Energy Requirement For Solvent Regeneration Research Articles

Synthesis of refinery desulfurization solvent network with multi-stage solvent regeneration

Increasing process of sour crude oil and demand of low-sulfur oil products expand the desulfurization units in refineries, which raises the desulfurization solvent circulation as well as the energy cost for solvent regeneration. In this work, synthesis of desulfurization solvent network with multi-stage solvent regeneration is investigated to reduce the energy cost. Firstly, this work presents superstructures for desulfurization solvent network with regeneration considering one-stage structure, two-stage cascaded structure, and two-stage parallel structure, respectively. Next, mathematical models for the three cases are formulated as nonlinear programming problems where the objective function aims to minimize the total energy consumption. Finally, a case study is conducted to illustrate the proposed method. The results show that the two-stage structures reduce more energy costs than the one-stage structure by 7.65% and 8.46%, respectively, which means that two-stage regeneration is more attractive. Besides, the parallel structure is better than the cascaded structure, because the energy requirement for solvent regeneration is more sensitive to the outlet concentration of hydrogen sulfide than the inlet concentration.

Recent Advances in Small-Scale Carbon Capture Systems for Micro-Combined Heat and Power Applications

To restrict global warming and relieve climate change, the world economy requires to decarbonize and reduce carbon dioxide (CO2) emissions to net-zero by mid-century. Carbon capture and storage (CCS), and carbon capture and utilization (CCU), by which CO2 emissions are captured from sources such as fossil power generation and combustion processes, and further either reused or stored, are recognized worldwide as key technologies for global warming mitigation. This paper provides a review of the latest published literature on small-scale carbon capture (CC) systems as applied in micro combined heat and power cogeneration systems for use in buildings. Previous studies have investigated a variety of small- or micro-scale combined heat and power configurations defined by their prime mover for CC integration. These include the micro gas turbine, the hybrid micro gas turbine and solid-state fuel cell system, and the biomass-fired organic Rankine cycle, all of which have been coupled with a post-combustion, amine-based absorption plant. After these configurations are defined, their performance is discussed. Considerations for optimizing the overall system parameters are identified using the same sources. The paper considers optimization of modifications to the micro gas turbine cycles with exhaust gas recirculation, humidification, and more advanced energy integration for optimal use of waste heat. Related investigations are based largely on numerical studies, with some preliminary experimental work undertaken on the Turbec T100 micro gas turbine. A brief survey is presented of some additional topics, including storage and utilization options, commercially available CC technologies, and direct atmospheric capture. Based on the available literature, it was found that carbon capture for small-scale systems introduces a large energy penalty due to the low concentration of CO2 in exhaust gases. Further development is required to decrease the energy loss from CC for economic feasibility on a small scale. For the micro gas turbine, exhaust gas recirculation, selective gas recirculation, and humidification were shown to improve overall system economic performance and efficiency. However, the highest global efficiencies were achieved by leveraging turbine exhaust waste heat to reduce the thermal energy requirement for solvent regeneration in the CC plant during low- or zero-heating loads. It was shown that although humidification cycles improved micro gas turbine cycle efficiencies, this may not be the best option to improve global efficiency if turbine waste heat is properly leveraged based on heating demands. The biomass-organic Rankine cycle and hybrid micro gas turbine, and solid-state fuel cell systems with CC, are in early developmental stages and require more research to assess their feasibility. However, the hybrid micro gas turbine and solid-state fuel cell energy system with CC was shown numerically to reach high global efficiency (51.4% LHV). It was also shown that the biomass-fired organic Rankine cycle system could result in negative emissions when coupled with a CC plant. In terms of costs, it was found that utilization through enhanced oil recovery was a promising strategy to offset the cost of carbon capture. Direct atmospheric capture was determined to be less economically feasible than capture from concentrated point sources; however, it has the benefit of negative carbon emissions.

Nonlinear Model Predictive Control of Post-combustion CO2 Capture Process for Flexible Operation

A large amount of energy requirement for solvent regeneration is a major barrier to the widespread adoption of amine-based post-combustion CO2 capture (PCC). Flexible operation is one of the ways to lower the energy penalty by responding to changes in economic factors like the energy price. However, for effective implementation of flexible operation strategies, it is necessary to identify the most economic operating condition under various potential scenarios and to establish an appropriate control strategy to operate the process. As flexible operation will inherently involve a large operating envelope, we investigate the use of nonlinear model predictive control (NMPC) technology. To circumvent the problem of solving a large-scale nonlinear programming problem online, a simpler NARX model is identified and used. With the NARX model, an offset-free NMPC is designed and simulated under various dynamic scenarios. The developed NARX-based NMPC shows satisfactory control performance, stabilizing the CO2 capture rate faster than LMPC by 60-100 min.

