CN219861239U - Coke oven gas deamination system for producing large-particle ammonium sulfate - Google Patents
Coke oven gas deamination system for producing large-particle ammonium sulfate Download PDFInfo
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- CN219861239U CN219861239U CN202321010530.5U CN202321010530U CN219861239U CN 219861239 U CN219861239 U CN 219861239U CN 202321010530 U CN202321010530 U CN 202321010530U CN 219861239 U CN219861239 U CN 219861239U
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- 229910052921 ammonium sulfate Inorganic materials 0.000 title claims abstract description 116
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 title claims abstract description 112
- 235000011130 ammonium sulphate Nutrition 0.000 title claims abstract description 111
- 239000000571 coke Substances 0.000 title claims abstract description 35
- 239000002245 particle Substances 0.000 title claims abstract description 29
- 230000009615 deamination Effects 0.000 title claims abstract description 28
- 238000006481 deamination reaction Methods 0.000 title claims abstract description 28
- 239000012452 mother liquor Substances 0.000 claims abstract description 203
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 161
- 238000010438 heat treatment Methods 0.000 claims abstract description 148
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 108
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 80
- 238000010521 absorption reaction Methods 0.000 claims abstract description 60
- 238000002425 crystallisation Methods 0.000 claims abstract description 26
- 230000008025 crystallization Effects 0.000 claims abstract description 26
- 238000003860 storage Methods 0.000 claims abstract description 15
- 230000001105 regulatory effect Effects 0.000 claims description 38
- 238000005259 measurement Methods 0.000 claims description 24
- 238000000034 method Methods 0.000 claims description 21
- 239000007788 liquid Substances 0.000 claims description 18
- 238000011144 upstream manufacturing Methods 0.000 claims description 15
- 239000010413 mother solution Substances 0.000 claims description 12
- 238000005485 electric heating Methods 0.000 claims description 8
- 239000003595 mist Substances 0.000 claims description 6
- 238000005554 pickling Methods 0.000 claims description 5
- 239000013078 crystal Substances 0.000 abstract description 49
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 24
- 230000002195 synergetic effect Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 158
- 230000008569 process Effects 0.000 description 15
- 239000000047 product Substances 0.000 description 12
- 239000003034 coal gas Substances 0.000 description 10
- 230000015572 biosynthetic process Effects 0.000 description 5
- 230000001276 controlling effect Effects 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 230000005611 electricity Effects 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 238000010899 nucleation Methods 0.000 description 2
- 230000006911 nucleation Effects 0.000 description 2
- 238000013021 overheating Methods 0.000 description 2
- 238000010903 primary nucleation Methods 0.000 description 2
- 238000010900 secondary nucleation Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
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Abstract
The utility model relates to a coke oven gas deamination system for producing large-particle ammonium sulfate, which comprises an ammonia absorption system, a sulfuric acid overhead tank, a full flow tank, a mother liquor storage tank, a crystallization pump, a large mother liquor circulating pump and a small mother liquor pump; the system also comprises a gas heating system, a mother liquor heating system, an acidity control system and a heat control system; the water content, solubility and acidity of the mother liquor are adjusted through the synergistic effect of a gas heating system, an ammonia absorption system, a fine crystal eliminating system, a heat control system and an acidity control system, the growth speed of ammonium sulfate crystals is controlled, the generation amount of crystal nucleus is reduced, and then a large-particle ammonium sulfate product is obtained; the utility model realizes the purpose of producing large-particle ammonium sulfate and improves the economic added value of ammonium sulfate products.
Description
Technical Field
The utility model relates to the technical field of deamination of coke oven gas, in particular to a deamination system of coke oven gas for producing large-particle ammonium sulfate.
Background
During the coking process, nitrogen in the coal is partially converted into ammonia and enters a coke oven gas system,usually the ammonia content in the raw gas is 6-9 g/m 3 . Ammonia, which is a corrosive medium and a valuable chemical raw material, must be removed from coke oven gas. From the point of view of recycling ammonia resources, can be used for preparing ammonium sulfate and anhydrous ammonia products. In particular, sulfuric acid is used for absorbing ammonia in coke oven gas, the absorption driving force is large, no reversible reaction exists, and compared with other processes, the ammonia content in the clean gas is the lowest. Meanwhile, the ammonium sulfate is a solid product, is easy to store and transport, is suitable for continuous and large-scale production, and is particularly suitable for removing ammonia in coke oven gas.
