CN1569635A - Method for increasing production of industrial ammonium chloride by adding salt to crystallizer - Google Patents
Method for increasing production of industrial ammonium chloride by adding salt to crystallizer Download PDFInfo
- Publication number
- CN1569635A CN1569635A CN 03130438 CN03130438A CN1569635A CN 1569635 A CN1569635 A CN 1569635A CN 03130438 CN03130438 CN 03130438 CN 03130438 A CN03130438 A CN 03130438A CN 1569635 A CN1569635 A CN 1569635A
- Authority
- CN
- China
- Prior art keywords
- salt
- crystallizer
- cold
- cool crystallizer
- mother liquor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a process for preparing industrial ammonium chloride from ammonium chloride in cold separating crystallizer which comprises the steps of, premixing the mother liquor and salts in combination alkali production process, obtaining salt grout or saline solution, loading into cold crystallizer, or charging salt directly into cold crystallizer, wherein the ratio of the weight ratio of the cold AI volume throwing amount for cold crystallizer and the admission weight amount of salts is 100:0.5-6.5.
Description
Technical field
The present invention relates to a kind of production method of industrial ammonium chloride, the invention particularly relates to a kind of production method of in cool crystallizer, increasing production industrial ammonium chloride with salt.
Background technology
Second process of soda and sociation center is system ammonium process, in order to produce agriculture ammonium chloride manufacture ammonium chloride (being called for short smart ammonium) in the time of (being called for short agricultural ammonium), needs to adopt and the materials flow journey.It is that the mother liquor I (MI) behind the separation sodium bicarbonate is once inhaled ammonia, heat exchange cooling, become cold AI, cold AI enters cool crystallizer after metering, continuous circulation cooling through outer cooler, ammonium chloride in the mother liquor is separated out because of the reduction of solubleness, become the higher ammonium chloride of purity after taking-up, stiff, separation, the drying, promptly smart ammonium.Cool crystallizer overflowing liquid half mother liquor II (half II) enters salting-out crystallizer, add the desalinization of soil by flooding or leaching (crude salt is the desalinization of soil by flooding or leaching through pulverizing after partial impurities is removed in washing) simultaneously in the salting-out crystallizer, because common-ion effcet, ammonium chloride in the mother liquor is further separated out, the influence that last products obtained therefrom is brought system's impurity into when being subjected to adding the desalinization of soil by flooding or leaching, quality does not reach the standard of smart ammonium and becomes agricultural ammonium.Salting-out crystallizer overflowing liquid mother liquor II (MII) carries out becoming ammonia mother liquor II (AII) behind heat exchange, the suction ammonia, and first process of delivering to is made alkali after carbonization.
Generally speaking, the C of AI
NH3For about 80tt, the C of cool crystallizer overflowing liquid half II
NH3For about 66tt, the C of salting-out crystallizer overflowing liquid MII
NH3For about 42tt.Mother solution C after cold analysis
NH3Drop-out value be 80-66=14tt, mother solution C after saltouing
NH3Drop-out value be 66-42=24tt, 14 ÷ (14+24) * 100%=38%, the smart ammonium output of Theoretical Calculation accounts for 38% of ammonium chloride ultimate production.And in the actual production, the magma that cool crystallizer has the magma of half to take out (smart ammonium) and salting-out crystallizer approximately takes out (agricultural ammonium) and enters mixing stiff device together, in order to dilution with wash salt in the agricultural ammonium, so in fact, the output of smart ammonium only accounts for the 15-20% of ammonium chloride ultimate production.
Summary of the invention
The object of the present invention is to provide a kind of method of increasing production smart ammonium in cool crystallizer with salt, the production method that is proposed without any influence, reaches the purpose of smart ammonium volume increase to production system when guaranteeing smart ammonium constant product quality.
The objective of the invention is to realize by following proposal.
Method of the present invention may further comprise the steps: be pre-mixed with mother liquor in the combined soda method production process and salt, modulate salifiable magma or salts solution, add in the cool crystallizer, or salt directly added in the cool crystallizer, the add-on of described cool crystallizer inner salt is that the ratio of the weight of the cold AI volume of cool crystallizer throwing amount and salt is 100: 0.5-6.5.
