$	(7)
Momentum balance	$- ∂ P ∂ z = 150 μ 1 - ε b 2 ε b 3 2 r p ψ 2 v g + 1.75 1 - ε b 2 r p ψ ε b 3 ρ g v g v g$	(8)
LDF	$∂ q i ∂ t = k L D F, i (q i * - q i)$	(9)
LDF	$k L D F, i = 15 D p, i R p 2$	(10)
Ideal gas law	$P V i = n i R T$	(11)

表3 AC、13X和5A的扩展型Langmuir吸附模型拟合参数

Table 3 Fitting parameters of extended Langmuir adsorption models for AC， 13X and 5A

Adsorbent	Parameters	H₂	Ar	CO
AC	q_m(mmol∙g^-1)	10.68	7.00	6.82
	b₀(bar^-1)	2.16E-5	1.76E-4	9.05E-6
	ΔH/kJ∙mol^-1	-12.84	-13.53	-22.58
13X	q_m(mmol∙g^-1)	6.50	4.41	3.18
	b₀(bar^-1)	1.33E-4	2.92E-4	8.49E-5
	ΔH/kJ∙mol^-1	-8.00	-11.00	-21.00
5A	q_m(mmol∙g^-1)	1.15	4.24	2.24
	b₀(bar^-1)	2.82E-4	1.67E-4	6.14E-6
	ΔH/kJ∙mol^-1	-9.23	-13.30	-29.77

表4 Cu（I）/AC的扩展型Langmuir吸附模型拟合参数

Table 4 Fitting parameters of extended Langmuir adsorption model for Cu（I）/AC

Adsorbate	H₂	Ar	CO	CH₄	N₂	CO₂
q_m(mmol∙g^-1)	38.87	6.56	2.00	3.23	7.18	5.38
b₀(bar^-1)	1.0E-5	1.8E-4	1.0E-5	5.0E-5	1.9E-5	7.5E-6
ΔH/kJ∙mol^-1	-8.50	-13.74	-31.45	-20.60	-15.87	-26.83

图3 在Aspen Adsorption平台上构建的DR PSA模型图

Fig.3 Constructed DR PSA model based on the Aspen Adsorption platform

图4 DR PSA工艺半个周期的流程示意图

Fig.4 Schematic diagram of the DR PSA process for half a cycle

表5 DR PSA工艺循环时间表

Table 5 Cycle schedule of DR PSA process

Duration/s	100	20	100	20
Bed1	AD	VU	PU	PR
Bed2	PU	PR	AD	VU

图5 不同平衡气对CO穿透曲线的影响

Fig.5 The influence of different equilibrium gases on CO breakthrough curves

图6 一个循环周期内床层压力与温度分布

Fig. 6 Pressure and temperature distribution across the bed within one cycle

图7 一个循环周期内各步骤结束后AC、13X和5A复合吸附剂和Cu(I)/AC吸附床内CO轴向浓度分布

Fig. 7 Axial concentration distribution of CO in AC, 13X and 5A composite adsorbent and Cu(I)/AC adsorption beds after each step within a cycle

图8 不同轻重回流比对产品气纯度的影响（AC、13X和5A分子筛复合吸附剂和Cu(I)/AC单吸附剂床）

Fig. 8 The influence of different light to heavy reflux ratios on the purity of product gas on AC, 13X and 5A composite and Cu(I)/AC adsorbents

图9 不同轻重回流比对AD步骤结束后轴向CO负载量的影响

Fig. 9 The effect of different light to heavy reflux ratios on axial CO loading amounts after AD step

图10 不同进料气浓度对Cu(I)/AC床产品气纯度的影响

Fig. 10 The influence of different feed gas concentrations on the purity of product gas in Cu(I)/AC adsorbent bed

图11 多组分竞争吸附条件下H2/CO/CO2/CH4/N2合成气各循环步骤结束时的固相浓度分布

Fig. 11 Solid phase concentration distribution at the end of each cycle of H2/CO/CO2/CH4/N2 synthesis gas under multi-component competitive adsorption conditions

图12 不同进料位置对AD步骤结束后各组分固相浓度分布的影响

Fig. 12 Effects of different feed positions on the solid phase concentration distribution of each component after AD step

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双回流变压吸附高效分离CO/H₂制备高纯H₂和CO

Preparation of high-purity H₂ and CO by efficient separation of CO/H₂ using dual-reflux pressure swing adsorption process

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