Process for separating ammonia and acid gases from waste waters containing fixed ammonia salts

• US 4,104,131 A
• Filed: 07/08/1976
• Issued: 08/01/1978
• Est. Priority Date: 07/08/1976
• Status: Expired due to Term

• Current Assignee: Aristech Chemical Corporation (Energy Transfer LP)
• Original Assignee: United States Steel Corporation (U.S. Steel)
• Inventors: Glassman, Donald, Maier, Edward E., Didycz, William J., Saniga, George T.
• Primary Examiner(s): Bascomb, Jr., Wilbur L.
• Application Number:
  US05/703,407
• Time in Patent Office: 754 Days
• Field of Search: 203/10, 203/11, 203/7, 203/36, 203/71, 203/84, 203/85, 203/79, 203/78, 203/25, 203/49, 203/47, 203/33, 203/37, 203/92, 203/93, 203/96, 203/95, 203/97, 423/356, 423/357, 210/58
• US Class Current: 203/7
• CPC Class Codes: B01D 19/0005 with one or more auxiliary substances
• CPC Class Codes: B01D 3/38 Steam distillation
• CPC Class Codes: C02F 1/048 Purification of waste water by evaporation
• CPC Class Codes: C02F 1/586 by removing ammoniacal nitrogen for biological methods C02F3/00
• CPC Class Codes: C02F 1/66 by neutralisation; pH adjustment for degassing C02F1/20; using ion-exchange C02F1/42; for flocculation or precipitation of suspended impurities C02F1/52; for removing dissolved compounds C02F1/58
• CPC Class Codes: C02F 5/14 containing phosphorus
• CPC Class Codes: Y10S 210/903 Nitrogenous
• CPC Class Codes: Y10S 210/904 -CN containing

Abstract

A water purification process is described for the removal of ammonia and optionally one or more acid gases from waste waters such as coke-plant or coal conversion waste waters. The process involves adding lime to these waste waters in amounts sufficient to react with fixed ammonia salts present in the waste water and to enable substantial amounts of the ammonia to be evolved upon distillation, adding a threshold amount of a scale inhibitor compound chosen from the class of certain organic phosphonates and subjecting the thus treated waste water to distillation to remove substantial amounts of the ammonia and acid gases present from the waste water. Preferably, this process is achieved by two separate and successive distillations. In this preferred process, the first distillation substantially reduces the amount of the acid gases and free ammonia and is conducted at a pH of more than 9. In the second distillation, the amount of fixed ammonia is substantially reduced. To conserve energy, the stripping vapors from the second distillation are reused as stripping vapors for the first distillation.

Claims

1. A process for separating acid gases and ammonia from a dilute aqueous solution thereof, said solution being derived from a coal conversion process and also containing free and fixed ammonia salts and sulfate ion in a concentration of less than about 1500 ppm, said process comprising:

(a) subjecting said solution to a first countercurrent multi-stage continuous distillation, said distillation being conducted by having a gradient of ammonia concentration decreasing towards the region of bottom liquid withdrawal which results in said bottom liquid having a pH of more than 9,

(i) withdrawing an overhead vapor stream containing a major proportion of stripping vapor, some of said acid gases from said solution, and some of the ammonia from said free ammonia salts,

(ii) withdrawing an aqueous bottom stream which contains a major proportion of water, acid gases, free ammonia salts and substantially all of said fixed ammonia salts;

(b) adding lime to said withdrawn bottom stream, said lime being added in an amount sufficient to form an insoluble precipitate and evolve ammonia contained in the fixed ammonia salts during a second distillation of said mixture;

(c) adding a threshold amount of at least one scale inhibitor compound of the general formula ##STR5## where R is ##STR6## R'"'"' is selected from the group consisting of R and --CH₂ CH₂ OH, and

R" is selected from the group consisting of R, --CH₂ CH₂ OH, and ##STR7## where each M is independently selected from the group consisting of H, NH₄, and alkali metal, "n" is a whole number from 1 to 3, to said dilute aqueous solutions to thereby inhibit the deposition of scale on the trays of the distillation towers; and

(d) subjecting said withdrawn bottom stream to a second countercurrent multi-stage continuous distillation,

(i) withdrawing an overhead vapor stream, said vapor stream containing a major proportion of stripping vapor and a portion of the ammonia from the fixed ammonia salts and reusing this overhead vapor stream as a stripping vapor in the first distillation, and

(ii) withdrawing an aqueous bottom stream, said stream having a substantially reduced concentration of acid gases and ammonia as compared to said aqueous solution.

2. Process as in claim 1 wherein said dilute aqueous solution comprises a coke plant waste water and wherein the insoluble precipitate comprises calcium sulfate, calcium sulfite, calcium carbonate, calcium fluoride, calcium phosphate or mixtures thereof.

3. Process as in claim 2 wherein the acid gases comprise carbon dioxide, hydrogen sulphide, hydrogen cyanide or mixtures thereof.

4. Process as in claim 3 wherein the dilute aqueous solution immediately prior to lime addition and subsequent to the first distillation contains fixed ammonia in a concentration between about 50 and about 50,000 ppm, free ammonia in a concentration between about 3000 and about 100,000 ppm, and acid gases in a concentration between about 250 and about 50,000 ppm.

5. Process as in claim 2 wherein the trays of the distillation tower in which the second distillation is conducted are dualflow trays.

6. Process as in claim 5 wherein said dualflow trays contain substantially circular holes having an average diameter of at least one-half inch.

7. Process as in claim 6 wherein the trays have an average diameter between about 3 feet and 20 feet and contain between about 10 and about 30% hole area.

8. Process as in claim 1 wherein the scale inhibitor compound is of the formula ##STR8## where each M is independently selected from the group consisting of H, NH₄, and alkali metal, the amount of said compound added being no more than a threshold amount up to about 200 ppm and in a weight ratio of said compound to the cation component of said scale-forming salts not in excess of 0.5 to 1.

9. Process as in claim 8 in which the concentration of scale inhibitor compound does not exceed about 80 ppm.

10. Process as in claim 8 in which the concentration of scale inhibitor compound does not exceed about 20 ppm.

11. Process as in claim 8 wherein the scale inhibitor compound is a water soluble alkali metal salt of an aminotri (lower alkylidene phosphonic acid).

12. Process as in claim 10 wherein the scale inhibitor compound is penta sodium aminotri (methylphosphonate).

13. Process as in claim 2 wherein said aqueous solution includes an ammoniacal liquor.

14. Process as in claim 2 wherein the said bottom water stream from step (d) is subjected to biological degradation to reduce the content of toxic substances in said bottom water stream.

15. Process as in claim 1 wherein said overhead vapor stream withdrawn in step (d) is used to provide heat for the first distillation of step (a).

16. Process as in claim 1 including the additional step of removing readily separable solids while adding said alkali to said withdrawn bottoms stream in step (b).

17. Process as in claim 3 wherein said acid gases and said free and final ammonia comprises up to 0.6 percent by weight of said aqueous solution.

18. Process as in claim 1 wherein said aqueous solution also contains tars, phenols, fluorides, chlorides, sulfates, thiosulfates and thiocyanates and includes the preliminary step of removing the tars prior to step (a).

19. Process as in claim 1 wherein the stripping vapor withdrawn in step (a) consists essentially of steam and is in the temperature range of about 140°

to 265°

F.

20. Process as in claim 1 wherein the stripping vapor withdrawn in step (a) consists essentially of steam and the aqueous bottom stream of step (a) is in the temperature range of about 160°

to about 275°

F.

21. Process as in claim 1 wherein said aqueous bottom stream in step (a) has a pH range of from 9 to 12 when measured at 50°

C.

22. Process as in claim 1 wherein said aqueous solution stream in step (a) has a concentration of free ammonia of from about 3000 to about 100,000 parts per million.

23. Process as in claim 1 wherein the ratio of solution flow to vapor flow within the columns is in the range of about 10/1 to 2/1.

24. Process as in claim 1 wherein the bottom stream withdrawn in step (d) has a pH in the range of about 9.5 to about 12.

25. Process as in claim 1 wherein said lime added in step (b) comprises calcium hydroxide, calcium oxide, magnesium hydroxide, magnesium oxide or mixtures thereof.

26. Process as in claim 25 wherein said lime added in step (b) comprises pebbles of calcium oxide.

27. Process as in claim 3 wherein the scale inhibitor compound subsequent to the addition of the lime.

28. A process of purifying a waste water of a composition comprising:

(a) free ammonia of a concentration above about 3000 ppm, (b) fixed ammonia in a concentration of between about 50 and about 50,000 ppm, (c) acid gases in a concentration of between about 250 and about 50,000 ppm, and (d) sulfate ion in a concentration of less than about 1500 ppm, said process comprising (a) adding lime to said waste water, said lime and fixed ammonia salts being present in amounts sufficient to form an insoluble precipitate and evolve ammonia contained in the fixed ammonia salts during a distillation of said mixture;

(b) adding a threshold amount of at least one scale inhibitor compound of the general formula ##STR9## where R is ##STR10## R'"'"' is selected from the group consisting of R and --CH₂ CH₂ OH, and R" is selected from the group consisting of R, --CH₂ CH₂ OH, and ##STR11## where each M is independently selected from the group consisting of H, NH₄, and alkali metal, "n" is a whole number from 1 to 3 to said dilute aqueous solutions to thereby inhibit the deposition of scale on the trays of the distillation tower in which the distillation is conducted;

(c) subjecting the thus treated waste water to a countercurrent multi-stage continuous distillation, (i) withdrawing an overhead vapor stream, said vapor stream containing a major proportion of stripping vapor and a portion of the ammonia from the fixed ammonia salts, (ii) withdrawing an aqueous bottom stream.

29. Process as in claim 28 wherein the insoluble precipitate comprises calcium sulphate, calcium carbonate, calcium fluoride, calcium phosphate or mixtures thereof.

30. Process as in claim 29 wherein the distillation tower in which the distillation is conducted contains more than 12 trays.

31. Process as in claim 30 wherein the trays of the distillation tower in which the distillation is conducted are dualflow trays.

32. Process as in claim 31 wherein said dualflow trays have substantially circular holes having an average diameter of greater than about 1 inch.

33. Process as in claim 32 wherein the scale inhibitor compound is of the formula ##STR12## where each M is independently selected from the group consisting of H, NH₄, and alkali metal, the amount of said compound added being no more than a threshold amount up to about 200 ppm and in a weight ratio of said compound to the cation component of said scale-forming salts not in excess of 0.5 to 1.

34. Process as in claim 33 in which the concentration of said scale inhibitor compound does not exceed about 80 parts by weight per million parts of water.

35. Process as in claim 34 wherein the scale inhibitor compound is a water soluble alkali metal salt of an amino tri (lower alkylidene phosphonic acid).

36. Process as in claim 35 wherein the scale inhibitor compound is penta sodium aminotri (methylphosphonate).

37. Process as in claim 28 wherein the free ammonia salts are present in the waste water in a concentration between about 3000 and about 100,000 ppm, the fixed ammonia salts are present in a concentration between about 3000 and about 5000 ppm, and carbon dioxide is present in a concentration of between about 250 and about 700 ppm.

38. Process as in claim 37 wherein the concentration of sulfate ion is less than about 800 ppm.