CN103333128A - Novel melamine gas phase quenching technology - Google Patents
Novel melamine gas phase quenching technology Download PDFInfo
- Publication number
- CN103333128A CN103333128A CN2013102798721A CN201310279872A CN103333128A CN 103333128 A CN103333128 A CN 103333128A CN 2013102798721 A CN2013102798721 A CN 2013102798721A CN 201310279872 A CN201310279872 A CN 201310279872A CN 103333128 A CN103333128 A CN 103333128A
- Authority
- CN
- China
- Prior art keywords
- gas
- crystallizer
- trimeric cyanamide
- cold air
- quenching
- 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
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a novel melamine gas phase quenching technology. Specifically, special heat-exchange equipment is utilized to cool a reaction gas, and one part of the cooled gas is sent into a crystallizer by a cool air blower to be mixed with a pure high temperature reaction gas and quenched, so that crystals can be precipitated out. Another part enters a compressor to serve as a reaction gas carrier gas, and the third part is sent into a tail gas treatment system to manufacture other chemical products. By perfecting the gas phase quenching technology and equipment, the method further reduces the energy consumption of a melamine gas phase quenching production process, and improves the product quality and continuous stable operation ability.
Description
Technical field
The present invention relates to chemical technology field, relate in particular to a kind of novel trimeric cyanamide gas phase quenching processing method.
Background technology
Trimeric cyanamide gas phase quenching single stage method is born from the early 1990s in last century and begins, and through 20 years of development, has become the main flow technology of Melamine Production, has occupied 90% domestic market, the world market more than 50% at present.
The main technique flow process of trimeric cyanamide gas phase quenching single stage method is: urea is finished the reaction that generates trimeric cyanamide in reactor under the condition of carrier gas existence and other work, the trimeric cyanamide that exists with gaseous form and the by product ammonia of carrier gas and reaction, anabolic reaction gas such as carbonic acid gas, enter the cooling of hot gas water cooler, enter the impurity in the hot gas filtration device filtering gas then, the dustless gas that comes out from strainer is entered in the crystallizer by the crystallizer top, mix with the cold technological cycle gas that comes up from the bottom, quenching, temperature drops to 210 ℃, the trimeric cyanamide crystallization is separated out, enter together in the finished product cyclone trap with gas mixture, finished product namely gets the trimeric cyanamide product through packing.
From the gas that comes out in trimeric cyanamide trap top, contain the triamine dust of trace and do not generate urea and the intermediate product of trimeric cyanamide, after boosting, blower fan enters in the liquid urine washing tower, divided three the tunnel to send by liquid urine washing, purifying and cooling back: carrier gas recycles the first via as reaction bed after the carrier gas compressor boosts, the second the tunnel returns crystallizer after the cold air gas blower boosts recycles as quenching gas, and Third Road advances exhaust treatment system.
To be the trimeric cyanamide that exists with gaseous form with reaction gas remove through the hot gas filtration device gas phase quenching technology that impurity is laggard goes into crystallizer, liquidate, mix (quenching) with the cold cycle gas that the cold air blower fan is sent into, when mixture temperature is reduced to certain value, trimeric cyanamide is sublimated, and the powdering crystallization is separated out.Find in the production that there is following problem in this technology:
(1) air conditioning quantity generally is 4 times of load volume, and the preparation of a large amount of cold air need consume a large amount of power, has a strong impact on the power consumption of product;
(2) the cold air blower fan is worked under 150 ℃ of left and right sides conditions, contains a large amount of ammonias, carbonic acid gas in the tail gas, and carries the residual of a small amount of trimeric cyanamide, urea secretly, and rugged environment is easy to cause unstable and frequent parking of fan operation;
(3) process of reaction gas cooling and crystallization descends reaction gas recovery of heat amount and recovery of heat grade, and the improper bituminous coal that causes of afterheat utilization consumes height;
(4) urinate the corrosion thing of washing in the tower and be difficult in the exhaust gas body, remove totally, mix when separating out crystallization with high-temperature gas, pollute the trimeric cyanamide product easily.
(5) after the urine of carrying secretly in the carrier gas is washed corrosion thing in the tower and entered reactor, pollute catalyst easily, make that catalyst activity descends, side reaction increases.
Summary of the invention
The purpose of this invention is to provide a kind of novel trimeric cyanamide gas phase quenching processing method, this method is by improving gas phase quenching technology and equipment, further reduce the energy consumption of trimeric cyanamide gas phase quenching production process, improve the quality of products and the ability of continous-stable operation.
