CN105524006A - Energy-saving environment-friendly co-production process of cyanuric acid, food-grade sulfuric acid and sulfamic acid - Google Patents
Energy-saving environment-friendly co-production process of cyanuric acid, food-grade sulfuric acid and sulfamic acid Download PDFInfo
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- CN105524006A CN105524006A CN201610012902.6A CN201610012902A CN105524006A CN 105524006 A CN105524006 A CN 105524006A CN 201610012902 A CN201610012902 A CN 201610012902A CN 105524006 A CN105524006 A CN 105524006A
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- sulfuric acid
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-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D251/00—Heterocyclic compounds containing 1,3,5-triazine rings
- C07D251/02—Heterocyclic compounds containing 1,3,5-triazine rings not condensed with other rings
- C07D251/12—Heterocyclic compounds containing 1,3,5-triazine rings not condensed with other rings having three double bonds between ring members or between ring members and non-ring members
- C07D251/26—Heterocyclic compounds containing 1,3,5-triazine rings not condensed with other rings having three double bonds between ring members or between ring members and non-ring members with only hetero atoms directly attached to ring carbon atoms
- C07D251/30—Only oxygen atoms
- C07D251/32—Cyanuric acid; Isocyanuric acid
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/48—Sulfur dioxide; Sulfurous acid
- C01B17/50—Preparation of sulfur dioxide
- C01B17/54—Preparation of sulfur dioxide by burning elemental sulfur
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/082—Compounds containing nitrogen and non-metals and optionally metals
- C01B21/087—Compounds containing nitrogen and non-metals and optionally metals containing one or more hydrogen atoms
- C01B21/093—Compounds containing nitrogen and non-metals and optionally metals containing one or more hydrogen atoms containing also one or more sulfur atoms
- C01B21/096—Amidosulfonic acid; Salts thereof
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to the technical field of chemical industry production, and specifically relates to an energy-saving environment-friendly co-production technology of cyanuric acid, food-grade sulfuric acid and sulfamic acid. The co-production process comprises the steps of (1) cyanuric acid production; (2) food-grade sulfuric acid production including sulfur melting, sulfur burning, conversion, absorption and drying, and residual heat recovery; and (3) sulfamic acid production. With the co-production process, defects in independent production links of cyanuric acid, food-grade sulfuric acid and sulfamic acid are solved, and no additional environmental treatment equipment is needed, such that the production process is greatly simplified, and the production period is shortened. The process is safe, energy-saving and environment-friendly.
Description
Technical field
The invention belongs to the technical field of Chemical Manufacture, be specifically related to the joint process of a kind of energy saving and environment friendly cyanuric acid, food grade sulfuric acid and thionamic acid.
Background technology
Cyanuric acid has another name called tricyanic acid, white crystals, separates out from water, is with two crystal water.Mildly bitter flavor, substantially nontoxic, can be dissolved in hot water, be slightly soluble in cold water, the aqueous solution, in acid, can be dissolved in the aqueous solution of potassium hydroxide and sodium hydroxide, be insoluble to the organic solvents such as cold alcohol, ether, benzene.There is two kinds of isomer, i.e. keto-acid and enol-type structure, normally exist with the mixture of two kinds of isomer.Current production cyanuric acid adopts urea pyrolysis method, obtains cyanuric acid by the pyrolysis cyclisation of urea.Urea pyrolysis cyclisation in pyrolysis oven can produce a large amount of ammonia, needs to spend great amount of cost to carry out environmental protection treatment to the ammonia produced in existing cyanuric acid production technique, and investment is large, and income is low, complex procedures.Pyrolysis oven needs for the pyrolysis cyclisation of urea provides a large amount of heats simultaneously, and not only energy consumption later stage desulphurization and denitration dust removal process expense that is large but also coal combustion causes greatly production cost to go up.
Food grade sulfuric acid is souring agent or acidic flavoring agent, and purposes is processing aid, for containing alcoholic beverage, cheese etc.; For manufacturing glucose by Starch Hydrolysis; Regulate hydrolysising condition, to manufacture the starch syrup containing more than 25% dextrin; Sulphuric acid soln with 2% ~ 4% removes oranges and tangerines endocarp to manufacture oranges and tangerines can; During table oil with the vitriol oil (add about 1%) in 15 ~ 20 DEG C of stirring, remove through washing after making the organics dehydration charing in grease.Prevent the damage of CO2 from answering in beer production.Can produce a large amount of heat energy in the production process of food grade sulfuric acid, but prior art is extremely low for this part heat utilization rate, causes the waste of the energy.
The gas phase ammoniation process that the production employing ammonia of thionamic acid and sulphur trioxide react under gas phase condition.Carry out sulfonation by ammonia and sulphur trioxide and generate thionamic acid crude product, then add water and carry out crystallization and obtain thionamic acid finished product.
Summary of the invention
The object of the invention is to the joint process that a kind of energy saving and environment friendly cyanuric acid, food grade sulfuric acid and thionamic acid are provided for the defect in current cyanuric acid, food grade sulfuric acid and thionamic acid separately independent production link, this joint process not only solves cyanuric acid, food grade sulfuric acid and the thionamic acid defect separately in independent production link, and without the need to additional Environmental-protecting treater, enormously simplify Production Flow Chart and shorten the production cycle, safety energy-conserving environment protection.
Technical scheme of the present invention is: the joint process of a kind of energy saving and environment friendly cyanuric acid, food grade sulfuric acid and thionamic acid, comprises the following steps:
(1) production of cyanuric acid: urea is placed in pyrolysis oven and carries out pyrolysis cyclisation, pyrolysis cyclisation produces the ammonia of 150 ~ 250 DEG C;
(2) production of food grade sulfuric acid: molten sulphur; Burn sulphur; Transform; Absorption, drying; Waste heat recovery; Wherein enter convertor at the sulfur dioxide gas burning 850 ~ 1000 DEG C of sulfur dioxide gas producing in sulphur process and first become after the pyrolysis oven during step (1) cyanuric acid is produced carries out heat exchange 420 DEG C;
(3) production of thionamic acid: first the ammonia in the production of described step (1) cyanuric acid removes solid impurity by air filtration cotton after drawing via induced draft fan, then carry out entering soda-wash tower after heat exchange through high-performance heat exchanger, remove a small amount of HCN acid to wait the ammonia of acidic substance after alkali cleaning to enter electrostatic precipitator to carry out electric demist, the ammonia after demist is stored to ammonia surge tank by compressor after moisture eliminator drying; Ammonia in ammonia surge tank is delivered to injection reactor by ammonia flow gauge, the sulphur trioxide in sulphur trioxide storage tank is delivered to injection reactor simultaneously; Reactant in injection reactor is delivered to sulphonation kettle, controls the temperature of reaction of sulphonation kettle at 45 ~ 55 DEG C; Sulfonated products is delivered in condenser through power-driven pump carries out cooling rear portion and is back in sulphonation kettle, and a part is delivered in dilution still; Sulfonated products after dilution obtains thionamic acid crude product after filtration; Finally carry out the refining of thionamic acid crude product.
In described step (3), the heat-eliminating medium of high-performance heat exchanger is low temperature soft water, and the high temperature soft water after heat exchange is used for boiler.
The water ratio controlling electrostatic precipitator exit ammonia in described step (3) is 0.02 ~ 0.05%.
The temperature controlling injection reactor in described step (3) is 45 ~ 70 DEG C.
The inlet temperature controlling condenser in described step (3) is 55 ~ 70 DEG C, and controlling temperature out is 45 ~ 55 DEG C.
In dilution still, diluent media is the crystalline mother solution in pure water or thionamic acid crude product refining in described step (3).
Beneficial effect of the present invention is: the joint process of energy saving and environment friendly cyanuric acid of the present invention, food grade sulfuric acid and thionamic acid not only solves cyanuric acid, food grade sulfuric acid and the thionamic acid defect separately in independent production link, and without the need to additional Environmental-protecting treater, enormously simplify Production Flow Chart and shorten the production cycle, safety energy-conserving environment protection.
Make a concrete analysis of from the following aspects according to practical condition below.
One, energy utilization
It is 32620 tons/year that food grade sulfuric acid production system produces 100000 tons of (amounting to 100% sulfuric acid) sulphur used per year, sulphur amount per hour is (within 11 months, calculate by annual production in 4.12 tons/time, within 1 month, be wherein the repair time) show that release of heat per hour is 4120kg × 9282KJ/kg=38241840KJ according to the combustion heat of sulphur, amounting to standard coal is that (dilute sulphuric acid according to producing 50%-56% in the requirement Description on Production of Sulfaminic Acid of product in production process can as part NH in cyanuric acid production for 1306.52kg
3recycling H
2sO
4+ 2NH
3→ (NH
4) 2SO
4generating a kind of industry, all available fertilizer of agricultural is sold, therefore will consider the output size of pyrolysis kiln when building cyanuric acid production plant.When dropping to 420 DEG C according to the heat of 1306.52kg standard coal, unnecessary heat is: SO
2heat 128.75kmol/h × 530 × 42.25KJ/Kmol=2883034.375KJ/h, O
2heat is 128.75kmol/h/2 × 530 × 29.936KJ/Kmol=1021378.9KJ/h, N
2heat is that to amount to standard coal be 482.03kg/h to 10.25 × 128.75kmol/h/2 × 530 × 29.18KJ/Kmol=10204747.53KJ/h, Q=14109160.805KJ/h; Can amount to standard coal every day is 24 × 482.03kg/h=11568.72kg/ days.
Cyanuric acid processing requirement and reaction principle thereof: (NH
2)
2cO=NH
3+ CHNO3CHNO=C
3h
3n
3o
3; I.e. 3mol (NH
2)
2cO adds production 3molNH in pyrolysis kiln
3often 1molC is produced with in 1mol cyanuric acid namely its reaction process
3h
3n
3o
3(CA) 3molNH will be generated
3discharge pyrolysis kiln, and need to take away a part of heat, NH
3middle outflow temperature is greatly about 250-260 DEG C.
Calculate according to producing ton cyanuric acid crude product standard coal production requirement year: the Heat of fusion of urea is for (to add NH
4cl makes catalyzer) be about 0.426 ton/ton according to practical condition coal, be far longer than the numerical value of Theoretical Calculation, reason is the heat part that absorbs in pyrolytic process due to urea is by NH for the decomposition of urea and quite a few
3pyrolysis kiln is taken out of by gaseous form.Therefore the consumption of actual production is taked to carry out the accounting of energy as foundation when calculating its reaction institute's heat requirement.
Concrete computation process is following, and (namely cyanuric acid production coal per ton calculates, and NH
3heat is adjusted):
1. the pyrolysis kiln of my company existing cyanuric acid production wherein every bar kiln per tour inlet amount ((NH
2)
2cO): 21 × 95 × 5kg=9975kg [(NH
2)
2cO] 9975 × 0.03%=299.25kg [NH
4cl] in normal material ratio calculate the actual add-on of 3%-4% be 175kg therefore reality heat be greater than theoretical amount, the present situation of equally also realistic production.(pyrolysis temperature is between 285 DEG C-290 DEG C) but in quality product, chloride ion content is less, and white color, purity is high, according to market major part requirement, is also desirable.
2. according to actual recovery situation cyanuric acid consumption urea per ton between 1.68 tons-1.70 tons, therefore the output of every bar pyrolysis kiln is: 9975kg/1680kg=5.9375 ton, so annual production is 5878.125 tons.
3. NH is produced
3amount be 9.975 × 3 × 30 × 11-5878.125=3997.125 ton, according to Theoretical Calculation NH
3amount:
(NH
2)
2cO charging capacity is 9875.25 tons, and cyanuric acid output is 7079.03 tons, NH
3amount be 2796.22 tons (theoretical values), actual NH
3generation should be within 3997.125 tons-2796.22 tons.Reason is because urea some urea distillation in pyrolytic process does not produce CA, also ammonia is not generated, an ammonia part is used to bring in CA crude product containing a small amount of trimeric cyanamide and biuret in some CA in addition, therefore the actual generation of ammonia is 9875.25-0.7 × 9875.25=2962.575 ton, therefore needing by the amount of sulphur trioxide is 2962.575 × 1.86/0.395=13950.35 ton, and producing thionamic acid per year is 2962.575 × 2.255/0.395=16912.93 ton.
Two, the temperature whereabouts of ammonia and the methods analyst of ammonia removal of impurities thereof in producing about cyanuric acid.
Because ammonia used in Description on Production of Sulfaminic Acid is necessary for solid that is dry and that do not have other or gaseous impurities, before therefore will entering Description on Production of Sulfaminic Acid to the ammonia produced, carry out necessary process.For solid impurity because the temperature of ammonia in CA production is higher, can first lower the temperature to it, at employing air filtration cotton removing solid impurity, due to temperature reduce decrease ammonia high temperature time with a small amount of urea sublimate, therefore only containing a small amount of carbon dioxide, air in the ammonia after cooling, do not have other gas to produce, the requirement of Description on Production of Sulfaminic Acid ammonia can be met.
Control to ammonia flow: must control the ammonia flow entering sulphonation kettle to thionamic acid workshop through Cemented filling after being drawn by induced draft fan from the ammonia in CA pyrolysis kiln, therefore installs an ammonia flow controller additional to guarantee steadily carrying out of reaction on sulfonation reaction still.In order to control convenient suggestion, the ammonia from pyrolysis kiln is generated thionamic acid by being entered in reactor by gas meter after ammonia pressurization with sulphur trioxide reaction by pressure exerting device in addition.The thionamic acid equipment that existing interval is fed intake normally uses, but output and the suggestion of yield instability adopt the method for continuously feeding to achieve the continuity of Description on Production of Sulfaminic Acid in production process, save manpower and facility investment, and all secure to the seed output and quality of thionamic acid.
Three, sulphur trioxide enters sulfonation reaction still
Be sulphonating agent and reactant as sulfonation reaction main raw material sulphur trioxide, therefore the feeding manner of sulphur trioxide and inlet amount also have very important impact to the quality of thionamic acid.In sulfonation reaction, sulphur trioxide is the strongest sulphonating agent, and it is very violent with ammonia gas react, therefore require to control well temperature of reaction, the heat that reaction is produced takes away the situation reducing local temperature rise rapidly, mode (spraying reaction and tower reactor) front a kind of reactive mode that ammonia is entered be convenient to control and also facility investment less, but early stage, the design of injection reactor dropped into comparatively large, working cost is lower.Then a kind of tower reactor making is simple but red-tape operati is more complicated, fluctuation of service, and therefore suggestion adopts injection reactor to operate.
It is feasible for producing thionamic acid according to above analytical procedure, not only saves production cost to enterprise, and decreases raw-material trucking costs, for enterprise creates considerable economic benefit.
The water ratio controlling electrostatic precipitator exit ammonia in described step (3) is 0.05 ~ 0.02%; The temperature controlling injection reactor is 45 ~ 70 DEG C; The inlet temperature controlling condenser is 55 ~ 70 DEG C, and controlling temperature out is 45 ~ 55 DEG C.Strict control temperature of reaction and NH in operating process
3in water ratio, otherwise not only can cause starting material (SO
3, NH
3) significant wastage, and resultant is (NH
4)
2sO
4(ammonium sulfate) instead of thionamic acid, also can make temperature of reaction raise simultaneously and occur security incident.
Embodiment
Below by embodiment, the present invention will be described in detail.
A joint process for energy saving and environment friendly cyanuric acid, food grade sulfuric acid and thionamic acid, comprises the following steps:
(1) production of cyanuric acid: urea is placed in pyrolysis oven and carries out pyrolysis cyclisation, pyrolysis cyclisation produces the ammonia of 150 ~ 250 DEG C;
(2) production of food grade sulfuric acid: molten sulphur; Burn sulphur; Transform; Absorption, drying; Waste heat recovery; Wherein enter convertor at the sulfur dioxide gas burning 850 ~ 1000 DEG C of sulfur dioxide gas producing in sulphur process and first become after the pyrolysis oven during step (1) cyanuric acid is produced carries out heat exchange 420 DEG C;
(3) production of thionamic acid: first the ammonia in the production of described step (1) cyanuric acid removes solid impurity by air filtration cotton after drawing via induced draft fan, then carry out after heat exchange, entering soda-wash tower through high-performance heat exchanger and remove the acidic substance such as a small amount of HCN, ammonia after alkali cleaning enters electrostatic precipitator and carries out electric demist, and the ammonia after demist is stored to ammonia surge tank by compressor after moisture eliminator drying; Ammonia in ammonia surge tank is delivered to injection reactor by ammonia flow gauge, the sulphur trioxide in sulphur trioxide storage tank is delivered to injection reactor simultaneously; By the reactant in injection reactor to sulphonation kettle, control the temperature of reaction of sulphonation kettle at 45 ~ 55 DEG C; Sulfonated products is delivered in condenser through power-driven pump carries out condensation rear portion and is back in sulphonation kettle, and a part is delivered in dilution still; Sulfonated products after dilution obtains thionamic acid crude product after filtration; Finally carry out the refining of thionamic acid crude product.
In described step (3), the heat-eliminating medium of high-performance heat exchanger is low temperature soft water, and the high temperature soft water after heat exchange is used for boiler.
The water ratio controlling electrostatic precipitator exit ammonia in described step (3) is 0.02 ~ 0.05%.
The temperature controlling injection reactor in described step (3) is 45 ~ 70 DEG C.
The inlet temperature controlling condenser in described step (3) is 55 ~ 70 DEG C, and controlling temperature out is 45 ~ 55 DEG C.
In dilution still, diluent media is the crystalline mother solution in pure water or thionamic acid crude product refining in described step (3).
Claims (6)
1. a joint process for energy saving and environment friendly cyanuric acid, food grade sulfuric acid and thionamic acid, comprises the following steps:
(1) production of cyanuric acid: urea is placed in pyrolysis oven and carries out pyrolysis cyclisation, pyrolysis cyclisation produces the ammonia of 150 ~ 250 DEG C;
(2) production of food grade sulfuric acid: molten sulphur; Burn sulphur; Transform; Absorption, drying; Waste heat recovery; Wherein enter convertor at the sulfur dioxide gas burning 850 ~ 1000 DEG C of sulfur dioxide gas producing in sulphur process and first become after the pyrolysis oven during step (1) cyanuric acid is produced carries out heat exchange 420 DEG C;
(3) production of thionamic acid: first the ammonia in the production of described step (1) cyanuric acid removes solid impurity by air filtration cotton after drawing via induced draft fan, then carry out after heat exchange, entering soda-wash tower through high-performance heat exchanger and remove a small amount of acidic substance, ammonia after alkali cleaning enters electrostatic precipitator and carries out electric demist, and the ammonia after demist is stored to ammonia surge tank by compressor after moisture eliminator drying; Ammonia in ammonia surge tank is delivered to injection reactor by ammonia flow gauge, the sulphur trioxide in sulphur trioxide storage tank is delivered to injection reactor simultaneously; Reactant in injection reactor is delivered to sulphonation kettle, controls the temperature of reaction of sulphonation kettle at 45 ~ 55 DEG C; Sulfonated products through power-driven pump be delivered in condenser carry out condensation cooling rear portion be back in sulphonation kettle, a part be delivered to dilution still in; Sulfonated products after dilution obtains thionamic acid crude product after filtration; Finally carry out the refining of thionamic acid crude product.
2. the joint process of energy saving and environment friendly cyanuric acid, food grade sulfuric acid and thionamic acid according to claim 1, is characterized in that, in described step (3), the heat-eliminating medium of high-performance heat exchanger is low temperature soft water, and the high temperature soft water after heat exchange is used for boiler.
3. the joint process of energy saving and environment friendly cyanuric acid, food grade sulfuric acid and thionamic acid according to claim 1, is characterized in that, the water ratio controlling electrostatic precipitator exit ammonia in described step (3) is 0.02 ~ 0.05%.
4. the joint process of energy saving and environment friendly cyanuric acid, food grade sulfuric acid and thionamic acid according to claim 1, is characterized in that, the temperature controlling injection reactor in described step (3) is 45 ~ 70 DEG C.
5. the joint process of energy saving and environment friendly cyanuric acid, food grade sulfuric acid and thionamic acid according to claim 1, is characterized in that, the inlet temperature controlling condenser in described step (3) is 55 ~ 70 DEG C, and controlling temperature out is 45 ~ 55 DEG C.
6. the joint process of energy saving and environment friendly cyanuric acid, food grade sulfuric acid and thionamic acid according to claim 1, is characterized in that, in described step (3), in dilution still, diluent media is the crystalline mother solution in pure water or thionamic acid crude product refining.
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|---|---|---|---|
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|---|---|---|---|
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106699679A (en) * | 2016-12-02 | 2017-05-24 | 广西洋荣科技有限公司 | Preparation method of high-yield trichloroisocyanuric acid |
| CN110975531A (en) * | 2019-12-31 | 2020-04-10 | 河北六合化工有限公司 | Ammonia gas treatment method in cyanuric acid production |
| CN111848530A (en) * | 2020-08-03 | 2020-10-30 | 山东兴达化工有限公司 | Energy-saving and low-pollution preparation method of cyanuric acid |
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| CN1792796A (en) * | 2005-10-22 | 2006-06-28 | 河北冀衡化学股份有限公司 | Process for recoverying cyanuric acid three wastes |
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2016
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| CN1792796A (en) * | 2005-10-22 | 2006-06-28 | 河北冀衡化学股份有限公司 | Process for recoverying cyanuric acid three wastes |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106699679A (en) * | 2016-12-02 | 2017-05-24 | 广西洋荣科技有限公司 | Preparation method of high-yield trichloroisocyanuric acid |
| CN110975531A (en) * | 2019-12-31 | 2020-04-10 | 河北六合化工有限公司 | Ammonia gas treatment method in cyanuric acid production |
| CN111848530A (en) * | 2020-08-03 | 2020-10-30 | 山东兴达化工有限公司 | Energy-saving and low-pollution preparation method of cyanuric acid |
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Application publication date: 20160427 |