Differential temperature control in heat-integrated pressure-swing distillation for separating azeotropes to deal with operating pressure fluctuations: Basic and explanatory data

This data article contains basic and explanatory data of “Differential temperature control in heat-integrated pressure-swing distillation for separating azeotropes to deal with operating pressure fluctuations” [1], including thermodynamic models, vapor-liquid equilibrium diagrams, steady-state flowsheets, temperature profiles of columns, description and setpoint units of the abbreviation of inventory control loops, description of control loops of control flowsheet with DTC, control flowsheets of PCTC and DTC, temperature and composition tuning constants, faceplates and flowsheet equations, dynamic performances and integral absolute errors. It also contains other important information.


Specifications
Chemical Engineering (General) Specific subject area Control of distillation processes for separating azeotropes Type of data Table  Image Graph Figure  How  Value of the Data • The data provide the insights on simulations of steady-state design and dynamic control of the investigated processes, including full information of thermodynamic models, vapor-liquid equilibrium diagrams, steady-state flowsheets, temperature profiles of columns, description and setpoint units of the abbreviation of inventory control loops, description of control loops of control flowsheet with DTC, control flowsheets of PCTC and DTC, temperature and composition tuning constants, faceplates and flowsheet equations, dynamic performances and integral absolute errors. • The data will be useful for the related researchers to understand how the simulations are established. • The data provide a baseline for exploring other potential aspects of DTC in future. Table 1 shows thermodynamic models of all the mixtures. Table 2 shows the description and setpoint units of the abbreviation of inventory control loops of the control faceplate.  2nd column sump level controller m a The 1st column represents the left column in the process flowsheet and the 2nd column represents the right column in the process flowsheet.  Table 3 shows controller tuning constants of the proposed control structure with DTC of PHI-PSD for separating the toluene/ethanol mixture. Table 4 shows controller tuning constants of the proposed control structure with PCTC of PHI-PSD for separating the toluene/ethanol mixture. Table 5 shows controller tuning constants of the proposed control structure with DTC of PHI-PSD for separating the acetone/methanol mixture. Table 6 shows controller tuning constants of the proposed control structure with PCTC of PHI-PSD for separating the acetone/methanol mixture. Table 7 shows controller tuning constants of the proposed control structure with DTC of FHI-PSD for separating the toluene/ethanol mixture.  Table 8 shows controller tuning constants of the proposed control structure with PCTC of FHI-PSD for separating the toluene/ethanol mixture. Table 9 shows controller tuning constants of the proposed control structure with DTC of FHI-PSD for separating the methanol/chloroform mixture. Table 10 shows controller tuning constants of the proposed control structure with PCTC of FHI-PSD for separating the methanol/chloroform mixture. Table 11 shows controller tuning constants of the proposed control structure with DTC of FHI-PSD for separating the ethyl acetate/ethanol mixture.  