Serial flow crystallization at linearly decreasing pressures

• US 3,932,142 A
• Filed: 11/01/1972
• Issued: 01/13/1976
• Est. Priority Date: 09/26/1969
• Status: Expired due to Term

• Current Assignee: Stork Werkspoor Sugar BV, Suiker UNIE Holding BV
• Original Assignee: Stork Werkspoor Sugar BV, Suiker UNIE Holding BV
• Inventors: DE Vries, Gerbertus H., DE Bruyn, Gerrit C.
• Primary Examiner(s): Yudkoff, Norman
• Assistant Examiner(s): Emery, S. J.
• Application Number:
  US05/302,850
• Time in Patent Office: 1,168 Days
• Field of Search: 23/273 R, 23/301 R, 23/312 S, 23/270 R, 62/58, 202/173
• US Class Current: 23/301
• CPC Class Codes: B01D 9/0022 by reducing pressure
• CPC Class Codes: B01D 9/0036 Crystallisation on to a bed of product crystals; Seeding
• CPC Class Codes: B01D 9/0059 General arrangements of crystallisation plant, e.g. flow sheets
• CPC Class Codes: B01D 9/0063 Control or regulation control per se G05
• CPC Class Codes: C13B 30/02 Crystallisation; Crystallising apparatus

Abstract

A process and apparatus for obtaining crystals of a particular substance from a flowing solution thereof, by supplying the seeding crystals to one n^th portion of the saturated solution and supplying one n^th portion of the solution to the crystalliser further downstream at each of (n-1) places. The supersaturation of the solution is maintained at the required value by keeping the static pressure so low that self-vaporisation occurs, whereas this static pressure is caused to drop gradually in the crystalliser from its inlet end toward its discharge end.

Claims

1. A process for continuously obtaining crystals of a particular substance from a continuously flowing solution thereof, which comprises the steps of:

a. providing a crystallizer having a number n of stages which are in serial flow relation, there being an initial stage at one end of the crystallizer and a final stage at the opposite end thereof;

b. continuously introducing equal volumes of at least saturated solution of said particular substance into each of said n stages with continuous stirring in each stage, the solution being at a predetermined pressure and a predetermined temperature;

c. introducing seed crystals of said particular substance into that solution flowing into said initial stage and maintaining the pressure in said initial stage and in all the other stages at values less than said predetermined pressure so that supersaturated solution containing seed crystals flows from said initial stage serially through the remaining stages;

d. maintaining the pressures in said n stages at linearly decreasing values from said initial stage to said final stage so that self evaporation occurs in each stage with continuous and substantially constant growth of said seed crystals from said initial through said final stage; and

e. continuously withdrawing said solution with size-increased seed crystals from said final stage.

2. The method as defined in claim 1 wherein each stage is pressure-isolated from the others and the pressures in the different stages are step-wise adjusted to differ by equal amounts sequentially through the stages.

3. The method as defined in claim 2 wherein said stages are of progressively increasing lengths such that the residence time of solution in each stage is the same.

4. The method as defined in claim 1 wherein said stages are formed in an elongate vessel having its axis inclined at an acute angle with the horizontal whereby said linearly decreasing values of pressure are effected continuously from the lower to the upper end of the vessel.

5. The method according to claim 4, wherein said stages are of equal lengths but of progressively increasing volume such that the residence time of solution in each stage is the same.