In one embodiment, a carbon dioxide capturing system includes an absorber to absorb CO2 from first gas into lean liquid, and produce rich liquid that is the lean liquid absorbing the CO2 and second gas that is the first gas removing the CO2, and a regenerator to separate third gas including the CO2 from the rich liquid flowing from the absorber, and provide the lean liquid and the third gas. The system further includes a flowmeter to measure a flow rate of the third gas, a liquid level gauge to measure a liquid level of the lean liquid and/or the rich liquid, and a controller to regulate a quantity of heat energy supplied to the regenerator based on the flow rate of the third gas, and regulate a total amount of the lean liquid and the rich liquid in the system based on the liquid level.

The present invention provides a method for operating a rectification column (1000) for separating a mixture (S) containing a component A and a component B having a boiling point higher than that of the component A at an operating pressure of the rectification column (1000) which is lower than ambient pressure, wherein the method comprises a step for controlling the mass fraction of the component B in the product stream of the component A (P1) to a value within a first target range from 0.1% to 5.0% and the mass fraction of the component A in the product stream of the component B (P2) to a value within a second target range from 0.1% to 5.0%, wherein the control is carried out as a function of a controlling temperature (TC) for which a setpoint TC.sub.setpoint is calculated according to the equation TC.sub.setpoint=T2+F.Math.(T1−T2), where F is a factor which is in the range from 0.1 to 0.9 and T1 and T2 are reference temperatures, wherein in the case of a deviation in the measured control temperature (TC) from its setpoint TC.sub.setpoint being found the control temperature (TC) is readjusted to the setpoint TC.sub.setpoint by varying one or more of the following actuating variables: (i) heating of the column bottom (130) by the evaporator (200), (ii) the mass flow {dot over (m)}.sub.A42 of the reflux (A42) fed back into the rectification column, (iii) the mass flow {dot over (m)}.sub.P2 of the product stream P2 and (iv) the mass flow {dot over (m)}.sub.P1 of the product stream P1.

The present invention provides a method for operating a rectification column (1000) for separating a mixture (S) containing a component A and a component B having a boiling point higher than that of the component A at an operating pressure of the rectification column (1000) which is lower than ambient pressure, wherein the method comprises a step for controlling the mass fraction of the component B in the product stream of the component A (P1) to a value within a first target range from 0.1% to 5.0% and the mass fraction of the component A in the product stream of the component B (P2) to a value within a second target range from 0.1% to 5.0%, wherein the control is carried out as a function of a controlling temperature (TC) for which a setpoint TC.sub.setpoint is calculated according to the equation TC.sub.setpoint=T2+F.Math.(T1−T2), where F is a factor which is in the range from 0.1 to 0.9 and T1 and T2 are reference temperatures, wherein in the case of a deviation in the measured control temperature (TC) from its setpoint TC.sub.setpoint being found the control temperature (TC) is readjusted to the setpoint TC.sub.setpoint by varying one or more of the following actuating variables: (i) heating of the column bottom (130) by the evaporator (200), (ii) the mass flow {dot over (m)}.sub.A42 of the reflux (A42) fed back into the rectification column, (iii) the mass flow {dot over (m)}.sub.P2 of the product stream P2 and (iv) the mass flow {dot over (m)}.sub.P1 of the product stream P1.

Methods and apparatus for processing hydrocarbon and other feedstocks that contain lighter volatile component(s) along with heavier volatile or non-volatile component(s) and/or contaminant(s). The principal benefit being that a feedstock can be processed and separated into its distinct volatile components down to elemental and/or molecular levels, including the ability to handle the heaviest tars and bitumen within the system. This effectively provides onsite value add to the feedstock resource (minus the waste streams such as water, sulfur, or sand; which may have value as isolated components in their own right). The system is robust and can include innovative hardware, methods, and/or software. The system can isolate water, chemical, various hydrocarbon, and particle contaminants of arbitrary concentrations and sizes. These factors provide for significant increases in processing efficiencies and capabilities in the fields of refining and environmental recovery. In a variety of operating scenarios, near-zero emissions can be achieved while processing.

Methods and apparatus for processing hydrocarbon and other feedstocks that contain lighter volatile component(s) along with heavier volatile or non-volatile component(s) and/or contaminant(s). The principal benefit being that a feedstock can be processed and separated into its distinct volatile components down to elemental and/or molecular levels, including the ability to handle the heaviest tars and bitumen within the system. This effectively provides onsite value add to the feedstock resource (minus the waste streams such as water, sulfur, or sand; which may have value as isolated components in their own right). The system is robust and can include innovative hardware, methods, and/or software. The system can isolate water, chemical, various hydrocarbon, and particle contaminants of arbitrary concentrations and sizes. These factors provide for significant increases in processing efficiencies and capabilities in the fields of refining and environmental recovery. In a variety of operating scenarios, near-zero emissions can be achieved while processing.

A device may include a memory storing instructions and a processor configured to execute the instructions to determine an initial mass of a sample; distill the sample up to at least a thermal destruction temperature; record, at a set of time points during the distilling, vapor temperature values, liquid temperature values, and vapor pressure values associated with the sample; and determine a residual mass of the sample. The processor may be further configured to generate a pressure curve based on the vapor pressure values; calculate a summary integral surface for the generated pressure curve; and generate a distillation curve that relates the vapor temperature values and the liquid temperature values to mass percentage of the sample that has evaporated, based on the calculated summary integral surface, the initial mass of the sample, and the residual mass of the sample.

The present disclosure provides a control method for a rectification and purification system of electronic-grade chlorine trifluoride. A rectification device of electronic-grade chlorine trifluoride includes a two-stage cryogenic rectification device including a low-boiling column and a high-boiling column. An extraction agent is arranged in the two-stage cryogenic rectification device for further dissociating associated molecules of hydrogen fluoride and chlorine trifluoride to meet the requirements of electronic-grade chlorine trifluoride. The reflux ratio parameter stability of a vapor-liquid (chlorine trifluoride-hydrogen fluoride) phase equilibrium system can be effectively improved by a column plate temperature control method, thus realizing wide dynamic smooth running under various working conditions. The column plate temperature control method can achieve an effective separation of chlorine trifluoride and various impurity components by deep rectification technology, yielding electronic-grade chlorine trifluoride through purification.

The present disclosure provides a control method for a rectification and purification system of electronic-grade chlorine trifluoride. A rectification device of electronic-grade chlorine trifluoride includes a two-stage cryogenic rectification device including a low-boiling column and a high-boiling column. An extraction agent is arranged in the two-stage cryogenic rectification device for further dissociating associated molecules of hydrogen fluoride and chlorine trifluoride to meet the requirements of electronic-grade chlorine trifluoride. The reflux ratio parameter stability of a vapor-liquid (chlorine trifluoride-hydrogen fluoride) phase equilibrium system can be effectively improved by a column plate temperature control method, thus realizing wide dynamic smooth running under various working conditions. The column plate temperature control method can achieve an effective separation of chlorine trifluoride and various impurity components by deep rectification technology, yielding electronic-grade chlorine trifluoride through purification.

A system of interlocks for controlling flow of low temperature process streams in a manufacturing process through a cold box to equipment or piping not specified for such temperatures by opening and closing valves and starting and stopping pumps. At least one interlock affects streams heated in the cold box. At least one interlock affects the streams cooled in the cold box. The interlocks are activated by temperatures of process lines to prevent exposure of equipment and piping to low temperatures while preventing the shutdown of the cold box. An override controller including a predictive failure capability is also provided.

A method of separating an organic solvent which may easily separate and recover an organic solvent from a mixed solution containing the organic solvent, and an organic solvent separation system capable of performing the same are disclosed herein. In some embodiments, the method includes introducing a first mixed solution into a first distillation column to recover an organic solvent and discharge a first fraction containing an unrecovered organic solvent and a high boiling point compound A to a bottom of the column, introducing a second mixed solution into a second distillation column to recover organic solvent and discharge a second fraction containing an unrecovered organic solvent and a high boiling point compound B, and introducing the first fraction and the second fraction into a third distillation column to recover an organic solvent-rich fraction and a high boiling point compound-rich fraction.