Process variables data from the lean vapour compressor campaign at Technology Centre Mongstad

The lean vapor compressor (LVC) unit at Technology Centre Mongstad (TCM), Norway has been tested. The aim of this research has been to create knowledge on the process performance of LVC on the CO2 capture efficiency and energy profile of the TCM plant. The data presented in this paper is supplementary to the study “Results of the fourth Technology Centre Mongstad campaign: LVC testing” [1]. The dataset gives unique information on the LVC campaign in which 16 cases have been tested with various campaign process parameters such as LVC pressure, solvent flow, inlet flue gas CO2 concentration, and stripper pressure. Absorber and stripper process conditions were recorded during these tests and are presented.


Data
The data presented in this article is providing the supplementary information from the lean vapor compression (LVC) campaign at Technology Centre Mongstad, Norway. A detailed description of the LVC campaign is presented in the work by Fosbøl et al. [1]. The LVC campaign was performed in June 2018. The campaign was divided into two main phases a base case and a LVC test phase. Cases from 1A to 1F represent the base cases and the cases ranging from 2A to 2F are the LVC test phase. The process variables from the pilot campaign are shown in Table 1. The standard deviations given in the table are based on averaged raw data given over 5 min intervals. The table gives information such as the inlet conditions to absorber and stripper. It also provides details on temperatures around the main heat exchanger.
The absorber temperature profiles for the base cases are given in Tables 2 and 3. The stripper temperature profiles for the base and the LVC cases are listed in Tables 4 and 5 respectively.

Experimental design, materials, and methods
A lean vapor compressor (LVC) campaign was performed at Technology Centre Mongstad using 30 wt% aqueous monoethanolamine (MEA) and flue gas, with a CO 2 content of 3.5% supplied by the combined heat and power (CHP) plant at the nearby Equinor refinery.
The amine plant was designed and constructed by Aker Solutions and Kvaerner. The LVC compressor (Pinnacle LF2140 single stage) was manufactured by Sundyne Compressors. The packing height of absorber and stripper were 18 m and 8 m respectively. Both columns were packed with structured Flexipac 2X.
A simplified process flow diagram illustrating the TCM amine plant configuration with CCGT based CHP flue gas feed, CO 2 recycle, and the large stripper designed for high CO 2 content flue gas is exemplified in Fig. 1. This set-up was utilized in the LVC test campaign.
Specifications Table   Subject Renewable Energy, Sustainability and the Environment Specific subject area Carbon Capture and Storage  Type of data  Tables  How data were acquired The data were acquired through the comprehensive SCADA system for the process plant. This include information from flow, temperature, pressure transmitters. Samples were taken in order to determine CO 2 loading through standardized methods. Data format Calculated steady state data based on averaged raw data over 5 minutes intervals Parameters for data collection The data were collected under standard operational conditions Description of data collection The data were collected under standard operational conditions Data          The CHP flue gas is conditioned in a direct contact cooler (DCC) after being enriched with CO 2 from the CO 2 product recycle stream. The conditioned flue gas is contacted counter-currently with amine solvent in the absorber. CO 2 is absorbed, yielding a solvent rich in CO 2 and a depleted flue gas with low CO 2 content. The depleted flue gas is released to the atmosphere after being conditioned in the water wash sections. The rich solvent loaded with CO 2 is pre-heated in the lean/rich cross heat exchanger before entering the stripper column. Additional heat is supplied by steam to the stripper reboiler in  order to desorb CO 2 and regenerate the solvent. The product CO 2 gas is released to the atmosphere, while the regenerated lean solvent is pumped back to the absorber via the lean/rich cross heat exchanger and the lean cooler. The amine plant is described in detail elsewhere [2e4].
The large stripper section designed for high CO 2 content flue gas is also equipped with an optional lean vapor compressor system, as illustrated in Fig. 1. In the LVC system (see Fig. 2), hot lean amine exiting the stripper bottom is throttled to a lower pressure and fed to a flash drum generating vapor. The vapor is compressed and returned to the stripper bottom, while the lean amine is circulated back to the lean amine solvent loop. The LVC has for safety reasons a built-in anti-surge option which is used when flow to the compressor is below design flow. The control of the LVC automatically recycles gas in order to maintain correct compressor operation.
The superheated steam provides additional energy for regeneration of solvent in the stripper, which has the potential of reducing consumption of low pressure steam in the stripper reboiler. Table 6 gives an overview of the adjustable process parameters applied in the LVC campaign at TCM. The LVC campaign was operated in a way that only one parameter was adjusted at a time allowing the plant to reach steady state faster. The campaign was performed with case durations between 3 and 24 hours out of which 1e8 hours were used for calculation of average steady state conditions.