Vapor compression steam stripping
The invention provides systems and methods for the pre-concentration of a target molecule from feed solution comprising a low concentration of the target molecule.
1. A process for concentration of ethanol from a dilute feed solution comprising ethanol comprising the steps of
(a) counter-current contacting of the dilute feed solution and a vapor phase input to a counter-current vapor-liquid contactor with the counter-current vapor-liquid contactor to produce a vapor phase output of the counter-current vapor-liquid contactor and an outgoing depleted feed solution;
(b) condensing in a condenser of the vapor phase output of the counter-current vapor-liquid contactor, wherein the vapor phase output of the counter-current vapor-liquid contactor is conveyed to the condenser such that the composition of the vapor phase output is substantially maintained, to produce a condensed liquid product that leaves the condenser, with transfer of latent heat released by condensation to an evaporator;
(c) evaporating of a liquid feed to provide the vapor phase input to the counter-current vapor-liquid contactor;
(d) compressing of the vapor phase output of the counter-current vapor-liquid contactor or the vapor phase input to the counter-current vapor-liquid contactor, wherein compression of the vapor phase may occur before the counter-current vapor-liquid contactor, after the counter-current vapor-liquid contactor, or both before and after the counter-current vapor-liquid contactor, wherein the action of the compressor must result in a pressure that is higher in the condenser than in the evaporator, wherein no membrane is used in the process and whereby ethanol is concentrated; and
(e) reducing by a heat exchanger the temperature of the outgoing depleted feed solution leaving the counter-current vapor-liquid contactor to a temperature close to the temperature of the dilute feed solution before said dilute feed solution enters said heat exchanger.
2. The process of claim 1 in which the mass of the dilute feed solution entering the counter-current vapor-liquid contactor is substantially the same as the mass of depleted feed solution leaving the counter-current vapor-liquid contactor.
3. The process of claim 1 in which the mass of the vapor phase entering the counter-current vapor-liquid contactor is substantially equal to the mass of the vapor phase leaving the counter-current vapor-liquid contactor.
4. The process of claim 1 in which the mass of the liquid feed to the evaporator is substantially equal to the mass of the condensed liquid product leaving the condenser.
5. The process of claim 1 in which heat required to produce the vapor phase input to the counter-current vapor-liquid contactor is substantially equal to the latent heat released by condensation of the vapor phase output of the counter-current vapor-liquid contactor.
6. The process of claim 1 in which the heat exchanger used to heat the incoming dilute feed solution and cool the outgoing depleted feed solution is a counter-current heat exchanger.
7. The process of claim 1 in which condensation and evaporation occur in a heat exchanger.
8. The process of claim 1 in which the increase in pressure caused by the compressor is sufficient to result in complete condensation of the vapor phase output of the counter-current vapor-liquid contactor at a temperature greater than the boiling temperature of the liquid feed used to provide the vapor phase input to the counter-current vapor-liquid contactor.
9. The process of claim 1 in which the temperature in the condenser is approximately the temperature in the evaporator.
10. The process of claim 1 in which the temperature of the dilute feed solution entering the vapor-liquid contactor is close to its boiling temperature.
11. The process of claim 1 in which the temperature of the liquid feed entering the evaporator is dose to its boiling point.
12. The process of claim 1 in which the process is operated in such a manner that positive gauge pressure is maintained throughout the steps of the process.
13. The process of claim 1 in which the dilute feed solution is at least partially degassed before entering the counter-current vapor liquid contactor.
14. The process of claim 1 in which a portion of the vapor phase output of the counter-current vapor-liquid contactor that has passed through the condenser containing a substantial amount of incondensable gas is sent to a counter-current heat exchanger in which the condensable vapor is condensed to transfer its latent heat to raise the temperature of the liquid feed to the evaporator and the incondensable gas is vented.
15. The process of claim 1 in which the liquid feed to the evaporator is at least partially degassed before entering the evaporator.
16. The process of claim 1 in which a part of the depleted feed solution exiting the bottom of the counter-current vapor liquid contactor is sent to the evaporator.
17. The process of claim 1 in which the concentration of ethanol in the condensed liquid product is at least 5 times the concentration of ethanol in the dilute feed solution.
18. The process of claim 1 in which the dilute feed solution is less than 1 wgt % ethanol.
19. The process of claim 1 in which the dilute feed solution is less than 0.5 wgt % ethanol.
20. The process of claim 1 wherein there are two stages of purification arranged so that the output of the first stage becomes the input of the second stage.
21. The process of claim 1 in which the bulk of the dilute feed solution, the vapor phase input, the vapor phase output, the depleted feed solution, the condensed liquid product and the liquid feed are water.
22. The process of claim 1 in which the condensed liquid product comprises primarily water.
23. The process of claim 1 in which the heat exchanger is heat exchanger ( 18 ).
24. A process for concentration of ethanol from a dilute feed solution comprising ethanol comprising the steps of
(a) counter-current contacting of the dilute feed solution and a vapor phase input o a counter-current vapor-liquid contactor with the counter-current vapor-liquid contactor to produce a vapor phase output of the counter-current vapor-liquid contactor and an outgoing depleted feed solution;
(b) condensing in a condenser of the vapor phase output of the counter-current vapor-liquid contactor, wherein the vapor phase output of the counter-current vapor-liquid contactor is conveyed to the condenser such that the composition of the vapor phase output is substantially maintained, to produce a condensed liquid product that leaves the condenser, with transfer of latent heat released by condensation to an evaporator;
(c) evaporating of a liquid feed to provide the vapor phase input o the counter-current vapor-liquid contactor;
(d) compressing of the vapor phase output of the counter-current vapor-liquid contactor or the vapor phase input to the counter-current vapor-liquid contactor, wherein compression of the vapor phase may occur before the counter-current vapor-liquid contactor, after the counter-current vapor-liquid contactor, or both before and after the counter-current vapor-liquid contactor, wherein the action of the compressor must result in a pressure that is higher in the condenser than in the evaporator, wherein no membrane is used in the process and whereby ethanol is concentrated; and
(e) reducing by a heat exchanger the temperature of the condensed liquid product leaving the condenser to a temperature close to the temperature of the liquid feed to the evaporator before said liquid feed to the evaporator enters said heat exchanger.
25. The process of claim 24 in which the heat exchanger used to heat the liquid feed to the evaporator and cool the condensed liquid product is a counter-current heat exchanger.
26. The process of claim 24 in which the heat exchanger is heat exchanger ( 24 ).
27. A process for concentration of ethanol from a dilute feed solution comprising ethanol comprising the steps of
(a) counter-current contacting of the dilute feed solution and a vapor phase input to a counter-current vapor-liquid contactor with the counter-current vapor-liquid contactor to produce a vapor phase output of the counter-current vapor-liquid contactor and an outgoing depleted feed solution;
(b) condensing in a condenser of the vapor phase output of the counter-current vapor-liquid contactor, wherein the vapor phase output of the counter-current vapor-liquid contactor is conveyed to the condenser such that the composition of the vapor phase output is substantially maintained, to produce a condensed liquid product that leaves the condenser, with transfer of a n heat released by condensation to an evaporator;
(c) evaporating of a liquid feed to provide the vapor phase input to the counter-current vapor-liquid contactor; and
(d) compressing of the vapor phase output of the counter-current vapor-liquid contactor or the vapor phase input to the counter-current vapor-liquid contactor, wherein compression of the vapor phase may occur before the counter-current vapor-liquid contactor, after the counter-current vapor-liquid contactor, or both before and after the counter-current vapor-liquid contactor, wherein the action of the compressor must result in a pressure that is higher in the condenser than in the evaporator, wherein no membrane is used in the process, whereby ethanol is concentrated and wherein energy required by the process is less than 10% of the heating value of the ethanol in the condensed liquid product.