The energy system is changing and is becoming more important in the spatial-economic development of the Netherlands. The current energy planning system is insufficiently equipped to deal with these changes. Therefore transmission and distribution system operators, provinces and municipalities have come together in the process of integraal programmeren to aid in making democratic legitimate decisions on energy infrastructure investments.
The process of integraal programmeren can play a role in mitigating uncertainties in the energy system by accumulating knowledge on developments, drawing up an energy vision and assisting in making decisions. Market parties are now minimally involved in the process, while they are essential in the realisation of sustainable developments. This dependency can lead to uncertainties in the process of integraal programmeren.
This research aims to construct the contours of design guidelines which could serve as a basis for the collaboration process for integraal programmeren to better suit the uncertainties in the process. A theoretical framework and a case study are used to analyse both theoretical and practical perspectives on integraal programmeren.
Integraal programmeren is a process mainly between provinces, municipalities and system operators of electricity, heat and hydrogen networks. The actors work together in a network of interdependencies and work together to achieve shared goals. The focus of the actors has mostly been on the uncertainties in the process itself since it is all very new. However, it is recognised that uncertainties stemming from the uncertainties with market parties can eventually have a big, unforeseen influence on the regional energy system. Therefore it is important to take them into account.
This research described a novel relationship between uncertainties and process design. Uncertainties among market parties can be dealt with in the process of integraal programmeren in two ways. 1.) By obtaining more information about it, or in the case when this information does not exist or is unavailable, 2.) by formulating a shared vision. Involving market parties, more actively than they are involved now, can help with these mechanisms. Involving new actors in the process leads to more complexity and new process rules are needed. Designing a process such as integraal programmeren is not a linear process, during the process, the design requirements can change based on new situations and ideas and thus it calls for flexibility, while still keeping its credibility.

The steel making industry is highly energy intensive and a great contributor of greenhouse gas (GHG) emissions. It generated between 7% and 9% of direct emissions from the global use of fossil fuels in 2017 [1]. Gas emissions in an integrated steel mill (ISM) arise mainly from three streams: coke oven gas (COG), blast furnace gas (BFG) and basic oxygen furnace gas (BOFG).

This study focuses on the short term solutions to become a carbon neutral steelmaker where blast furnaces (BF) and basic oxygen furnaces (BOF) are still a fundamental part of the steel making process. The Rectisol® process is used to capture CO2 from the works arising gases (WAGs) of an ISM and to generate syngas which can be used as a chemical building block to produce liquid fuels among others.

The Rectisol® wash is a patented process by Air Liquide and Linde which uses chilled MeOH as a solvent. Both processes were first validated against stream data provided by the patents. PC-SAFT EOS was used to simulate the purification plant because of its strong theoretical foundation and its ability to adapt the parameters to predict component behaviour. Various binary interaction parameters proposed in literature were used to simulate the purification plants. From these simulations, it was found that the standard binary interaction parameters with the adjusted parameter for H2S-CH3OH, as proposed by Sun et al. [2], showed the best results.
The configurations of Air Liquide and Linde were used as base configuration to clean the feed stream. From these simulations, it was observed that in both configurations large portions of CO2 are lost in the stripping process of both configurations. Enhanced CCS configurations were investigated to increase the CO2 recovery of both configurations. The desorption of CO2 was altered by introducing multiple intermediate flashes to increase the desorption of CO2. Without optimisation, the downstream constraint for the CO2-rich stream of 95% CO2 content was almost met in the Linde configuration and requires further upgrading in the Air Liquide configuration. The decision was made to use the Linde enhanced CCS configuration as a base configuration since this would solely require a change in operating conditions to meet the downstream CO2 requirement of 95% content in the CO2-rich stream.

HCN and H2O require a seperate wash to avoid accumulation in the main wash. To treat these components together with H2S and COS, two pre-wash configurations combined with the Linde enhanced CCS configuration were looked into. A pre-wash configuration with a separate absorber column and dividing wall column (DWC) and a pre-wash configuration with a separate absorber column and rectifier with purge were examined. Both configurations meet the downstream requirements for the purified gas stream and CO2-rich stream. The main difference between the two configurations is the difference in thermal utility consumption and make-up MeOH. The decision was made to move forward with the pre-wash integrated configuration comprising of a rectifier and purge since additional make-up MeOH would be more cost-effective. The energy recovery method proposed by Linnhoff [3] was used to identify any potential energy saving of the purification plant. A heat exchanger network was designed which reduced the cooling duty by 57% to 54,9 MWth and the reboiler duty by 50,6% to 26,8 MWth. Finally, an economic evaluation was made of the final energy integrated configuration. Equivalent annual cost and operating expenditures of the purification plant were estimated at €12.32m and €51.13m respectively per year. This gives a cost per ton captured CO2 of €37,87.