CN105381627A - Melamine fluidized bed crystallizer - Google Patents
Melamine fluidized bed crystallizer Download PDFInfo
- Publication number
- CN105381627A CN105381627A CN201510929829.4A CN201510929829A CN105381627A CN 105381627 A CN105381627 A CN 105381627A CN 201510929829 A CN201510929829 A CN 201510929829A CN 105381627 A CN105381627 A CN 105381627A
- Authority
- CN
- China
- Prior art keywords
- gas
- crystallizer
- housing
- melamine
- crystallization
- 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.)
- Granted
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0004—Crystallisation cooling by heat exchange
- B01D9/0013—Crystallisation cooling by heat exchange by indirect heat exchange
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D2009/0086—Processes or apparatus therefor
Abstract
The invention belongs to the field of chemical engineering and relates to a fluidized bed crystallizer and especially relates to a melamine fluidized bed crystallizer. The melamine fluidized bed crystallizer comprises a housing (1), an uncrystallized gas inlet (1a) located at the bottom of the housing (1), a gas distributor (2) located in a space at the bottom of the housing (1), a cooling device (3) located above the gas distributor (2), a crystallized gas outlet (1c) located at the top of the housing (1) and an external cyclone separator (5) located outside the housing (1). The melamine fluidized bed crystallizer has the advantages of high heat energy utilization rate, low power consumption and good product quality.
Description
Technical field
The invention belongs to chemical field, relate to a kind of crystallizer, it is a kind of fluidized-bed crystallizer, in particular for the fluidized-bed crystallizer of melamine crystallization.
Background technology
At present, melamine is that raw material is produced usually with urea, and its production method can be divided into low-pressure process and high-pressure process two kinds.
High-pressure process preparation technology of melamine belongs to liquid phase reactor, catalyst-free.Reaction pressure is generally 7 ~ 20MPa, and reaction temperature is 360 ~ 420 DEG C.
High-pressure process preparation technology of melamine generally adopts liquefied ammonia, ammoniacal liquor or mother liquor etc. to carry out quenching as liquid phase quenching medium, just can obtain melamine product after need refining.
The advantage of high-pressure process is that tail gas (ammonia and carbon dioxide) pressure is high, directly can return urea plant, effectively can reduce material loss; Its shortcoming need introduce liquid phase quenching medium to carry out quenching and re-refine, and technological process is long, steam consumption high (product per ton need consume steam 6 ~ 10 tons), and has waste water to produce in production process.
Low-pressure process preparation technology of melamine belongs to gas phase catalytic reaction, generally makes catalyst with aluminium oxide, Alusil or silica gel.Reaction pressure is generally 0.1 ~ 0.7MPa, and reaction temperature is 350 ~ 450 DEG C.
Low-pressure process preparation technology of melamine generally adopts gas phase quenching technique to carry out post processing to product, namely with the gaseous mixture of ammonia and carbon dioxide for quenching medium completes crystallization and the purification of product.
The advantage of low-pressure process is that technological process is short, and equipment investment is few, produces without waste water; Its shortcoming: one is that tail gas pressure is low, directly can not be sent to urea plant and utilize.Two is because system pressure is low, power consumption high (product per ton needs power consumption 800 ~ 1500 degree).Three is because system pressure is low, and contour size of the unit(s) is large, is unfavorable for the maximization of device.
There is following shortcoming in existing low-pressure process gas phase quenching technique:
1. heat utilization rate is low.
Melamine is by the crystallization of cold air quenching, and its heat produces 0.1 ~ 0.3MPa steam through urea washes system.Because steam pressure is low, grade is low, cannot utilize, and the general air cooler that adopts cools to remove heat, causes the waste (melamine per ton about produces 4 tons of steam) of amount of heat.
2. power consumption is high.
Low-pressure process gas phase quenching technique needs a large amount of cold air crystallization, and its air conditioning quantity is about 4 times of load volume, and the operate power of Cool gas blower exceedes the operate power of Carrier Gas Compressor, and the power consumption of melamine Cool gas blower per ton is about 300 degree.
Low-pressure process gas phase quenching technique needs a large amount of liquid to urinate circulation cleaning, and melamine liquid urine circulating pump power consumption per ton is about 50 degree.
3. tail gas directly can not be sent to urea plant utilization.
Because low-pressure process gas phase quenching process system pressure is low, vent gas treatment difficulty, can only absorb with water, and directly can not be sent to urea plant and utilize, its vent gas treatment cost is high.
4. larger-scale unit difficulty.
In low-pressure process gas phase quenching technique, because system pressure is low, contour size of the unit(s) is large, larger-scale unit difficulty.
For the defect of low-pressure process gas phase quenching technique, more domestic research and development institutions propose a kind of recirculating fluidized bed crystallizer technology (Chinese patent 95104455.9).The feature of this technology is that recirculating fluidized bed adopts main bed to add the structure of companion's bed, and arranges internal cyclone separators and heat-exchanging tube bundle.The phase transformation of heat exchange liquid in pipe is utilized a large amount of crystallization heats to be removed, to maintain crystallization temperature at about 220 DEG C.
Melamine in this recirculating fluidized bed crystallizer circulates between main bed and companion's bed.Due to the poor fluidity of melamine pressed powder, the tremie pipe of internal cyclone separators easily blocks, and causes device to run.
Summary of the invention
One of the object of the invention is to provide a kind of fluidized-bed crystallizer that simultaneously can carry out crystallisation by cooling.
Another object of the present invention be to provide a kind of can long-term safety and the normal fluidized-bed crystallizer used.
Another object of the present invention is to provide a kind of fluidized-bed crystallizer improving heat recovery efficiency.
The object of the invention is to be achieved through the following technical solutions:
The invention provides a kind of fluidized-bed crystallizer, it is characterized in that comprising housing, be positioned at housing bottom the import of non-crystallization gas, be positioned at housing bottom space gas distributor, be positioned at the cooling device above gas distributor and be positioned at case top crystallization gas outlet; Described crystallizer is also provided with the external cyclone being positioned at hull outside.
Gear gas deduster is also provided with above described cooling device.Gear gas deduster is preferably provided with two-layer above gear gas except knoisphere, and more preferably more than three layers gear gas are except knoisphere.
This crystallizer product gas phase be suitable in carrier gas is sublimated crystallization, in process of production, uncrystallized gas (is generally carrier gas+gas product, it forms (wt%): ammonia 40 ~ 50%, carbon dioxide 40 ~ 50%, melamine 5 ~ 10%) enter in housing by the non-crystallization gas import of bottom, be distributed to the space below gear gas deduster by gas distributor, carry out crystallization within this space.
In described enclosure interior, the top that gas distributor keeps at a certain distance away, be provided with the gear gas deduster for intercepting solid particle, this gear gas deduster can be perforated panel (such as having the hole of multiple circle, square or other shapes) or parts that are netted, sieve-like, preferably has two-layer or more in the perforated panel mutually distributed up and down or parts that are netted, sieve-like.When crystallizing gas passes through this gear gas deduster together with solid particle, gas can continue to diffuse to the space above gear gas deduster, and melamine solid particle is subject to larger resistance thus major part is blocked in space below gear gas deduster, thus, below gear gas deduster until space above gas distributor is the solid particle emulsion zone in crystallizer, melamine is fully utilized, crystallization cooling is carried out with higher speed, and the superjacent air space keeping off gas deduster forms another solid particle dilute-phase zone, so that gas final being effectively separated with melamine further.
By the setting of this gear gas deduster, the air pocket in crystallizer can be abolished, the a large amount of melamines carried secretly in gas are separated simultaneously, make to enter melamine concentration in the gas of crystallizer hull outside cyclone separator greatly to reduce, alleviate the load of cyclone separator, improve the separating effect of cyclone separator.As the preferred embodiment of one, described gear gas deduster is the sieve-like parts be made up of multiple claw-like chi structure.Claw-like chi structure defines certain overlay region up and down, and certain void region, thus form into the sieve texture of upper and lower spatial distribution (distributed in three dimensions).Gear gas deduster have two-layer more than, the claw-like structures of every layer of gear gas deduster be that vertical interlaced distributes.
It is important to note that the setting of this gear gas deduster is very favorable, especially in the crystallization processes of melamine.In the crystallization processes of melamine, carrier gas+melamine gas enters emulsion zone from bottom by gas distributor, this emulsion zone is limited between the two by gas distributor and gear gas deduster and forms, the solids ratios contained in the emulsion zone formed thus is high, thus high heat transfer coefficient can be formed, high heat transfer coefficient for melamine crystallization be very important, this is because, heat transfer coefficient is high, heat transfer temperature difference can be reduced, improve the vapourizing temperature of water side, thus produce high-grade steam.
The lower space of emulsion zone needs to be empty, and upper space is then provided with cooling device.The space be available is in fact as crystal region, because find in experiment, violent crystallization reaction occurs in this lower space, only has this segment space vacant, and crystalline particle just can be prevented to be bonded on tube wall, ensures the trouble-free operation of crystallizer.
Described housing bottom is also provided with solid particle outlet, so that when overhaul of the equipments by solid particle device for transferring.
Described housing wall is also provided with the entrance that feeds intake, to drop into melamine solid particle before crystallization reaction starts, to be conducive to fluidisation and the crystallization process of the melamine powder imported further.
In order to be particularly suitable for the crystallization of melamine, the present invention is provided with external cyclone such as external hanging type cyclone separator in hull outside.
In fact, the overall structure of present device has used for reference the methanation fluidized-bed reactor recorded in the Chinese patent of the patent No. 201410255842.1.
At the crystallization art of melamine, never people adopted, also never people imagined that employing gas-gas type reaction stream gasifying device was used as gas-solid formula crystallization apparatus, this is because the viscosity of melamine is very large, solid particle flow is poor, crystallisation by cooling easily ties wall, adopts the through engineering approaches difficulty of fluidized-bed crystallizer crystallization large.
And the present invention is by applying discovery cleverly, the principle of fluidized bed reaction may be used for the crystallization of melamine, it can make melamine carry out crystallization in real fluidized state, this results in huge benefit: it can make melamine crystallization fully complete, produce a large amount of high-grade steam, heat utilization ratio significantly improves simultaneously.
Preferably, the housing in described distribution device in gas-fluid top position is provided with a separating solids entrance; The incoming end of described external cyclone exports with described crystallization gas and is connected, the output of external cyclone be located at separating solids entrance and be connected.
But compared to methanation fluid bed, equipment of the present invention needs to be set to by cyclone separator especially external-type.This is because the blanking principle as the cyclone separator in methanation fluid bed is a baiting valve by arranging lower end, carrys out blanking by the balance of weight of material and enclosure interior air pressure.But, if adopt built-in cyclone separator in melamine, but cannot operationalize completely, the solid particle separated in cyclone separator due to viscosity too large, poor fluidity, it cannot utilize the relation between this weight of material and air pressure and fall voluntarily, but retains in separator, results in blockage.Therefore, it is very important for being arranged at by cyclone separator the outside crystallization process for melamine.By external force such as mechanical force, it can be exported from external hanging type cyclone separator to the separating solids entrance on housing alternatively, because the grain diameter now separated in cyclone separator is less, return enclosure interior crystal region further and carry out crystallization again, the crystalline particle that granular size is more suitable can be produced.
In prior art, a kind of recirculating fluidized bed crystallizer is disclosed in the patent No. 95213850.6 utility model, due to melamine particulate powders poor fluidity, recirculating fluidized bed circulation difficulty, and internal cyclone separators tremie pipe easily blocks, cause internal cyclone separators to lose efficacy, be difficult to realize industrialization.The present invention adopts external hanging type cyclone separator, be separated the melamine particulate powders carried secretly, and in the bottom of cyclone separator, the mechanical devices such as scraper are installed, the melamine particulate powders separated is sent in time back to the crystal region of fluidized-bed crystallizer bottom, the emulsion zone height of fluidized-bed crystallizer is made to keep stable, to maintain the stable operation of fluidized-bed crystallizer.
Preferably, described gas distributor comprises a gas distributor and secondary air distributor, and a described gas distributor comprises multiple nozzle being distributed in basic same level; Described secondary air distributor is the plate with multiple perforate, is positioned at above a described gas distributor.
Preferably, described secondary air distributor can against a gas distributor and be arranged at above a gas distributor; A described gas distributor and non-crystallization gas inlet communication (preferably by pipeline communication).
Open Side Down for described nozzle, such as, towards crystalliser feet or at an angle towards crystalliser feet.When housing inner bottom part is loaded into solid particle (melamine), when non-crystallization gas starts to enter crystallizer, down spray from each nozzle gas uniform, and blow solid particle (melamine) loss formation fluidisation, now, the upper space of gas distributor forms solid particle emulsion zone, and below forms bottom solid particle dilute-phase zone due to the effect of nozzle and porous plate; After stopping fluidisation, melamine will a large amount of slowly fall after rise, and now, secondary air distributor (porous plate) serves the larger a part of melamine of obstruct simultaneously and falls effect to bottom after rise, thus solves gas distributor and hold susceptible to plugging problem.
Preferably, described nozzle comprises spray orifice and is positioned at the pipeline of extension of spray orifice outside, at an angle towards crystalliser feet.
Above-mentioned certain angle can be such as be greater than 0 ° to be less than 45 °.
By adopting the setting of gas distributor of the present invention, still can trouble-free operation when the diameter of crystallizer can be made to reach 8 meters.
In a preferred embodiment of the invention, gas distributor comprises and is multiplely distributed in conplane ring pipe, ring pipe is connected by radial branched pipe, the branched pipe of each radial direction is summarized in central tube, and central tube is the pipeline being communicated with the import of non-crystallization gas and a gas distributor.Nozzle is connected on ring pipe, to be distributed in crystallizer equably.
Further preferably, described cooling device is heat-exchanger rig; Preferably described heat-exchanger rig has many groups heat exchanger tube in parallel.
Preferably, described emulsion zone heat-exchanger rig has a water inlet and a steam (vapor) outlet; Described water inlet is communicated with the drum delivery port be located at bottom drum, and described steam (vapor) outlet is communicated with the medial inlet being located at drum.
In the melamine emulsion zone of fluidized-bed crystallizer, arrange many heat exchanger tubes, in heat exchanger tube, medium is water.Water in crystallization heat heating heat exchanger tube in melamine bed, make water vapor, steam water interface is risen in the drum outside fluidized-bed crystallizer by outlet header, steam after Separation of Water is drawn by steam outlet pipe, the water separated flows into the water inlet house steward of fluidized-bed crystallizer heat exchanger tube bottom by potential difference, forms Natural Circulation.
The steam (vapor) outlet of drum is equipped with pressure-regulating valve, and the pressure for vaporization being controlled water by pressure-regulating valve controls corresponding vapourizing temperature.Control steam pressure is 1.5MPa, and vapourizing temperature should be 200 DEG C mutually, and can control melamine bed temperature is 220 DEG C; Because steam forms natural cycle system, as long as constant pressure is constant, temperature also can be invariable, and melamine bed would not overtemperature.
Melamine fluidized-bed crystallizer of the present invention has the following advantages:
1. heat utilization rate is high.
The present invention, owing to adopting fluidized-bed crystallizer crystallization technique, makes high-grade heat be reclaimed, and produces a large amount of high-grade steam (melamine per ton produces 1.5MPa steam about 4 tons), and heat utilization rate increases substantially.
2. power consumption is low.
The present invention is owing to eliminating Cool gas blower and liquid urine circulating pump, and with existing low-pressure process gas phase quenching technics comparing, estimate that the power consumption of melamine per ton reduces about 400 degree, power savings clearly.
3. invest little.
The present invention is owing to eliminating cold gas system and urea washes system, process simplification, and eliminate the main equipments such as Cool gas blower, urea washes tower, cold air demister, liquid urine circulating pump, equipment investment significantly declines.With existing low-pressure process gas phase quenching technics comparing, the investment of its identical scale set reduces about 30%.
4. good product quality.
Existing low-pressure process gas phase quenching technique, because cold gas system adopts urea washes, often there is the situation having stain in product, have a strong impact on the use of product in the seriously corroded such as equipment and pipeline.The present invention is owing to eliminating urea washes system, and the corrosion such as equipment and pipeline alleviates greatly, and do not have the situation of stain in product, this product can meet the requirement of high-end user.
Accompanying drawing explanation
Fig. 1. show a kind of melamine fluidized-bed crystallizer of the present invention structural representation.
1-housing
The import of 1a-non-crystallization gas
1b-separating solids entrance
1c-crystallization gas exports
2-gas distributor
2a-gas distributor
2b-secondary air distributor
3-cooling device
3a-water inlet
3b-steam (vapor) outlet
4-keeps off gas deduster
5-external cyclone
5a-process gas exports
6-drum
6a-drum delivery port
6b-medial inlet (steam inlet)
7-solid particle exports
8-feeds intake entrance
9-water inlet house steward
10-steam (vapor) outlet house steward
11-external cyclone incoming end
12-external cyclone output
13-water compensating valve
14-scraper
15-products export
16-pressure-regulating valve
17-steam (vapor) outlet
18-water inlet
Detailed description of the invention
As shown in Figure 1, a kind of melamine fluidized-bed crystallizer comprises the vertical cylinder housing 1 that upper and lower two ends are end socket, described circular cylindrical shell 1 low head is provided with non-crystallization gas import 1a, housing 1 upper cover is equipped with crystallization gas outlet 1c, be positioned at housing and be provided with gas distributor 2 near the space place of bottom, gas distributor 2 comprises a gas distributor 2a and secondary air distributor 2b, and a described gas distributor 2a comprises multiple nozzle being distributed in basic same level; Described secondary air distributor 2b is the plate with multiple perforate, is positioned at above a described gas distributor 2a.
Open Side Down for described nozzle, such as, towards crystalliser feet or at an angle towards crystalliser feet.When housing inner bottom part is loaded into solid particle (melamine), when non-crystallization gas starts to enter crystallizer, down spray from each nozzle gas uniform, and blow solid particle (melamine) loss formation fluidisation, now, the upper space of gas distributor 2 forms solid particle emulsion zone, and below forms bottom solid particle dilute-phase zone due to the effect of nozzle and porous plate; After stopping fluidisation, melamine will a large amount of slowly fall after rise, and now, secondary air distributor 2b serves the larger a part of melamine of obstruct simultaneously and falls effect to bottom after rise, thus solves gas distributor 2 and hold susceptible to plugging problem.
Inner at described housing 1, the top that gas distributor 2 keeps at a certain distance away, be provided with the gear gas deduster 4 for intercepting solid particle, this gear gas deduster 4 can be perforated panel (such as having the hole of multiple circle, square or other shapes) or parts that are netted, sieve-like, preferably has two-layer or more in the perforated panel mutually distributed up and down or parts that are netted, sieve-like.When crystallizing gas passes through this gear gas deduster 4 together with solid particle, gas can continue to diffuse to the space above gear gas deduster 4, and melamine solid particle is subject to larger resistance thus major part is blocked in space below gear gas deduster 4, thus, below gear gas deduster 4 until space above gas distributor 2 is the solid particle emulsion zone in crystallizer, melamine is fully utilized, crystallization cooling is carried out with higher speed, and the superjacent air space keeping off gas deduster 4 forms another solid particle dilute-phase zone, so that gas final being effectively separated with melamine further.
By the setting of this gear gas deduster 4, the air pocket in crystallizer can be abolished, the a large amount of melamines carried secretly in gas are separated simultaneously, make to enter melamine concentration in the gas of crystallizer housing 1 external cyclone 5 greatly to reduce, alleviate the load of cyclone separator, improve the separating effect of cyclone separator.
Gear gas deduster 4 is the sieve-like parts be made up of multiple claw-like chi structure.Claw-like chi structure defines certain overlay region up and down, and certain void region, thus form into the sieve texture of upper and lower spatial distribution (distributed in three dimensions).Gear gas deduster 4 has two-layer, and the claw-like structures of every layer is vertical interlaced distribution.
From fluidized-bed crystallizer top crystallization gas outlet 1c gas out, carry a small amount of melamine particulate powders secretly, external hanging type cyclone separator is entered through external cyclone incoming end 11, be separated the melamine particulate powders carried secretly, process gas after separation exports 5a out from the top process gas of cyclone separator, enters rear workshop section.The melamine particulate powders separated through cyclone body 5 falls back to bottom cyclone separator, mechanical device such as scraper 14 grade is installed in the bottom of cyclone separator, through external cyclone output 12, the melamine particulate powders separated is sent back in the crystal region of fluidized-bed crystallizer bottom through separating solids entrance 1b in time, the emulsion zone height of fluidized-bed crystallizer is made to keep stable, to maintain the stable operation of fluidized-bed crystallizer.At fluidized-bed crystallizer intercrystalline melamine product out through products export 15 out, finished product packing workshop section is entered.
In the melamine emulsion zone of fluidized-bed crystallizer, be provided with heat-exchanger rig 3, heat-exchanger rig 3 is made up of many heat exchanger tubes, and in heat exchanger tube, medium is water.Water in crystallization heat heating heat exchanger tube in melamine bed, make water vapor, steam water interface by steam (vapor) outlet house steward 10 out, enter in drum 6 through medial inlet (steam inlet) 6b, steam after Separation of Water is drawn through steam (vapor) outlet 17, the water separated flows into the water inlet house steward 9 of fluidized-bed crystallizer heat exchanger tube bottom by potential difference through water out 6a, form Natural Circulation.
Water is controlled by water compensating valve 13, enters in drum through water inlet 18, and the steam (vapor) outlet of drum is equipped with pressure-regulating valve 16, and the pressure for vaporization being controlled water by pressure-regulating valve 16 controls corresponding vapourizing temperature.
Crystallizer runs:
First add melamine solid particle in a crystallizer, then import non-crystallization gas (containing carrier gas and melamine gas), non-crystallization gas by melamine solid particle fluidisation, carries out crystallisation by cooling in a crystallizer.Controlling drum steam pressure is 1.5MPa, and vapourizing temperature should be 200 DEG C mutually, and now melamine bed temperature can be controlled in about 220 DEG C; Melamine gas to be sublimated crystallization at crystal region (below heat exchanger tube), and cool at cooling zone (heat exchanger tube position), part melamine particulate powders continues to rise with carrier gas, intercepted major part by gear gas deduster, remainder melamine particulate powders exports from the outlet of crystallization gas with carrier gas, enter external cyclone, process gas after separation of melamine particulate powders exports out from the top process gas of external cyclone, enters rear workshop section.The crystal region that the melamine particulate powders separated imports crystallizer bottom by bottom scraper and the mechanical device of external cyclone again via separating solids entrance carries out further crystallization.Because steam forms natural cycle system, as long as constant pressure is constant, temperature also can be invariable, and melamine bed would not overtemperature.
Operation result is as shown in table 1.
Table 1 melamine fluidized-bed crystallizer compares (often to produce 1 ton of melamine) with the overall target of existing low-pressure process gas phase quenching equipment
Claims (10)
1. a fluidized-bed crystallizer, is characterized in that comprising housing (1), is positioned at the non-crystallization gas import (1a) of housing (1) bottom, is positioned at the gas distributor (2) of housing (1) bottom space, be positioned at the cooling device (3) of gas distributor (2) top and be positioned at crystallization gas outlet (1c) at housing (1) top; Described crystallizer is also provided with and is positioned at the outside external cyclone (5) of housing (1).
2. crystallizer as claimed in claim 1, is characterized in that described cooling device (3) top is also provided with gear gas deduster (4).
3. crystallizer as claimed in claim 1, it is characterized in that, the housing (1) in described gas distributor (2) top position is provided with a separating solids entrance (1b); The incoming end of described external cyclone (5) exports (1c) with described crystallization gas and is connected, the output of external separator (5) be located at separating solids entrance (1b) and be connected.
4. crystallizer as claimed in claim 1, is characterized in that being provided with an idle space above described cooling device (3) below, gas distributor (2); Preferably, described cooling device (3) is heat-exchanger rig; Preferably, described heat-exchanger rig has many groups heat exchanger tube in parallel.
5. equipment as claimed in claim 4, is characterized in that described heat-exchanger rig (3) has a water inlet (3a) and a steam (vapor) outlet (3b); Described water inlet (3a) is communicated with the drum delivery port (6a) being located at drum (6) bottom, and described steam (vapor) outlet (3b) is communicated with the steam inlet (6b) being located at drum (6).
6. crystallizer as claimed in claim 1, it is characterized in that described gas distributor (2) comprises a gas distributor (2a) and secondary air distributor (2b), a described gas distributor (2a) comprises multiple nozzle being distributed in basic same level; Described secondary air distributor (2b), for having the plate of multiple perforate, is positioned at a described gas distributor (2a) top.
7. crystallizer as claimed in claim 1, is characterized in that described housing (1) bottom is also provided with crystalline particle outlet (7).
8. crystallizer as claimed in claim 1, is characterized in that described housing (1) wall is also provided with the entrance that feeds intake (8).
9. crystallizer as claimed in claim 2, it is characterized in that described gear gas deduster (4) is provided with two-layer above gear gas except knoisphere, more preferably more than three layers gear gas are except knoisphere.
10. the crystallizer as described in as arbitrary in claim 1 ~ 9, is characterized in that it is melamine fluidized-bed crystallizer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510929829.4A CN105381627B (en) | 2015-12-14 | 2015-12-14 | A kind of melamine fluidized-bed crystallizer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510929829.4A CN105381627B (en) | 2015-12-14 | 2015-12-14 | A kind of melamine fluidized-bed crystallizer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105381627A true CN105381627A (en) | 2016-03-09 |
| CN105381627B CN105381627B (en) | 2018-03-06 |
Family
ID=55414787
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510929829.4A Active CN105381627B (en) | 2015-12-14 | 2015-12-14 | A kind of melamine fluidized-bed crystallizer |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105381627B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1124236A (en) * | 1995-06-14 | 1996-06-12 | 蒋大洲 | Process for producing melamine and its equipment |
| CN2229829Y (en) * | 1995-06-14 | 1996-06-26 | 蒋大洲 | Equipment for crystallisation of melamine |
| WO2012062724A2 (en) * | 2010-11-10 | 2012-05-18 | Siemens Aktiengesellschaft | Preparation of an amine based solvent contaminated by the introduction of sulfur oxides |
| CN104001457A (en) * | 2014-06-10 | 2014-08-27 | 尹明大 | Methanation fluidized bed reactor |
| CN104277006A (en) * | 2014-10-30 | 2015-01-14 | 安徽金禾实业股份有限公司 | Method for switching hot gas coolers on line in melamine production |
| CN205340200U (en) * | 2015-12-14 | 2016-06-29 | 尹明大 | Melamine fluidized bed crystallizer |
-
2015
- 2015-12-14 CN CN201510929829.4A patent/CN105381627B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1124236A (en) * | 1995-06-14 | 1996-06-12 | 蒋大洲 | Process for producing melamine and its equipment |
| CN2229829Y (en) * | 1995-06-14 | 1996-06-26 | 蒋大洲 | Equipment for crystallisation of melamine |
| WO2012062724A2 (en) * | 2010-11-10 | 2012-05-18 | Siemens Aktiengesellschaft | Preparation of an amine based solvent contaminated by the introduction of sulfur oxides |
| CN104001457A (en) * | 2014-06-10 | 2014-08-27 | 尹明大 | Methanation fluidized bed reactor |
| CN104277006A (en) * | 2014-10-30 | 2015-01-14 | 安徽金禾实业股份有限公司 | Method for switching hot gas coolers on line in melamine production |
| CN205340200U (en) * | 2015-12-14 | 2016-06-29 | 尹明大 | Melamine fluidized bed crystallizer |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105381627B (en) | 2018-03-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105503758A (en) | Melamine production system and technique | |
| CN101818088B (en) | Efficient continuous preparation method and device for natural gas hydrate | |
| CN104001457B (en) | A kind of methanation fluidized-bed reactor | |
| CN103571557B (en) | Method for preparing natural gas hydrate | |
| CN102759225B (en) | Riser spiral-flow type falling-film evaporator for refrigerating air conditioner | |
| WO2012146056A1 (en) | Energy-saving low-cost system and process for producing melamine by means of gas quenching | |
| CN205340200U (en) | Melamine fluidized bed crystallizer | |
| CN104876242B (en) | Three-phase fluidization equipment and method for producing ammonia from urea by virtue of catalytic hydrolysis | |
| CN113477051A (en) | Device and method for continuously capturing CO2 by double-bed hydrate method | |
| CN109438251A (en) | A kind of methanol vapor phase catalytic ammoniation method prepares the method and device thereof of trimethylamine | |
| CN101928016B (en) | Process for producing ammonium sulfate by adopting negative pressure double-countercurrent evaporation and crystallization mode | |
| CN105478023B (en) | Ammoniacal liquor preparation system | |
| CN105859502B (en) | A kind of reaction system and method preparing ethylene | |
| CN208471948U (en) | A kind of Melamine Production system | |
| CN105381627B (en) | A kind of melamine fluidized-bed crystallizer | |
| CN101822960B (en) | Reactor, system and method for producing tripolycyanamide | |
| CN100415698C (en) | Method for continuous preparation of solid natural gas | |
| CN206424752U (en) | Exhaust gas processing device for producing melamine | |
| CN204714766U (en) | A kind of methanation fluidized bed plant and methanation system | |
| CN203635177U (en) | Self-circulation synthetic reaction system capable of executing separation and preheating through refrigeration device | |
| CN106824018A (en) | Shell and tube paste state bed reactor and reaction system | |
| CN203620609U (en) | Special device for manufacturing natural gas hydrate | |
| CN206051888U (en) | A kind of response system for preparing ethylene | |
| CN110090543A (en) | It is a kind of to realize continuous separation CH using fluidized bed4/CO2Method | |
| CN206045989U (en) | A kind of response system of utilization prepared in slurry bed reactor for ethylene |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |