Search Images Maps Play YouTube News Gmail Drive More »
Sign in
Screen reader users: click this link for accessible mode. Accessible mode has the same essential features but works better with your reader.

Patents

  1. Advanced Patent Search
Publication numberUS1693786 A
Publication typeGrant
Publication dateDec 4, 1928
Filing dateSep 10, 1925
Priority dateSep 17, 1924
Also published asDE522557C
Publication numberUS 1693786 A, US 1693786A, US-A-1693786, US1693786 A, US1693786A
InventorsIsaachsen Isak
Original AssigneeKrystal As
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Process for the crystallization of solid substances in a coarse granular form from solutions
US 1693786 A
Abstract  available in
Images(1)
Previous page
Next page
Claims  available in
Description  (OCR text may contain errors)

PROCESS lFOR THE CR Dec. v4, 1928.

Patented u 4, 1928.

UNITED STAT-Es :sax Isaacnsan, or osLo,

, 1.693.186. P.vraN'roFFlcl-z.

NORWAY, AssIeNoa To urrnsnnsxnrnr xmrszrnr., .or osLo, Noaway.

IPBOGESS FOB THE CBYBTALLIZIATION OI SOLID SUBSTANCES IN A COABSE GRANULAB` FORM FROM SOLUTIONS.

Application med September 10, 1925, lerial No. 55,802, and in Norway September 17,'1924.

with very great drawbacks, among other` things because the creation of new small kernels in the apparatus has taken place.

completely uncontrolled. If the intensity of production is maintained onl moderately igh, the liquidwill become sov ighly heaped with crystalsJthat the contents lof the a paratus will form a thick mass before t e separate granules have obtained moderately large dimensions. If, for instance, the separate granules were cause to grow from` '25 llOO mm. to 4 mm. in average diameter,

eir total volume would increase to the (iLOOOOOO-double one.` Therefore, it has been necessar either to remove the precipitationsl before the granules have attained larger dimensions, such as used in vacuum apparatus for the manufacture of common salt, or it has been necessary to operate the apparatus intermittentl with a low intensit vveach time new kernels ad to be created an as long as they were still small, such as has been proposed in respect of vacuum apparatus for' sugar. Otherwise, a su erlluous numbery of new kernels would be ormed, because any changerequires a comparativel o owing to the lar e quantities of apparatus, and t ese small lkernels will thereafter grow quite catastrophically, as just intimated. 4

In addition, one had not by a` constrained guiding ofthe liquid-circulation taken carey of maintaining the granules in., suspensionv until they were large enou h.

The present invention oes away with these inconveniences bycombining three elements fomerly known separately but never utilized simultaneously hitherto.

1. A constrained .guiding ofthe circulating stream of liquid wherein the kernels are long time. quid'in the suspended, with so high velocities that the kernels can nowhere deposit before they have attained the-desired size'. v f 4 2. A. regular removal of kernels which havev rown to the size desired. f

' 3. regulation of the number ofthe small kernels by introducing regularly smallsker-so nels or causing them to form automatically in the apparatus or by removing them according as the mass of. kernels in the a paratus is increasing or decreasing durab y.

l The removal of large kernels and the regulated introduction of small kernels in the apparatus need not be quite constant. Small variations play no part. v y

The important point consists in takin care that the totalsuperficial area of kerne s "10' in the apparatus, in spite of the re ular' rethe read -grown ones, is a ways so large that the sai area at afull intensity of the o eration can take up the most essential part f the crystallizations.

If the present surface of kernels should be too small and thereby the new formation of small kernels so great that the constant increase ofthe latter lcannot be regulated by the present means for taking out smallkernels, the catastrophical growth of these small kernels will transform the contents of the apparatus into a thick mass, before the larg` est kernels have attained the desired size.

The accompanying drawin illustrates as examples two uti izations of t e methoddiagrammatically. Figurel showsan apparatus for continuous manufacture of coarse-gran` ular precipitations by cooling, and Figure 2 an apparatus for continuous manufacture of coarse-granular precipitations by the evap-` oration of a solution.

`In Figure` 1, w is a vessel havin thel shape of a closed annular channel and eing vfilled with a solution and a suspension of larger or smaller kernels of the substance to be precipitated. b is a propeller which passes the solution in the direction indicated by the arrows. 0 is a cooling device consisting of pipes through` which the contents ofthe apparatus are passing. y j

The cross sectional areas of the vessel are all over so small that the suspension is taken along and circulates with the liquid.

All superfluous small crystals are removed before having time to grow up, by a pipe d los - large spaces f these small kernels facing its funnel-shaped opening e against the stream so'that a portion of the solutionv will takevits-waythrough thepipe d, the

space f and the aperture g. As the propeller b produces a rotation of the column of liquid, so that the coarser crystals .will be forced towards the wall of the vessel by the rcentrifugal force, the solution passing into the centrally disposed funnel e will contain only crystals of smaller dimensions. The quantity `of liquid-passing through d may be regulated by a cock lw. In comparatively will sink down -more or less completely and may be taken out through the cock h. The liquid passes on throughth'e aperture g into the main stream again.

When the main stream passes by the'aperture g1, a portion of the largest crystals will fall down through p g and the pipe i to.the

'conveyor'ls which removes them from the apparatus. The stream of liquid. coming from e through d prevents smaller crystals which have 4still not grown to the desired size from falling down through the aperture g.

l is a cross which smooths the rotation of liquid produced by the propeller, so that the crystalsinthe lower `part of the apparatus will not be flung against the wall, where they would 'be less completely 'taken along by the stream of liquid.

At m solution is taken out continuously,

at 'nf-new solution with a higher temperature and a higher proportion of the dissolved substancev is introduced continuously, vand at n, new, small crystals are introduced,

apparatus. In other words, care is taken systematically that only the same number of small kernels are allowed to o'row as the number of large kernels-'desired to remove. Each small kernel, namely, grows into. a large one, and if, therefore, the number of the kernels are not limited while they are small, diculties must arise.

In Figure 2, a is a ain a vessel of such a sha as to form a c osed annular channel. It 1s filled with a solutioncarrying a suspension of larger and smaller kernels of the substance or substances to be precipitated. A propeller b passes the contentsA in' the direction indicated by the arrows, ol is a superheater consisting of pipe through which the liquid and sus nsion are passing. At the level p the liqui is boiling and the steam passes out through g.

From a place r, -where the larger crystals will not arrive owing to an enlargement of the vessel a, a pump s sucks a solution mixed with small crystals out through va sedimentation compartment t, wherein a greater or smaller-part of the small crystals aresinking down and may be removed through the -cock h. Atu the liquid is then passed into` the vessel again. w is also a cock by which the quantity'of the liquid passing lthrough may l bev regulated.

From the same place r anotherpump lv sucks liquid which is free of largercrystals,

and drives them up through the-removalaperture g :for large crystals. The large crystals will fall down through the 'pipe i into the conveyor k.

Instead of removing the small crystals by sedimentation in t, other known methods may be used, such as for instance a throwing-out in a centrifugal separator, or filtration. Also the known peculiarity may be utilized that small crystals are more easily 4soluble than large ones, by'dissolving the lsmall crystals by passing under-saturated solution into the compartment t. v

New lsolution is introduced through the pipen.-

If the apparatus does notcreate' itself a suicient number of new small crystals, no

crystals are removed-through r t h, but-small crystals are introduced from outside through the aperture fnq.

These small crystals introduced from outside, may also be produced in a separate portion of the same apparatus, a higher supersaturation being vcreated here than'innother parts for instance by extra cooling. 1

The method of crystallizing out solid substances from supersaturated solutions thereof wherein the solution and a sus ension of granules of the substances circu ate cyclically which comprises circulatin the solution and suspension as a stream o relatively small ycross sectional area whereby the granules are normallyV positively carried along by the circulating stream', regulating the number of granules before they have.

vmaterially increased in size, and removing granules from the circulating stream -at esignated places therein.

In testimony that I claim lthe foregoing as my invention, I have signed my name.

ISAK ISAACHSEN.

losy

Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US2424206 *Jun 25, 1943Jul 15, 1947Fuel Refining CorpProduction of ammonium sulphate
US2761768 *Mar 18, 1953Sep 4, 1956Pouderies Reunis De BelgiquesCirculation nitrating apparatus
US3181593 *Jul 5, 1960May 4, 1965Atomic Energy Authority UkApparatus for concentrating solutions
US3193361 *Apr 7, 1961Jul 6, 1965Otto Saurebau U Keramikwerke DMethod of and device for continuously crystallizing iron sulfate hepta-hy-drate fromsulfates of mordanting solutions
US3503803 *Mar 22, 1968Mar 31, 1970Whiting CorpContinuous production of crystalline sucrose
US6670431Feb 27, 2003Dec 30, 2003Exxonmobil Chemical Patents, Inc.Continuous slurry polymerization volatile removal
US6743869Jun 20, 2002Jun 1, 2004Phillips Petroleum CompanyHigh polymer solids slurry polymerization employing 1-olefin comonomer
US6800698Mar 11, 2003Oct 5, 2004Exxonmobil Chemical Patents, Inc.Continuous slurry polymerization volatile removal
US6806324Jun 20, 2002Oct 19, 2004Phillips Petroleum CompanyHigh solids slurry polymerization using heat exchange to condense the flashed diluent
US6833415Feb 19, 2002Dec 21, 2004Exxonmobil Chemical Patents, Inc.Continuous slurry polymerization process and appparatus
US6858682Mar 11, 2003Feb 22, 2005Exxonmobil Chemical Patents, Inc.Continuous slurry polymerization volatile removal
US6926868Nov 6, 2001Aug 9, 2005Exxonmobil Chemical Patents Inc.Continuous slurry polymerization volatile removal
US7034090Feb 14, 2002Apr 25, 2006Exxonmobil Chemical Patents Inc.Continuous slurry polymerization volatile removal
US7268194Feb 28, 2002Sep 11, 2007Exxonmobil Chemical Patents Inc.Continuous slurry polymerization process and apparatus
US7575724Aug 1, 2007Aug 18, 2009Exxonmobil Chemical Patents Inc.Continuous slurry polymerization apparatus
US20020086955 *Feb 14, 2002Jul 4, 2002Kendrick James AustinContinuous slurry polymerization volatile removal
US20020132936 *Nov 6, 2001Sep 19, 2002Kendrick James AustinContinuous slurry polymerization volatile removal
US20030050409 *Aug 26, 2002Mar 13, 2003Hottovy John D.High solids slurry polymerization
US20030083444 *Dec 5, 2002May 1, 2003Mcelvain Robert R.Slotted slurry take off
US20030161765 *Feb 28, 2002Aug 28, 2003Kendrick James AustinContinuous slurry polymerization process and apparatus
US20030204031 *Mar 11, 2003Oct 30, 2003Exxonmobil Chemical CompanyContinuous slurry polymerization volatile removal
US20040192860 *May 19, 2004Sep 30, 2004Hottovy John D.Method and apparatus for high solids slurry polymerization
US20070274873 *Aug 1, 2007Nov 29, 2007Kendrick James AContinuous Slurry Polymerization Process and Apparatus
WO2003039739A1 *Nov 6, 2001May 15, 2003Robert G DepierriContinuous removal of polymerization slurry
Classifications
U.S. Classification23/301, 23/295.00R, 159/45
International ClassificationB01J19/18, B01D9/00
Cooperative ClassificationB01D9/0013, B01J19/1837
European ClassificationB01D9/00B4, B01J19/18C8