The ammonia in the coke oven gas is utilized to produce ammonium sulfate, which is an absorption and crystallization process, the quality of the absorption process determines the ammonia content in the clean gas, and the quality of the crystallization process directly determines the quality of the ammonium sulfate product. Ammonium sulfate crystallization consists essentially of several stages of supersaturated solution formation, nucleation and crystal growth. The ammonium sulfate slurry forms supersaturated solution, and solid-phase microscopic grains are precipitated after reaching a certain supersaturation degree, which is a crystal nucleus forming process and is also called primary nucleation; this is followed by a growth process, also known as crystal growth, of the nuclei. Meanwhile, new crystal nuclei are generated due to the flow of crystal liquid, friction and collision between crystals and equipment, and scouring of the surfaces of the crystals by the liquid, and are called secondary nucleation. Usually, the formation of crystal nuclei and the growth of crystals are performed simultaneously. During crystallization, the solute in the solution is consumed, whether the crystal nucleus is formed or grown; namely, a certain supersaturation degree is used as a driving force. Each crystal is formed by growing a crystal nucleus, under certain conditions, the larger the nucleation rate of the crystal nucleus is, the more the crystal nucleus is generated, and the lower the growth rate of the crystal nucleus is, the larger the crystal nucleus is, so that a large amount of fine crystals are caused because a limited solute in the solution is required to simultaneously supply a large amount of crystal nuclei for growth; on the other hand, the smaller the amount of crystal nuclei formed, the larger the grain size. Therefore, to obtain a large-particle ammonium sulfate product, the formation process of primary nucleation and secondary nucleation is controlled to avoid the formation of excessive crystal nuclei. The common technological means are as follows: reducing impurities (such as dust, ions, etc.) in the system, adjusting supersaturation degree of mother liquor (controlling temperature and acidity), etc.
The reduction of impurities (e.g., dust, ions, etc.) within the system can be achieved by optimizing the operation of the upstream unit. And the supersaturation degree is adjusted by considering various factors such as temperature, acidity and the like, so that the realization is relatively complex. The Chinese patent application with publication number of CN114772611A discloses a production system and a method for preparing ammonium sulfate from ammonia-containing gas, which have the advantages of reducing power energy consumption, facilitating the leakage of mother liquor and scaling of a spraying device by stirring the mother liquor by heated compressed air, being beneficial to the formation of concentration gradient to a certain extent, but being only aimed at a non-gas system, the process is not suitable for producing ammonium sulfate from coke oven gas. The Chinese patent with the publication number of CN216837850U discloses a coke oven gas ammonia removal system, which comprises a gas preheater, a spray saturator, a cyclone plate mist catcher, a mother liquor circulating pump and the like, and the system is simple and can not control the temperature, acidity and other key parameters of the mother liquor, so that the quality of the obtained ammonium sulfate product can not be ensured. The Chinese patent publication No. CN216571638U discloses a coking ammonium sulfate production control system, which is characterized in that a full-flow tank regulating valve is arranged in a pipeline connected with a liquid level balance pump and a full-flow tank, and an acid adding regulating valve is arranged in a pipeline connected with a sulfuric acid overhead tank and the full-flow tank, and the acidity of a mother solution is continuously detected, so that the acid adding amount is automatically regulated, the defect of manual detection is avoided, the development of the automation of the ammonium sulfate system production is promoted, and the quality of the mother solution cannot be controlled.
Disclosure of Invention
The utility model provides a coke oven gas deamination system for producing large-particle ammonium sulfate, which realizes the purpose of producing large-particle ammonium sulfate and improves the economic added value of ammonium sulfate products through the synergistic effect of a gas heating system, an ammonia absorption system, a fine crystal elimination system, a heat control system and an acidity control system.
In order to achieve the above purpose, the utility model is realized by adopting the following technical scheme:
a coke oven gas deamination system for producing large-particle ammonium sulfate comprises an ammonia absorption system, a sulfuric acid overhead tank, a full flow tank, a mother liquor storage tank, a crystallization pump, a large mother liquor circulating pump and a small mother liquor pump; the gas inlet of the ammonia absorption system is connected with a coke oven gas pipeline through a gas inlet pipeline, and a gas inlet valve is arranged on the gas inlet pipeline; the gas outlet of the ammonia absorption system is connected with a deamination gas pipeline through a gas outlet pipeline, and a mist catcher, a gas outlet valve and a liquid discharge funnel are sequentially arranged on the gas outlet pipeline along the gas flowing direction, and the liquid discharge funnel is connected with a gas liquid seal groove; the gas outlet pipeline is connected with the gas inlet pipeline through a traffic pipe, and a traffic valve is arranged on the traffic pipe; the sulfuric acid outlet of the sulfuric acid overhead tank is connected with the sulfuric acid inlet of the mother solution storage tank through a sulfuric acid outlet pipeline; the ammonium sulfate mother liquor outlet of the mother liquor storage tank is connected with the ammonium sulfate mother liquor inlet of the ammonia absorption system through an ammonium sulfate mother liquor pipeline, and a small mother liquor pump and a flow regulating valve are sequentially arranged on the ammonium sulfate mother liquor pipeline along the flow direction of the ammonium sulfate mother liquor; the small mother liquid pump and the flow regulating valve are controlled in an interlocking way; the ammonium sulfate outlet of the ammonia absorption system is connected with a full flow groove through an ammonium sulfate outlet pipeline, and the full flow groove is connected with a mother liquor storage tank through a full flow mother liquor pipeline; the ammonia absorption system is provided with a circulating mother liquor outlet I which is connected with a circulating mother liquor inlet of the ammonia absorption system through a circulating mother liquor pipeline, and a large mother liquor circulating pump is arranged on the circulating mother liquor pipeline; the crystallization-containing mother liquor outlet of the ammonia absorption system is connected with a crystallization-containing mother liquor delivery pipeline, and a crystallization pump is arranged on the crystallization-containing mother liquor delivery pipeline; the coke oven gas deamination system also comprises a gas heating system, a mother liquor heating system, an acidity control system and a heat control system; the gas heating system is arranged on the gas inlet pipeline; the ammonia absorption system is provided with a circulating mother liquor outlet which is connected with a circulating mother liquor pipeline at the upstream of the large mother liquor circulating pump through a heating circulating mother liquor pipeline; a mother liquor heating system is arranged on the heating circulating mother liquor pipeline; the acidity control system comprises an acidity measurement module, a sulfuric acid regulating valve and an observation mirror; the acidity measurement module is arranged in the ammonia absorption system and is used for detecting the acidity of the ammonium sulfate mother liquor; the sulfuric acid high-level tank is provided with an adjusting sulfuric acid outlet which is respectively connected with an ammonium sulfate outlet pipeline and a circulating mother liquor pipeline at the upstream of the large mother liquor circulating pump through adjusting sulfuric acid pipelines; a sulfuric acid regulating valve and an observation mirror are arranged on the sulfuric acid regulating pipeline; the acidity measurement module is controlled by interlocking with a sulfuric acid regulating valve; and the gas heating system and the mother liquor heating system are connected with the corresponding heat control systems.
Further, the heat control system consists of a heat regulating valve, an input parameter measuring module, an output parameter measuring module, a heat operation module and a heat control module; the heat regulating valve is respectively arranged on a heat input pipeline of the gas heating system and a heat input pipeline of the mother liquor heating system; input parameter measurement modules are respectively arranged on a gas inlet pipeline at the upstream of the gas heating system and a heating circulating mother liquor pipeline at the upstream of the mother liquor heating system, and output parameter measurement modules are respectively arranged on the gas inlet pipeline at the downstream of the gas heating system and the heating circulating mother liquor pipeline at the downstream of the mother liquor heating system; the control end of the heat control valve, the input parameter measuring module, the output parameter measuring module and the heat operation module are respectively connected with the heat control module.
Further, the gas heating system is a steam heating system, an electric heating system or a microwave heating system.
Further, the ammonia absorption system is a saturator or a pickling tower.
Further, the mother liquor heating system is a steam heating system, an electric heating system or a microwave heating system.
Compared with the prior art, the utility model has the beneficial effects that:
1) The water content, the solubility and the acidity of the ammonium sulfate mother liquor are cooperatively regulated, the growth speed of ammonium sulfate crystals is controlled, and the generation amount of crystal nucleus is minimized, so that large-particle ammonium sulfate crystals are obtained;
2) Setting a gas heating system, a mother liquor heating system, a heat control system, an acidity control system and an ammonia absorption system to cooperatively operate; the gas heating system is used for heating gas to be deaminated, the ammonia absorption system is used for absorbing ammonia in the gas, the mother liquor heating system is used for removing fine crystals in the ammonium sulfate mother liquor, the heat control system is used for precisely adjusting the heat of the gas heating system and the mother liquor heating system, and the acidity control system is used for controlling the acidity of the ammonium sulfate mother liquor; the control is accurate, and the degree of automation is high;
3) The grain diameter of the obtained ammonium sulfate product ranges from 400 mu m to 3000 mu m, thereby meeting the requirement of producing large-grain ammonium sulfate products and improving the economic added value of the ammonium sulfate products.
Drawings
FIG. 1 is a schematic structural view of a coke oven gas deamination system of the present utility model.
In the figure: 1. the system comprises a gas inlet valve 2, a gas outlet valve 3, a traffic valve 4, a liquid discharge hopper 5, a gas liquid seal tank 6, a mist catcher 7, an ammonia absorption system 8, a gas heating system 9, a mother liquor heating system 10, a heat control system 11, an input parameter measuring module 12, an output parameter measuring module 13, a heat calculating module 14, a heat control module 15, a heat regulating valve 16, an acidity control system 17, an acidity measuring module 18, a sulfuric acid high-level tank 19, a sulfuric acid regulating valve 20, a sight glass 21, a large mother liquor circulating pump 22, a crystallization pump 23, a small mother liquor pump 24, a flow regulating valve 25, a full flow tank 26, a mother liquor storage tank 27 and a slag box
Detailed Description
The following is a further description of embodiments of the utility model, taken in conjunction with the accompanying drawings:
as shown in FIG. 1, the coke oven gas deamination system for producing large-particle ammonium sulfate comprises an ammonia absorption system 7, a sulfuric acid overhead tank 18, a full flow tank 25, a mother solution storage tank 26, a crystallization pump 22, a large mother solution circulating pump 21 and a small mother solution pump 23; the gas inlet of the ammonia absorption system 7 is connected with a coke oven gas pipeline through a gas inlet pipeline, and a gas inlet valve 1 is arranged on the gas inlet pipeline; the gas outlet of the ammonia absorption system 7 is connected with a deamination gas pipeline through a gas outlet pipeline, a mist catcher 6, a gas outlet valve 2 and a liquid discharge funnel 4 are sequentially arranged on the gas outlet pipeline along the gas flowing direction, and the liquid discharge funnel 4 is connected with a gas liquid seal groove 5; the gas outlet pipeline is connected with the gas inlet pipeline through a traffic pipe, and a traffic valve 3 is arranged on the traffic pipe; the sulfuric acid outlet of the sulfuric acid overhead tank 18 is connected with the sulfuric acid inlet of the mother liquor storage tank 26 through a sulfuric acid outlet pipeline; the ammonium sulfate mother liquor outlet of the mother liquor storage tank 26 is connected with the ammonium sulfate mother liquor inlet of the ammonia absorption system 7 through an ammonium sulfate mother liquor pipeline, and a small mother liquor pump 23 and a flow regulating valve 24 are sequentially arranged on the ammonium sulfate mother liquor pipeline along the flow direction of the ammonium sulfate mother liquor; the small mother liquor pump 23 is controlled in an interlocking way with the flow regulating valve 24; the ammonium sulfate outlet of the ammonia absorption system 7 is connected with a full flow groove 25 through an ammonium sulfate outlet pipeline, and the full flow groove 25 is connected with a mother liquor storage tank 26 through a full flow mother liquor pipeline; the ammonia absorption system 7 is provided with a circulating mother liquor outlet I which is connected with a circulating mother liquor inlet of the ammonia absorption system 7 through a circulating mother liquor pipeline, and a large mother liquor circulating pump 21 is arranged on the circulating mother liquor pipeline; the crystallization-containing mother liquor outlet of the ammonia absorption system 7 is connected with a crystallization-containing mother liquor delivery pipeline, and a crystallization pump 22 is arranged on the crystallization-containing mother liquor delivery pipeline; the coke oven gas deamination system also comprises a gas heating system 8, a mother liquor heating system 9, an acidity control system 16 and a heat control system 10; the gas heating system 8 is arranged on the gas inlet pipeline; the ammonia absorption system 7 is provided with a circulating mother liquor outlet which is connected with a circulating mother liquor pipeline at the upstream of the large mother liquor circulating pump 21 through a heating circulating mother liquor pipeline; a mother liquor heating system 9 is arranged on the heating circulation mother liquor pipeline; the acidity control system 16 comprises an acidity measurement module 17, a sulfuric acid regulating valve 19 and an observation mirror 20; the acidity measuring module 17 is arranged in the ammonia absorption system 7 and is used for detecting the acidity of the ammonium sulfate mother liquor; the sulfuric acid overhead tank 18 is provided with an adjusting sulfuric acid outlet which is respectively connected with an ammonium sulfate outlet pipeline and a circulating mother liquor pipeline at the upstream of the large mother liquor circulating pump 21 through adjusting sulfuric acid pipelines; a sulfuric acid regulating valve 19 and an observation mirror 20 are arranged on the sulfuric acid regulating pipeline; the acidity measurement module 17 is controlled in an interlocking way with the sulfuric acid regulating valve 19; the gas heating system 8 and the mother liquor heating system 9 are connected with corresponding heat control systems 10.
The heat control system 10 consists of a heat regulating valve 15, an input parameter measuring module 11, an output parameter measuring module 12, a heat computing module 13 and a heat control module 14; the heat regulating valve 15 is respectively arranged on the heat input pipeline of the gas heating system 8 and the heat input pipeline of the mother liquor heating system 9; input parameter measurement modules 11 are respectively arranged on a gas inlet pipeline at the upstream of the gas heating system 8 and a heating circulation mother liquor pipeline at the upstream of the mother liquor heating system 9, and output parameter measurement modules 12 are respectively arranged on the gas inlet pipeline at the downstream of the gas heating system 8 and the heating circulation mother liquor pipeline at the downstream of the mother liquor heating system 9; the control end of the heat control valve 15, the input parameter measuring module 11, the output parameter measuring module 12 and the heat operation module 13 are respectively connected with the heat control module 14.
Further, the gas heating system 8 is a steam heating system, an electric heating system or a microwave heating system.
Further, the ammonia absorption system 7 is a saturator or a pickling tower.
Further, the mother liquor heating system 9 is a steam heating system, an electric heating system or a microwave heating system.
According to the coke oven gas deamination system for producing large-particle ammonium sulfate, disclosed by the utility model, the crystal growth speed of ammonium sulfate is controlled by cooperatively adjusting the water content, the solubility and the acidity of mother liquor, so that the crystal nucleus generation amount is reduced, and a large-particle ammonium sulfate product is further obtained; the process comprises the following steps:
1) When the temperature of the inlet gas is lower than 40 ℃, a gas heating system 8 is started, the gas is heated to 40-65 ℃, and the water content in the ammonium sulfate mother liquor is controlled by controlling the temperature of the gas; this step is omitted when the outlet gas temperature is higher than 65 ℃;
2) The heated gas enters an ammonia absorption system 7, sulfuric acid reacts with ammonia in the gas to generate ammonium sulfate, and the ammonia content in the gas after ammonia absorption by sulfuric acid is lower than 30mg/Nm 3 ；
3) Heating the ammonium sulfate mother liquor through a mother liquor heating system 9 to form a local overheating zone, controlling the solubility of the ammonium sulfate mother liquor and eliminating fine crystals;
4) The acidity of the ammonium sulfate mother liquor is controlled to be within the range of 2% -6% by an acidity control system 10;
5) The heat of the gas heating system 8 and the mother liquor heating system 9 is accurately regulated through the heat control system 10; the heat control system 10 comprises an input parameter measurement module 11, an output parameter measurement module 12, a heat operation module 13 and a heat control module 14; the variables measured by the input parameter measurement module 11 include: inlet temperature T of gas/ammonium sulfate mother liquor in Inlet flow q of gas/ammonium sulfate mother liquor in The method comprises the steps of carrying out a first treatment on the surface of the Variables measured by the output parameter measurement module 12 include: outlet temperature T of gas/ammonium sulfate mother liquor out Outlet flow q of gas/ammonium sulfate mother liquor out The method comprises the steps of carrying out a first treatment on the surface of the The heat calculation module 13 calculates the input heat Q of the gas heating system 8/mother liquor heating system 9 according to the actual measurement values returned by the input parameter measurement module 11 and the output parameter measurement module 12 in Output heat Q of gas heating system 8/mother liquor heating system 9 out Gas heating system 8/mother liquor heatingThe system 9 supplements heat QD, and the calculation formula is:
Q in ＝C in q in T in ；C in specific heat for inputting coal gas/ammonium sulfate mother liquor;
Q out ＝C out q out T out ；C out specific heat for outputting coal gas/ammonium sulfate mother liquor;
QD＝Q out -Q in 。
the particle size of the obtained large-particle ammonium sulfate ranges from 400 μm to 3000 μm.
The heating mode of the gas heating system 8 is steam heating, electric heating or microwave heating.
The process of absorbing ammonia by sulfuric acid is carried out in a saturator or a pickling tower.
The heating mode of the ammonium sulfate mother liquor is steam heating, electric heating or microwave heating; the mother liquor heating system 9 adopts an intermittent operation mode, and when the proportion of fine crystals with the particle size of less than 2mm reaches 35%, the mother liquor heating system 9 is started; after the mother liquor heating system is started, when the proportion of fine crystals with the particle size of less than 2mm is less than 30%, the mother liquor heating system 9 is turned off.
When the mother liquor heating system 9 stops running, the heat control system 10 automatically increases the heat supply of the gas heating system 8 according to a preset value; conversely, when the mother liquor heating system 9 is put into operation, the heat control system 10 automatically reduces the heat supply of the gas heating system 8.
The water quantity of the coal gas carried out from the ammonia absorption system 7 is equal to the water quantity carried by the coal gas, the water quantity carried by other gases, the water quantity carried by sulfuric acid, the water quantity carried by a centrifugal machine, the water quantity carried by a tail gas cleaning tower and the water quantity carried by the ammonium sulfate after the centrifugal machine.
The heat quantity fed into the gas heating system 8 by the heat control system 10 is QDg, and the heat quantity fed into the mother liquor heating system 9 is QDc; total heat added Σq= QDg + QDc, i.e. total heat added = gas carry-over heat + wet ammonium sulfate carry-over heat + mother liquor carry-over heat of crystallization tank + heat loss in saturator/pickling tower-gas carry-over heat-other gas carry-over heat-sulfuric acid dilution heat-washing water carry-over heat-return mother liquor carry-over heat-ammonium sulfate generation heat-ammonium sulfate crystallization heat. The utility model discloses a coke oven gas deamination system for producing large-particle ammonium sulfate, which consists of a gas heating system, an ammonia absorption system, a mother solution heating system, a heat control system and an acidity control system, and achieves the aim of producing large-particle ammonium sulfate through the cooperative operation of the 5 systems.
1. A gas heating system;
the coke oven gas (abbreviated as gas) is heated to 40-65 ℃ by means of steam, electricity or microwaves, and the water content in the ammonium sulfate mother liquor is controlled by utilizing the property that the heated gas can carry more water vapor. In order to ensure the normal operation of the deamination process, the coke oven gas deamination system needs to work continuously. When the temperature of inlet gas is lower than 40 ℃ in the beginning of working, a gas heating system is required to be started; when the temperature of the outlet gas is higher than 65 ℃, the gas heating system is closed in an interlocking way.
2. An ammonia absorption system;
the ammonia in the gas is absorbed by the chemical reaction of sulfuric acid and ammonia, so as to achieve the purpose of removing ammonia from the gas. The ammonia content in the absorbed gas is lower than 30mg/Nm 3 ；
3. A mother liquor heating system;
the circulating mother liquor is heated by means of steam, electricity or microwaves, and the formed local overheating zone can control the solubility of the ammonium sulfate mother liquor, is beneficial to eliminating fine crystals and reducing the aspect ratio of crystals, so that better crystal forms are obtained. The mother liquor heating system can select a continuous operation mode or an intermittent operation mode according to the proportion of fine crystals in the ammonium sulfate mother liquor. When the ammonium sulfate mother liquor has more fine crystals (the granularity is 2mm fine crystals are more than or equal to 35 percent), the mother liquor heating system is started, and after the fine crystals are eliminated (the granularity is 2mm fine crystals less than 30 percent), the mother liquor can be closed.
4. A heat control system;
the method is used for accurately allocating the heat of the gas heating system and the heat of the mother liquor heating system, is favorable for realizing the control and the distribution of the heat between the two systems, and needs to correspondingly reduce the heat supply of the gas heating system when the mother liquor heating system operates.
5. An acidity control system;
is used for controlling the acidity of the ammonium sulfate mother liquor, so that the acidity of the ammonium sulfate mother liquor in the ammonia absorption system is kept in the normal range of 2-6 percent.
The working principle and the control process of the coke oven gas deamination system for producing large-particle ammonium sulfate are as follows:
the gas to be deaminated from the external unit is heated to 40-65 ℃ by a gas heating system, the heating means can adopt modes of steam, electricity or microwaves, and the like, the gas heating system mainly comprises a gas preheater, an attached valve, a pipeline, an instrument, and the like, and the added heat QDg can be adjusted by a heat control system. When the gas temperature is lower than 40 ℃ in the initial stage of working, the gas heating system is required to be forcibly started, and when the gas temperature is higher than 65 ℃, the gas heating system is required to be closed in an interlocking way.
The heated gas enters an ammonia absorption system, and ammonia in sulfuric acid and the gas is reacted in a saturator or an acid washing tower to generate ammonium sulfate, wherein the chemical equation is as follows:
2NH 3 +H 2 SO 4 →(NH 4 ) 2 SO 4
after the ammonia in the gas is absorbed, the ammonia content can be reduced to 30mg/Nm 3 The following is given. In order to avoid corrosion of downstream devices and pipelines by entrained acidic fog drops, a fog catcher is also arranged on an outlet gas pipeline of the ammonia absorption system.
The amount of water carried by the gas from the ammonia absorption system is calculated as follows:
coal gas water yield = coal gas water yield + water yield of other gases + water yield of sulfuric acid + water yield of centrifuge + water yield of tail gas cleaning tower + water yield of centrifuge-ammonium sulfate water yield after centrifuge
In order to ensure that the absorption reaction is continuously carried out, the ammonium sulfate mother solution containing crystals is continuously sprayed to an ammonia absorption system under the action of a large mother solution circulating pump. And a mother liquor heating system is also arranged on the upstream pipeline of the suction end of the large mother liquor circulating pump. The mother solution heating system generates local high temperature by means of steam, electricity or microwaves, and the like, so that the solubility of the ammonium sulfate mother solution is increased, fine crystals are eliminated, the aspect ratio of the crystals is reduced, and the quality of ammonium sulfate products is improved.
The mother liquor heating system can adopt an intermittent operation mode according to the proportion of fine crystals in the ammonium sulfate mother liquor, namely, the mother liquor heating system is started when the proportion of fine crystals with the granularity of less than 2mm reaches 35 percent, and is closed when the proportion is reduced to 30 percent. The mother liquor heating system mainly comprises a tube type mother liquor heater, an attached valve, a pipeline, an instrument and the like, and the added heat QDc can be adjusted through a heat control system.
In order to ensure heat balance in the whole coke oven gas deamination system, the utility model provides a heat control system for regulating heat of two heating systems, wherein the heat control system comprises an input parameter measurement module, an output parameter measurement module, a heat operation module and a heat control module, and the operation principle is as follows:
first, the input parameter measuring module measures the inlet temperature T of the coal gas/ammonium sulfate mother liquor in And inlet flow q in (q when there is no flow meter in site in Based on the flow rate of the fluid delivery device); then, the output parameter measuring module measures the outlet temperature T of the coal gas/ammonium sulfate mother liquor out And outlet flow q out (q when there is no flow meter in site out Based on the flow rate of the fluid delivery device); then, the parameters are transmitted to a heat operation module and calculated according to the following formula:
input heat Q of gas heating system/mother liquor heating system in ＝C in q in T in ；
Output heat Q of gas heating system/mother liquor heating system out ＝C out q out T out ；
In the above formula, C in To input specific heat of coal gas/ammonium sulfate mother liquor, C out To output the specific heat of the coal gas/ammonium sulfate mother liquor.
Make-up heat qd=q for gas heating system/mother liquor heating system out -Q in
In the utility model, because the gas heating system and the mother liquor heating system are both required to be supplemented with heat (QDg and QDc), the sum of the two is the supplemented total heat:
Σq= QDg + QDc =gas take-out heat+wet ammonium sulfate take-out mother liquor take-out heat from crystallization tank+saturator heat loss-gas take-in heat-other gas take-in heat-sulfuric acid dilution heat-wash water take-in heat-return mother liquor take-in heat-ammonium sulfate generation heat-ammonium sulfate crystallization heat
However, because the operation system of the mother liquor heating system is intermittent operation, when the mother liquor heating system is stopped, the heat control system automatically increases the heat supply of the gas heating system according to the preset value. Conversely, when the mother liquor heating system is put into operation, the heat control system automatically reduces the heat supply of the gas heating system. In summary, the heat control system is a guarantee that the whole system maintains heat balance.
6. An acidity control system;
the device mainly comprises an acidity measuring module, a sulfuric acid overhead tank, a sulfuric acid regulating valve, an observation mirror, an attached valve, a pipeline, an instrument and the like. In normal operation, the sulfuric acid regulating valve is automatically opened when the acidity of the ammonia absorption system is below 2%, and is closed when the acidity is above 6%.
The following examples are given by way of illustration of detailed embodiments and specific procedures based on the technical scheme of the present utility model, but the scope of the present utility model is not limited to the following examples.
[ example ]
As shown in fig. 1, in this example, the process flow of the coke oven gas deamination system for producing large-particle ammonium sulfate is as follows:
the gas to be deaminated from the external unit enters a gas heating system 8 through a gas inlet valve 1, is heated to 60 ℃, enters an ammonia absorption system 7 to absorb ammonia, is separated into tiny acid liquid drops through a mist catcher 6, is sent to the next unit through a gas outlet valve 2, and the ammonia content of the gas is reduced to 30mg/Nm 3 The following is given.
A traffic pipe and a traffic valve 3 are arranged between the gas inlet valve 1 and the upstream pipeline of the gas outlet valve 2, which is convenient for use in overhauling the ammonium sulfate unit.
The circulating ammonium sulfate mother liquor required for the ammonia absorption system 7 is provided by a large mother liquor circulation pump 21. In order to control the fine crystal content in the ammonium sulfate mother liquor, part of the ammonium sulfate mother liquor at the inlet end of the large mother liquor circulating pump 21 needs to pass through the mother liquor heating system 9, and when the fine crystal proportion of the ammonium sulfate mother liquor with the granularity of less than 2mm reaches 35%, the mother liquor heating system 9 is started, and the mother liquor heating system is closed until the proportion is reduced to 30%.
The heat of the gas heating system 8 and the heat of the mother liquor heating system 9 are controlled by a heat control system 10, and the heat control system 10 comprises an input parameter measuring module 11, an output parameter measuring module 12, a heat operation module 13 and a heat control module 14 (controlled by a heat regulating valve 15).
The acidity of the ammonia absorption system 7 is regulated by an acidity control system 16, and the acidity control system 16 comprises an acidity measurement module 17, a sulfuric acid overhead tank 18, a sulfuric acid regulating valve 19 and an observation mirror 20, and the acidity is controlled to be 4%.
The liquid level of the ammonium sulfate mother liquor in the ammonia absorption system 7 is controlled by a full flow tank 25, the generated residues are collected by a residue tank 27, and the generated ammonium sulfate crystals are conveyed to a subsequent process by a crystallization pump 22. Mother liquor overflowed from the ammonia absorption system 7 flows through the full flow tank 25 to the mother liquor storage tank 26 and is returned to the ammonia absorption system 7 by the small mother liquor pump 23 for spraying.
The particle size range of the ammonium sulfate product produced by the coke oven gas deamination system is 400-3000 mu m, and the production requirement of the large-particle ammonium sulfate product is met.
The foregoing is only a preferred embodiment of the present utility model, but the scope of the present utility model is not limited thereto, and any person skilled in the art, who is within the scope of the present utility model, should make equivalent substitutions or modifications according to the technical scheme of the present utility model and the inventive concept thereof, and should be covered by the scope of the present utility model.
Claims (5)
1. A coke oven gas deamination system for producing large-particle ammonium sulfate comprises an ammonia absorption system, a sulfuric acid overhead tank, a full flow tank, a mother liquor storage tank, a crystallization pump, a large mother liquor circulating pump and a small mother liquor pump; the gas inlet of the ammonia absorption system is connected with a coke oven gas pipeline through a gas inlet pipeline, and a gas inlet valve is arranged on the gas inlet pipeline; the gas outlet of the ammonia absorption system is connected with a deamination gas pipeline through a gas outlet pipeline, and a mist catcher, a gas outlet valve and a liquid discharge funnel are sequentially arranged on the gas outlet pipeline along the gas flowing direction, and the liquid discharge funnel is connected with a gas liquid seal groove; the gas outlet pipeline is connected with the gas inlet pipeline through a traffic pipe, and a traffic valve is arranged on the traffic pipe; the sulfuric acid outlet of the sulfuric acid overhead tank is connected with the sulfuric acid inlet of the mother solution storage tank through a sulfuric acid outlet pipeline; the ammonium sulfate mother liquor outlet of the mother liquor storage tank is connected with the ammonium sulfate mother liquor inlet of the ammonia absorption system through an ammonium sulfate mother liquor pipeline, and a small mother liquor pump and a flow regulating valve are sequentially arranged on the ammonium sulfate mother liquor pipeline along the flow direction of the ammonium sulfate mother liquor; the small mother liquid pump and the flow regulating valve are controlled in an interlocking way; the ammonium sulfate outlet of the ammonia absorption system is connected with a full flow groove through an ammonium sulfate outlet pipeline, and the full flow groove is connected with a mother liquor storage tank through a full flow mother liquor pipeline; the ammonia absorption system is provided with a circulating mother liquor outlet I which is connected with a circulating mother liquor inlet of the ammonia absorption system through a circulating mother liquor pipeline, and a large mother liquor circulating pump is arranged on the circulating mother liquor pipeline; the crystallization-containing mother liquor outlet of the ammonia absorption system is connected with a crystallization-containing mother liquor delivery pipeline, and a crystallization pump is arranged on the crystallization-containing mother liquor delivery pipeline; the method is characterized in that:
the coke oven gas deamination system also comprises a gas heating system, a mother liquor heating system, an acidity control system and a heat control system; the gas heating system is arranged on the gas inlet pipeline; the ammonia absorption system is provided with a circulating mother liquor outlet which is connected with a circulating mother liquor pipeline at the upstream of the large mother liquor circulating pump through a heating circulating mother liquor pipeline; a mother liquor heating system is arranged on the heating circulating mother liquor pipeline; the acidity control system comprises an acidity measurement module, a sulfuric acid regulating valve and an observation mirror; the acidity measurement module is arranged in the ammonia absorption system and is used for detecting the acidity of the ammonium sulfate mother liquor; the sulfuric acid high-level tank is provided with an adjusting sulfuric acid outlet which is respectively connected with an ammonium sulfate outlet pipeline and a circulating mother liquor pipeline at the upstream of the large mother liquor circulating pump through adjusting sulfuric acid pipelines; a sulfuric acid regulating valve and an observation mirror are arranged on the sulfuric acid regulating pipeline; the acidity measurement module is controlled by interlocking with a sulfuric acid regulating valve; and the gas heating system and the mother liquor heating system are connected with the corresponding heat control systems.
2. The coke oven gas deamination system for producing large-particle ammonium sulfate according to claim 1, wherein the heat control system consists of a heat regulating valve, an input parameter measuring module, an output parameter measuring module, a heat calculating module and a heat control module; the heat regulating valve is respectively arranged on a heat input pipeline of the gas heating system and a heat input pipeline of the mother liquor heating system; input parameter measurement modules are respectively arranged on a gas inlet pipeline at the upstream of the gas heating system and a heating circulating mother liquor pipeline at the upstream of the mother liquor heating system, and output parameter measurement modules are respectively arranged on the gas inlet pipeline at the downstream of the gas heating system and the heating circulating mother liquor pipeline at the downstream of the mother liquor heating system; the control end of the heat control valve, the input parameter measuring module, the output parameter measuring module and the heat operation module are respectively connected with the heat control module.
3. A coke oven gas deamination system for producing large particle ammonium sulfate according to claim 1, wherein the gas heating system is a steam heating system, an electric heating system or a microwave heating system.
4. A coke oven gas deamination system for producing large particle ammonium sulfate according to claim 1, wherein the ammonia absorption system is a saturator or a pickling tower.
5. A coke oven gas deamination system for producing large particle ammonium sulfate as claimed in claim 1, wherein the mother liquor heating system is a steam heating system, an electric heating system or a microwave heating system.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321010530.5U CN219861239U (en) | 2023-04-28 | 2023-04-28 | Coke oven gas deamination system for producing large-particle ammonium sulfate |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202321010530.5U CN219861239U (en) | 2023-04-28 | 2023-04-28 | Coke oven gas deamination system for producing large-particle ammonium sulfate |
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