Method for recovering HCI from a HCI containing gas stream
The invention pertains to a method for recovering HCl from a HCl containing gas stream wherein a HCl containing gas stream with a temperature of −20 to 25° C. is provided to an adiabatic absorption unit where it is contacted with water as an absorbent, resulting in the formation of a top gas stream and a aqueous HCl product solution, wherein the temperature of the top gas stream is at least 70° C. and wherein the aqueous HCl product solution has a HCl concentration in the range of 5-20 wt. %. It is preferred for the HCl-containing gas stream to be derived from a hydrogenation step wherein a feed comprising monochloroacetic acid (MCA) and dichloroacetic acid (DCA) is reacted with hydrogen to form a HCl-containing gas stream and a product stream comprising MCA and a reduced amount of DCA. The HCl product solution is preferably diluted to a concentration of 1-8 wt. %, and the diluted solution is used as absorbent in a second absorption step, wherein HCl is absorbed from a further HCl-containing gas stream to form a second aqueous HCl solution. The further HCl-containing gas stream is preferably derived from a chlorination step wherein acetic acid is reacted with chlorine, resulting in the formation of the further HCl-containing gas stream and a feed comprising monochloroacetic acid (MCA) and dichloroacetic acid (DCA).
1. A method for recovering HCl from a HCl containing gas stream, the method comprising
providing a HCl containing gas stream with a temperature of −20 to 25° C. to an adiabatic absorption unit where it is contacted with water as an absorbent, resulting in the formation of a top gas stream and an aqueous HCl product solution,
providing steam to the adiabatic absorption unit to maintain the temperature of the top gas stream to be at least 70° C. and at most 95° C. and wherein the amount of water is selected such that the aqueous HCl product solution has a HCl concentration in the range of 5-20 wt. %.
2. The method according to claim 1 , wherein the absorbent provided to the unit generally has a HCl concentration of below 1 wt. %.
3. The method according to claim 1 , wherein the HCl-containing gas stream is obtained as a by-product of a hydrogenation step wherein a feed comprising monochloroacetic acid (MCA) and dichloroacetic acid (DCA) is reacted with hydrogen to form a HCl-containing gas stream and a product stream comprising MCA and a reduced amount of DCA.
4. The method according to claim 1 , wherein steam is added to the adiabatic absorption unit at a pressure of above 1 to 12 bar (absolute).
5. The method according to claim 1 , wherein the top gas stream has a temperature of at least 77° C.
6. The method according to claim 1 , wherein the temperature of the HCl-containing gas stream provided to the absorption unit is in the range of −5 to 20° C.
7. The method according to claim 1 , wherein the aqueous HCl product solution has a HCl concentration in the range of 10-20 wt. %.
8. The method according to claim 1 , wherein the HCl product solution is diluted to a concentration of 1-8 wt. %, and the diluted solution is used as absorbent in a second absorption step, wherein HCl is absorbed from a further HCl-containing gas stream to form a second aqueous HCl solution.
9. The method according to claim 1 , wherein the HCl-containing gas stream comprises one or more organic contaminants selected from the group consisting of acetic acid, monochloroacetic acid, acetaldehyde, chloroacetaldehyde, and dichloroacetaldehyde.
10. The method for recovering HCl from a HCl containing gas stream comprising the steps of
providing a HCl containing gas stream with a temperature of −20 to 25° C., which is obtained as a by-product of a hydrogenation step wherein a feed comprising monochloroacetic acid (MCA) and dichloroacetic acid (DCA) is reacted with hydrogen to form a HCl-containing gas stream and a product stream comprising MCA and a reduced amount of DCA,
feeding the HCl containing gas stream to an adiabatic absorption unit where it is contacted with water as an absorbent, resulting in the formation of a top gas stream and an aqueous HCl product solution,
providing steam to the adiabatic absorption unit to maintain the temperature of the top gas stream to be at least 70° C. and wherein the amount of water is selected such that the aqueous HCl product solution has a HCl concentration in the range of 5-20 wt. %,
diluting the aqueous HCl product solution to a concentration of 1-8 wt. %, and
providing the diluted solution as absorbent in a second absorption step, wherein HCl is absorbed from a further HCl-containing gas stream to form a second aqueous HCl solution, which further HCl-containing gas stream is obtained as a by-product of a chlorination step wherein acetic acid is reacted with chlorine resulting in the formation of the second HCl-containing gas stream and a feed comprising monochloroacetic acid (MCA) and dichloroacetic acid (DCA).
11. The method of claim 10 , wherein the HCl concentration in the absorbent water is below 0.5 wt. %.
12. The method of claim 10 , wherein the steam added to the adiabatic absorption unit has a temperature of 100-200° C. and a pressure of 1 to 4 bar (absolute).
13. The method of claim 10 , wherein the top gas stream has a temperature of at least 87° C. and at most 92° C.
14. The method of claim 10 , wherein the temperature of the HCl-containing gas stream provided to the absorption unit is in the range of 10 to 15° C.
15. The method of claim 10 , wherein the aqueous HCl product solution has a HCl concentration in the range of 13-18 wt. %.