CN107934996A - A kind of technique using triamine End gas production sodium bicarbonate and ammonium chloride - Google Patents
A kind of technique using triamine End gas production sodium bicarbonate and ammonium chloride Download PDFInfo
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- CN107934996A CN107934996A CN201810010954.9A CN201810010954A CN107934996A CN 107934996 A CN107934996 A CN 107934996A CN 201810010954 A CN201810010954 A CN 201810010954A CN 107934996 A CN107934996 A CN 107934996A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
- C01D7/18—Preparation by the ammonia-soda process
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/16—Halides of ammonium
- C01C1/164—Ammonium chloride
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
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Abstract
This hair discloses a kind of utilize and produces the technique that the tail gas of melamine prepares sodium bicarbonate and ammonium chloride, melamine tail gas and bittern or brine of the technology utilization containing ammonia and carbon dioxide are raw material, using bittern or salt refining, deamination tail gas and triamine tail gas inhale ammonia, ammonial brine is carbonated and weight alkali separation, weight alkali is sized mixing and hygroscopic water solution, clarify refined filtration, lye heavy carbonic, sodium bicarbonate centrifugal drying, weight alkali filtrate deamination, multiple-effect evaporation concentrates salt manufacturing, the technical process such as multiple-effect shwoot ammonium and separation are dry, make to be utilized effectively with the tail gas that urea production melamine produces.Big and the shortcomings that soda and sociation center mother liquor is not easy to balance the present invention overcomes ammonia-soda process waste liquid discharge capacity, installation area is small, only uses low-grade steam.
Description
Technical field
The present invention relates to a kind of recycling of melamine tail gas and sodium bicarbonate ammonium chloride combined producing process.More particularly to one kind
The tail gas of melamine, the method for preparing sodium bicarbonate and ammonium chloride are produced using urea as raw material.
Background technology
Melamine (C3H6N6) be also referred to as melamine, be a kind of important basic organic chemical industry raw material, be widely used in coating,
The industries such as building materials, papermaking, leather, weaving.Melamine resin is made with formaldehyde condensation in melamine, which has resistance to
The excellent specific properties such as hot, corrosion-resistant, resistance to electric arc, high glaze, high rigidity.Melmac is mediated with filler, pigment, lubricant,
It can be made into the thermosetting property aminoplast of superior performance.Modified melamine resin can be made into bright in colour, durable, high
The coating such as the strong baking finish of hardness, toughness.Melamine resin, which is used for paper industry, can be used as paper treating agent, be made anti-
Contracting, moistureproof paper；Binding agent or making decoration veneer for timber industry；Anti- crape, anti-shrinkage, anticreep for textile industry
Color, wash fast fabric finishing agent；For building industry as preparation of high efficient concrete water-reducing agent, the tanning extracts of leather industry, applies
Expect crosslinking agent of industry etc., purposes is extremely wide.
The main production process of melamine is divided into urea method, dicyandiamide method and hydrogen cyanide method, and first two side by raw material
Method has been achieved with industrialized production.Urea method raw material is easy to get, and process, safe operation, production cost is low, the seventies later stage
Since, whole world melamine is mostly by urea method production.Urea method is divided into dry method, wet method and half-dried by technique
Method.It is different according to the pressure that fusing urea is pyrolyzed, the process route of urea method production melamine be divided into again high-pressure process (7~
10MPa), method production melamine belongs to liquid phase reactor, and temperature range is 370~450 DEG C.Low-pressure process (0.5~1MPa), this
Method production melamine falls within liquid phase reactor, and temperature range is 380~440 DEG C, and the low-pressure vapor phase extraction of recent domestic-developed is cold
Method is also applied successfully.Non-pressure process (below 0.3MPa) production melamine belongs to gas phase reaction, and temperature range is at 390 DEG C
Left and right.
The existing melamine plant in China is all using urea method, in addition to the high-pressure method device of several introductions, other productions
Device is using the domestic non-pressure process production technology oneself developed.
Whether the carrier gas in fluidized-bed reactor recycles, and non-pressure process technique is divided into one-step method and round-robin method again,
Occur " a step two-phase method " for two covering device of high-low pressure series connection production among recent one-step method again.Circulating carried method, after crystallization
The cold air of generation is most of to make carrier gas recycling after Carrier Gas Compressor boosts into reactor, and discharge small part tail gas truncates
Gas processing system.One-step method then all uses ammonia as recirculating fluidized bed reaction carrier gas, and the cold air produced after crystallization is all sent
Go out system and enter exhaust treatment system.
Urea method produces melamine, and overall reaction can be represented by the formula：
6CO(NH2)2→C3N3(NH2)3+6NH3+3CO2
The mixing of one ton of melamine product, that is, by-product 809.5kg ammonia and 1047.6kg carbon dioxide is often produced in theory
Gas.In actual production, due to urea quality, the supplement factor such as ammonia, one ton of melamine product of production will produce 2100~
The mixed tail gas of 2300kg.Recycling, the comprehensive utilization of triamine tail gas are to restrict the bottleneck of Melamine Production, influence the whole of enterprise
Body economic benefit.For the mixed tail gas, there are a variety of processing modes：Carbonated aqueous ammonia is produced, co-producing ammonium bicarbonate, is neutralized with acid and given birth to
Sulphur ammonium, ammonium nitrate or nitro-compound fertilizer are produced, using " non-equilibrium absorption decarburization-rectifying divides ammonia " technique and " pressurization dilution decarburization-essence
Cut ammonia " technique, carries out ammonia, carbon separation, joint-producing anhydrous sodium carbonate, ammonium chloride etc..Wherein joint-producing anhydrous sodium carbonate and ammonium chloride, ammonia in tail gas and
Carbon dioxide, which is obtained for, to be made full use of, and added value of product is high, is a kind of presently preferred vent gas treatment mode.
Melamine tail gas alkaline, because the process route of melamine is different, exhaust gas component is also different, and that designs for this is pure
Alkali flow is also just not quite similar.
By taking normal pressure one-step one-stage process triamine flow tail gas as an example, tail gas total amount is 6257.1kg, wherein ammonia 5209.5kg,
Percentage by weight is about 83.26%；Carbon dioxide 1047.6kg, percentage by weight are about 16.74%.Because wherein carbon dioxide contains
Measure relatively low and the influence of distich alkali is little, the cooperation production for the high triamine tail gas of such a ammonia content and connection alkali, almost to tradition
Connection alkali items Con trolling index does not produce bad influence, can join alkali flow according to traditional cold process completely, using normal device into
Row connection alkali production.
For atmospheric circulating method, the concentration of carbon dioxide is far above one-step method in tail gas, its ammonia and carbon dioxide
Content accounts for 47%, 52% (wt%), 69%, 30% (v%) respectively, and other is isocyanic acid and inert gas.For such a dioxy
For changing the high tail gas of carbon content, carbonisation degree is higher while inhaling ammonia, and gas concentration lwevel increases very fast in liquid phase, just needs
To be controlled by, and to carry out inhaling ammonia operation premised on meeting gas concentration lwevel.It should be noted that in order to improve as far as possible
Amine base ratio, namely the connection alkali of same size can try one's best multiprocessing melamine tail gas, can be by carbon dioxide in ammonia mother II
Concentration directly brings up to the degree of the pre- carbodiimide solution of tradition connection alkali, i.e., gas concentration lwevel can allow to reach in ammonia mother II
28tt.To ensure β value (FNH in ammonia mother II3/Na+) between 1.02~1.12, insufficient NH3Mended by absorbing pure ammonia to adjust
Fill.
When carrying out the suction ammonia of mother I using such a gaseous mixture, due to CO2With NH3Absorb this characteristic (CO jointly in female I2Inhale
Rate of producing effects is calculated by 0.9), it can make it that gas concentration lwevel also and then goes up while the concentration of free ammonia goes up in ammonia I, to system
Into α values (FNH3/CO2) be 2.15~2.35 qualified mother liquor, free ammonia and gas concentration lwevel, which well beyond join alkali, to be needed to control
The technic index of system, can not complete to produce.Therefore for tradition connection alkali, the mixed tail gas that round-robin method produces is to be not suitable for mother
I inhales ammonia, and mother I, which inhales ammonia, to be used as ammonia source using pure ammonia.
Melamine plant operation should strictly control tail gas index, reduce impurity carrying amount, ensure soda ash and ammonium chloride production
Quality.From the point of view of the operating condition of current combined production of melamine soda ash and Production of Ammonium Chloride producer, triamine tail gas is used as raw material
Into connection alkali system, do not show tail gas carrying impurity also influences caused by soda ash and ammonium chloride product.
Combined soda method has two kinds of different implications, is ammonia synthesizing industry and alkaline and the connection of ammonium chloride industry in a broad sense
Close, i.e. NH needed for production soda ash and side product sodium chloride3And CO2There is provided by synthetic ammonia installation；Say it is to refer to soda ash life merely in the narrow sense
Production is combined with Production of Ammonium Chloride.
The raw material of soda and sociation center is salt, ammonia and carbon dioxide.Melamine tail gas producing soda ash and ammonium chloride,
It is that soda ash in the narrow sense is combined with Production of Ammonium Chloride, triamine device provides the raw material of part connection alkali production.
Soda and sociation center includes two processes：First process and ammonia-soda process are essentially identical, by ammonia be passed through by II process Lai
Ammonium chloride filtrate and ammonification mother liquor II, then be passed through carbon dioxide generation sodium acid carbonate precipitation, it is filtered, wash to obtain NaHCO3Knot
Crystalline substance, then obtained soda ash product is calcined, its filtrate is the solution containing ammonium chloride and sodium chloride.Second process is from containing chlorination
Crystalline deposit goes out ammonium chloride in the filtrate of ammonium and sodium chloride.It is low since the solubility of ammonium chloride at normal temperatures is bigger than sodium chloride
Solubility when warm is then smaller than sodium chloride, and solubility of the ammonium chloride in the concentrated solution of sodium chloride is than the dissolving in water
Spend much smaller.So under cryogenic, fine-powdered sodium chloride is added into I process filtrate of suction ammonia, chlorination can be made
The independent crystalline deposit of ammonium separates out, filtered, wash and be drying to obtain ammonium chloride product.Gained after chloride precipitation is filtered out at this time
Filtrate, is substantially chlorinated sodium saturation, and closed circulation is formed back to I process.This combined soda method genealogy of law " cold process " ammonium chloride,
It is mainly characterized by being carbonated later mother liquor by frozen cooling and adds the method that the cooling of solid salt saltouts, it is necessary to equipped with cold
Jelly machine directly freezes by coolant refrigeration or with liquefied ammonia to have the function that to cool down mother liquor, is then separating out the cold mother liquor of ammonium chloride
Middle addition sodium chloride, common-ion effect separate out ammonium chloride, and mother liquor forms a closed circulation flow, referred to as " O " shape circulation process.
" hot method " ammonium chloride in soda and sociation center, is the method abjection ammonia and titanium dioxide that will filter mother liquor first to heat
Carbon, then be evaporated, analyse salt, cooling separates out ammonium chloride, it need not freeze mechanism cold, can meet work using room temperature cooling water
Skill requirement.First process can be identical with ammonia alkali process flow, separate out the later mother liquor of ammonium chloride return to before evaporation with
Deamination mother liquor convert and, therefore mother liquor does not form the closed circulation of overall process, but in the flow of the second process repeats itself, referred to as
For " 6 " shape circulation process.
1 ton of ammonium chloride of by-product while soda and sociation center often produces 1 ton of soda ash.Ammonium chloride is mainly used for agricultural and is used as nitrogen
Fertilizer, is applied to the good rice terrace of irrigation and drainage, not only obvious effect of increasing production in China, and fertilizer efficiency is not only fast but also lasting.Ammonium chloride
Also there is different degrees of effect of increasing production to corn, wheat, cotton, millet, rape, crudefiber crop.The crop poor to chlorine-resistant is preferably used less
Or do not have to；Fear-chlorion crop should not be applied.Industrial ammonium chloride is used for the manufacture of dry cell and storage battery, for metal welding, electricity
Plating, printing and dyeing, medicine, hot investment casting, flame-retardant agent, chemical reagent and manufacture inorganic polymer etc..
Sodium bicarbonate is the trade name of prepared calcium carbonate hydrogen sodium, is a kind of important bases product.Sodium bicarbonate is widely used in
Food industry, makees raising agent or swelling agent, for producing various biscuits, bread and pan work；For dioxy in Soda Water
Change propellant, the preservative agent of butter of carbon；Cleaning for surfaces such as aircraft, circuit board, teeth；Pharmaceutically it is used for manufacturing various
Medicine and medicament.It is also widely used in ore dressing, smelting, metal heat treatmet, tanning, dyestuff, fiber, rubber, foamed plastics, metal
Sodium manufacture, detergent, personal daily nursing product, fire foam and dry powder fire extinguishing agent etc. are industrial.
The production method of sodium bicarbonate mainly has two methods at present：One kind is to add ammonium hydrogen carbonate double decomposition with natural bittern
Sodium bicarbonate processed, another kind are sodium carbonate liquor carbonating legal system sodium bicarbonate.
Double decomposition legal system sodium bicarbonate flow includes brine refining, metathesis reaction, sodium bicarbonate filtration washing, sodium bicarbonate drying
The processes such as packaging, sodium bicarbonate filtrate deamination, evaporation salt manufacturing, cooling ammonium chloride processed.
The carbonization legal system sodium bicarbonate technological process of production can be divided into two parts：(1) prepared by sodium carbonate liquor；(2) carbonating and
Other process.
Produce the usually available light soda ash dissolving of sodium carbonate liquor of sodium bicarbonate, trona dissolving, weight alkali hygroscopic water solution and
Calciner gas ground caustic recycles four kinds of methods and prepares.By taking light soda ash dissolves as an example, the sodium carbonate liquor total alkalinity 100 of preparation~
105tt, Na2CO365~80tt of content, temperature are maintained at 80~85 DEG C.Raw material production is recovered as with light soda ash and furnace gas ground caustic
Sodium bicarbonate technique, covers whole processes of ammonia-soda process or soda and sociation center (cold process connection alkali) alkaline.
Sodium carbonate liquor prepared by a kind of any of the above described method, before carbonating being introduced into settling tank is clarified, and is removed
Insoluble impurities.Clarified solution send accurate filter to remove trickleer impurity particle.Lye is with being pumped into carbonating column after filtering
Top, the CO being from top to bottom passed through with bottom2Back flow of gas contacts, and carries out carbonation reaction, generates NaHCO3Crystallization.Carbonating
The NaHCO that tower takes out3Magma is thickened through thickener, separating, washing, drying, metering packing obtain sodium bicarbonate product, sodium bicarbonate filtrate
Closed circulation is formed back to sodium carbonate liquor preparation section.
Although there is very big advantage by waste sodium bicarbonate of trona, restricted be subject to Natural resources condition,
There is its limitation.In addition to trona raw material sodium bicarbonate is used, be carbonized the raw materials used generally use ammonia alkali of legal system sodium bicarbonate
It is prepared by method (Sol dimension method) and soda and sociation center (cold process connection alkali) production technology.
Ammonia-soda process handicraft product quality is good, mother liquor equivalent is small, but its major defect has two：First, raw material chlorination
The utilization rate of sodium is low, can only achieve 28~30%；Second, there is a large amount of liquid and waste slag produced discharges, soda ash discharge waste liquid amount per ton is about
10m3, the solid quantity of slag about 150~300kg, processing and utilization are all relatively difficult, unfriendly to environment.
The Recycling Mother Solution of cold process connection alkali production technology uses, and the utilization rate of sodium chloride disappears up to more than 90% in actual production
Except a large amount of waste liquids and waste residue.But cold process connection alkali there is also it is very big the shortcomings that, mainly mother liquor equivalent it is big, volume of equipment profit
It is relatively low with coefficient；System water must maintain a balance between receipts and payments, and otherwise mother liquor amount increases processing difficulty, increase loss；Carbonating generation
Crystallization of sodium bicarbonate quality it is poorer than ammonia-soda process, add the production cost of subsequent handling；Extensive united alkali-making factory can only use washing salt
Or high-quality solid salt.
The content of the invention
The object of the present invention is to provide a kind of flow is simple, floor space is small, only needs to be less than the low-grade steam of 1.0MPa
Sodium bicarbonate production technology, make using urea as raw material produce melamine produce tail gas be fully used, avoid ammonia alkali
Disadvantage existing for method and cold process connection alkali itself, while had the advantages of respective concurrently again, ammonia-soda process and cold process is joined the excellent of alkali
Power set is.
The technological process of the present invention includes the following steps：
(1) melamine is produced by raw material of urea；
(2) triamine tail gas ammonia absorption tower is passed through containing ammonia and carbon dioxide tail gas by what production melamine in step (1) obtained,
Absorbed with the light ammonial brine from step (11), can also use refined brine or bittern to absorb, through cooling down and clarification is carbonated
Ammonial brine；
(3) the carbonating ammonial brine of step (2) is passed into the top of weight alkali carbonators, the titanium dioxide being passed through with tower lower part
Carbon back flow of gas carries out carbonation reaction, removes reaction heat with cooling water, the heavy alkali magma of generation is taken out by tower bottom.In the mistake
Cheng Zhong, overall reaction are as follows：
NaCl+NH3+CO2+H2O→NH4Cl+NaHCO3(Gu)
(4) the heavy alkali magma of step (3) is subjected to separation of solid and liquid；
(5) the sodium bicarbonate filtrate (directly adding water first) that the wet big and heavy alkali for obtaining step (4) is obtained with step (8)
And a small amount of supplement water is added in mixing cirtern, obtains weight alkali adjusting slurry；
(6) the heavy alkali adjusting slurry for obtaining step (5) is passed into wet decomposition tower, makes the NH in weight alkali adjusting slurry4HCO3、
(NH4)2CO3、NH4OH is substantially completely decomposed, NaHCO3Resolution ratio reaches more than 65%, and the CO for producing decomposition2、NH3Into
Enter gas phase；Tower top outlet is CO2、NH3And saturated vapor, carbon-dioxide gas compressor is entered through cooling, net ammonia, is returned after boosting
Return to step (3)；Tower reactor connects reboiler, and by 0.4~0.8MPa (G) low-pressure steam indirectly heat, bottom temperature is controlled 120
~150 DEG C, preferably 125~135 DEG C；Wet decomposed solution is taken out by tower reactor, through exchanging heat and clarifying, be sent to after refined filtration with sodium bicarbonate filtrate
Sodium bicarbonate carbonators；
(7) the sodium bicarbonate material liquid obtained by step (6) enters the top of sodium bicarbonate carbonators, is passed through with tower lower part
Carbon dioxide adverse current carries out carbonation reaction, and lye heavy carbonic reaction heat is removed with cooling water, is taken out and given birth to by tower bottom
Into sodium bicarbonate magma.Overall reaction in this process is as follows：
Na2CO3+CO2+H2O→2NaHCO3(Gu)
(8) the sodium bicarbonate magma of step (7) is subjected to separation of solid and liquid, isolated sodium bicarbonate filtrate passes through and wet decomposed solution
Step (5) is returned to after heat exchange heating；
(9) the wet sodium bicarbonate of solid phase obtained by step (8) enters sodium bicarbonate drier, heated to go moisture removal to be made small
Soda product；
(10) the weight alkali filtrate obtained by step (4) temperature after heat exchange enters deammoniation tower up to more than 65 DEG C, makes weight alkali
NH in filtrate4HCO3、(NH4)2CO3、NH4OH is substantially completely decomposed, and the CO for producing decomposition2、NH3Into gas phase；Tower top
Outlet is CO2、NH3And saturated vapor；Tower reactor connects reboiler, by 0.2~0.4MPa (G) low-pressure steam indirectly heat, tower reactor
Temperature control is at 110~120 DEG C；Deamination liquid is taken out by tower reactor；
(11) by the deamination tail gas that step (10) obtains through with removing deamination tail gas after the heat exchange of weight alkali filtrate and cooling water cooling
Ammonia absorption tower, is absorbed with refined brine or bittern, and obtaining light ammonial brine through cooling is back to step (2)；
(12) containing ammonium chloride and the deamination liquid of sodium chloride obtained step (10), in 45~120 DEG C and relevant temperature
Under saturated vapour pressure, salt manufacturing is carried out using multi-effect evaporation scheme is predicted.Deamination liquid initially enters the evaporation of salt end effect after heat exchange
Device, finally enters I effect evaporator；0.2~0.4MPa (G) low-pressure steam initially enters salt I and imitates heater, the indirect steam of generation
The heater of lower 1st effective evaporator is sequentially entered, emptying after the secondary vapour that last evaporator produces is condensed；Deamination liquid is adding
NaCl is reached saturation in thermal evaporation process and generate NaCl crystallizations, while obtain salt manufacturing and complete liquid clear liquid, salt magma is through solid-liquid
Salt filtrate and the wet NaCl of byproduct are obtained after separation；
(13) liquid is completed into the salt manufacturing that step (12) obtains and is sent to ammonium flash evaporation, multiple-effect shwoot is carried out at 120~45 DEG C,
Make NH in shwoot, temperature-fall period4Cl reaches saturation and generates NH4Cl is crystallized, while obtains the clear liquid that ammonium processed completes liquid, is taken out
NH4Cl magmas obtain ammonium filtrate and wet NH after separation of solid and liquid4Cl；
(14) ammonium processed that step (13) obtains is completed into liquid and return to step (12), with deamination liquid convert and after to enter salt last
Evaporator is imitated, forms closed circulation；
(15) the wet NH for obtaining step (13)4Cl is dried, and obtains NH4Cl products；
Step (1) preparation technology of melamine using urea as raw material can be high-pressure process, low-pressure process or non-pressure process.
The degree of carbonisation for the carbonating ammonial brine that step (2) described process obtains should be not more than 75~80%, avoid in triamine
Generation NaHCO in tail gas ammonia absorption tower3Crystallization, and influence the operation index control of weight alkali carbonating process.Be carbonated ammonial brine
FNH3/Na+Operation index should be produced in the tail gas that melamine produces between 1.12~1.16 according to using urea as raw material
NH3、CO2The difference of content, and triamine tail gas absorption equipment absorb CO2The difference of efficiency, the carbonization of control carbonating ammonial brine
Degree is less than 75~80%, insufficient NH3Supplement is adjusted by absorbing pure ammonia.
Wet decomposed solution is 65~90 DEG C with temperature after the heat exchange of sodium bicarbonate filtrate, clarified bucket clarification and accurate filter filtering
Obtain sodium bicarbonate material liquid.Settling tank removes more than 20 μm of insoluble granule impurity by gravitational settling；Accurate filter is adopted
With sinterable polymer microfiltration tube, stainless steel sintered meshwork filter core or other nontoxic free of contamination high-efficiency filtration medias, remove
Remove 0.1~20 μm of fine impurity particle.Into preferably 80~85 DEG C of sodium bicarbonate carbonators material liquid temperature, cooling water flow is adjusted
Sodium bicarbonate carbonators magma is controlled to take out liquid temperature degree at 55~65 DEG C.
The sodium bicarbonate filtrate that step (8) obtains should discharge a part and go brine or brine refining process, make to enter sodium bicarbonate
The NaCl contents of carbonators material liquid are able to maintain that less than 20tt (wt% 4.8%) below.Sodium bicarbonate filtrate discharge rate with
Big and heavy alkali salt content into weight alkali mixing cirtern is related, and big and heavy alkali salt content is except related with the crystalline quality and leaching requirement of weight alkali
Outside, most important, preferred horizontal vacuum belt filter or the piston material pushing centrifugal separator of efficiency height of filtration of bicarbonate equipment.
The deamination liquid that step (10) described process obtains, free ammonia removal efficiency are more than 99.5%, and carbon dioxide is substantially complete
Full removing.The higher corrosivity to equipment of temperature of deamination liquid is stronger, therefore tower reactor liquid phase operation temperature is no more than 120
℃.Deammoniation tower tower top pressure can make tower reactor deamination liquid temperature control below 110 DEG C using negative-pressure operation, be to mitigate equipment corruption
The effective way of erosion.
Step (12) the effect number for predicting multiple-effect evaporation, preferably four-effect evaporation flow, can make salt I imitate mother liquid evaporation temperature
Degree control is at 105~115 DEG C, the heavy corrosion for avoiding high temperature mother liquor from producing equipment, while the effect indirectly heat of salt I steam can be with
Use the low-grade steam of 0.2~0.4MPa (G).
The effect number of step (13) the following current multiple-effect shwoot, preferably triple effect shwoot flow, dodge III effect using vacuum system
Hair device reaches required evaporating pressure, ammonium processed is completed liquid temperature control at 45~55 DEG C.
Step (12), (13) described process can also use following current to evaporate and produce NaCl, and end effect mother liquid evaporation temperature 78~
82℃；After isolating NaCl, complete evaporation of liquid is cooled down, and makes NH at 30~35 DEG C4Cl reaches saturation and generates NH4Cl is tied
Crystalline substance, ammonium processed is obtained after separation of solid and liquid and completes liquid and wet NH4Cl, ammonium completion liquid processed are back to last evaporator composition closing and follow
Ring.
The NaCl raw materials needed for sodium bicarbonate are produced, can be that brine made of dissolved solid crude salt can also be underground mining
Bittern, 4.8~5.35kmol/m of NaCl contents need to be refined into3(96~107tt), Na2SO4≤ 6g/L, Mg2+≤ 6mg/L, Ca2 +The refined brine or bittern of≤20mg/L, turbidity≤30ppm.Refined method can use lime-Method of Soda or lime-carbon
Sour ammonium method, preferably lime-Method of Soda, can be such that the high salt sodium bicarbonate filtrate (30~45tt of total alkalinity) of outer row obtains effectively
Utilize, reduce the consumption of finished product soda ash.Lime-Method of Soda, i.e., using Ca (OH)2Make magnesium precipitate, use Na2CO3Make calcium precipitate；Mg
(OH)2And CaCO3Precipitation, its chemical reaction are：
Na2CO3+Ca(OH)2→2NaOH+CaCO3↓
NaHCO3+Ca(OH)2→NaOH+CaCO3↓+H2O
Mg2++2NaOH→Mg(OH)2↓+2Na+
Ca2++Na2CO3→CaCO3↓+2Na+
This production technology requires supplementation with a part of CO 2 raw material gas.Decarbonization gas, the stone that can be provided by synthetic ammonia installation
The carbon dioxide that the kiln gas or flue gas through pressure swing Adsorption Concentration of ash furnace device are produced, the unstripped gas source of the gas as supplement.
This production technology is without using the weight alkali calcining stove that 2.5~3.2MPa (G) middle pressure steam is heat source, it is only necessary to 0.1~
The low-grade steam of 1.0MPa (G) is as technique heat source.
The present invention has the advantages that as described below：
(1) contain ammonia and carbon dioxide tail gas that melamine produces are produced and provides original for production sodium bicarbonate combined producting ammonium chloride
Material, makes the urea raw material availability of production melamine close to 100%.
(2) raw material salt can not only use solid salt but also can use bittern water, avoid soda and sociation center (cold process connection alkali)
The limitation of washing salt or high-quality solid salt can only be used.
(3) utilization rate of sodium chloride is high, without liquid and waste slag produced discharge, solves the discharge problem of ammonia-soda process, solves at the same time
The water imbalance problem to occur now and then in cold process connection alkali, it is environmentally friendly.
(4) flow is simple, and without the large-scale cumbersome running device such as calcining furnace, ice maker, floor space is small, and operating cost is low.
(5) crystalline quality of intermediate products (weight alkali) reduces the consumption of subsequent handling better than the quality of cold process connection alkali.It is female
Liquid equivalent proportion cold process connection alkali is small, and power consumption is low.
(6) mother liquor is free of free ammonia during ammonium chloride processed, avoids free ammonia during cold process connection alkali ammonium chloride
Walk-off-loss, reduces the consumption of raw material ammonia.
(7) low-pressure steams of 1.0MPa (G) below are only used, low grade residual heat steam can be made to be utilized effectively.
Brief description of the drawings
Attached drawing 1 is the process flow diagram of the present invention that sodium bicarbonate and ammonium chloride are produced using melamine tail gas.
Embodiment
The present invention will produce sodium bicarbonate and ammonium chloride to melamine tail gas of the present invention with the following Examples
Technique is further described.Certainly, it is it will be apparent to those skilled in the art that discussed below excellent
Select embodiment to be exemplary in itself, and can be changed in the case of without departing from scope and spirit of the present invention
Become.
Embodiment 1
The existing melamine plant in China is all using urea method, in addition to the high-pressure method device of several introductions, other productions
Device is using domestic non-pressure process (below 0.3MPa) production technology oneself developed.Non-pressure process is divided into one-step method and circulating carried again
The different production technology such as method.Atmospheric circulating method is that carbon dioxide content is highest in tail gas, to sodium bicarbonate production technology index
Control influences maximum.Atmospheric circulating method often produces the NH that 1t melamines produce 2145kg3、CO2Mixed tail gas, wherein NH3Content
For 994kg, CO2Content is 1130kg, remaining is noble gas, and temperature is 135~145 DEG C, and pressure is 0.15~0.3MPa (G).
As shown in Figure 1, being passed through triamine tail gas ammonia absorption tower containing ammonia and carbon dioxide tail gas by what production melamine obtained, use
35~40 DEG C of light ammonial brines that deamination tail gas ammonia absorption tower comes absorb, through cooling down and clarification obtains carbonating ammonial brine.Be carbonated ammonia
Brine is 257.4~263.3g/L, FNH containing NaCl3/Na+For 1.12~1.16, temperature is 38~42 DEG C, and should control carbonating
The degree of carbonisation of ammonial brine is less than 80%, insufficient NH3Supplement is adjusted by absorbing pure ammonia.
The ammonial brine that is carbonated is passed into the top of weight alkali carbonators, wet decomposed tail gas is mixed with the carbon dioxide gas supplemented
Into the carbon dioxide gas more than 80%, after compressor boosts and is cooled to 30~40 DEG C, it is inverse with ammonial brine to be passed into tower lower part
Stream carries out carbonation reaction.Temperature should maintain 60~70 DEG C at 2/3 tower height of weight alkali carbonators, be conducive to obtain good
NaHCO3Crystal.Reaction heat is removed in cooling section cooling water, the heavy alkali magma of generation is taken out by tower bottom, takes out suspension liquid crystal
Slurry temperature degree is 27~30 DEG C.
Separation of solid and liquid is carried out using horizontal vacuum belt filter counterweight alkali magma, and adds appropriate wash water to Washing of Filter Cake,
Wet big and heavy alkali is obtained, is formed as (wt%)：
Wet big and heavy alkali and the sodium bicarbonate filtrate after heat exchange and a small amount of supplement water are added in mixing cirtern, obtain temperature as 80
~100 DEG C of heavy alkali adjusting slurry.
Weight alkali adjusting slurry is passed into wet decomposition tower with delivery pump, makes the NH in weight alkali adjusting slurry4HCO3、(NH4)2CO3、
NH4OH is substantially completely decomposed, NaHCO3Resolution ratio reaches more than 65%, and the CO for producing decomposition2、NH3Into gas phase.Tower
Ejection gas is CO2、NH3And saturated vapor, carbon-dioxide gas compressor is entered through cooling, net ammonia, duplicate removal alkali is carbonized after boosting
Tower.Wet decomposition tower tower reactor connects reboiler, by 0.6MPa (G) low-pressure steam indirectly heat, 130~135 DEG C of bottom temperature.
It it is 80~85 DEG C by the wet decomposed solution that tower reactor is taken out and temperature after the heat exchange of sodium bicarbonate filtrate, clarified bucket relies on gravity
Sedimentation removes more than 20 μm of insoluble granule impurity, and 0.1~20 μm is removed using sinterable polymer pipe micropore fine filtration device
Fine impurity particle, obtain sodium bicarbonate material liquid.
Sodium bicarbonate material liquid is passed into the top of sodium bicarbonate carbonators, content is more than 40% supplement carbon dioxide gas,
After compressor boosts and is cooled to 35~45 DEG C, it is passed into tower lower part and carries out carbonation reaction with sodium bicarbonate material liquid adverse current.
Reaction heat is removed in cooling section cooling water slow cooling, the sodium bicarbonate magma of generation is taken out by tower bottom, takes out suspension liquid crystal
Temperature control is starched at 60 DEG C or so.
Sodium bicarbonate magma takes out liquid and carries out separation of solid and liquid with centrifuge after thickener is thickened to regarding solid-to-liquid ratio 50~60%.
Isolated sodium bicarbonate filtrate after the heat exchange heating of wet decomposed solution back to weight alkali mixing cirtern through with sizing mixing.Aqueous 5~7% consolidate
Mutually wet sodium bicarbonate goes pneumatic conveyer dryer to dry, heating steam pressure 0.8MPa (G), 140~150 DEG C of hot blast temperature, exhaust temperature
60~65 DEG C, sodium bicarbonate product is made after dry.
27~30 DEG C of weight alkali filtrate temperature after heat exchange enter deammoniation tower up to more than 65 DEG C, make in weight alkali filtrate
NH4HCO3、(NH4)2CO3、NH4OH is substantially completely decomposed, and the CO for producing decomposition2、NH3Into gas phase, same to saturated vapor
Discharged together by tower top.Tower reactor connects reboiler, and by 0.4MPa (G) low-pressure steam indirectly heat, bottom temperature is controlled 115
DEG C, deamination liquid is taken out by tower reactor.
The crude salt halogen of underground mining, is refined using lime-Method of Soda, and the high salt filtrate arranged outside sodium bicarbonate process is made
Used for a part of soda ash of soda ash refining agent.4.8~5.35kmol/m of bittern NaCl contents after refined3(96~107tt),
Na2SO4≤ 6g/L, Mg2+≤ 6mg/L, Ca2+≤ 20mg/L, turbidity≤30ppm.
The deamination tail gas of deammoniation tower discharge is through with removing deamination tail gas ammonia absorption tower after the heat exchange of weight alkali filtrate and cooling water cooling, using
Refined bittern absorbs, and obtaining light ammonial brine through cooling goes triamine tail gas ammonia absorption tower absorption triamine tail gas that carbonization ammonial brine is made.
By the deamination liquid that ammonium chloride content is 194.25g/L, sodium chloride content is 67.25g/L, led with the effect of salt II, III, IV
Go out liquid heat exchange cooling, convert and ammonium processed completes countercurrent evaporation after liquid, initially enter the IV effect salt evaporator that evaporating temperature is 50 DEG C, so
Export liquid sequentially enters an effect salt evaporator afterwards, finally enters the I effect evaporator that evaporating temperature is 110 DEG C.0.4MPa(G)
Low-pressure steam initially enters salt I and imitates heater indirectly heat, and the indirect steam of generation sequentially enters adding for lower 1st effective evaporator
Hot device, the condensed rear emptying of secondary vapour that last evaporator produces.Deamination liquid makes NaCl reach saturation during heating evaporation
And NaCl crystallizations are generated, while obtain the clear liquid that liquid is completed in salt manufacturing.The NaCl magmas of taking-up through push-type centrifuge separation of solid and liquid,
Obtain salt filtrate and it is aqueous be less than 5% the wet NaCl of byproduct.
Salt manufacturing completion liquid is sent to the following current of ammonium flash evaporation and carries out triple effect shwoot, III effect flash evaporation is reached sudden strain of a muscle using vacuum pump
Send out the temperature evaporating pressure required at 54 DEG C or so.In shwoot, temperature-fall period, NH4Cl reaches saturation and generates NH4Cl is tied
Crystalline substance, while obtain the clear liquid that ammonium processed completes liquid.The NH of taking-up4Cl magmas obtain ammonium filtrate after push-type centrifuge separation of solid and liquid
With wet NH4Cl.Ammonium processed complete liquid and deamination liquid convert and after enter IV effect salt evaporator, formation closed circulation.
Wet NH4Cl is dried using the dry ammonium stove of internal heat type fluid bed.Heat source is the steam of 0.8MPa (G), dry
After obtain NH4Cl products.
Embodiment 2
Melamine is produced using atmospheric circulating method using urea as raw material, 1t melamines is often produced and produces 2200kg's
NH3、CO2Mixed tail gas, wherein NH3Content is 1019kg, CO2Content is 1159kg, and temperature is 135~145 DEG C, and pressure is
0.15~0.3MPa (G).
Triamine tail gas ammonia absorption tower is passed through containing ammonia and carbon dioxide tail gas by what production melamine obtained, is inhaled with deamination tail gas
35~40 DEG C of light ammonial brines that ammonia tower comes absorb, through cooling down and clarification obtains carbonating ammonial brine.Carbonating ammonial brine contains NaCl
For 257.4~263.3g/L, FNH3/Na+For 1.12~1.16, temperature is 38~42 DEG C, and should control the carbon of carbonating ammonial brine
Change degree is less than 80%, insufficient NH3Supplement is adjusted by absorbing pure ammonia.
The ammonial brine that is carbonated is passed into the top of weight alkali carbonators, wet decomposed tail gas is mixed with the carbon dioxide gas supplemented
Into the carbon dioxide gas more than 80%, after compressor boosts and is cooled to 30~40 DEG C, it is inverse with ammonial brine to be passed into tower lower part
Stream carries out carbonation reaction.Temperature should maintain 60~70 DEG C at 2/3 tower height of weight alkali carbonators, be conducive to obtain good
NaHCO3Crystal.Reaction heat is removed in cooling section cooling water, the heavy alkali magma of generation is taken out by tower bottom, takes out suspension liquid crystal
Slurry temperature degree is 27~30 DEG C.
Separation of solid and liquid is carried out using rotary drum vacuum filter counterweight alkali magma, and adds appropriate wash water to obtain Washing of Filter Cake
Wet big and heavy alkali, forms as (wt%)：
Wet big and heavy alkali and the sodium bicarbonate filtrate after heat exchange and a small amount of supplement water are added in mixing cirtern, obtain temperature as 90
~100 DEG C of heavy alkali adjusting slurry.
Weight alkali adjusting slurry is passed into wet decomposition tower with delivery pump, makes the NH in weight alkali adjusting slurry4HCO3、(NH4)2CO3、
NH4OH is substantially completely decomposed, NaHCO3Resolution ratio reaches more than 67.2%, and the CO for producing decomposition2、NH3Into gas phase.
Tower top outlet is CO2、NH3And saturated vapor, carbon-dioxide gas compressor is entered through cooling, net ammonia, duplicate removal alkali is carbonized after boosting
Tower.Wet decomposition tower tower reactor connects reboiler, by 0.6MPa (G) low-pressure steam indirectly heat, 137 DEG C of bottom temperature.
It it is 80~85 DEG C by the wet decomposed solution that tower reactor is taken out and temperature after the heat exchange of sodium bicarbonate filtrate, clarified bucket relies on gravity
Sedimentation removes more than 20 μm of insoluble granule impurity, and 0.1~20 is removed using 304 stainless steel sintered meshwork filter core accurate filters
μm fine impurity particle, obtain sodium bicarbonate material liquid.
Sodium bicarbonate material liquid is passed into the top of sodium bicarbonate carbonators, from pressure-swing absorption apparatus content more than 80%
Carbon dioxide gas is supplemented, after compressor boosts and is cooled to 35~45 DEG C, is passed into tower lower part and sodium bicarbonate material liquid adverse current
Carry out carbonation reaction.Reaction heat is removed in cooling section cooling water slow cooling, the sodium bicarbonate that generation is taken out by tower bottom is brilliant
Slurry, takes out suspension magma temperature control at 60 DEG C or so.
Sodium bicarbonate magma takes out liquid and carries out separation of solid and liquid with centrifuge after thickener is thickened to regarding solid-to-liquid ratio 50~60%.
Isolated sodium bicarbonate filtrate after the heat exchange heating of wet decomposed solution back to weight alkali mixing cirtern through with sizing mixing.Aqueous 5~7% consolidate
Mutually wet sodium bicarbonate goes pneumatic conveyer dryer to dry, heating steam pressure 0.8MPa (G), 140~150 DEG C of hot blast temperature, exhaust temperature
62~65 DEG C, sodium bicarbonate product is made after dry.
27~30 DEG C of weight alkali filtrate temperature after heat exchange enter deammoniation tower up to more than 65 DEG C, make in weight alkali filtrate
NH4HCO3、(NH4)2CO3、NH4OH is substantially completely decomposed, and the CO for producing decomposition2、NH3Into gas phase, same to saturated vapor
Discharged together by tower top.Tower reactor connects reboiler, and by 0.4MPa (G) low-pressure steam indirectly heat, bottom temperature is controlled 110
DEG C, deamination liquid is taken out by tower reactor, and free ammonia ammonia removal efficiency is more than 99.5%.
The crude salt halogen of underground mining, is refined using lime-Method of Soda, and the high salt filtrate arranged outside sodium bicarbonate process is made
Used for a part of soda ash of soda ash refining agent.4.8~5.35kmol/m of bittern NaCl contents after refined3(96~107tt),
Na2SO4≤ 6g/L, Mg2+≤ 6mg/L, Ca2+≤ 20mg/L, turbidity≤30ppm.
Deammoniation tower discharge deamination tail gas pass through with weight alkali filtrate heat exchange and cool down water cooling after remove deamination gas ammonia absorption tower, with essence
Brewed brine water absorbs, and obtaining light ammonial brine through cooling goes triamine tail gas ammonia absorption tower absorption triamine tail gas that carbonization ammonial brine is made.
The deamination liquid that ammonium chloride content is 204.9g/L, sodium chloride content is 71.87g/L is sent into I effect evaporator, mother liquor
115~120 DEG C of evaporating temperature, I effect export liquid with filter ammonium liquid convert and after enter II effect evaporator continuation heating evaporation, make NaCl
Reach saturation and generate NaCl crystallizations.0.4MPa (G) low-pressure steam initially enters I effect heater indirectly heat, generation it is secondary
Steam enters II effect heater.Using hydraulic ejector make II effect evaporator reach evaporating temperature at 80 DEG C or so it is required
Evaporating pressure.II effect divides the salt magma that salt cellar takes out through push-type centrifuge separation of solid and liquid, obtains salt filtrate and aqueous is less than 5%
The wet NaCl of byproduct.
Salt filtrate is sent into the growing crystallizer of outer circulation, aspirate mother liquor by axial-flow pump carries out clear liquid circulation by Outer Cooler
Cooling, cooling medium is recirculated cooling water, crystallizer mother liquor temperature is dropped to 30~35 DEG C, NH4Cl reaches saturation and generates
NH4Cl is crystallized.The NH taken out by crystallizer lower part4Cl suspensions magma obtains after stiff thickening and push-type centrifuge separation of solid and liquid
To ammonium filtrate and wet NH4Cl.Ammonium filtrate and I effect export liquid convert and after enter II effect evaporator, formation closed circulation.
Wet NH4Cl is dried using the dry ammonium stove that seethes with excitement, and cold air heating heat source is the steam of 0.8MPa (G).From dry ammonium stove
Lower part is by dried dry NH4Cl takes out, and obtains NH4Cl products.
Claims (10)
1. a kind of utilize produces the technique that the tail gas of melamine prepares sodium bicarbonate and ammonium chloride, it is characterised in that including as follows
Step：
(1) collect using urea as raw material production melamine and contain ammonia and carbon dioxide tail gas；
(2) tail gas in step (1) is passed through triamine tail gas ammonia absorption tower, is absorbed using light ammonial brine, refined brine or bittern, warp
Cooling and clarification obtain carbonating ammonial brine；
(3) the carbonating ammonial brine of step (2) is passed into the top of weight alkali carbonators, the carbon dioxide gas being passed through with tower lower part
Body adverse current carries out carbonation reaction, removes reaction heat with cooling water, the heavy alkali magma of generation is taken out by tower bottom；
(4) the heavy alkali magma of step (3) is subjected to separation of solid and liquid；
(5) the wet big and heavy alkali for obtaining step (4) is added in mixing cirtern with sodium bicarbonate filtrate and supplement water, is obtained weight alkali and is sized mixing
Liquid；
(6) the heavy alkali adjusting slurry for obtaining step (5) is passed into wet decomposition tower, makes the NH in weight alkali adjusting slurry4HCO3、(NH4)2CO3、NH4OH is fully decomposed, NaHCO3Resolution ratio reaches more than 65%, and the CO for producing decomposition2、NH3Into gas phase；Tower top
Outlet is CO2、NH3And saturated vapor, carbon-dioxide gas compressor is entered through cooling, net ammonia, step (3) is returned to after boosting；
Tower reactor connects reboiler, and by 0.4~0.8MPa gauge pressure low-pressure steam indirectly heats, bottom temperature is controlled at 120~150 DEG C；It is wet
Decomposed solution is taken out by tower reactor, through exchanging heat and clarifying with sodium bicarbonate filtrate, be sent to sodium bicarbonate carbonators after refined filtration；
(7) the sodium bicarbonate material liquid obtained by step (6) enters the top of sodium bicarbonate carbonators, the dioxy being passed through with tower lower part
Change carbon back flow of gas and carry out carbonation reaction, lye heavy carbonic reaction heat is removed with cooling water, and generation is taken out by tower bottom
Sodium bicarbonate magma；
(8) the sodium bicarbonate magma of step (7) is subjected to separation of solid and liquid, isolated sodium bicarbonate filtrate passes through to be exchanged heat with wet decomposed solution
Step (5) is returned to after heating；
(9) the wet sodium bicarbonate of solid phase obtained by step (8) enters sodium bicarbonate drier, heated to go moisture removal that sodium bicarbonate is made
Product；
(10) the weight alkali filtrate obtained by step (4) temperature after heat exchange enters deammoniation tower up to more than 65 DEG C, makes weight alkali filtrate
In NH4HCO3、(NH4)2CO3、NH4OH is fully decomposed, and the CO for producing decomposition2、NH3Into gas phase；Tower top outlet is CO2、
NH3And saturated vapor；Tower reactor connects reboiler, by 0.2~0.4MPa gauge pressure low-pressure steam indirectly heats, bottom temperature control
At 110~120 DEG C；Deamination liquid is taken out by tower reactor；
(11) by the deamination tail gas that step (10) obtains through with going deamination tail gas to inhale ammonia after the heat exchange of weight alkali filtrate and cooling water cooling
Tower, is absorbed with refined brine or bittern, and obtaining light ammonial brine through cooling is back in step (2) ammonia absorption tower；
(12) containing ammonium chloride and the deamination liquid of sodium chloride obtained step (10), in 45~120 DEG C and the saturation of relevant temperature
Under steam pressure, salt manufacturing is carried out using multi-effect evaporation scheme is predicted.Deamination liquid initially enters salt last evaporator after heat exchange, most
Enter I effect evaporator afterwards；0.2~0.4MPa (G) low-pressure steam initially enters salt I and imitates heater, and the indirect steam of generation is successively
The heater of lower 1st effective evaporator is entered, emptying after the secondary vapour that last evaporator produces is condensed；Deamination liquid is steamed in heating
NaCl is reached saturation during hair and generate NaCl crystallizations, while obtain salt manufacturing and complete liquid clear liquid, salt magma is through separation of solid and liquid
After obtain salt filtrate and the wet NaCl of byproduct；
(13) liquid is completed into the salt manufacturing that step (12) obtains and is sent to ammonium flash evaporation, multiple-effect shwoot is carried out at 120~45 DEG C, is being dodged
Make NH in hair, temperature-fall period4Cl reaches saturation and generates NH4Cl is crystallized, while obtains the clear liquid that ammonium processed completes liquid, taking-up
NH4Cl magmas obtain ammonium filtrate and wet NH after separation of solid and liquid4Cl；
(14) ammonium processed that step (13) obtains is completed into liquid and return to step (12), with deamination liquid convert and after enter the steaming of salt end effect
Device is sent out, forms closed circulation；
(15) the wet NH for obtaining step (13)4Cl is dried, and obtains NH4Cl products.
2. technique according to claim 1, it is characterised in that step (1) melamine using urea as raw material is given birth to
Production. art can be high-pressure process, low-pressure process or non-pressure process.
3. technique according to claim 1, it is characterised in that the carbonating ammonial brine that step (2) described process obtains
Degree of carbonisation is not more than 75~80%.
4. technique according to claim 1, it is characterised in that the sodium bicarbonate material liquid inlet temperature of stabilizer described in step (7) is
65~90 DEG C, magma taking-out temperature is 55~65 DEG C.
5. technique according to claim 1, it is characterised in that the sodium bicarbonate filtrate that step (8) obtains first discharges a part
Brine or brine refining process are gone, the NaCl contents into sodium bicarbonate carbonators material liquid is able to maintain that less than 4.8wt%.
6. technique according to claim 1, it is characterised in that the deamination liquid that step (10) described process obtains, free ammonia
Removal efficiency is more than 99.5%, and carbon dioxide fully removes.
7. technique according to claim 1, it is characterised in that step (12), (13) described process can also use following current
NaCl, 78~82 DEG C of end effect mother liquid evaporation temperature are produced in evaporation；After isolating NaCl, complete evaporation of liquid is cooled down, 30~
Make NH at 35 DEG C4Cl reaches saturation and generates NH4Cl is crystallized, and ammonium processed is obtained after separation of solid and liquid and completes liquid and wet NH4Cl, ammonium processed
Complete liquid and be back to last evaporator composition closed circulation.
8. technique according to claim 1, it is characterised in that produce the NaCl raw materials needed for sodium bicarbonate, can be dissolving
Brine made of solid crude salt can also be the bittern of underground mining, need to be refined into 4.8~5.35kmol/m of NaCl contents3,
Na2SO4≤ 6g/L, Mg2+≤ 6mg/L, Ca2+The refined brine or bittern of≤20mg/L, turbidity≤30ppm；Can use lime-
Method of Soda or lime-ammonium carbonate method are refined.
9. technique according to claim 1, it is characterised in that decarbonization gas, or boiler flue need to be provided by synthetic ammonia installation
The carbon dioxide that gas pressure-variable adsorption is produced, the supplement source of the gas as carbon dioxide.
10. technique according to claim 1, it is characterised in that using the low-pressure steam of 0.1~1.0MPa gauge pressures as heat
Source.
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| CN109252839A (en) * | 2018-11-02 | 2019-01-22 | 江西晶昊盐化有限公司 | A kind of ammonia-soda process alkaline mixing liquid two-phase note well adopts halogen technology |
| CN110589857A (en) * | 2019-10-29 | 2019-12-20 | 常州大学 | Method for preparing alkali by using waste salt in combination manner |
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| CN111704149A (en) * | 2020-05-27 | 2020-09-25 | 山东海天生物化工有限公司 | Process for producing sodium bicarbonate |
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| CN101519383A (en) * | 2009-03-25 | 2009-09-02 | 北京烨晶科技有限公司 | Process for jointly producing cyanuramide, sodium carbonate and ammonium chloride by using carbamide |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101519383A (en) * | 2009-03-25 | 2009-09-02 | 北京烨晶科技有限公司 | Process for jointly producing cyanuramide, sodium carbonate and ammonium chloride by using carbamide |
| CN101519383B (en) * | 2009-03-25 | 2010-08-25 | 北京烨晶科技有限公司 | Process for jointly producing cyanuramide, sodium carbonate and ammonium chloride by using carbamide |
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Application publication date: 20180420 |