The objective of the invention is to be achieved through the following technical solutions: utilize special heat-exchange equipment that reaction gas is lowered the temperature, a part of gas after the cooling by the cold air blower fan deliver in the crystallizer with pure pyroreaction gas mix, quenching, crystallization is separated out.Another part enters compressor and uses as the reaction gas carrier gas, and third part is sent into exhaust treatment system and made other Chemicals.
Preferably, go out the mixed gas that contains gaseous state trimeric cyanamide, 370-430 ℃ of reactor, after the cooling removal of impurities, temperature control enters crystallizer at 300-340 ℃, the cold air of sending here with the cold air blower fan mixes, temperature control is at 210 ℃-260 ℃, the trimeric cyanamide that generates behind the quenching is discharged by the crystallizer bottom, the gas that top is comparatively clean imports special heat-exchange equipment reaction gas is lowered the temperature, a part of gas after the cooling by the cold air blower fan deliver in the crystallizer with pure pyroreaction gas mix, quenching, crystallization is separated out; Another part enters compressor and uses as the reaction gas carrier gas; Third part is sent into exhaust treatment system and is made other Chemicals.
Gas behind the fractional crystallization enters special heat-exchange equipment cooling again, carries out so repeatedly.
Beneficial effect of the present invention:
(1) avoids using the energy consumption height, pollute the temperature-fall period that the urea washing reaction gas technology of production system is carried out easily.
(2) the air blast tolerance of cold air blower fan is less than reaction tolerance, and air conditioning quantity descends significantly, reduces the power consumption of the gas preparation of feeling cold.
(3) do not contain vaporific urea and pollutent in the gas, improved the working conditions of cold air blower fan, avoided fluctuation of service and frequent parking of cold air blower fan;
(4) the working temperature height of reaction gas process of cooling improves reaction gas recovery of heat amount and recovery of heat grade, and bituminous coal consumption is descended.
Description of drawings
Describe embodiments of the invention in detail below in conjunction with accompanying drawing
Fig. 1 is process flow sheet of the present invention
Fig. 2 is the process flow sheet of prior art
Embodiment
Embodiment one: what go out reactor contains gaseous state trimeric cyanamide, 390 ℃ mixed gas, after the cooling removal of impurities, temperature control enters crystallizer at 320 ℃, the cold air of sending here with the cold air blower fan mixes, temperature control is at 230 ℃, and the trimeric cyanamide that generates behind the quenching is discharged by the crystallizer bottom, and the gas that top is comparatively clean imports special heat-exchange equipment reaction gas is lowered the temperature, a part of gas after the cooling by the cold air blower fan deliver in the crystallizer with pure pyroreaction gas mix, quenching, crystallization is separated out.Another part enters compressor and uses as the reaction gas carrier gas, and the third part exhaust treatment system of making a gift to someone is made other Chemicals.
Claims (2)
1. a novel trimeric cyanamide gas phase quenching processing method is characterized in that utilizing special heat-exchange equipment that reaction gas is lowered the temperature, a part of gas after the cooling by the cold air blower fan deliver in the crystallizer with pure pyroreaction gas mix, quenching, crystallization is separated out.Another part enters compressor and uses as the reaction gas carrier gas, and third part is sent into exhaust treatment system and made other Chemicals.
2. a kind of novel trimeric cyanamide gas phase quenching processing method according to claim 1, what it is characterized in that reactor contains the gaseous state trimeric cyanamide, 370-430 ℃ mixed gas, after the cooling removal of impurities, temperature control enters crystallizer at 300-340 ℃, the cold air of sending here with the cold air blower fan mixes, temperature control is at 210 ℃-260 ℃, the trimeric cyanamide that generates behind the quenching is discharged by the crystallizer bottom, the gas that top is comparatively clean imports special heat-exchange equipment reaction gas is lowered the temperature, a part of gas after the cooling is delivered in the crystallizer with pure pyroreaction gas by the cold air blower fan and is mixed, quenching is separated out crystallization; Another part enters compressor and uses as the reaction gas carrier gas; Third part is sent into exhaust treatment system and is made other Chemicals, and the gas behind the fractional crystallization enters special heat-exchange equipment cooling again, carries out so repeatedly.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013102798721A CN103333128A (en) | 2013-06-25 | 2013-06-25 | Novel melamine gas phase quenching technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013102798721A CN103333128A (en) | 2013-06-25 | 2013-06-25 | Novel melamine gas phase quenching technology |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103333128A true CN103333128A (en) | 2013-10-02 |
Family
ID=49241351
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013102798721A Pending CN103333128A (en) | 2013-06-25 | 2013-06-25 | Novel melamine gas phase quenching technology |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103333128A (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3496176A (en) * | 1968-06-19 | 1970-02-17 | Allied Chem | Melamine purification |
| CN1188761A (en) * | 1998-02-24 | 1998-07-29 | 蒋大洲 | Preparation technology of melamine and its device |
| WO2001000597A2 (en) * | 1999-06-29 | 2001-01-04 | Dsm N.V. | Process for the production of melamine from urea |
| CN101863848A (en) * | 2010-05-28 | 2010-10-20 | 北京烨晶科技有限公司 | System and method for preparing melamine |
| CN101979385A (en) * | 2010-10-26 | 2011-02-23 | 丁泽华 | Method for co-producing melamine, nitric acid and ammonium nitrate |
| CN102093299A (en) * | 2009-12-09 | 2011-06-15 | 丁泽华 | Method for producing melamine and urea |
| CN102558079A (en) * | 2011-12-30 | 2012-07-11 | 南通紫鑫实业有限公司 | Process for producing melamine |
-
2013
- 2013-06-25 CN CN2013102798721A patent/CN103333128A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3496176A (en) * | 1968-06-19 | 1970-02-17 | Allied Chem | Melamine purification |
| CN1188761A (en) * | 1998-02-24 | 1998-07-29 | 蒋大洲 | Preparation technology of melamine and its device |
| WO2001000597A2 (en) * | 1999-06-29 | 2001-01-04 | Dsm N.V. | Process for the production of melamine from urea |
| CN102093299A (en) * | 2009-12-09 | 2011-06-15 | 丁泽华 | Method for producing melamine and urea |
| CN101863848A (en) * | 2010-05-28 | 2010-10-20 | 北京烨晶科技有限公司 | System and method for preparing melamine |
| CN101979385A (en) * | 2010-10-26 | 2011-02-23 | 丁泽华 | Method for co-producing melamine, nitric acid and ammonium nitrate |
| CN102558079A (en) * | 2011-12-30 | 2012-07-11 | 南通紫鑫实业有限公司 | Process for producing melamine |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102583468B (en) | From flyash, the method for aluminum oxide is extracted based on ammonium sulfate activation process | |
| CN104876250B (en) | Method for extracting lithium and removing aluminum by treating lepidolite with sulfuric acid | |
| CN101811712A (en) | Method for preparing metallurgical-grade aluminum oxide by using fluid-bed fly ash | |
| CN101891695B (en) | Normal pressure one-step circulation method of melamine | |
| CN103102320A (en) | Production method of melamine by slow cooling crystallization | |
| CN103693665A (en) | Method for preparing high-purity aluminum oxide from fly ash | |
| CN102698585B (en) | Method for recyling carbon dioxide in boiler flue gas | |
| CN106435197A (en) | Process and device for alkaline extraction and recovery from waste catalysts in SCR (selective catalytic reduction) denitrification | |
| CN103693666A (en) | Method for extracting aluminum oxide | |
| CN102923776B (en) | Method for producing high-purity vanadium pentoxide | |
| CN109053615B (en) | Melamine production system and method | |
| CN109336147B (en) | Method for producing alumina by using industrial solid waste rich in alumina | |
| CN201658945U (en) | Sintering smoke purifying system based on heat pipe afterheat recovery technology | |
| CN101439880B (en) | Production process for coproduction of iron oxide red and concentrated sulfuric acid | |
| CN101671311A (en) | Energy-saving technology for producing melamine by one-step method | |
| CN103896280A (en) | Operation method of polycrystalline silicon cold hydrogenation | |
| CN101973948B (en) | Method for producing melamine | |
| CN102989266B (en) | The technique of ammonium sulfate crystallization technical finesse ammonia and equipment | |
| CN101585547B (en) | Method for preparing ammonium sulfate as fertilizer by phosphogypsum through ball milling | |
| CN104628020A (en) | Method for producing metallurgy-grade alumina by taking pulverized fuel ash and recycled ammonium salt as raw materials | |
| CN102584730B (en) | Equipment and process for producing melamine under low pressure | |
| CN104907012A (en) | Reactor for deep decomposition of aluminum ammonium sulfate and application method thereof | |
| CN103601630A (en) | Method utilizing calcium carbide slag and carbon monoxide to synthesize calcium formate | |
| CN103333128A (en) | Novel melamine gas phase quenching technology | |
| CN105293556A (en) | Method for extracting tungsten from tungsten-containing sodium carbonate solution and comprehensively utilizing extracted solution |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C05 | Deemed withdrawal (patent law before 1993) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20131002 |