The present invention does not do any change to original production process flow process and equipment, and only needing increases simple equipment, and cold analysis and saltout and carry out simultaneously in cool crystallizer realizes cold analysis and the combination of saltouing, and reaches the purpose that smart ammonium increases production.Smart ammonium constant product quality, to production system without any influence.1 ton of salt of every adding, smart ammonium volume increase 0.65-0.9t, many more with salt not influencing under the product quality premise, the amplitude of smart ammonium volume increase is big more.Farming ammonium and smart ammonium have tangible price difference, and smart ammonium volume increase can be enterprise and brings remarkable economic efficiency.In general, ammonia alkali factory by-product refine salt, so the present invention is particularly suitable for the producer of ammonia connection alkali and product.
Embodiment
Below the present invention is further illustrated.
Mother liquor and salt enter salt slurry bucket by arbitrary proportion, are pre-mixed modulation salify slurry or salts solution in salt slurry bucket.With brine pump above-mentioned salt slurry or salts solution are beaten to cool crystallizer, the add-on of salt is in the cool crystallizer: the cold AI throwing of cool crystallizer amount (volume, m
3) and the ratio of salt (weight, ton) be 100: 0.5-6.5.Miscellaneous equipment and flow process are not done change.
The available mother liquor has cold AI, half II, hot AI, or more than one the mixing mother liquor in the above-mentioned mother liquor, considers the temperature and the composition of mother liquor, the preferably cold AI of used mother liquor.Is salt modulation salify slurry or salts solution in order salt to be partly dissolved in advance or all dissolvings, to prevent that the particle of salt from entering smart ammonium product.For ease of the design selection of operation and equipment, the preferred proportion that modulation salt is starched used mother liquor and salt is: mother liquor (volume, m
3): salt (weight, ton)=10: 1-5.Salt also can directly add cool crystallizer.Can add continuously with salt, also can add discontinuously.The cool crystallizer that adds with salt can be a separate unit, also can be many.Requirement to salt: because the granularity of salt directly influences the dissolution time of salt in cool crystallizer, so the granularity of salt should satisfy salt all dissolvings in cool crystallizer; The kind of impurities and content do not influence the quality of smart ammonium product in the salt.Used salt can be: the refine salt of refined salt, the measured desalinization of soil by flooding or leaching of matter, ammonia alkali factory, or the mixing salt of more than one salt.
Embodiment 1
The cold AI throwing of separate unit cool crystallizer amount 100m
3/ h, with hot AI modulation salify slurry, the harmonic proportion that modulation salt is starched the weight of the volume of used mother liquor and salt is 10: 2, with brine pump salt is starched and is squeezed into this cool crystallizer, the add-on 6.5t/h of salt, the cold AI throwing of cool crystallizer amount (volume, m refine salt
3) and the ratio of salt (weight, ton) be 100: 6.5, continue 4 hours with salt, smart ammonium quality product reaches country-level product standard, during this period the smart ammonium volume increase of this cool crystallizer 4.2t/h.
Embodiment 2
The cold AI throwing of separate unit cool crystallizer amount 100m
3/ h, with cold AI modulation salify slurry, the harmonic proportion that modulation salt is starched the weight of the volume of used mother liquor and salt is 10: 3, with brine pump salt is starched and is squeezed into this cool crystallizer, the add-on 4t/h of salt, the cold AI throwing of cool crystallizer amount (volume, m refined salt
3) and the ratio of salt (weight, ton) be 100: 4, continue 4 hours with salt, smart ammonium quality product reaches country-level product standard, the smart ammonium volume increase of this cool crystallizer 2.8t/h.
Embodiment 3
The cold AI throwing of separate unit cool crystallizer amount 100m
3/ h, with half II modulation salify slurry, the harmonic proportion that modulation salt is starched the weight of the volume of used mother liquor and salt is 10: 1, with brine pump salt is starched and is squeezed into this cool crystallizer, the add-on 0.5t/h of salt, the cold AI throwing of cool crystallizer amount (volume, m the desalinization of soil by flooding or leaching
3) and the ratio of salt (weight, ton) be 100: 0.5, operation continuously, smart ammonium quality product reaches country-level product standard, the smart ammonium volume increase of this cool crystallizer 0.45t/h.
Embodiment 4
The cold AI throwing of separate unit cool crystallizer amount 100m
3/ h, with cold AI, half II modulation salify slurry, the harmonic proportion that modulation salt is starched the weight of the volume of used mother liquor and salt is 10: 2 refine salt and the desalinization of soil by flooding or leaching, with brine pump the salt slurry is squeezed into this cool crystallizer, the add-on 2t/h of salt, the cold AI throwing of cool crystallizer amount (volume, m
3) and the ratio of salt (weight, ton) be 100: 2, operation continuously, smart ammonium quality product reaches country-level product standard, the smart ammonium volume increase of this cool crystallizer 1.6t/h.
Embodiment 5
Two the cold AI throwing of cool crystallizer amounts respectively are 100m
3/ h, with hot AI, half II modulation salify slurry, the harmonic proportion that modulation salt is starched the weight of the volume of used mother liquor and salt is 10: 2 refine salt and refined salt, with brine pump the salt slurry is squeezed into this cool crystallizer, the add-on 2t/h of salt in every cool crystallizer, the cold AI throwing of cool crystallizer amount (volume, m
3) and the ratio of salt (weight, ton) be 100: 2, operation continuously, smart ammonium quality product reaches country-level product standard, the smart ammonium volume increase of this cool crystallizer 1.6t/h.
Embodiment 6
The cold AI throwing of separate unit cool crystallizer amount 100m
3/ h, with cold AI modulation salify slurry, the harmonic proportion that modulation salt is starched the weight of the volume of used mother liquor and salt is 10: 5, with brine pump salt is starched and is squeezed into this cool crystallizer, the add-on 2t/h of salt, the cold AI throwing of cool crystallizer amount (volume, m the desalinization of soil by flooding or leaching and refined salt
3) and the ratio of salt (weight, ton) be 100: 2, operation continuously, smart ammonium quality product reaches country-level product standard, the smart ammonium volume increase of this cool crystallizer 1.6t/h.
Embodiment 7
Two the cold AI throwing of cool crystallizer amounts respectively are 100m
3/ h, with cold AI modulation salify slurry, the harmonic proportion that modulation salt is starched the weight of the volume of used mother liquor and salt is 10: 4 refine salt, the add-on 2t/h of salt in every cool crystallizer, with brine pump the salt slurry is squeezed into two cool crystallizers, the cold AI throwing of cool crystallizer amount (volume, m
3) and the ratio of salt (weight, ton) be 100: 2, operation continuously, smart ammonium quality product reaches country-level product standard, two smart ammoniums volume increase of cool crystallizer add up to 3.2t/h.
Embodiment 8
The cold AI throwing of separate unit cool crystallizer amount 100m
3/ h directly adds cool crystallizer to refine salt, the add-on 3t/h of salt, the cold AI throwing of cool crystallizer amount (volume, m
3) and the ratio of salt (weight, ton) be 100: 3, continue 4 hours with salt, smart ammonium quality product reaches country-level product standard, the smart ammonium volume increase of this cool crystallizer 2.25t/h.
Claims (3)
- One kind in cool crystallizer with the method for salt volume increase industrial ammonium chloride, it is characterized in that, it may further comprise the steps: be pre-mixed with mother liquor in the combined soda method production process and salt, modulate salifiable magma or salts solution, add in the cool crystallizer, or salt directly added in the cool crystallizer, the add-on of described cool crystallizer inner salt is that the ratio of the weight of the cold AI volume of cool crystallizer throwing amount and salt is 100: 0.5-6.5.
- 2. according to claim 1 in cool crystallizer with the method for salt volume increase industrial ammonium chloride, it is characterized in that: the ratio that described modulation salt is starched the weight of the volume of used mother liquor and salt is 10: 1-5.
- 3. the method for increasing production industrial ammonium chloride in cool crystallizer with salt according to claim 1, it is characterized in that: described mother liquor is cold AI mother liquor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03130438 CN1569635A (en) | 2003-07-23 | 2003-07-23 | Method for increasing production of industrial ammonium chloride by adding salt to crystallizer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03130438 CN1569635A (en) | 2003-07-23 | 2003-07-23 | Method for increasing production of industrial ammonium chloride by adding salt to crystallizer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1569635A true CN1569635A (en) | 2005-01-26 |
Family
ID=34469741
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03130438 Pending CN1569635A (en) | 2003-07-23 | 2003-07-23 | Method for increasing production of industrial ammonium chloride by adding salt to crystallizer |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1569635A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102284189A (en) * | 2010-06-18 | 2011-12-21 | 大连化工研究设计院 | Novel slurry circular-type crystallizer and application thereof |
-
2003
- 2003-07-23 CN CN 03130438 patent/CN1569635A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102284189A (en) * | 2010-06-18 | 2011-12-21 | 大连化工研究设计院 | Novel slurry circular-type crystallizer and application thereof |
| CN102284189B (en) * | 2010-06-18 | 2013-10-16 | 中昊(大连)化工研究设计院有限公司 | Novel slurry circular-type crystallizer and application thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105036852B (en) | Utilize the method for industrial grade monoammonium phosphate mother liquor production a great number of elements water-soluble fertilizer | |
| CN100532260C (en) | Vacuum crystallization technique for producing potassium nitrate from potassium chloride by sodium nitrate | |
| CN106335889B (en) | The method for producing sodium tripolyphosphate using thick sodium pyrophosphate | |
| CN108285427A (en) | A kind of method of phosphoric acid by wet process round-robin method continuous production big particle industrial grade urea phosphate | |
| CN110745803A (en) | Method for preparing potassium dihydrogen phosphate from wet-process phosphoric acid | |
| CN107382709B (en) | Water phase crystallization method for refining dodecanedioic acid | |
| CN1318303C (en) | Method for preparing potassium nitrate using nitric acid conversion methdo | |
| CN106044802B (en) | A kind of complete water-soluble crystal process for producing potassium sulfate | |
| CN104961578B (en) | The production technology of high-concentration suspension liquid drip irrigation fertilizer | |
| CN1569635A (en) | Method for increasing production of industrial ammonium chloride by adding salt to crystallizer | |
| CN107720703B (en) | Production process of sodium persulfate | |
| CN110483127B (en) | Clear high-concentration liquid water-soluble fertilizer and preparation method thereof | |
| CN1238308C (en) | Method for preparing chemical fertilizer from salt-making mother liquor (bittern) or salt water | |
| CN1211284C (en) | Process for producing high grade crystal potassium chloride | |
| CN1179882C (en) | Process for preparing potassium sulfate | |
| CN106966425A (en) | A kind of method of white vitriol particle increase | |
| CN105237049A (en) | Production process of potassium sulfate specially used for drop irrigation | |
| CN103803586B (en) | Production method of potassium sulfate in subsection way | |
| CN1045576C (en) | Preparing method for industrial ammonium phosphate and series compound fertilizer | |
| CN102336685B (en) | Method for preparing cyanoacetic acid through continuous dehydration | |
| CN1239392C (en) | Inversely feeding ammonium chloride producing process in serial system | |
| CN111170338A (en) | Process for preparing fully water-soluble potassium sulfate from magnesium sulfate subtype salt lake brine | |
| CN102417192B (en) | Process for processing potassium chloride raw material for making ion membrane potassium hydroxide | |
| EP1154955B1 (en) | Method of producing sodium dicyanamide | |
| CN110790685A (en) | Method for producing urea phosphate by wet-process phosphoric acid reduced pressure evaporation coupled elution crystallization |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |