公开(公告)号：US3446587A

公开(公告)日：1969-05-27

申请号：US3446587D

申请日：1966-11-23

Applicant: BASF AG

Inventor： JOCKERS KURT ,  MEIER HERMANN ,  TAGLINGER LUDWIG

IPC: C01B21/24

CPC classification number: C01B21/24

公开(公告)号：CA967722A

公开(公告)日：1975-05-20

申请号：CA136378

申请日：1972-03-06

Applicant: BASF AG

Inventor： KARTTE KLAUS ,  JOCKERS KURT ,  MEIER HERMANN ,  TAGLINGER LUDWIG

IPC: C01B17/90 ,  C01B21/14

公开(公告)号：FR1392764A

公开(公告)日：1965-03-19

申请号：FR966439

申请日：1964-03-06

Applicant: BASF AG

Inventor： JOCKERS KURT ,  MEIER HERMANN ,  EBERHARDT ERNST ,  TAGLINGER LUDWIG

IPC: C01B21/14

公开(公告)号：FR1502586A

公开(公告)日：1967-11-18

申请号：FR86034

申请日：1966-12-02

Applicant: BASF AG

Inventor： JOCKERS KURT ,  MEIER HERMANN ,  TAGLINGER LUDWIG

IPC: C01B21/24

Abstract: 1,159,399. Nitric oxide. BADISCHE ANILIN- & SODA-FABRIK A.G. 2 Dec., 1966 [4 Dec., 1965]. No. 54079/66. Heading C1A. Nitric oxide is produced by reacting sulphur with aqueous nitric acid at an HNO 3 ; S molar ratio of at least 4 : 3 in a reactor at 350- 650‹ C. The sulphur may be supplied to the reactor in vapour or liquid form, in the latter case by spraying, and the nitric acid in vapour form. The nitric acid used may have a concentration of 30-70 wt. per cent. At an HNO 3 : S molar ratio of 4 : 3 the principal by-product is SO 2 , and at 6 : 3 or more it is H 2 SO 4 . In the latter case, nitric oxide of 99% purity and pure dilute sulphuric acid may be obtained by passing the hot reaction gases to a distillation column, separately condensing out the sulphuric acid and any excess nitric acid present, and freeing the NO from other nitrogen oxides by washing with e.g. caustic soda solution.

公开(公告)号：GB1159399A

公开(公告)日：1969-07-23

申请号：GB5407966

申请日：1966-12-02

Applicant: BASF AG

Inventor： JOCKERS KURT ,  MEIER HERMANN ,  TAGLINGER LUDWIG

IPC: C01B21/24

Abstract: 1,159,399. Nitric oxide. BADISCHE ANILIN- & SODA-FABRIK A.G. 2 Dec., 1966 [4 Dec., 1965]. No. 54079/66. Heading C1A. Nitric oxide is produced by reacting sulphur with aqueous nitric acid at an HNO 3 ; S molar ratio of at least 4 : 3 in a reactor at 350- 650‹ C. The sulphur may be supplied to the reactor in vapour or liquid form, in the latter case by spraying, and the nitric acid in vapour form. The nitric acid used may have a concentration of 30-70 wt. per cent. At an HNO 3 : S molar ratio of 4 : 3 the principal by-product is SO 2 , and at 6 : 3 or more it is H 2 SO 4 . In the latter case, nitric oxide of 99% purity and pure dilute sulphuric acid may be obtained by passing the hot reaction gases to a distillation column, separately condensing out the sulphuric acid and any excess nitric acid present, and freeing the NO from other nitrogen oxides by washing with e.g. caustic soda solution.

公开(公告)号：GB1046656A

公开(公告)日：1966-10-26

申请号：GB706964

申请日：1964-02-20

Applicant: BASF AG

Inventor： JOCKERS KURT ,  MEIER HERMANN ,  EBERHARDT ERNST ,  TAGLINGER LUDWIG

IPC: C01B21/14

Abstract: In the preparation of hydroxylammonium salts, in a continuous process by catalytic reduction of No with H2 in contact with Pt catalysts in the presence of dilute inorganic acids, the reduction is carried out in at least two successive stages; fresh acid is supplied at the first stage and hydroxylammonium salt withdrawn from the last stage, the acid concentration decreases from stage to stage. The catalyst may be periodically gassed with NO, a mixture of NO and N2 or a mixture of NO and CO2, in each case in the absence of hydrogen. Reaction temperature may be 40 DEG to 50 DEG C. and the catalyst may have Pt content of 0.3 to 5%. Fig. 3 illustrates a four-stage process for this reaction. E.g. 4 to 5 N H2So4 together with Pt catalyst from the separator S are introduced into reactor I and passed through reactors II, III and IV to the separator S. The normalities of H2SO4 in the zones range from 3.20 to 0.30. No and H2 mixture is passed in parallel through reactors IV, III and II, the off-gas from these reactors is collected and passed through reactor I. After leaving I, remaining off-gas is burnt. Fig. 1 (not shown) illustrates a system in which 8 reactors are arranged in two parallel lines of 4. Fig. 2 (not shown) is a 5-stage system where Stages I and II are fed with off-gas from Stages III, IV and V.