USH1510H - Continuous process for crystallizing nitroguanidine - Google Patents
Continuous process for crystallizing nitroguanidine Download PDFInfo
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- USH1510H USH1510H US07210881A US21088188DA USH1510H US H1510 H USH1510 H US H1510H US 07210881 A US07210881 A US 07210881A US 21088188D A US21088188D A US 21088188DA US H1510 H USH1510 H US H1510H
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- Prior art keywords
- nitroguanidine
- solution
- vinyl alcohol
- aqueous
- partially hydrolyzed
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C279/00—Derivatives of guanidine, i.e. compounds containing the group, the singly-bound nitrogen atoms not being part of nitro or nitroso groups
- C07C279/30—Derivatives of guanidine, i.e. compounds containing the group, the singly-bound nitrogen atoms not being part of nitro or nitroso groups having nitrogen atoms of guanidine groups bound to nitro or nitroso groups
- C07C279/32—N-nitroguanidines
- C07C279/34—N-nitroguanidine
Definitions
- This invention relates to guanidines and more particularly to nitroguandine.
- Nitroguanidine is a mass detonating explosive. It is a white crystalline powder with a specific gravity of 1.77. Tests conducted at the Naval Ordnance Laboratory in White Oak, Maryland, (Feb. 1968) showed that in its range of detonability, nitroguanidine behaves as a group I Explosive Class 1, Division 1 (Old Class 7), DOT Class A. This means that it is a mass detonating hazard. The entire quantity will explode virtually instantaneously when a small portion is subjected to the impulse of an initiating agent, or to the effect of a considerable discharge of energy from without, or from sympathetic detonation or propagation.
- Nitroguanidine is a powerful high explosive which when incorporated in a propellant in appreciable quantities, results in a propellant that burns in a gun with a temperature so cool that a little muzzle flash is produced.
- Nitroguanidine was first prepared by Jousselin in 1877, and found its original application in cool, burning triple-base, Naval gun propellants in trench mortar shells. Its principal use, however, is in smokeless propellant, due to its property of eliminating flash. In later years nitroguanidine has been developed as an ingredient in propellants for rockets and missiles. High bulk density nitroguanidine (HBNQ) is prepared for these later applications.
- the alpha form crystallizes from hot water as long, thin, flexible, lustrous needles which are tough and pulverize with difficulty. It is the form most commonly used in the explosive industry.
- the beta form crystallizes from hot water in fern-like clusters of small, thin, elongated plates. The beta form may, be converted into the alpha by dissolution in concentrated sulfuric acid and drowning in water.
- a communitor with a hammer speed of 7500 RPM is used to reduce the HBNQ particles to desired size.
- a uniform feed rate is essential for uniform end product.
- a built-in feeder permits continuous operation and maximum performance. Once the communitor is set to deliver a certain product it will continue to produce exactly the same results. This last step is very labor-consuming and has a high potential for exploding during the crushing and also the drying operations. Also, the convection oven drying of the nitroguanidine releases undesirable organic chemicals into the environment.
- the HBNQ which is produced by these prior art methods is rodshaped or needleshaped and therefore difficult to use in explosive manufacturing processes such as extrusion and melt casting.
- an object of this invention is to provide high bulk density nitroguanidine.
- Another object of this invention is to provide a safer method of producing high bulk density nitroguanidine.
- a further object of this invention is to eliminate the need for reducing nitroguanidine particle size by hammering.
- Yet another object of this invention is to provide a method which will produce spheroidal rather than rodshaped or needleshaped nitroguanidine crystals.
- a still further object of this invention is to provide a continuous process for producing spheroidal high bulk density nitroguanidine.
- a continuous process for recrystallizing nitroguandine comprising the following steps in order:
- T 1 which is in the range of from about 70° C. to about 100° C. wherein the solution also contains from 0.5 to 2.0 weight percent of methylcellulose and from 0.5 to 2.0 weight percent of a partially hydrolyzed poly(vinyl alcohol);
- step (2) feeding the solution formed in step (1) into a crystallizer containing a saturated aqueous solution of nitroguanidine which is maintained at a constant temperature of T 2 wherein 20° C. ⁇ T 1 -T 2 ⁇ 50° C. and wherein the methylcellulose and partially hydrolyzed poly(vinyl alcohol) concentrations are the same as in the feed solution;
- the FIGURE is a block diagram of the equipment used in the general continuous process.
- the present process is used to convert needleshaped, rodshaped, or jagged granular nitroguanidine (NQ) crystals into spheroidal or ovate (egg-shaped) high bulk density nitroguanidine (HBNQ).
- NQ needleshaped, rodshaped, or jagged granular nitroguanidine
- HBNQ high bulk density nitroguanidine
- the round HBNQ spheroidal or ovate crystals produce explosive compositions which are easier to process (mix, extrude, etc.) than do the sharp, jagged NQ crystals.
- the present process uses an aqueous solution of nitroguanidine with methylcellulose and partially hydrolyzed poly(vinyl alcohol) as crystal habit modifiers.
- a saturated aqueous solution of nitroguanidine at a temperature of T 1 and corresponding saturation concentration of C 1 is fed from a feed solution reservoir 24 through feed stream line 26 to a crystallizer 28.
- the aqueous nitroguanidine solution in the crystallizer 28 is maintained at a constant temperature T 2 with corresponding saturation concentration C 2 where T 1 >T 2 and C 1 >C 2 .
- the solution in the crystallizer 28 is well agitated by suitable means such as a high speed stirrer. In maintaining the constant temperature T 2 in the crystallizer 28, the following factors come into play: (1) the size of the crystallizer 28, (2) the rate of feed of solution from line 26, and (3) the use of cooling means.
- Supernatant liquid is removed from the crystallizer 28 and returned through line 30 to the feed solution resevoir 24.
- a slurry of HBNQ crystals and aqueous nitroguanidine solution is transferred from the crystallizer 28 through product stream line 32 to a separator 34 where the HBNQ crystals are removed and placed into storage 36.
- the remaining supernatant liquid is transferred from the separator 34 through line 38 to the feed solution reservoir 24.
- the temperature and nitroguanidine concentration of the solutions from lines 30 and 38 are raised again to T 1 and C 1 .
- raw solid nitroguanidine is added from storage 22 to the feed solution reservoir 24 to maintain the nitroguanidine concentration at C 1 .
- the temperature in reservoir 24 is kept at constant T 1 by the following: (1) the capacity of the resevoir, (2) the flow of solution (T 2 , C 2 ) from lines 30 and 38 into the reservoir 24, and (3) heating means.
- methylcellulose and partially hydrolyzed poly(vinyl alcohol) as a crystal modifier pair is critical to this invention. If no crystal modifier is used, or if methylcellulose alone or partially hydrolyzed poly(vinyl alcohol) alone is used as a crystal modifier, needleshaped or rodshaped nitroguanidine crystals are produced. However, when a mixture of methylcellulose and partially hydrolyzed poly(vinyl alcohol) is used as a crystal modifier, high bulk density spheroidal or egg-shaped nitroguanidine crystals (HBNQ) are produced.
- HBNQ high bulk density spheroidal or egg-shaped nitroguanidine crystals
- methyl cellulose is used in the present process.
- Poly(vinyl alcohol) is prepared by the alcoholysis of poly(vinyl acetate). A 85 to 90% hydrolyzed (acetal content 15 to 10%) and preferably 87 to 89% hydrolyzed (acetal content 13 to 11%) poly(vinyl alcohol) is used in the present process. These partially hydrolyzed poly(vinyl alcohols) have good solubilities in water for both the high (T 1 ) and the low (T 2 ) temperature ranges of this process, with 87-89% hydrolyzed poly(vinyl alcohols) being optimal.
- the Merck Index (10th edition) page 1095, monograph No. 7458, provides information on and a list of proprietary names for poly(vinyl alcohol).
- the feed solution temperature T 1 and the crystallizer temperature T 2 are selected to produce spheroidal or ovate high bulk density nitroguanidine crystals (HBNQ) at an efficient rate.
- the feed solution temperature T 1 is preferably in the range of 70° C. ⁇ T 1 ⁇ 100° C. and more preferably in the range of 80° C. ⁇ T 1 ⁇ 100° C.
- the concentration of the feed solution C 1 is the saturation concentration of nitroguanidine in water at T 1 .
- the crystallizer solution temperature T 2 is defined in terms of the feed solution temperature. Preferably 20° C. ⁇ T 1 -T 2 ⁇ 50° C. and more preferably 30° C. ⁇ T 1 -T 2 ⁇ 40° C.
- Particle size and distribution are determined primarily by the residence time of the crystals in the crystallizer 28. Other factors such as the nitroguanidine concentration or the agitation rate in the crystallizer do have influence but to a lessor extent.
- the residence time of crystals is controlled by the rate of the feed stream 26 into the crystallizer 28. When the crystals reach the desired size they fall to the bottom of the crystallizer 28 and are drawn off in the product stream 32.
- Distilled water was heated by a hot plate in a 3-liter beaker to 68° C. (155° F.). Distilled water was also heated to 68° C. (155° F.) in a 3-liter reactor placed in a steam bath.
- NQ nitroguanidine
- the solution in the 3-liter beaker was heated to boiling.
- the solution in the reactor was heated to 96° C. (205° F.) and then cooled to the desired operating temperature.
- Air operated agitator round bottomed blade 8 cm ⁇ 2 cm
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A continuous process for forming spheroidal high bulk density nitroguanidine crystals from an aqueous solution of nitroguanidine which contains methylcellulose and partially hydrolyzed poly(vinyl alcohol) as crystal habit modifiers. A saturated aqueous solution of nitroguanidine is formed at a temperature T1 where 70 DEG C.</=T1</=100 DEG C. and crystallization occurs at a lower temperature T2 where 20 DEG C.</=T1-T2</=50 DEG C.
Description
This invention relates to guanidines and more particularly to nitroguandine.
Nitroguanidine is a mass detonating explosive. It is a white crystalline powder with a specific gravity of 1.77. Tests conducted at the Naval Ordnance Laboratory in White Oak, Maryland, (Feb. 1968) showed that in its range of detonability, nitroguanidine behaves as a group I Explosive Class 1, Division 1 (Old Class 7), DOT Class A. This means that it is a mass detonating hazard. The entire quantity will explode virtually instantaneously when a small portion is subjected to the impulse of an initiating agent, or to the effect of a considerable discharge of energy from without, or from sympathetic detonation or propagation. Such an explosion normally will cause severe structural damage to adjacent objects and the simultaneous explosion of other separated explosives and ammunition placed sufficiently close to the initially exploding mass. Casting powder, bulk explosives such as TNT, HMX, RDX, and most warheads and bombs are in this class.
Nitroguanidine is a powerful high explosive which when incorporated in a propellant in appreciable quantities, results in a propellant that burns in a gun with a temperature so cool that a little muzzle flash is produced. Nitroguanidine was first prepared by Jousselin in 1877, and found its original application in cool, burning triple-base, Naval gun propellants in trench mortar shells. Its principal use, however, is in smokeless propellant, due to its property of eliminating flash. In later years nitroguanidine has been developed as an ingredient in propellants for rockets and missiles. High bulk density nitroguanidine (HBNQ) is prepared for these later applications.
Nitroguanidine exists in at least 2 crystal forms: an alpha and a beta. The alpha form crystallizes from hot water as long, thin, flexible, lustrous needles which are tough and pulverize with difficulty. It is the form most commonly used in the explosive industry. The beta form crystallizes from hot water in fern-like clusters of small, thin, elongated plates. The beta form may, be converted into the alpha by dissolution in concentrated sulfuric acid and drowning in water.
A communitor with a hammer speed of 7500 RPM is used to reduce the HBNQ particles to desired size. There are two variables to control the particle size: screen size and feed rate. By keeping the screen and hammer speed constant, but changing to a heavier gauge screen, a smaller particle size is achieved. Therefore, when going to heavier gauge screens for greater strength, it is necessary to increase the size of the opening if the same product size is needed. A uniform feed rate is essential for uniform end product. A built-in feeder permits continuous operation and maximum performance. Once the communitor is set to deliver a certain product it will continue to produce exactly the same results. This last step is very labor-consuming and has a high potential for exploding during the crushing and also the drying operations. Also, the convection oven drying of the nitroguanidine releases undesirable organic chemicals into the environment.
Moreover, the HBNQ which is produced by these prior art methods is rodshaped or needleshaped and therefore difficult to use in explosive manufacturing processes such as extrusion and melt casting.
It would be desirable to provide a continuous process for producing round ovate or spheroidal high bulk density nitroguandine crystals.
Accordingly, an object of this invention is to provide high bulk density nitroguanidine.
Another object of this invention is to provide a safer method of producing high bulk density nitroguanidine.
A further object of this invention is to eliminate the need for reducing nitroguanidine particle size by hammering.
Yet another object of this invention is to provide a method which will produce spheroidal rather than rodshaped or needleshaped nitroguanidine crystals.
A still further object of this invention is to provide a continuous process for producing spheroidal high bulk density nitroguanidine.
These and other objects of this invention are accomplished by providing:
A continuous process for recrystallizing nitroguandine comprising the following steps in order:
(1) forming a saturated aqueous nitroguanidine solution at a constant temperature T1 which is in the range of from about 70° C. to about 100° C. wherein the solution also contains from 0.5 to 2.0 weight percent of methylcellulose and from 0.5 to 2.0 weight percent of a partially hydrolyzed poly(vinyl alcohol);
(2) feeding the solution formed in step (1) into a crystallizer containing a saturated aqueous solution of nitroguanidine which is maintained at a constant temperature of T2 wherein 20° C.≦T1 -T2 ≦50° C. and wherein the methylcellulose and partially hydrolyzed poly(vinyl alcohol) concentrations are the same as in the feed solution;
(3) separating the product spheroidal or ovate nitroguanidine crystals from the supernatant aqueous nitroguanidine solution; and
(4) recycling the separated supernatant aqueous nitroguanidine solution to be used again in step (1).
Other objects and many of the attendant advantages of the present invention will be readily appreciated as the same becomes better understood by reference to the following detailed description when considered in connection with the accompanying drawing wherein:
The FIGURE is a block diagram of the equipment used in the general continuous process.
The present process is used to convert needleshaped, rodshaped, or jagged granular nitroguanidine (NQ) crystals into spheroidal or ovate (egg-shaped) high bulk density nitroguanidine (HBNQ). In addition to higher bulk densities, the round HBNQ spheroidal or ovate crystals produce explosive compositions which are easier to process (mix, extrude, etc.) than do the sharp, jagged NQ crystals.
The present process uses an aqueous solution of nitroguanidine with methylcellulose and partially hydrolyzed poly(vinyl alcohol) as crystal habit modifiers. Referring to the FIGURE, a saturated aqueous solution of nitroguanidine at a temperature of T1 and corresponding saturation concentration of C1 is fed from a feed solution reservoir 24 through feed stream line 26 to a crystallizer 28. The aqueous nitroguanidine solution in the crystallizer 28 is maintained at a constant temperature T2 with corresponding saturation concentration C2 where T1 >T2 and C1 >C2. The solution in the crystallizer 28 is well agitated by suitable means such as a high speed stirrer. In maintaining the constant temperature T2 in the crystallizer 28, the following factors come into play: (1) the size of the crystallizer 28, (2) the rate of feed of solution from line 26, and (3) the use of cooling means.
Supernatant liquid is removed from the crystallizer 28 and returned through line 30 to the feed solution resevoir 24. A slurry of HBNQ crystals and aqueous nitroguanidine solution is transferred from the crystallizer 28 through product stream line 32 to a separator 34 where the HBNQ crystals are removed and placed into storage 36. The remaining supernatant liquid is transferred from the separator 34 through line 38 to the feed solution reservoir 24.
In the feed solution reservoir 24, the temperature and nitroguanidine concentration of the solutions from lines 30 and 38 are raised again to T1 and C1. Note that raw solid nitroguanidine is added from storage 22 to the feed solution reservoir 24 to maintain the nitroguanidine concentration at C1. The temperature in reservoir 24 is kept at constant T1 by the following: (1) the capacity of the resevoir, (2) the flow of solution (T2, C2) from lines 30 and 38 into the reservoir 24, and (3) heating means.
The use of methylcellulose and partially hydrolyzed poly(vinyl alcohol) as a crystal modifier pair is critical to this invention. If no crystal modifier is used, or if methylcellulose alone or partially hydrolyzed poly(vinyl alcohol) alone is used as a crystal modifier, needleshaped or rodshaped nitroguanidine crystals are produced. However, when a mixture of methylcellulose and partially hydrolyzed poly(vinyl alcohol) is used as a crystal modifier, high bulk density spheroidal or egg-shaped nitroguanidine crystals (HBNQ) are produced. Preferably from about 0.5 to about 2.0 and more preferably from 0.6 to 1.0 weight percent of methylcellulose is used with from about 0.5 to about 2.0 and more preferably from 0.6 to 1.0 weight percent of partially hydrolyzed poly(vinyl alcohol) in the aqueous nitroguanidine solution.
Commercial methyl cellulose is used in the present process. The Merck Index (10th edition), page 866, monograph No. 5917, states that commercial methylcellulose (or methyl cellulose ether) has a methoxyl content of 29% (degree of substitution about 1.8) and that it is available under proprietary names such as Methocel, Cellothyl, Syncelose, Bagolax, Cethylose, Cethytin, Cologel Cellumeth, Hydrolose, Nicel, Tearisol, Tylose, etc.
Poly(vinyl alcohol) is prepared by the alcoholysis of poly(vinyl acetate). A 85 to 90% hydrolyzed (acetal content 15 to 10%) and preferably 87 to 89% hydrolyzed (acetal content 13 to 11%) poly(vinyl alcohol) is used in the present process. These partially hydrolyzed poly(vinyl alcohols) have good solubilities in water for both the high (T1) and the low (T2) temperature ranges of this process, with 87-89% hydrolyzed poly(vinyl alcohols) being optimal. The Merck Index (10th edition) page 1095, monograph No. 7458, provides information on and a list of proprietary names for poly(vinyl alcohol).
Other critical parameters of this process are the feed solution temperature T1 and the crystallizer temperature T2. These temperatures are selected to produce spheroidal or ovate high bulk density nitroguanidine crystals (HBNQ) at an efficient rate. The feed solution temperature T1 is preferably in the range of 70° C.≦T1 ≦100° C. and more preferably in the range of 80° C.≦T1 ≦100° C. The concentration of the feed solution C1 is the saturation concentration of nitroguanidine in water at T1. The crystallizer solution temperature T2 is defined in terms of the feed solution temperature. Preferably 20° C.≦T1 -T2 ≦50° C. and more preferably 30° C.≦T1 -T2 ≦40° C.
Particle size and distribution are determined primarily by the residence time of the crystals in the crystallizer 28. Other factors such as the nitroguanidine concentration or the agitation rate in the crystallizer do have influence but to a lessor extent. The residence time of crystals is controlled by the rate of the feed stream 26 into the crystallizer 28. When the crystals reach the desired size they fall to the bottom of the crystallizer 28 and are drawn off in the product stream 32.
The general nature of the invention having been set forth, the following examples are presented as specific illustrations thereof. It will be understood that the invention is not limited to these examples but is susceptible to various modifications that will be recognized by one of ordinary skill in the art.
In the following examples 1-14, processes were run under conditions which simulated a continuous process. A 3-liter beaker was used as the feed solution reservoir 24 and a 3-liter reactor with stirrer was used as the crystallizer 28 in the FIGURE. The concentrations of methycellulose and partially hydrolyzed poly(vinyl alcohol) were the same in both the beaker (feed solution resevoir) and the reactor (crystallizer) as they would be in a recycling continuous process. Specifically, the following procedure was used in examples 1 through 14:
1. Distilled water was heated by a hot plate in a 3-liter beaker to 68° C. (155° F.). Distilled water was also heated to 68° C. (155° F.) in a 3-liter reactor placed in a steam bath.
2. While being agitated, dry Methocel or partially hydrolyzed poly(vinyl alcohol) or a combination of both were added to the beaker and reactor.
3. The solutions in the 3-liter reactor and beaker were heated further to to 82° C. (180° F.), then cooled to below 32° C. (90° F.).
4. The solutions were then diluted with an equal volume of water and reheated to 82° C. (180° F.).
5. While being agitated, the desired concentrations of nitroguanidine (NQ) were added to the solutions.
6. The solution in the 3-liter beaker was heated to boiling. The solution in the reactor was heated to 96° C. (205° F.) and then cooled to the desired operating temperature.
7. While being agitated, the hot beaker of nitroguanidine solution was poured into the 3-liter reactor. The rate of addition was dictated by the rate of cooling, i.e., to maintain a constant temperature within the reactor.
8. Immediately after the addition was complete, the agitator was turned off and the crystals were allowed to settle.
9. The supernatant liquid was decanted off and the crystals were washed with distilled water in the 3-liter flask.
10. The crystals were collected on a fritted polyethylene Buchner funnel and then sent for analysis.
Equipment used:
3-liter beaker (as the feed solution resevoir)
Hot plate and magnetic stirrer
Thermometer
3-liter round-bottomed reactor (as the crystallizer)
Air operated agitator (round bottomed blade 8 cm×2 cm)
Steam bath
Vacuum source
Fritted polyethylene Buchner funnel
The reaction conditions and results of examples 1 through 14 are presented in Table 1.
TABLE 1
__________________________________________________________________________
CONTINUOUS RECRYSTALLIZATION RESULTS NITROGUANIDINE (NQ)
Experi-
Agitator Temperature
NQ Concentration
NQ Concentration
Additive(s).sup.1,2
Bulk
ment Speed Temperature
of feed
In Crystallizer
in Solution
Feed Solution
Density
Crystal
Number
(rpm) of Crystallizer
Solution
% % and Crystallizer
g/cm.sup.3
Shape(s)
__________________________________________________________________________
1 500 50° C.
100° C.
0.0 5.0 0.6% Methocel
0.56 N
2 450 37° C.
100° C.
0.0 5.0 0.6% Methocel
-- N
3 500 31° C.
100° C.
0.0 5.0 0.6% Methocel
0.59 N
4 400 70° C.
100° C.
2.2 5.0 0.6% Methocel
-- N
5 200 70° C.
100° C.
2.2 5.0 0.6% VINOL 540
0.83 N, G
0.6% Methocel
6 200 70° C.
100° C.
2.2 5.0 0.6% VINOL 540
0.91 E
0.6% Methocel
7 300 52° C.
100° C.
0.8 4.0 0.6% VINOL 540
0.91 E
0.6% Methocel
8 300 52° C.
100° C.
0.8 4.0 0.6% VINOL 540
0.72 N, G
9 250 52° C.
100° C.
0.8 4.0 0.6% % Methocel
-- E
0.6% VINOL 540
10 500 79° C.
100° C.
4.0 5.0 0.6% Methocel
-- N, G
0.6% VINOL 540
11 100 79° C.
100° C.
4.0 5.0 0.6% Methocel
0.90 N, G
0.6% VINOL 540
12 50 52° C.
100° C.
1.0 5.0 0.6% Methocel
0.80 N, G
0.6% VINOL 540
13 500 65° C.
100° C.
4.0 5.0 0.6% Methocel
0.87 E
0.6% VINOL 540
14 600 65° C.
100° C.
2.0 4.0 0.6% Methocel
1.0 E
0.6% VINOL 540
__________________________________________________________________________
1. Crystal habit modifier concentrations are identical in the feed
solution and in the crystalizer as they would be in a continously
recycling process.
2. VINOL 540 is a partially hydrolyzed (87-89%) poly(vinyl alcohol)
polymer [900289-5] (PVA) which is available from the Polymer Chemicals
Division of Air Products and Chemicals, Inc. Box 538, Allentown, Pa 18105
A 4% aqueous solution of VINOL 540 has a viscosity of 22-26 CPS at
20° C. and a pH range of 4.0-6.0.
3. N = needleshaped, G = jagged granular, and E = eggshaped (ovate)
Obviously, numerous modifications and variations of the present invention are possible in light of the above teachings. It is therefore to be understood that within the scope of the appended claims the invention may be practiced otherwise than as specifically described herein.
Claims (8)
1. A continuous process for recrystallizing nitroguanidine comprising the following steps in order:
(1) forming a saturated aqueous nitroguanidine solution at a constant temperature T1 which is in the range of from about 70° C. to about 100° C. wherein the solution also contains from 0.5 to 2.0 weight percent of methylcellulose and from 0.5 to 2.0 weight percent of a partially hydrolyzed poly(vinyl alcohol);
(2) feeding the solution formed in step (1) into a crystallizer containing a saturated aqueous solution of nitroguanidine which is maintained at a constant temperature of T2 wherein 20° C.≦T1 -T2 ≦50° C. and wherein the methylcellulose and partially hydrolyzed poly(vinyl alcohol) concentrations are the same as in the feed solution;
(3) separating the product spheroidal or ovate nitroguanidine crystals from the supernatant aqueous nitroguanidine solution; and
(4) recycling the separated supernatant aqueous nitroguanidine solution to be used again in step (1).
2. The process of claim wherein the solution in the crystalizer in step (2) is continuously agitated.
3. The process of claim 1 wherein 80° C.≦T1 ≦100° C.
4. The process of claim 3 wherein 30° C.≦T1 -T2 ≦40° C.
5. The process of claim 1 wherein 30° C.≦T1 -T2 ≦40° C.
6. The process of claim 1 wherein the concentration of methylcellulose in the aqueous nitroguanidine solutions is from 0.5 to 1.0 percent by weight.
7. The process of claim 6 wherein the concentration of partially hydrolyzed poly(vinyl alcohol) in the aqueous nitroguanidine solutions is from 0.5 to 1.0 percent by weight.
8. The process of claim 1 wherein the concentration of partially hydrolyzed poly(vinyl alcohol) in the aqueous nitroguanidine solutions is from 0.5 to 1.0 percent by weight.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US07210881A USH1510H (en) | 1988-06-23 | 1988-06-23 | Continuous process for crystallizing nitroguanidine |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US07210881A USH1510H (en) | 1988-06-23 | 1988-06-23 | Continuous process for crystallizing nitroguanidine |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| USH1510H true USH1510H (en) | 1995-12-05 |
Family
ID=90354812
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US07210881A Abandoned USH1510H (en) | 1988-06-23 | 1988-06-23 | Continuous process for crystallizing nitroguanidine |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | USH1510H (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20120165497A1 (en) * | 2009-12-28 | 2012-06-28 | Erema Engineering Recycling Maschinen Und Anlagen Gesellschaft M.B.H. | Method and device for producing semicrystalline polymer material |
-
1988
- 1988-06-23 US US07210881A patent/USH1510H/en not_active Abandoned
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20120165497A1 (en) * | 2009-12-28 | 2012-06-28 | Erema Engineering Recycling Maschinen Und Anlagen Gesellschaft M.B.H. | Method and device for producing semicrystalline polymer material |
| US8932404B2 (en) * | 2009-12-28 | 2015-01-13 | Erema Engineering Recycling Maschinen Und Anlagen Gesellschaft M.B.H. | Method and device for producing semicrystalline polymer material |
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