Amino-2-methyl-1-propanol-based Post-combustion Capture Process with Solvent Storage for Decarbonisation of Natural Gas Combined Cycle Power Plant

Meeting the Paris Agreement targets is challenging because a high proportion of the global energy generation is based on the combustion of fossil fuels. Carbon capture and storage is expected to provide a cost-effective means of reducing CO2 emission from the fossil fuel-fired power sector. In recent times, natural gas has become the most preferred fossil fuel due to the low prices and low carbon emissions associated with its combustion in comparison to coal and other fossil fuels. Among the commonly employed carbon capture technologies, amine solvent-based post-combustion CO2 capture is known as an appropriate option for retrofitting the natural gas combined cycle (NGCC) power plants. However, the energy requirement for solvent regeneration remains a major challenge due to less electricity sold and causing an energy penalty. One way to reduce this parasitic load on the NGCC is to use alternative solvents with superior performance than the widely used monoethanolamine (MEA). Another way to address this challenge is the addition of the solvent storage system, which enables the energy penalty to be deferred until times of low electricity prices. However, investing in solvent storage will only be profitable if there is a substantial difference between the high and the low electricity prices. In this work, a process model of the NGCC with the CO2 capture plant using 2-amino-2-methyl-1-propanol (AMP) is used to evaluate the feasibility of solvent storage and its effect on economic performance. The net efficiency of the process with solvent storage was obtained to be 46.7% compared to 45.6% LHV basis for the process without solvent storage. Despite this lower efficiency, the process with solvent storage was found to increase the profit by approximately 1% compared to that without solvent storage. Thus, this would result in a higher profit than the power plant if the carbon tax exceeds €25/tCO2.

Post-combustion carbon capture for tank to propeller via process modeling and simulation

The International Maritime Organization (IMO) has issued a long-term sustainable strategy to gradually phase out the major ship-related sources of greenhouse gas emissions. While the post-combustion carbon capture has been well investigated for onshore plants, the maritime carbon capture system is still in an early stage due to its unique characteristics and design limitations. Aiming at providing a holistic way to find the most efficient and sustainable PCC solution for an LNG tanker, this work proposed a system of the tank to propeller post-combustion carbon capture which integrates ship engine process modeling with chemical absorption/desorption process modeling techniques. A rate-based aqueous monoethanolamine (MEA) process model was developed and validated, then scaled up and modified to capture CO2 from the flue gas. To increase the carbon capture efficiency and decrease the energy penalty, this work provided detailed steps for process model development covering innovative absorber/stripper design under variation of solvents, packed type, and liquid to gas ratio. This work also included a thorough sustainability evaluation based on emission reduction efficiency, energy penalty, and carbon cyclic capacity among two single aqueous amines, MEA and diisopropanolamine (DIPA), and one blended amine with a promoter, methyldiethanolamine (MDEA) with piperazine (PZ). Although DIPA presented a better performance on energy requirement for solvent regeneration, the blended amine was the optimal solvent to meet the requirement of the IMO carbon abatement strategy. Compared to the seven molality MEA, the MDEA-PZ option could capture more than 57 % CO2 while around 25 % specific reboiler duty can be saved.

New Technologies for Energy Reduction in Biogas Upgrading

Biogas has a significant potential for commercial growth in the energy sector. However, CO2 and other impurities should be removed to produce a higher content of CH4 called biomethane. This process is known as biogas upgrading and the technology adopted is called CO2 Capture. This study focuses on the chemical absorption-desorption process using Mono-ethanolamine (MEA). One of the main disadvantages of this process is the high energy requirement for solvent regeneration. Therefore, new additives which may enhance the performance of the technology while reducing the energy requirement, are being ventured into. To calculate the performance of CO2 capture by the aqueous mixture of MEA and the energy reducing additives, simulators need to use accurate thermodynamic models, capable of calculating phase equilibria and thermal properties of the system. This work shows a brief validation of the existing model parameters in the extended UNIQUAC relevant to the complex mixtures of the species involved.

Modification of postcombustion CO2 capture process: A techno‐economic analysis

AbstractPostcombustion CO2 separation using aqueous amine solution has a great potential to minimize CO2 emissions but is expensive due to huge energy requirement for solvent regeneration. Several structural modifications can be implemented to minimize the regeneration energy requirement and optimize the energy efficiency. In this study, we evaluated the techno‐economic benefits of three stripping modifications, namely lean vapor compression (LVC), stripper overhead exchanger (SOE), and an advanced hybrid configuration (LVCSOE) in a single flowsheet aimed at reducing the energy consumption of CO2 separation process using 30 wt.% monoethanolamine (MEA) solution. All the configurations were simulated using Aspen Plus® rate‐based modeling, while capital investment was evaluated using Aspen Economic Analyzer®. All the modifications reduced the energy consumption and showed economic benefit compared to the base case. The optimal configuration was LVCSOE, which reduced the energy requirement for solvent regeneration and the CO2 capture cost by 18% and 5.3%, respectively, and can save 5.4 million USD annually. Additionally, sensitivity analysis of economic variables suggested that CO2 capture cost is more sensitive to regeneration steam cost than any other economic parameter. Furthermore, the effect of regeneration steam cost revealed that the implementation of an advanced process configuration can result in higher net savings as compared to the base case at high fuel price. © 2020 Society of Chemical Industry and John Wiley & Sons, Ltd.

Techno-economic analysis of advanced stripper configurations for post-combustion CO2 capture amine processes

Abstract In chemical absorption processes for carbon capture, one of the main technical challenges is to overcome its high energy requirement for solvent regeneration. A techno-economic analysis was conducted on various modified carbon capture processes using a 30 wt% monoethanolamine (MEA) solvent. Five configurations of a stripper modified with two or more components of lean vapor compression (LVC), cold solvent split (CSS), and stripper overhead compression (SOC) were designed. Each configuration aimed to reduce the total equivalent work (Wtotal) via heat integration between the condenser and reboiler. The performance was compared with those of conventional and single-modified configurations based on 90% carbon capture from a coal-fired power plant. Compared with the reference results of a pilot plant operation, the thermal energy required from a reboiler could be reduced by 8.1–32.8% through the modified configurations. The developed combined configurations suggested that the Wtotal could be reduced by up to 9.0%, and the operating cost could be saved by up to 10.2%. Although an increase in capital costs is inevitable for process modifications, the advanced configurations can be considered as an alternative to the reference process because energy and operating costs are reduced.

A multiobjective experimental based optimization to the CO2 capture process using hybrid solvents of MEA-MeOH and MEA-water

To achieve the reduction of total energy consumption of CO2 capture without the major drawbacks of conventional amine solvents, the superior performance of a blended physical-chemical solvent, MEA-MeOH, was experimentally compared with that of MEA aqueous absorbent in lab-scale absorption/desorption towers, equipped with stainless steel pall ring packings. Considering the typical industrial requirements, the main operating variables accounted for each solvent were the operating temperature (35–55 °C), amine concentration (15–30 wt%), gas flow rate (50–100 l/min), liquid flow rate (0.75–1.25 l/min), CO2 concentration in the inlet gas (5–15 mol %), and the reboiler heat duty (1.4–2.2 kW). Response surface methodology was applied to give a quadratic mathematical model for obtained empirical volumetric overall mass transfer coefficients (KGaV). Based on the drastic increase of the energy requirement for solvent regeneration, a multiobjective optimization framework has been made to achieve the maximum desirable values for the KGaV, and the absorption percentage (Φ) with the minimum energy consumption (Ω). It was suggested that under the optimum operating condition, adding methanol to an aqueous MEA solution, reduces the regeneration energy consumption by 12%, while augmenting the CO2 absorption percentage (Φ) by 9.1%.

Review of liquid nano-absorbents for enhanced CO2 capture.

Liquid nano-absorbents have become a topic of interest as a result of their enhanced mass-transfer performance for CO2 capture. They are believed to have revolutionized the conventional CO2 chemisorption process by largely improving CO2 capture kinetics and reducing the energy requirement for solvent regeneration. Two classes of nanomaterial-based CO2 capture absorbents, amine-based nanoparticle suspensions (nanofluids) and nanoparticle organic hybrid materials (NOHMs), have been developed, with significant progress achieved in recent decades. This review addresses two key questions for these two state-of-the-art nanomaterials: how are the physical and chemical properties of the prepared liquid nano-absorbents transformed relative to those of the base fluids? And how does the transformation of the properties affect the CO2 capture behavior? While the current synthesis procedure for liquid nano-absorbents is quite straightforward, more advanced synthesis methods for long-term nanoparticle stability have been suggested for the future. Nanofluids have been shown to increase the CO2 uptake by over 20% and the CO2 capture rate by 2-93% compared with the values observed with neat amine solvents. Nanoparticles with catalytic effects on CO2 capture can significantly increase the CO2 desorption rate by as high as 4000%. NOHMs exhibit the interesting feature of enhanced mass transfer in CO2 capture because of the unique pathway network that is created in them for CO2 to reach specific functional groups. NOHMs promise an effect of combined CO2 capture and conversion, and can be used especially as electrolytes for CO2 electro-reduction. However, there are still some challenges for the application of these materials in real life, such as poor stability and high viscosity. Therefore, efficient CO2 capture processes using these solvents need to be urgently developed and studied in the future.

Mass transfer performance for CO2 absorption into aqueous blended DMEA/MEA solution with optimized molar ratio in a hollow fiber membrane contactor

Combination N,N-dimethylethanolamine(DMEA) and monoethanolamine (MEA) may represent a potential absorbent for CO2 capture due to the high absorption rate, high cyclic CO2 capacity and low energy requirement for solvent regeneration. Both the absorption and regeneration performances for 2 kmol/m3 DMEA/MEA with molar ratios of 2.0:0.0, 1.5:0.5, 1.0:1.0, 0.5:1.5, and 0.0:2.0 were estimated in terms of the absorption rate, regeneration rate and cyclic CO2 capacity using an improved rapid screening method. The experimental results showed that the highest cyclic CO2 capacities (i.e. low energy requirement) for the cyclic reaction time of 30 min and 60 min were obtained both by 1.0 M DMEA + 1.0 M MEA solution, indicating the synergistic effects existing in CO2 absorption into DMEA/MEA solution. Additionally, the mass transfer performance of CO2 absorption into 1.0 M DMEA + 1.0 M MEA solution was investigated in a hollow fiber membrane contactor. The effects of key operational parameters such as liquid velocity, inlet gas flow rate, CO2 partial pressure, feed temperature range, CO2 lean loading, amine concentration and membrane contactor height on the CO2 flux and overall gas phase mass transfer coefficient were investigated. Furthermore, a developed correlation was successfully applied for the prediction of overall gas phase mass transfer coefficient (KG) for CO2 absorption into DMEA/MEA solution, with an average absolute relative deviation (AARD) of 8.31%. Thus, a potential absorbent (i.e. DMEA/MEA) for CO2 capture was proposed in this work.

Performance and Mechanism of Metal Oxide Catalyst-Aided Amine Solvent Regeneration

CO2 capture from flue gas using the amine-based post-combustion technique is costly because of the high energy requirement for solvent regeneration. The addition of catalyst to the regeneration step can overcome this drawback. In this study, we investigate the regeneration performance of CO2-rich MEA solution without and with two solid metal oxide catalysts—ZrO2 and ZnO—within a temperature range of 40–86 °C. The solvent regeneration performance was evaluated in terms of CO2 desorption rate, total amount of desorbed CO2, solvent cyclic capacity, and CO2-lean loadings achieved from the catalytic solutions in comparison with the noncatalytic MEA solution. To understand and support the obtained results BET, NH3–TPD, pyridine–FTIR, and 13C NMR characterization techniques are performed. The obtained results suggest that both catalysts are capable of optimizing the solvent regeneration by desorbing up to 32% greater amounts of CO2, improving the CO2 desorption rate up to 54%, and increasing the solvent cyclic c...

Improving the energy cost of an absorber-stripper CO2 capture process through economic model predictive control

Carbon dioxide (CO2) is the major source of greenhouse gas and its capture and recovery is the key to effective reduction of CO2 emissions. Optimization of the CO2 capture process plays a critical role in the reduction of energy cost. The current strategy only deals with the steady state optimization of the CO2 capture process but the CO2 concentration in the plant varies with time and as a result a dynamic study of the economic assessment will reflect the true cost better. The economic model predictive control (EMPC) that combines real-time economic process optimization and feedback control is applied to the optimization of CO2 capture process. The large energy requirement for solvent regeneration is optimized in dynamic settings. Unlike the conventional steady state consideration of the economic performance assessment, the proposed method allows the cost to be adjusted to the volatile market conditions that varies rapidly. Case studies are then presented to show the benefits of the EMPC optimization for CO2 capture process.

Economic model predictive control of an absorber-stripper CO2 capture process for improving energy cost

Carbon dioxide (CO2) is the major source of greenhouse gas and its capture and recovery is the key to effective reduction of CO2 emissions. Optimization of the CO2 capture plays a critical role in the reduction of energy cost. CO2 concentration in the plant varies with time and a dynamic study of the economic optimization reflects the true cost better when compared to the current strategy of the steady state optimization. The economic model predictive control (EMPC) that combines real-time economic process optimization and feedback control is applied to the optimization of CO2 capture process. The large energy requirement for solvent regeneration is optimized in dynamic settings. Unlike the conventional steady state consideration of the economic optimization, the proposed method allows the cost to be adjusted to the changing condition such as feed composition and utility cost. Case studies are then presented to show the benefits of the EMPC optimization for CO2 capture process.

Experimental and simulation study of a novel hybrid absorption and stripping membrane contactor for carbon capture

Abstract Physical absorption is a commercial technology for the capture of high concentration carbon dioxide and features low energy requirement for solvent regeneration. The application of physical absorption for the capture of low concentration carbon dioxide from fossil fuel power plants requires improvement in the absorption efficiency. A novel hybrid absorption/stripping membrane contactor (HASMC) with parallel and contiguous configurations is proposed and studied for carbon dioxide absorption by propylene carbonate. Employing parallel-type and contiguous-type HASMCs, the experimental results show substantial enhancement of absorption flux relative to pure absorption operation with an enhancement factor of 1.16–1.61 and 1.55–2.21, respectively. Simulation work reveals the concentration boundary layers in the liquid channel and explains the mechanisms of absorption enhancement for both configurations. Both experimental and simulation results show increase of absorption flux with the increase of liquid velocity, flue gas velocity and flue gas carbon dioxide concentration. This study has shown that HASMCs with contiguous configuration can be high efficiency membrane contactors.

CO2 capture using piperazine-promoted, aqueous ammonia solution: Rate-based modelling and process simulation

Due to the fast reaction rate of piperazine (PZ) with CO2, it has the potential to act as a promoter in aqueous ammonia (NH3)-based CO2 capture processes. We have developed a rigorous, rate-based model for the NH3–PZ–CO2–H2O system using Aspen Plus®, and validated the model against experimental results. Absorption and desorption processes were simulated under real flue gas conditions to gain a practical understanding of the behaviour and characteristics of interactions between PZ‐promoted NH3 solution and CO2. Adding PZ significantly increased the CO2 absorption rate in the NH3-based CO2 capture process via a fast reaction between PZ carbamate and CO2. The temperature along the column was higher than in the absence of PZ, and more free ammonia was released into the solution, which led to higher ammonia loss. Adding PZ also reduced the stripping heat, resulting in a smaller energy requirement for solvent regeneration.

Reduction of energy requirement of CO2 desorption from a rich CO2-loaded MEA solution by using solid acid catalysts

In this work, the regeneration of rich CO2-loaded monoethanolamine (MEA) solvent with two catalysts (e.g. SAPO-34 and SO42−/TiO2) was investigated in order to reduce the energy requirement for solvent regeneration. The regeneration behavior with and without catalyst of a 5M MEA solution with an initial CO2 loading of 0.5molCO2/mol amine at 96°C was studied to compare their CO2 desorption rate and heat duties. The results show that the two solid acid catalysts can reduce the heat duty for solvent regeneration and increase the CO2 desorption rate in comparison with blank test. The mechanism of CO2 desorption with catalyst in 5M MEA was proposed based on the result of catalyst characterization (e.g. N2 absorption/desorption experiment, Py-IR, NH3-TPD, FT-IR and XRD) to better understand the desorption process. The results indicate that SAPO-34 with the higher joint value of Brϕnsted/Lewis acid sites ratio (B/L) and mesopore surface area (MSA) shows the faster CO2 desorption rate and lower heat duty than SO42−/TiO2. Based on the experimental results, the addition of solid acid catalysts into amine solution could be considered as one of choices to reduce the heat duty for CO2 desorption from CO2-loaded amine solvent.

Thermodynamic modeling and uncertainty quantification of CO2-loaded aqueous MEA solutions

The accurate characterization of the thermodynamic models of a reactive solvent-based CO2 capture system is essential for adequately capturing system behavior in a process model. Moreover, uncertainty in these models can significantly affect simulation results, although it is often neglected. With this incentive, a model of thermodynamic properties, including vapor-liquid equilibrium (VLE), enthalpy, and solution chemistry, has been developed using a rigorous methodology for the aqueous monoethanolamine (MEA) system as a baseline. The final thermodynamic framework consists of both a deterministic and stochastic model. The deterministic model is developed by regressing parameters of the e-NRTL activity coefficient model in Aspen Plus® to VLE, heat capacity, and heat of absorption data while downselecting the model’s large parameter space through use of information-theoretic criteria. The stochastic model is developed through an uncertainty quantification (UQ) procedure, using the results of the deterministic regression to determine a prior parameter distribution. This prior distribution and the experimental VLE data are used to derive a posterior distribution through Bayesian inference, which is used to represent the final stochastic model. A reaction model in which the kinetics are written in terms of the reaction equilibrium constants, to ensure consistency with the thermodynamics model, is developed. These new thermodynamic and reaction models are incorporated into an existing MEA system process model from the open literature, and the prior and posterior parameter distributions are propagated through the models. This provides valuable insight into the extent to which uncertainty in thermodynamic models affects key process variables, including CO2 capture efficiency and energy requirement for solvent regeneration.

Phase separation characteristics in biphasic solvents based on mutually miscible amines for energy efficient CO2 capture

One of the challenges with regard to the aqueous amine-based CO2 capture process is the considerable energy requirement for solvent regeneration. To overcome this challenge, a biphasic solvent was employed in this study. Here, the phase separation behavior of amine blends depending on the characteristic structures of the solvent component was investigated using a turbidity measurement apparatus. Amines were classified as (1) primary/secondary amines or tertiary/sterically hindered amines depending on the CO2 reaction species, such as carbamate and bicarbonate (2) alkyl and alkanolamines, depending on the presence of a hydroxyl group, (3) chain and cyclic amines, and (4) mono- and polyamines depending on the molecular structure. Easy phase separation occurred in solvent blends containing polyamines such as DETA (diethylenetriamine), TETA (triethylenetetramine), and DEEA (2-(diethylamino) ethanol). The types with the greatest potential were the DETA/DEEA blended solvents. A phase separation could be determined based on the difference in the reaction rate with CO2 and the low solubility between the carbamate species of DETA and DEEA.

Life cycle assessment of carbon capture and utilization from ammonia process in Mexico

Post-combustion CO2 capture (PCC) of flue gas from an ammonia plant (AP) and the environmental performance of the carbon capture utilization (CCU) technology for greenhouse gas (GHG) emissions to an enhanced oil recovery (EOR) system in Mexico was performed as case study. The process simulations (PS) and life cycle assessment (LCA) were used as supporting tools to quantify the CO2 capture and their environmental impacts, respectively. Two scenarios were considered: 1) the AP with its shift and CO2 removal unit and 2) Scenario 1 plus PCC of the flue gas from the AP primary reformer (AP-2CO2) and the global warming (GW) impact. Also, the GW of the whole of a CO2-EOR project, from these two streams of captured CO2, was evaluated. Results show that 372,426 tCO2/year can be PCC from the flue gas of the primary reformer and 480,000 tons/y of capacity from the AP. The energy requirement for solvent regeneration is estimated to be 2.8 MJ/kgCO2 or a GW impact of 0.22 kgCO2e/kgCO2 captured. GW performances are 297.6 kgCO2e emitted/barrel (bbl) for scenario one, and 106.5 kgCO2e emitted/bbl for the second. The net emissions, in scenario one, were 0.52 tCO2e/bbl and 0.33 tCO2e/bbl in scenario two. Based on PS, this study could be used to evaluate the potential of CO2 capture of 4080 t/d of 4 ammonia plants. The integration of PS-LCA to a PCC study allows the applicability as methodological framework for the development of a cluster of projects in which of CO2 could be recycled back to fuel, chemical, petrochemical products or for enhanced oil recovery (EOR). With AP-2CO2, “CO2 emission free” ammonia production could be achieved.