Table 12 shows controller tuning constants of the proposed control structure with PCTC of FHI-PSD for separating the ethyl acetate/ethanol mixture. Table 13 shows controller tuning constants of the proposed control structure with DTC of EA-PSD for separating the toluene/pyridine mixture. Table 14 shows controller tuning constants of the proposed control structure with PCTC of EA-PSD for separating the toluene/pyridine mixture. Table 15 shows controller tuning constants of the proposed control structure with DTC of the HPC-> LPC of PHI-PSD for separating the methanol/trimethoxysilane mixture. Table 16 shows controller tuning constants of the proposed control structure with PCTC of the HPC-> LPC of PHI-PSD for separating the methanol/trimethoxysilane mixture. Table 17 shows controller tuning constants of the proposed control structure with DTC of the LPC-> HPC of PHI-PSD for separating the methanol/trimethoxysilane mixture. Table 18 shows controller tuning constants of the proposed control structure with PCTC of the LPC-> HPC of PHI-PSD for separating the methanol/trimethoxysilane mixture.   Table 20 shows ratio of reboiler duty to feed flow rate. Fig. 1 shows T-xy diagram of toluene/ethanol.    Fig. 6 shows dynamic performances of PHI-PSD for separating the toluene/ethanol mixture under large feed disturbances. Fig. 7 shows T-xy diagram of acetone/methanol. Fig. 8 shows flowsheet of PHI-PSD for separating the acetone/methanol mixture. Fig. 9 shows temperature profiles PHI-PSD for separating the acetone/methanol mixture: (a) the LPC and (b) the HPC. Fig. 10 shows differential temperature of PHI-PSD with DTC for separating the acetone/methanol mixture. Fig. 11 shows the proposed control structure with DTC of PHI-PSD for separating the acetone/methanol mixture: (a) control flowsheet, (b) control faceplate and (c) flowsheet equations. Fig. 12 shows the proposed control structure with PCTC of PHI-PSD for separating the acetone/methanol mixture: (a) control flowsheet, (b) control faceplate and (c) flowsheet equations. Fig. 13 shows dynamic performances of PHI-PSD for separating the acetone/methanol mixture under ±10% feed disturbances. Fig. 14 shows dynamic performances of PHI-PSD for separating the acetone/methanol mixture under large feed disturbances. Fig. 15 shows flowsheet of FHI-PSD for separating the toluene/ethanol mixture. Fig. 16 shows temperature profiles of FHI-PSD for separating the toluene/ethanol mixture: (a) the LPC and (b) the HPC.    Fig. 19 shows dynamic performances of FHI-PSD for separating the toluene/ethanol mixture under large feed disturbances. Fig. 20 shows T-xy diagram of methanol/chloroform. Fig. 21 shows flowsheet of FHI-PSD for separating the methanol/chloroform mixture.         Fig. 26 shows dynamic performances of FHI-PSD for separating methanol/chloroform mixture under ±10% feed disturbances. Fig. 27 shows dynamic performances of FHI-PSD for separating methanol/chloroform mixture under large feed disturbances. Fig. 28 shows T-xy diagram of ethanol/ethyl acetate at 101.3 kPa. Fig. 29 shows flowsheet of FHI-PSD for separating the ethyl acetate/ethanol mixture.  Fig. 39 shows dynamic performances of EA-PSD for separating the toluene/pyridine mixture under large feed disturbances. Fig. 40 shows T-xy diagram of methanol/trimethoxysilane. Fig. 41 shows flowsheet of the HPC-> LPC sequence of PHI-PSD for separating the methanol/trimethoxysilane mixture.          Section.2 PHI-PSD for separating the toluene/ethanol mixture (LPC-> HPC sequence) The control loops of the proposed control structure with DTC of PHI-PSD for separating the toluene/ethanol mixture are listed as below:

Data description
(1) The fresh feed is flow controlled.
(2) The operating pressure of the LPC is controlled by manipulating the heat removal rate of the condenser. (9) Composition/temperature cascade control is used to control the 21st-stage temperature of the LPC (T21). The ethanol product purity is measured as the input of the composition controller, whose output is the setpoint of the temperature controller. The temperature controller is "on cascade". T21 is controlled by manipulating the heat removal rate of the auxiliary reboiler. (10) The differential temperature (DT) of the bottom and the 20th stage of the HPC is controlled by manipulating the ratio of the reboiler duty of the HPC to the feed flow rate.
Section.3 PHI-PSD for separating the acetone/methanol mixture (LPC-> HPC sequence) In the LPC, the 47th-stage temperature (T47) is selected to be controlled. In the HPC, the 55th-stage temperature (T55) is selected to be controlled for PCTC, while the difference between the bottom temperature and T55 is controlled for DTC. The diagram of operating pressure vs. differential temperature is shown in Fig. 10 .
The control loops of the proposed control structure with DTC of PHI-PSD for separating the acetone/methanol mixture are listed as below: (1) The fresh feed is flow controlled.
(2) The operating pressure of the LPC is controlled by manipulating the heat removal rate of the condenser.
(3) The reflux ratio of the HPC is fixed.
(4) The reflux ratio of the LPC is fixed.      Section.4 FHI-PSD for separating the toluene/ethanol mixture (LPC-> HPC sequence) The control loops of the proposed control structure with DTC of FHI-PSD for separating the toluene/ethanol mixture are listed as below: (1) The fresh feed is flow controlled.
(2) The operating pressure of the LPC is controlled by manipulating the heat removal rate of the condenser. Section.5 FHI-PSD for separating the methanol/chloroform mixture (LPC-> HPC sequence) In the LPC, the 19th-stage temperature (T19) is selected to be controlled. In the HPC, the 23rd-stage temperature (T23) is selected to be controlled for PCTC, while the difference between the bottom temperature and T23 is controlled for DTC. The diagram of operating pressure vs. differential temperature is shown in Fig. 23 .
The control loops of the proposed control structure with DTC of FHI-PSD for separating the methanol/chloroform mixture are listed as below: (1) The fresh feed is flow controlled.
(2) The operating pressure of the LPC is controlled by manipulating the heat removal rate of the condenser.  Section.6 FHI-PSD for separating the ethanol/ethyl acetate mixture (HPC-> LPC sequence) The control loops of the proposed control structure with DTC of FHI-PSD for separating the ethyl acetate/ethanol mixture are listed as below: (1) The fresh feed is flow controlled.
(2) The operating pressure of the LPC is controlled by manipulating the heat removal rate of the condenser.
(3) The reflux ratio of the HPC is fixed.
(4) The reflux drum level of the HPC is controlled by manipulating the distillate flow rate.    Section.7 EA-PSD for separating the toluene/pyridine mixture The control loops of the proposed control structure with DTC of EA-PSD for separating the toluene/pyridine mixture are listed as below: (1) The fresh feed is flow controlled.
(2) The distillate flow rate of the LPC is proportional to the feed flow rate, with the proportion being adjusted by a pyridine product composition controller. (3) The operating pressure of the LPC is controlled by manipulating the heat removal rate of the condenser.  Section.8 PHI-PSD for separating the methanol/trimethoxysilane mixture (HPC-> LPC sequence) The control loops of the proposed control structure with DTC of the HPC-> LPC sequence of PHI-PSD for separating the methanol/trimethoxysilane mixture are listed as below: (1) The fresh feed is flow controlled. (2) The operating pressure of the LPC is controlled by manipulating the heat removal rate of the condenser. Section.9 PHI-PSD for separating the methanol/trimethoxysilane mixture (LPC-> HPC sequence) The control loops of the proposed control structure with DTC of the LPC-> HPC sequence of PHI-PSD for separating the methanol/trimethoxysilane mixture are listed as below: (1) The fresh feed is flow controlled.
(2) The operating pressure of the LPC is controlled by manipulating the heat removal rate of the condenser.       (10) Composition/temperature cascade control is used to control the differential temperature (DT) of the 4th stage and the 27th stage of the LPC. Trimethoxysilane product purity is measured as the input of the composition controller, whose output is the setpoint of the temperature controller. The temperature controller is "on cascade". DT is controlled by manipulating the reflux ratio.
Section.10 Integral absolute error (IAE) Comparison of IAE of important variables between PCTC and DTC under large feed disturbances is shown in Table 19 . If 20% feed disturbance cannot be controlled, 15% feed disturbance is introduced. If 15% feed disturbance cannot be controlled, the values are not presented as the results of 10% feed disturbance have been shown.
Section.11 Other information

Experimental design, materials and methods
The simulations are implemented by Aspen Plus and Aspen Dynamics. Aspen Plus is used to establish steady-state designs. After steady-state designs are established, they are converted into dynamic processes. The dynamic research is implemented in Aspen Dynamics.

Declaration of Competing Interest
The authors declare that they have no known competing financial interests or personal relationships which have, or could be perceived to have, influenced the work reported in this article.