CN209322481U - The process units of ammonium hydrogen carbonate - Google Patents
The process units of ammonium hydrogen carbonate Download PDFInfo
- Publication number
- CN209322481U CN209322481U CN201822112822.5U CN201822112822U CN209322481U CN 209322481 U CN209322481 U CN 209322481U CN 201822112822 U CN201822112822 U CN 201822112822U CN 209322481 U CN209322481 U CN 209322481U
- Authority
- CN
- China
- Prior art keywords
- ammonia
- process units
- absorber
- hydrogen carbonate
- reaction
- 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.)
- Active
Links
Abstract
The utility model provides a kind of process units of ammonium hydrogen carbonate, it is related to ammonium hydrogencarbonate production field, the process units of the ammonium hydrogen carbonate, comprising: 1) absorber is used to form ammonia carbon solution, 2) ammonia carbon separation system, for the separation of melamine tail gas to obtain the carbon dioxide gas of high-purity, 3) reaction crystalizer, entrance are separately connected the absorber and the ammonia carbon separation system, 4) solid-liquid separator, entrance connect the outlet of the reaction crystalizer.The technical issues of being able to solve low efficiency existing for existing production method, at high cost, complex process using the process units reaches and improves production efficiency, reduces production cost and simplify the technical effect of production technology.
Description
Technical field
The utility model relates to ammonium hydrogencarbonate production fields, more particularly, to a kind of process units of ammonium hydrogen carbonate.
Background technique
Ammonium hydrogen carbonate, also known as ammonium bicarbonate, are a kind of carbonate, nitrogenous 17.7% or so, main application is to can be used as nitrogenous fertilizer
It uses, since it can be analyzed to NH3、CO2And H2Tri- kinds of gases of O and disappear, therefore also known as gas fertilizer；Next can be used for synthesis ammonium
Salt and fabric degreasing.
Currently, the production technology of domestic ammonium hydrogen carbonate is mainly with NH3、CO2And H2O is raw material, and concrete technology flow process is such as
Shown in Fig. 1, it is mother liquor using the solution containing ammonium hydrogen carbonate, ammonia is absorbed in ammonia scrubber, form concentrated ammonia liquor, concentrated ammonia liquor is logical
Overrich ammonia vessel, which enters in carbonators I, absorbs carbon gas.Carbon gas is the CO of purity 20-40%2Gas, such as Ammonia Production mistake
The conversion gas generated in journey.Most of CO2It is carbonized the absorption of tower I, contains a small amount of CO2Gas (CO2Content is 8-20%) enter carbon
Change and is absorbed again in tower II；After absorbing, containing 0.4%~1.5% carbon dioxide, contain 10~30mg/m3The exhaust gas of ammonia according to
It is secondary to be fixed secondary tower, gained inert gas is discharged after recovery and rinsing tower and knockout drum.The discharge of II bottom of carbonators contains carbonic acid
The solidliquid mixture of hydrogen ammonium obtains solid ammonium bicarbonate and mother liquor after thickener and centrifuge are separated by solid-liquid separation, mother liquor after
Continuous return to absorbs ammonia in ammonia scrubber, solid ammonium bicarbonate can be by being dried to obtain ammonium hydrogen carbonate product.
In production equipment used in above-mentioned production process, carbonators is tower structure, is not suitable for high-purity CO2Gas, only
Suitable for CO2Carbon gas of the gas content within the scope of 20-40%, main cause be carbon gas need from the bottom of carbonators into
Enter, carbon gas purity is higher, and reaction speed is faster, works as high-purity CO2When into carbonators, quickly in bottom total overall reaction, on
The liquid in portion also has neither part nor lot in reaction, this allow for carbonization tower bottom degree of supersaturation it is very big, for crystallize it is unfavorable, cause crystallization
Grain is too small, is not able to satisfy the requirement of separation of solid and liquid.The heat-exchanging tube bundle of 10-20 group is provided in carbonators simultaneously, easy fouling is made
At blocking.
By above-mentioned analysis it is found that main problem existing for the production technology of current ammonium hydrogencarbonate has: with pure ammonia and low
Purity silicon carbide gas is raw material, at high cost；Carbonators is not suitable for high-purity CO2It is produced, production efficiency is low, plant energy consumption
It is high；Carbonators is easy blocking, and the cycle of operation is short；Reaction will pass through two-stage carburizing reagent, and device technique is complicated, long flow path；Gained
The grain graininess of ammonium hydrogen carbonate is smaller, is not readily separated, and obtained ammonium hydrogen carbonate particle is mostly acicular texture, frangible.
Utility model content
The purpose of this utility model is to provide the process units of ammonium hydrogen carbonate, with solve the problems, such as it is above-mentioned it is mentioned in extremely
It is one few.
In order to realize the above-mentioned purpose of the utility model, the following technical scheme is adopted:
A kind of process units of ammonium hydrogen carbonate, comprising:
Absorber is used to form ammonia carbon solution,
Ammonia carbon separation system, for the separation of melamine tail gas to obtain the carbon dioxide gas of high-purity,
Reaction crystalizer, entrance are separately connected the absorber and the ammonia carbon separation system,
Solid-liquid separator, entrance connect the outlet of the reaction crystalizer.
Compared with the prior art, the utility model has the following beneficial effects:
The process units of ammonium hydrogen carbonate provided by the utility model, including for mixing melamine tail gas and mother liquor with shape
The absorber of ammonification carbon solution, for separating melamine tail gas to obtain the ammonia carbon segregative line of the carbon dioxide gas of high-purity
System, for carrying out the reaction crystalizer of carbonization crystallization reaction, and the solid-liquid separator for separating ammonium hydrogen carbonate and mother liquor.Its
In, absorber and ammonia carbon separation system are independent from each other, and the entrance of reaction crystalizer is separately connected absorber and the separation of ammonia carbon
System, in this way, while the ammonia carbon solution in absorber enters reaction crystalizer, the height isolated from ammonia carbon separation system
Purity CO2Gas can also enter in reaction crystalizer, and then carbonization crystallization reaction occurs.Reaction crystalizer connection is separated by solid-liquid separation
Device is carbonized after crystallization reaction, and the solidliquid mixture of ammonium hydrogen carbonate is then flowed out from reaction crystalizer, subsequently into solid-liquid point
From device, to realize the separation of ammonium hydrogen carbonate and mother liquor.
The process units is compared with the existing device with two-stage carbonators, and the carbonization reactor in the utility model is only
For level-one, device technique process shortens, and reduces the investment of device, and operating cost operates also more convenient.
When producing ammonium hydrogen carbonate using process units provided by the utility model, melamine tail gas can use as anti-
Raw material is answered, the CO of available liquefied ammonia and high-purity after melamine tail gas separation2Gas, CO2The purity of gas for example >=
70%, utilize the CO of obtained high-purity2Gas can be directly used for carburizing reagent, meanwhile, in the utility model, use melamine
Tail gas provides ammonia gas source, and for traditional pure ammonia and pure carbon dioxide gas, cost can reduce by 50% or more.
In addition, due to the CO using high-purity2Gas no longer selects carbonators as carbonization gas, reaction crystalizer, inside without pipe
Binding structure, it can thus be avoided the generation of tube body stopping state, extends the cycle of operation of equipment.In addition, in carbonization crystallization process
In, it can be crystallized by circulating repetition, to improve the size of ammonium hydrogen carbonate crystal grain, consequently facilitating point of ammonium hydrogen carbonate and mother liquor
From.
Detailed description of the invention
It, below will be right in order to illustrate more clearly of specific embodiment of the present invention or technical solution in the prior art
Specific embodiment or attached drawing needed to be used in the description of the prior art are briefly described, it should be apparent that, it is described below
In attached drawing be that some embodiments of the utility model are not paying creativeness for those of ordinary skill in the art
Under the premise of labour, it is also possible to obtain other drawings based on these drawings.
Fig. 1 is the production technological process of existing ammonium hydrogen carbonate；
Fig. 2 is a kind of structural schematic diagram of the process units of the ammonium hydrogen carbonate of embodiment of the utility model；
Fig. 3 is a kind of production technological process of the ammonium hydrogen carbonate of embodiment of the utility model.
Icon: 1- absorber；2- ammonia carbon separation system；3- reaction crystalizer；4- solid-liquid separator；The first cooler of 5-；
The second cooler of 6-；7- scrubbing tower；8- intermediate storage tank.
Specific embodiment
The technical solution of the utility model is clearly and completely described below in conjunction with attached drawing, it is clear that described
Embodiment is the utility model a part of the embodiment, instead of all the embodiments.Based on the embodiments of the present invention, originally
Field those of ordinary skill every other embodiment obtained without making creative work belongs to practical
Novel protected range.
It is in the description of the present invention, it should be noted that term " center ", "upper", "lower", "left", "right", " perpendicular
Directly ", the orientation or positional relationship of the instructions such as "horizontal", "inner", "outside" is to be based on the orientation or positional relationship shown in the drawings, and is only
For ease of description the utility model and simplify description, rather than the device or element of indication or suggestion meaning must have it is specific
Orientation, be constructed and operated in a specific orientation, therefore should not be understood as limiting the present invention.
In the description of the present invention, it should be noted that unless otherwise clearly defined and limited, term " is pacified
Dress ", " connected ", " connection " shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or integrally
Connection；It can be mechanical connection, be also possible to be electrically connected；Can be directly connected, can also indirectly connected through an intermediary,
It can be the connection inside two elements.For the ordinary skill in the art, on can understanding as the case may be
State the concrete meaning of term in the present invention.
The utility model provides a kind of process units of ammonium hydrogen carbonate, as shown in Figure 2, comprising:
Absorber 1 is used to form ammonia carbon solution,
Ammonia carbon separation system 2, for the separation of melamine tail gas to obtain the carbon dioxide gas of high-purity,
Reaction crystalizer 3, entrance are separately connected the absorber 1 and the ammonia carbon separation system 2,
Solid-liquid separator 4, entrance connect the outlet of the reaction crystalizer 3.
The process units of ammonium hydrogen carbonate provided by the utility model, including for mixing melamine tail gas and mother liquor with shape
The absorber of ammonification carbon solution, for separating melamine tail gas to obtain the ammonia carbon segregative line of the carbon dioxide gas of high-purity
System, for carrying out the reaction crystalizer of carbonization crystallization reaction, and the solid-liquid separator for separating ammonium hydrogen carbonate and mother liquor.Its
In, absorber and ammonia carbon separation system are independent from each other, and the entrance of reaction crystalizer is separately connected absorber and the separation of ammonia carbon
System, in this way, while the ammonia carbon solution in absorber enters reaction crystalizer, the height isolated from ammonia carbon separation system
Purity CO2Gas can also enter in reaction crystalizer, and then carbonization crystallization reaction occurs.Reaction crystalizer connection is separated by solid-liquid separation
Device is carbonized after crystallization reaction, and the solidliquid mixture of ammonium hydrogen carbonate is then flowed out from reaction crystalizer, subsequently into solid-liquid point
From device, to realize the separation of ammonium hydrogen carbonate and mother liquor.
The process units is compared with the existing device with two-stage carbonators, and the carbonization reactor in the utility model is only
For level-one, device technique process shortens, and reduces the investment of device, and operating cost operates also more convenient.
The process units of ammonium hydrogen carbonate provided by the utility model can be made when in use with the saturated solution of ammonium hydrogen carbonate
It is placed in absorber, and first can be led to a part of melamine tail gas using melamine tail gas as reaction raw materials for mother liquor
Enter in absorber, ammonia and carbon dioxide gas therein form ammonia carbon solution after being dissolved and absorbed by mother liquor, then again by ammonia carbon
Solution is passed through in reaction crystalizer；Meanwhile remainder melamine tail gas being passed through in ammonia carbon separation system and is separated, point
The liquefied ammonia obtained from after is sold as byproduct, and the CO of isolated high-purity2Gas, purity for example >=70%, then
It is passed through in reaction crystalizer and carries out carbonization crystallization reaction with ammonia carbon solution, be carbonized during crystallization reaction, ammonia carbon solution can absorb
CO2Gas is to form ammonium hydrogen carbonate with the ammonia in ammonia carbon solution, and in the state of supersaturation, the ammonium hydrogen carbonate of generation is from ammonia carbon
It crystallizes and is precipitated in solution, obtain the solidliquid mixture of ammonium hydrogen carbonate, solidliquid mixture carries out solid-liquid in solid-liquid separator later
Separation, finally obtains ammonium hydrogen carbonate and the mother liquor for recycling.Absorber in the utility model is, for example, absorption tower.
Using the tail gas during Melamine Production as raw material, cost is 20-40% well below pure ammonia and purity
CO2The cost of gas, cost of material can reduce by 50% or more.
