Purification of crude hydrogen chloride

• US 4,003,723 A
• Filed: 05/17/1976
• Issued: 01/18/1977
• Est. Priority Date: 05/20/1975
• Status: Expired due to Term

• Current Assignee: Hoechst Aktiengesellschaft (Sanofi )
• Original Assignee: Hoechst Aktiengesellschaft (Sanofi )
• Inventors: Schafer, Stefan, Gehrmann, Klaus, Ohorodnik, Alexander, Mainski, Albert
• Primary Examiner(s): Nozick, Bernard
• Application Number:
  US05/686,928
• Time in Patent Office: 246 Days
• Field of Search: 55/71, 423/240, 423/488, 260/539 A
• US Class Current: 95/199
• CPC Class Codes: C01B 7/01 Chlorine; Hydrogen chloride

Abstract

Crude hydrogen chloride gas obtained as a by-product in the production of chloroacetic acids by the catalytic chlorination of acetic acid with chlorine gas in contact with acetic anhydride and/or acetyl chloride, and contaminated with about 0.6 up to 3 % by volume of acetyl chloride is purified. To this end, crude hydrogen chloride gas is introduced into the base portion of a scrubbing zone and scrubbed countercurrently therein with 0.5 up to 20 liter, per normal cubic meter (S.T.P) of hydrogen chloride gas, of a cooled scrubbing liquid under circulation, consisting substantially of 20-80 weight % of concentrated H₂ SO₄, 15-60 weight % of acetic acid, and 5-50 weight % of water. The resulting purified moist hydrogen chloride gas issuing at the head of the scrubbing zone is introduced into the base portion of a drying zone and scrubbed countercurrently with precooled sulfuric acid under circulation.

Claims

1. A process for the purification of a crude hydrogen chloride gas by-product, which is obtained in the production of chloroacetic acids by the catalytic chlorination of acetic acid with chlorine gas in contact with acetic anhydride and/or acetyl chloride, and continues to be contaminated, even after having been prepurified, with about 0.6 up to 3 % by volume of acetyl chloride and optionally with some minor proportion of chloroacetyl chloride, which comprises:

introducing the crude hydrogen chloride gas into the base portion of a scrubbing zone and scrubbing it countercurrently therein with about 0.5 up to 20 liter, per normal cubic meter (S.T.P.) of hydrogen chloride gas, of a cooled scrubbing liquid under circulation and consisting substantially of about 20 up to 80 weight % of concentrated H₂ SO₄, about 15 up to 60 weight % of acetic acid, and about 5 up to 50 weight % of water;

introducing the resulting purified moist hydrogen chloride gas issuing at the head of the scrubbing zone into the base portion of a drying zone and drying it therein by scrubbing it countercurrently with precooled sulfuric acid under circulation, the sulfuric acid being used at a rate of about 0.5 up to 20 liter, per normal cubic meter of hydrogen chloride; and

removing dry hydrogen chloride near the head of the drying zone.

2. The process as claimed in claim 1, wherein the scrubbing liquid comprises a mixture consisting of 30-60 weight % of concentrated sulfuric acid, 20-50 weight % of acetic acid, and 10-40 weight % of water.

3. The process as claimed in claim 1, wherein the crude hydrogen chloride gas is scrubbed with 3-10 liter of scrubbing liquid, per normal cubic meter of gas.

4. The process as claimed in claim 1, wherein the concentrated sulfuric acid under circulation is cooled, prior to entering the drying zone, to the extent necessary to have a temperature of about 10°

-35°

C, in the base portion of the drying zone.

5. The process as claimed in claim 1, wherein 3-10 liter/hour of sulfuric acid is circulated, per normal cubic meter of hydrogen chloride.

6. The process as claimed in claim 1, wherein the scrubbing liquid under circulation is cooled, prior to entering the scrubbing zone, to the extent necessary to have a temperature of about 10°

-30°

C in the upper portion of the scrubbing zone.

7. The process as claimed in claim 6, wherein a temperature of 15°

-25°

C is established in the upper portion of the scrubbing zone.

8. The process as claimed in claim 1, wherein about 10-100 ml of concentrated sulfuric acid, per normal cubic meter of hydrogen chloride, is introduced continuously into the upper portion of the drying zone and an adequate proportion of sulfuric acid under circulation is simultaneously taken from the base portion of the drying zone, the sulfuric acid is diluted with water in a ratio by volume of about 1:

1 and used for partial replacement of the scrubbing liquid under circulation in the scrubbing zone.

9. The process as claimed in claim 8, wherein the upper portion of the drying zone is continuously supplied with 25-50 ml of concentrated sulfuric acid, per normal cubic meter of hydrogen chloride.

10. The process as claimed in claim 8, wherein a temperature of about 15°

-40°

C, is established in the upper portion of the drying zone.

11. The process as claimed in claim 8, wherein the scrubbing liquid under circulation in the scrubbing zone is partially replaced, an adequate proportion (adequate with respect to the quantity of sulfuric acid supplied) of acetic acid contaminated with scrubbing liquid is removed from the cycle and delivered to an acetic acid recovery stage.