The a large amount of tail gas of by-product in melamine preparation device, 1 ton of melamine of every production just generate 2 tons of tail gas, tail
The main component of gas is NH3And CO2Mixture, for molar ratio in 2:1 or so, it is as follows that melamine generates reaction:
Melamine reaction equation: CO (NH2)2→C3H6N6+6NH3+3CO2
Urea melamine
From in formula it can be seen that reaction after tail gas in NH3And CO2Molar ratio in 2:1.
Ammonium hydrogen carbonate, CO are directly produced using melamine tail gas2Be it is inadequate, the generation reaction equation of ammonium hydrogen carbonate is such as
Under:
The reaction equation of ammonium hydrogen carbonate: NH3+CO2+H2O→NH4HCO3。
The NH that the generation reaction of ammonium hydrogen carbonate needs3And CO2Molar ratio is directly given birth in 1:1, therefore using melamine tail gas
Ammonium hydrogen carbonate is produced, existing process is simultaneously not suitable for, and requires supplementation with external CO2。
When producing ammonium hydrogen carbonate using process units provided by the utility model, melamine tail gas can use as anti-
Raw material is answered, the CO of available liquefied ammonia and high-purity after melamine tail gas separation2Gas utilizes the CO of obtained high-purity2Gas
Body can be directly used for carburizing reagent, meanwhile, in the utility model, ammonia gas source is provided with melamine tail gas, relative to tradition
Pure ammonia and pure carbon dioxide gas for, cost can reduce by 50% or more.In addition, due to the CO using high-purity2Gas
Body no longer selects carbonators as carbonization gas, reaction crystalizer, inside without Pipe bundle structure, it can thus be avoided tube body is stifled
The occurrence of plug, extends the cycle of operation of equipment.In addition, can be crystallized by circulating repetition in carbonization crystallization process, with
The size for improving ammonium hydrogen carbonate crystal grain, consequently facilitating the separation of ammonium hydrogen carbonate and mother liquor.
In the utility model, since the process of carbonization crystallization is carried out in carbonators, relative to traditional vertical
For the carbonators in direction, the reaction crystalizer of the utility model can carry out in arbitrary container, thus in addition to that can obtain
To the ammonium hydrogen carbonate particle of acicular texture, the ammonium hydrogen carbonate particle of any other structure, such as spherical or ellipsoid can also be obtained
Shape etc..
In the utility model, after being separated using ammonia carbon separation system to melamine tail gas, obtained liquefied ammonia can be used as pair
Product is externally sold, obtained CO2Purity >=80% of gas, preferably >=90%, pressure are 0.1~2.0MPa, preferably
0.3~2.0MPa.Purity is higher, and pressure is bigger, can more promote the progress of carburizing reagent, improves reaction efficiency.
High-purity CO2It can achieve 90% or more, CO with the reaction efficiency of ammonia carbon solution2Utilization rate be largely increased,
And the low-purity carbon gas that traditional ammonium hydrogen carbonate production technology uses, reaction efficiency only have about 40% or so, therefore, utilize this
The process units that utility model provides, reaction efficiency greatly improve.
Wherein, ammonia carbon solution refers to that the solution containing ammonium hydrogen carbonate is formed by after absorbing ammonia and carbon dioxide gas
The substance of solution, specific ammonia and carbon dioxide existence form in the solution and generation according to the amount of ammonia and carbon dioxide and
It is fixed, specific restriction is not done in the utility model, because of referred to herein as ammonia carbon solution.
For the process units of the utility model in connection, the liquid inlet of absorber connects external mother liquor supply pipeline, inhales
The gas access for receiving device connects melamine tail gas supply pipeline, the liquid inlet of the outlet connection reaction crystalizer of absorber.
The entrance of ammonia carbon separation system connects melamine tail gas supply pipeline, and the one outlet of ammonia carbon separation system is used for collection liquid
Ammonia, another outlet connection reaction crystalizer, provides CO for reaction crystalizer2Gas.The outlet of reaction crystalizer connects solid-liquid
The entrance of separator.In order to realize that the cycling and reutilization of mother liquor, the liquid outlet of solid-liquid separator can pass through mother liquor supply pipe
Line is connected to the liquid inlet of absorber.
In some embodiments of the utility model, is connected between the absorber 1 and the reaction crystalizer 3
One cooler 5；In the utility model further preferably embodiment, the outlet of first cooler 5 is separately connected suction
The liquid inlet of device 1 and the liquid inlet of reaction crystalizer 3 are received, one in the first cooler 5 can be made by the connection structure
Part ammonia carbon solution is recycled in absorber 1 by pipeline, and remainder ammonia carbon solution enters in reaction crystalizer 3.
Mother liquor ammonia and CO in absorbing melamine tail gas2During, a large amount of heat can be released.In order to make to be carbonized
Reaction temperature in crystallization process controls within the scope of 20~80 DEG C, needs to carry out cooling treatment to the ammonia carbon solution of formation.
For example, the first cooler can be air cooler, cooling treatment is carried out to ammonia carbon solution using air cooler, utilizes air
The heat generated in course of dissolution is taken away, guarantees that the temperature for carrying out the ammonia carbon solution of carbonization crystallization is controlled in 20~80 DEG C of ranges
It is interior.
In this embodiment, the entrance of the first cooler of outlet connection of absorber, the outlet connection of the first cooler
The liquid inlet of reaction crystalizer, alternatively, the outlet of the first cooler is separately connected liquid inlet and the absorption of reaction crystalizer
The liquid inlet of device.Ammonia carbon solution in absorber enters in the first cooler to flow out from the outlet of the first cooler after cooling
Subsequently into reaction crystalizer.Alternatively, when the first cooler is air cooler, outlet stream of the ammonia carbon solution from the first cooler
After out, a part of ammonia carbon cooler enters reaction crystalizer, in another part ammonia carbon solution re-enter absorber.Pass through ammonia
The circulation of carbon solution, can be effectively reduced the temperature of ammonia carbon solution in absorber, to improve mother liquor to ammonia and carbon dioxide
Absorptivity.
In some embodiments of the utility model, the reaction crystalizer 3 is externally connected with the second cooler 6, is used for
The reaction crystalizer 3 is cooled down.
In order to guarantee that the temperature for the liquid being carbonized in crystallization process remains within the scope of 20~80 DEG C, can react
The second cooler of external setting of crystallizer cools down reaction crystalizer, so that liquid in carbonization crystallization process be effectively ensured
Temperature be in controlled range.
In the embodiment, the second cooler cools down to reaction crystalizer by providing cooling medium, for example, can be with
Cooling pipe is arranged in the enclosure interior of reaction crystalizer, to realize the effective temperature-reducing to reaction crystalizer.Cooled
Cheng Zhong, the circulation intake of cooling medium are 10~300 times of mother liquor amount, and the big internal circulating load of cooling medium reduces carbonization knot
The degree of supersaturation of mother liquor during crystalline substance, so that ammonium hydrogen carbonate particle is constantly grown up, so that the size to crystal grain controls.
By the reaction temperature in control carbonization crystallization process, the ammonium hydrogen carbonate formed after carbonization crystallization can control in mother
Solubility in liquid, and then control the grain size of the amount of precipitation of ammonium hydrogen carbonate and obtained ammonium hydrogen carbonate.
In some embodiments of the utility model, the reaction crystalizer is forced circulation reaction crystalizer, such as
OSL reaction crystalizer, the outside of the crystallizer are equipped with circulating pump, and the raw material in reaction crystalizer is under the action of circulating pump from out
Mouth is entered back into reaction crystalizer after flowing out and then secondary response.
Usually by the content of reaction temperature and reaction raw materials in control carbonization crystallization process, to gained ammonium hydrogen carbonate
Crystal grain size regulating degree it is limited, be difficult to obtain 10 μm of diameter or more of ammonium hydrogen carbonate particle and therefore pass through forced circulation
Reaction crystalizer may be implemented repeatedly to recycle carbonization crystallization, it is hereby achieved that the ammonium hydrogen carbonate particle of more big crystal grain size.?
In forced circulation reaction crystalizer, the solidliquid mixture of the ammonium hydrogen carbonate after carbonization crystallization is mixed with ammonia carbon solution again, and
With high-purity CO2Gas is reacted, at this point, the ammonium hydrogen carbonate crystal grain obtained before just exists in the form of crystal seed, carbonization knot
During crystalline substance, ammonium hydrogen carbonate crystal seed is constantly grown up, so as to obtain larger sized ammonium hydrogen carbonate particle.By controlling carbonic acid
The cycle-index of hydrogen ammonium solidliquid mixture, the ammonium hydrogen carbonate particle of available different-grain diameter.
In some embodiments of the utility model, the gas vent of the reaction crystalizer 3 connects scrubbing tower 7.
The tail gas generated from reaction crystalizer after carbonization crystallization reaction enters scrubbing tower and is washed, carrying out washing treatment
Externally discharge afterwards, for gained liquid as mother liquid recycling, washing medium used in carrying out washing treatment can be desalted water.Through washing
After washing, the content of the ammonia in the gas of discharge is lower than 50ppm.Since the tail gas scale of construction generated in carbonization crystallization process is less, only
The content of the ammonia in the gas for making discharge can be reached by once washing lower than 50ppm, and after carrying out washing treatment, row
The gas flow put can be reduced to the 20% of traditional handicraft hereinafter, can greatly reduce the influence to environment.And traditional production dress
In setting, after carburizing reagent, the content of the ammonia in tail gas is higher, it is therefore desirable to be arranged two-stage wash mill to tail gas into
Row washing, compared with traditional two-stage wash mill, in the process units of the utility model, due to ammonia absorption carburizing reagent compared with
To be thorough, the ammonia content in the tail gas of generation is just few, therefore in the utility model, first grade scrubber only need to be arranged, simplifies
Device, while effectively shortening process flow.
In order to realize the recycling of cleaning solution, in the utility model further embodiment, the scrubbing tower 7
Liquid outlet connects the absorber 1.In the utility model further embodiment, the liquid discharge of the scrubbing tower 7
Mouth connects the absorber 1 through intermediate storage tank 8.By the setting structure, the cleaning solution that ammonia is absorbed after washing can be used as mother
Liquid is utilized again.And intermediate storage tank 8 both can be used as buffer reservoir, it can also be in the preparation place as mother liquor.
In some embodiments of the utility model, the solid-liquid separator is cyclone.
In some applicable cases, the subsequent reactions of ammonium hydrogen carbonate do not need ammonium hydrogen carbonate solid or ammonium hydrogen carbonate is molten
Liquid, it is desirable that the ammonium hydrogen carbonate with certain solid-to-liquid ratio solidliquid mixture, therefore, using cyclone as be separated by solid-liquid separation
Device can isolate partially liq to use as Recycling Mother Solution, and remainder is the solid-liquid mixing of obtained ammonium hydrogen carbonate
Object；Meanwhile the solid-to-liquid ratio for the solidliquid mixture isolated can also be accurately controlled using the separation method.The liquid isolated can
To continue to absorb NH as mother liquor3And CO2.During producing ammonium hydrogen carbonate using the entire process units of the utility model, liquid
Body recycles completely, non-wastewater discharge.
In the embodiment, the solidliquid mixture for the ammonium hydrogen carbonate that reaction generates in reaction crystalizer enters cyclone,
The separation of liquid is carried out in cyclone, cyclone top is provided with liquid outlet, and lower part is arranged solidliquid mixture and exports, passes through
The liquid outlet quantity for controlling liquid, can accurately control the solid-to-liquid ratio of solidliquid mixture.The liquid that cyclone apex comes out passes through bus
Supply pipeline is connected to the liquid inlet of absorber, continues to absorb NH3And CO2。
In order to realize the recycling of mother liquor, in the utility model further embodiment, the liquid of solid-liquid separator 4
Body outlet connection absorber 1.In the utility model further embodiment, in the liquid outlet warp of solid-liquid separator 4
Between storage tank 8 connect absorber 1.By the setting structure, the mother liquor obtained after separation of solid and liquid can be utilized again.And it is intermediate
Storage tank 8 both can be used as buffer reservoir, can also prepare place as the intermediate of mother liquor.
Using the process flow chart of process units provided by the utility model production ammonium hydrogencarbonate as shown in figure 3, the production
Using the saturated solution of ammonium hydrogen carbonate as mother liquor in technique, using melamine tail gas as reaction raw materials, specifically, the production technology
The following steps are included:
S1 150,000 tons of ammonium hydrogen carbonate devices) are produced per year, using the tail gas of 100,000 tons of melamine plants as raw material, melamine dress
The main component in tail gas set is the mixture of NH3 and CO2, and molar ratio is in 2:1 or so；
For the cost of material compared with existing pure ammonia and low concentration carbon gas, cost can reduce by 60%；
S2 100,000 tons of melamine tail gas) are divided into two parts, about 50,000 tons of a part is passed through absorber, is inhaled by mother liquor
Harvest is the ammonia carbon solution for being greater than 15% containing ammonia density；
A large amount of heat is discharged in reaction, absorber is connected to the air cooler of the first cooler, will dissolve using air
The torrid zone is walked, and after air cooler is cooling, a part returns and carries out cyclic absorption in absorber the ammonia carbon solution of absorber, another
It is sent into reaction crystalizer after part ammonia carbon solution is cooling and carries out carbonization crystallization reaction；
S3 50,000 tons of other melamine tail gas) are sent into ammonia carbon separation system, carry out point of ammonia and carbon dioxide gas
From；
Ammonia carbon separation system is completely separable by ammonia and carbon dioxide gas by the way of multistage rectification, ammonia warp therein
After supercooling or compression, available oil-free high purity liquid ammonia, the byproduct as the present apparatus is sold；Ammonia carbon separation system
The CO isolated2Gas is the high-purity CO that pressure is 2.0MPa2, purity reaches 99% or more；
S4) the high-purity CO that the ammonia carbon solution from absorber and ammonia carbon separation system generate2Gas enters reactive crystallization
Carbonization crystallization reaction is carried out in device；
The problem of reaction crystalizer is forced circulation reaction crystalizer, internal without heat-exchanging tube bundle, and fouling is not present；Carbonization knot
The external setting circulation pipe and the second cooler, the internal circulating load of cooling medium of brilliant device are 200 times of mother liquor amount, big cooling medium
Internal circulating load reduces the degree of supersaturation inside reaction crystalizer so that crystal is constantly grown up, crystalline particle can according to need into
Row control；
It is controlled by the cooling reaction temperature made in reaction crystalizer at 40 DEG C, high-purity CO2Gas and ammonia carbon solution
Reaction efficiency can achieve 92%, CO2The utilization rate of gas is largely increased；The tail gas amount of reaction crystalizer discharge is reduced,
The influence to environment is greatly reduced, by circulation crystallization, the particle balling preparation shape of obtained ammonium hydrogen carbonate, granularity is at 80 microns
More than；
S5) main component of the tail gas generated in reaction crystalizer is CO2With a small amount of NH3, which is passed through scrubbing tower
Middle recycling NH therein3And CO2, washing medium is desalted water, and ammonia content is lower than 50ppm in the tail gas after washing；Absorber absorbs
NH3And CO2The liquid generated afterwards can be used as mother liquor and be back to absorber, continue to absorb NH3And CO2；
S6) solidliquid mixture that the reaction of carburizing reagent crystallizer generates is the mixing of ammonium hydrogen carbonate solid and its saturated solution
Object enters cyclone after reaction crystalizer outflow, the separation of liquid is carried out in cyclone, cyclone top is provided with liquid
Body outlet, lower part are arranged solidliquid mixture and export, and by controlling liquid outlet quantity, accurately control the solid-to-liquid ratio of solidliquid mixture
50%；
The clear liquid that cyclone apex comes out returns to absorber as mother liquor, continues to absorb NH3And CO2。
In the production method, liquid recycles completely, non-wastewater discharge.
Finally, it should be noted that the above various embodiments is only to illustrate the technical solution of the utility model, rather than it is limited
System；Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art should
Understand: it is still possible to modify the technical solutions described in the foregoing embodiments, or to some or all of
Technical characteristic is equivalently replaced；And these are modified or replaceed, it does not separate the essence of the corresponding technical solution, and this is practical new
The range of each embodiment technical solution of type.
Claims (10)
1. a kind of process units of ammonium hydrogen carbonate characterized by comprising
Absorber is used to form ammonia carbon solution,
Ammonia carbon separation system, for the separation of melamine tail gas to obtain the carbon dioxide gas of high-purity,
Reaction crystalizer, entrance are separately connected the absorber and the ammonia carbon separation system,
Solid-liquid separator, entrance connect the outlet of the reaction crystalizer.
2. process units according to claim 1, which is characterized in that connect between the absorber and the reaction crystalizer
It is connected to the first cooler.
3. process units according to claim 2, which is characterized in that the outlet of first cooler is separately connected absorption
The liquid inlet of the liquid inlet of device and the reaction crystalizer.
4. process units according to claim 2, which is characterized in that it is cooling that the reaction crystalizer is externally connected with second
Device, for being cooled down to the reaction crystalizer.
5. process units according to claim 1-4, which is characterized in that the reaction crystalizer is forced circulation
Reaction crystalizer.
6. process units according to claim 5, which is characterized in that the gas vent of the reaction crystalizer connects washing
The liquid outlet of tower, the scrubbing tower connects the absorber.
7. process units according to claim 6, which is characterized in that the liquid outlet of the scrubbing tower connects through intermediate storage tank
Connect the absorber.
8. process units according to claim 1-4, which is characterized in that the solid-liquid separator is cyclone.
9. process units according to claim 8, which is characterized in that described in the liquid outlet connection of the solid-liquid separator
Absorber.
10. process units according to claim 9, which is characterized in that the liquid outlet of the solid-liquid separator is through centre
Storage tank connects the absorber.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201822112822.5U CN209322481U (en) | 2018-12-14 | 2018-12-14 | The process units of ammonium hydrogen carbonate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201822112822.5U CN209322481U (en) | 2018-12-14 | 2018-12-14 | The process units of ammonium hydrogen carbonate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN209322481U true CN209322481U (en) | 2019-08-30 |
Family
ID=67726936
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201822112822.5U Active CN209322481U (en) | 2018-12-14 | 2018-12-14 | The process units of ammonium hydrogen carbonate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN209322481U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109467105A (en) * | 2018-12-14 | 2019-03-15 | 四川金象赛瑞化工股份有限公司 | The production method and process units of ammonium hydrogen carbonate |
| CN110642268A (en) * | 2019-09-30 | 2020-01-03 | 安徽金禾实业股份有限公司 | Ammonium bicarbonate carbonization system |
-
2018
- 2018-12-14 CN CN201822112822.5U patent/CN209322481U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109467105A (en) * | 2018-12-14 | 2019-03-15 | 四川金象赛瑞化工股份有限公司 | The production method and process units of ammonium hydrogen carbonate |
| CN110642268A (en) * | 2019-09-30 | 2020-01-03 | 安徽金禾实业股份有限公司 | Ammonium bicarbonate carbonization system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106315625B (en) | The method of the high-purity monohydrate lithium hydroxide of laminating production, pure Lithium Carbonate and battery-level lithium carbonate | |
| US8470055B2 (en) | Combined process for preparing calcined soda by applying surface engineering technology to natural soda preparation | |
| JP5676050B2 (en) | Energy saving capital saving vapor phase ching method melamine production system and method | |
| CN209322481U (en) | The process units of ammonium hydrogen carbonate | |
| CN105271347B (en) | Method for preparing high-purity barium salt by using witherite-barytocalcite industrial waste residues | |
| CN109534365B (en) | Cyclic manufacturing method for co-production of sodium bicarbonate and ammonium chloride | |
| CN102502708B (en) | Preparation method for preparing alkali metal or alkali earth metal cyanide with high purity and high yield | |
| CN109467105A (en) | The production method and process units of ammonium hydrogen carbonate | |
| CN101269825A (en) | 'Non-combined-soda process' production process for producing soda, ammonium chloride with melamine tail gas | |
| CN108862332A (en) | Carbonate preparation method of the crystallizer and application thereof with sodium bicarbonate | |
| CN108726542A (en) | The production method and production equipment of sodium bicarbonate | |
| CN102205204B (en) | Wet ammonia desulfurization concentration process of cold and hot state discharge | |
| CN209188467U (en) | A kind of device for sealing carbon dioxide in flue gas up for safekeeping using rich magnesium mineral | |
| CN103303946B (en) | Sodium bicarbonate crystal preparation equipment and process for preparing sodium bicarbonate crystals by utilizing same | |
| CN112516616A (en) | Crystallization device and method for purifying ethylene carbonate | |
| CN103755393B (en) | Device and method for co-producing potassium sulphate compound fertilizer from tripolycyanamide tail gas | |
| CN108751233A (en) | A method of improving sodium bicarbonate grain size number | |
| CN206328142U (en) | A kind of preparation system of anhydrous hydrogen chloride | |
| CN208732632U (en) | The production equipment of sodium bicarbonate | |
| CN209333718U (en) | A kind of ammonium hydrogen carbonate carbonizing plant | |
| CN205340200U (en) | Melamine fluidized bed crystallizer | |
| CN2868987Y (en) | Carbonizing tower for preparing sodium hydrogen carbonate | |
| CN110947201A (en) | Gas-liquid absorption type crystallization granulation equipment | |
| CN205773387U (en) | Ammonium carbonate process units | |
| CN105776248B (en) | Ammonium carbonate process units and its production method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |