CN115488139A - Raw material pretreatment system and method for producing acid by burning desulfurization waste liquid and crude salt - Google Patents
Raw material pretreatment system and method for producing acid by burning desulfurization waste liquid and crude salt Download PDFInfo
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- 150000003839 salts Chemical class 0.000 title claims abstract description 122
- 239000007788 liquid Substances 0.000 title claims abstract description 70
- 239000002699 waste material Substances 0.000 title claims abstract description 65
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 60
- 230000023556 desulfurization Effects 0.000 title claims abstract description 59
- 239000002253 acid Substances 0.000 title claims abstract description 26
- 239000002994 raw material Substances 0.000 title claims abstract description 24
- 238000004519 manufacturing process Methods 0.000 title description 6
- 239000000243 solution Substances 0.000 claims abstract description 66
- 239000012266 salt solution Substances 0.000 claims abstract description 38
- 238000010438 heat treatment Methods 0.000 claims abstract description 25
- 238000000034 method Methods 0.000 claims abstract description 18
- 230000005484 gravity Effects 0.000 claims abstract description 15
- 230000008569 process Effects 0.000 claims abstract description 13
- 229920006395 saturated elastomer Polymers 0.000 claims description 13
- 239000011344 liquid material Substances 0.000 claims 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 26
- 239000011593 sulfur Substances 0.000 abstract description 22
- 229910052717 sulfur Inorganic materials 0.000 abstract description 22
- 239000002245 particle Substances 0.000 abstract description 11
- 238000000926 separation method Methods 0.000 abstract description 5
- 239000002920 hazardous waste Substances 0.000 abstract description 3
- 238000002360 preparation method Methods 0.000 abstract description 3
- 238000002203 pretreatment Methods 0.000 abstract description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 238000003756 stirring Methods 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 3
- 230000008021 deposition Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
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- 239000011148 porous material Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- SOIFLUNRINLCBN-UHFFFAOYSA-N ammonium thiocyanate Chemical compound [NH4+].[S-]C#N SOIFLUNRINLCBN-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 230000002706 hydrostatic effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
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- 238000007781 pre-processing Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
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- 238000009279 wet oxidation reaction Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
- B09B3/45—Steam treatment, e.g. supercritical water gasification or oxidation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/80—Destroying solid waste or transforming solid waste into something useful or harmless involving an extraction step
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B2101/00—Type of solid waste
- B09B2101/02—Gases or liquids enclosed in discarded articles, e.g. aerosol cans or cooling systems of refrigerators
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to the technical field of industrial hazardous waste treatment, in particular to a raw material pretreatment system and a raw material pretreatment method for producing acid by burning desulfurization waste liquid and crude salt; this system is including being used for the concentrated enrichment facility of desulfurization waste liquid for the salt device that dissolves of crude salt, and the buffer tank, enrichment facility's solution output and buffer tank are connected, and the solution output of dissolving the salt device is connected with the buffer tank, and the buffer tank is including being used for maintaining the internal solution temperature of jar at 40 ~ 95 ℃ heating device, and enrichment facility all is provided with gravity settling chamber and filter on to the pipeline of buffer tank and on dissolving the pipeline of salt device to the buffer tank. The invention eliminates large sulfur particles by adopting modes of sectional utilization of heating steam, salt solution circulation, gravity settling and the like, reduces the separation of sulfur in the solution entering an incineration workshop section, maintains the temperature of the solution in the buffer tank at 40-95 ℃, reduces the separation of sulfur in the buffer process, can solve the problems of pipeline blockage and incomplete incineration, and improves the efficiency of acid preparation by incineration.
Description
Technical Field
The invention relates to the technical field of industrial hazardous waste treatment, in particular to a raw material pretreatment system and a raw material pretreatment method for producing acid by burning desulfurization waste liquid and crude salt.
Background
At present, the coking industry mostly adopts an ammonia wet oxidation cyanogen-removing process which takes HPF, PDS and the like as catalysts to remove H in coal gas 2 S and HCN, the byproduct desulfurization waste liquid of the process, and crude salt which is obtained after drying and reducing the desulfurization waste liquid and mainly comprises ammonium thiocyanate and ammonium sulfate flow are listed as hazardous waste in national waste records (2021 edition), are important points of environmental protection and supervision, and the effective treatment of the desulfurization waste liquid and the crude salt is not slow. Incineration acid makingIs a new way for carrying out harmless and resource treatment on the crude salt of the desulfurization waste liquid, and the general flow is as follows: heating, evaporating and concentrating the desulfurization waste liquid to obtain a rich-salt concentrated solution, dissolving and heating crude salt to obtain a crude-salt concentrated solution, and spraying the rich-salt concentrated solution and the crude-salt concentrated solution into an incinerator for incineration to obtain SO-containing 2 And finally, the flue gas passes through an acid making system to obtain the finished product sulfuric acid.
In the practical application process, the technology has the problems of pipeline blockage, incomplete incineration and the like, and the root of the problem is mainly that the raw material pretreatment does not reach the standard; for example, the large sulfur-containing particles (with a particle size of more than 0.5) in the rich salt concentrated solution, even the sulfur is fast, the concentration fluctuation of the salt solution is large, and the like, so that the yield of acid preparation by burning in the later period is reduced, and the pretreatment level of the raw materials needs to be improved.
Disclosure of Invention
In order to solve the above problems, in one aspect, the present invention provides a raw material pretreatment system for producing acid by burning desulfurization waste liquid and crude salt, including a concentration device for concentrating desulfurization waste liquid, a salt dissolving device for dissolving crude salt, and a buffer tank, wherein a solution output end of the concentration device is connected to the buffer tank, a solution output end of the salt dissolving device is connected to the buffer tank, the buffer tank includes a heating device for maintaining the temperature of the solution in the tank body at 40 to 95 ℃, a gravity settling chamber and a filter are arranged on a pipeline from the concentration device to the buffer tank and a pipeline from the salt dissolving device to the buffer tank, and a solution output end of the buffer tank is connected to a pipeline leading to a burning workshop section.
Further, the concentration device comprises a concentration tower, a heater and a first circulating pump, the first circulating pump is connected with the bottom of the concentration tower and conveys the solution to the heater, the heater is connected with the upper part of the concentration tower, saturated steam at 140-200 ℃ is introduced into the heater, and the output end of the first circulating pump is also connected with the buffer tank.
Furthermore, the concentration device also comprises a vacuum pump, the vacuum pump is connected with the top end of the concentration tower, and the pipelines of the concentration tower and the vacuum pump are also provided with coolers.
Further, the end point temperature of the salt solution in the concentration device does not exceed 110 ℃.
Further, the desulfurization waste liquid and the crude salt respectively reach 50-90% of salt mass fraction in the concentration device and the salt dissolving device, and enter the buffer tank.
Further, the salt dissolving device comprises a salt dissolving reactor and a second circulating pump, the inlet end of the second circulating pump is connected with the bottom of the salt dissolving reactor, the outlet end of the second circulating pump is connected with the upper end of the salt dissolving reactor, the outlet end of the second circulating pump is also connected with the buffer tank, and the salt dissolving reactor comprises a heating device for maintaining the temperature of the solution at 40-95 ℃.
Furthermore, the concentration device and the salt dissolving device are respectively connected with a differential pressure gauge.
Further, a stirrer is arranged in the buffer tank, the buffer tank is connected with a third circulating pump, and the third circulating pump is used for connecting the bottom and the upper part of the buffer tank and is used for circulating the solution.
In another aspect, the present invention further provides a method of using the above-mentioned desulfurization waste liquid and raw salt incineration acid-making raw material pretreatment system, including the following steps:
conveying the salt-rich solution after the desulfurization waste liquid is concentrated to a set concentration in a concentration device into a buffer tank;
conveying the crude salt solution with the crude salt dissolved to a set concentration in a salt dissolving device into a buffer tank;
and the salt-rich solution and the crude salt solution pass through a gravity settling chamber and a filter and then enter the buffer tank, and the temperature of the solution in the buffer tank is maintained to be 40-95 ℃.
Further, the treatment process of the desulfurization waste liquid and the crude salt in the concentration device and the salt dissolving device respectively comprises the following steps:
controlling the end point temperature of the salt solution in the concentration device not to exceed 110 ℃;
and maintaining the temperature of the solution in the salt dissolving device at 40-95 ℃.
Due to the adoption of the technical scheme, compared with the prior art, the invention has the following beneficial effects: according to the raw material pretreatment system and method for producing acid by burning the desulfurization waste liquid and the crude salt, provided by the invention, large sulfur particles are eliminated by adopting modes of sectional utilization of heating steam, circulation of salt solution, gravity settling and the like, the separation of sulfur in the solution entering a burning workshop section is reduced, the temperature of the solution in a buffer tank is maintained at 40-95 ℃, the separation of sulfur in the buffer process is reduced, the problems of pipeline blockage and incomplete burning can be solved, and the efficiency of producing acid by burning is improved; the concentration of the saline solution is accurately controlled by adopting an online density detection mode, so that the concentration of the saline solution meeting the feeding requirement of the incinerator is prepared, and the treatment efficiency of acid preparation by incineration is improved.
Drawings
FIG. 1 is a schematic structural diagram of a raw material pretreatment system for producing acid by burning desulfurized waste liquid and crude salt according to the present invention;
FIG. 2 is a schematic diagram of the salt solution-density function of the present invention.
1-desulfurization waste liquid; 2-a concentration tower; 3-a first circulation pump; 4-a heater; 5-first saturated steam; 6. 24-a differential pressure gauge; 7-a concentration tower outlet main pipe; 8-a concentrating tower circulating branch pipe; 9-outlet branch pipe of the concentration tower; 10-a cooler; 11-a vacuum pump; 12-gas manifold; 13-cooling water; 14. 25-gravity settling chamber; 15. 26-a filter; 16-second saturated steam; 17-crude salt; 18-dissolving solution; 19-a salt dissolving reactor; 20-a second circulation pump; 21-outlet header pipe of the dissolved salt reactor; 22-circulating branch pipes of the salt dissolving reactor; 23-outlet branch pipe of the salt dissolving reactor; 27-third saturated steam; 28-a buffer tank; 29-a third circulation pump; 30-buffer tank outlet manifold; 31-buffer tank circulation branch pipes; 32-buffer tank outlet branch pipe; 33-buffer tank outlet manifold.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments, and all other embodiments obtained by a person of ordinary skill in the art without creative efforts based on the embodiments of the present invention belong to the protection scope of the present invention. In the drawings, the size and relative sizes of certain features may be exaggerated for clarity.
In the description of the present invention, unless otherwise explicitly specified or limited, the terms "connected" and "connected" are to be construed broadly, e.g., as meaning fixedly connected, detachably connected, or integral with; can be mechanically or electrically connected; the terms may be directly connected or indirectly connected through an intermediate medium, and may be communication between two elements or interaction relationship between two elements, and those skilled in the art can understand the specific meaning of the terms in the present invention in specific cases.
In the description of the present invention, the terms "upper", "lower", "left", "right", "front", "rear", and the like are used in the orientations and positional relationships shown in the drawings only for convenience of description and simplicity of operation, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention.
In addition, in the description of the present invention, the terms "first" and "second" are used only for descriptive distinction.
Example 1
As shown in the attached figure 1, the invention provides a raw material pretreatment system for producing acid by burning desulfurization waste liquid and crude salt, which is used for treating desulfurization waste liquid and crude salt, wherein the treated salt solution is directly sprayed into a burning section or buffered for storage, the pretreatment system comprises a concentration device for concentrating desulfurization waste liquid 1, a salt dissolving device for dissolving crude salt 17 and a buffer tank 28, the solution output end of the concentration device is connected with the buffer tank 28, the solution output end of the salt dissolving device is connected with the buffer tank 28, the buffer tank 28 comprises a heating device for maintaining the temperature of the solution in the tank body at 40-95 ℃, gravity settling chambers 14 and 25 and filters 15 and 26 are arranged on the pipeline from the concentration device to the buffer tank 28 and the pipeline from the salt dissolving device to the buffer tank 28, the specification sizes of each gravity settling chamber and each filter can be the same or different, the output solution of the concentration device and the output solution of the salt dissolving device enter the buffer tank 28 after gravity settling and filtering, and the output end of the solution of the buffer tank 28 is connected with a burning pipeline leading to the burning section.
In an optimized implementation mode, the concentration device comprises a concentration tower 2, a first circulating pump 3 and a heater 4, the first circulating pump 3 is connected with the bottom of the concentration tower 2 and conveys a solution to the heater 4, the heater 4 is connected with the upper part of the concentration tower 2, first saturated steam 5 is introduced into the heater 4, the temperature of the first saturated steam is 140-200 ℃ and is used for heating and concentrating the desulfurization waste liquid, the output end of the first circulating pump 3 is further connected with the buffer tank 27, specifically, the outlet end of the first circulating pump 3 is connected with a concentration tower outlet main pipe 7 and enters the concentration tower 2 through a concentration tower circulating branch pipe 8 for circulation, the concentration tower outlet main pipe 7 conveys the concentrated salt-rich solution into the buffer tank 28 through a concentration tower outlet branch pipe 9, when the desulfurization waste liquid circulates in the concentration tower 2, the concentration tower outlet branch pipe 9 is closed, and when the desulfurization waste liquid enters the buffer tank 28, the concentration tower circulating branch pipe 8 can be closed; the concentrating device further comprises a vacuum pump 11, the vacuum pump 11 is connected with the top end of the concentrating tower 2, the concentrating tower 2 is further provided with a cooler 10 on a pipeline of the vacuum pump 11, the cooler 10 is filled with cooling water 13, the vacuum pump 11 extracts gas in the concentrating tower 2 through a connecting pipe at the top of the tower to manufacture a vacuum degree of 0.03-0.08MPa, the volatilization of moisture in the desulfurization waste liquid is accelerated, water vapor is condensed into liquid water in the cooler 10, and the uncondensed waste gas passes through a gas branch pipe 12 of the vacuum pump 11 to remove the waste gas treatment system.
The refinement implementation mode has the advantages that in the processes of heating and concentrating the desulfurization waste liquid and caching the salt solution, sulfur powder in the solution is easy to melt and gather to generate large sulfur particles and even sulfur blocks, and the main reasons are that the temperature of heating steam is too high and the heating time is too long. Aiming at the problem of generating large sulfur particles and sulfur blocks. In the embodiment, in the pretreatment process of desulfurization waste liquid concentration, the desulfurization waste liquid is circulated through the first circulating pump 3, sulfur particles are prevented from being separated out from the bottom of the tower, the temperature of heating steam is above the melting point of sulfur, the melting point of sulfur is 119 ℃, in order to ensure the heating concentration rate, the temperature of the used heating steam is 140-200 ℃, but the end point temperature of a salt solution in the concentration tower 2 is strictly controlled to be below 110 ℃, after the desulfurization waste liquid is concentrated to a set concentration, the desulfurization waste liquid is timely conveyed into the buffer tank 28, if the concentrated salt solution reaches 50-90% by mass fraction, the concentrated salt solution can be conveyed into the buffer tank, most of the sulfur particles are removed from the concentrated salt solution through the gravity settling chamber 14, the sulfur particles are further removed through the filter 15, and the pore diameter of the filter is 0.2-1 mm.
In the embodiment, the temperature of the heating steam is 160 ℃, and the sulfur separated out from the desulfurization waste liquid is strictly monitored in the concentration process, so that the separation out of the sulfur in the concentration process is reduced.
In an optimized embodiment, the salt dissolving device comprises a salt dissolving reactor 19 and a second circulating pump 20, crude salt 17 and a dissolving solution 18 pass through the inside of the salt dissolving reactor 19, the dissolving solution is clear water or a desulfurization waste liquid, the inlet end of the second circulating pump 20 is connected with the bottom of the salt dissolving reactor 19, the outlet end of the second circulating pump 20 is connected with the upper end of the salt dissolving reactor 19, the outlet end of the second circulating pump 20 is further connected with the buffer tank 28, the salt dissolving reactor 19 comprises a heating device for maintaining the temperature of the solution at 40-95 ℃, in the embodiment, the salt dissolving reactor 19 is provided with a jacket layer, second saturated steam 16 is introduced into the jacket layer, the temperature of the second saturated steam is 80-120 ℃ and is used for heating the solution, of course, an electric heating rod can be adopted for heating the crude salt solution, a stirring device is arranged in the salt dissolving reactor and is used for stirring, so that the deposition of the solution in the reactor and the uneven temperature of the solution are avoided, and the deposition of sulfur and the crude salt particles which are not dissolved in the solution at the bottom of the reactor is caused by the pipeline blockage; the circulating device connected with the salt dissolving reactor 19 can also reduce the deposition of particulate matters, the salt dissolving reactor 19 realizes the circulation of solution through a second circulating pump 20, the outlet of the second circulating pump 20 is connected with a salt dissolving reactor outlet manifold 21 and is connected with the upper part of the salt dissolving reactor 19 through a salt dissolving reactor circulating branch pipe 22, and the salt dissolving reactor outlet manifold 21 conveys the crude salt solution into a buffer tank 28 through a salt dissolving reactor outlet branch pipe 23.
In the refinement embodiment, the concentration of the crude salt solution in the salt dissolving reactor 19 reaches 50-90%, the crude salt solution enters the buffer tank 28, and the crude salt solution passes through the gravity settling chamber 25 and the filter 26 with the pore diameter of 0.2-1 mm in sequence before entering the buffer tank, so that insoluble impurities in the crude salt solution can be removed, and the pretreatment effect of the crude salt is improved.
In an optimized implementation mode, a stirrer is arranged in the buffer tank 28, the buffer tank 28 is provided with a jacket layer, third saturated steam 27 is introduced into the jacket layer, the temperature of the second saturated steam is 80-120 ℃ and is used for maintaining the solution in the tank at 40-95 ℃, the buffer tank 28 is connected with a third circulating pump 29, the third circulating pump 29 is used for connecting the bottom and the upper part of the buffer tank 28 and is used for circulating the solution, the outlet of the third circulating pump 29 is connected with a buffer tank outlet main pipe 30 which enters the upper part of the buffer tank 28 through a buffer tank circulating branch pipe 31 for circulating, and the buffer tank outlet main pipe 30 is further connected with a buffer tank outlet branch pipe 32 which is used for conveying a mixed salt solution 33 to a burning workshop section.
In actual use, valves for regulation and control, temperature sensors and pressure sensors for detection are arranged on the devices and pipelines, and the valves and the pressure sensors are used for ensuring the normal operation of the pretreatment system.
The desulfurization waste liquid and the crude salt respectively reach 50-90% of salt mass fraction in a concentration device and a salt dissolving device, the concentration device and the salt dissolving device are respectively connected with a differential pressure meter, specifically, a differential pressure meter 6 is connected to a concentration tower, and a differential pressure meter 24 is also connected to a salt dissolving reactor. The pretreatment of the desulfurization waste liquid and the pretreatment of the crude salt are mutually independent treatment processes, and when only the desulfurization waste liquid exists, the salt dissolving reactor can be closed, and only the desulfurization waste liquid is treated.
The concentration of the salt solution is difficult to control and has large fluctuation, and the salt concentration is mainly difficult to measure. In the embodiment, the solution concentration is indirectly calculated by testing the solution density, and the specific scheme is as follows:
firstly, a series of concentration gradient salt solutions are prepared by drying crude salt and clear water, the densities of the salt solutions are respectively measured, and a concentration-density correspondence is establishedThe relation table can be further established, for example, the salt concentration-density corresponding relation of a certain salt solution is shown in table 1, the function relation is shown in figure 2, y =186x-193, R is 2 =0.974, wherein x is the abscissa, y is the ordinate, and R is the degree of fit. Selecting two points A and B of vertical height difference h on the container or pipeline, and respectively testing hydrostatic pressure P of the two points A and B A And P B . The solution density is obtained according to the formula 1), and the solution concentration value is obtained by the density table lookup or the function relation.
ρ＝(P A -P B ) /gh formula 1)
In formula 1), ρ -density; p is A 、P B -a static pressure; g-the gravitational constant; h-height difference.
TABLE 1 determination of certain salt concentration-density correspondence
| Mass concentration (%) | 50 | 60 | 70 | 80 | 90 |
| Density (g/cm) 3 ) | 1.252 | 1.378 | 1.421 | 1.454 | 1.515 |
Preferably, the points A and B should not be affected by stirring, and are preferably arranged on the vertical pipe section at the outlet of the bottom of the container, no stirring paddle is arranged in the concentration tower 2, and the points A and B can also be arranged at the bottom of the concentration tower 2, and the differential pressure gauge of the salt dissolving reactor is arranged on the outlet pipeline.
In the preprocessing process of this application, there is the risk that forms sulphur granule or sulphur piece in the concentrated section of desulfurization waste liquid, and this risk aggravates along with the improvement of concentration, precipitate for reducing the sulphur, can suitably reduce the concentrated section of desulfurization waste liquid and get rid of liquid salt concentration, improve the thick salt solution concentration of thick salt dissolving section exhaust simultaneously, readjust the volume ratio that both got into the buffer tank, obtain the mixed salt solution of specified concentration. For example, assuming that the concentration of the discharged liquid from the desulfurization waste liquid concentration section is C 1 The concentration of the discharged solution of the salt dissolving section is C 2 Specifying the concentration of the mixed salt solution in the buffer tank as C 3 ，C 2 ＞C 3 ＞C 1 Volume V of the discharged liquid of the desulfurization waste liquid concentration section 1 Volume V of discharged liquid of salt dissolving stage 2 Satisfies formula 2).
V 1 /V 2 ＝(C 2 -C 3 )/(C 3 -C 1 ) Formula 2)
In some embodiments, it may be desirable to reduce the concentrated effluent concentration of the desulfurized waste stream to reduce sulfur precipitation in the solution.
Example 2
The invention also provides a method for adopting the raw material pretreatment system for producing acid by burning the desulfurization waste liquid and the crude salt, which comprises the following steps:
heating, concentrating and circulating the desulfurization waste liquid in a concentration tower 2, and conveying a salt-rich solution obtained by concentrating the desulfurization waste liquid in the concentration tower 2 to a set concentration into a buffer tank 28;
specifically, the desulfurization waste liquid is heated and concentrated by adopting saturated steam at the temperature of 140-200 ℃, a vacuum pump is further connected to a concentration tower and is used for manufacturing the vacuum degree of 0.03-0.08MPa, the volatilization of water in the desulfurization waste liquid is accelerated, when the mass fraction of the discharge liquid after the desulfurization waste liquid is concentrated is 50-90%, the discharge liquid is conveyed into a buffer tank, the end point temperature of the discharge liquid in the concentration tower is controlled to be below 110 ℃, and the concentrated discharge liquid enters the buffer tank after gravity settling and filter filtration.
Conveying the crude salt solution with the crude salt dissolved to a set concentration in a salt dissolving device into a buffer tank;
specifically, the crude salt is dissolved in clear water or desulfurization waste liquid, the solution is dissolved through saturated steam at the temperature of 80-120 ℃, the temperature of the solution in the salt dissolving reactor is kept at 40-95 ℃, the crude salt solution is circulated through a second circulating pump, and the crude salt solution reaches a set concentration, then sequentially passes through gravity settling and a filter and then enters a buffer tank.
Mixing and circulating the concentrated discharge solution and the crude salt solution in a buffer tank, and heating the mixture by a heating device to maintain the temperature of the solution in the buffer tank at 40-95 ℃.
In summary, the invention provides a system and a method for pretreating desulfurization waste liquid and crude salt incineration acid, which adopt ways of graded utilization of heating steam, circulation of salt solution, gravity settling and the like, reduce sulfur particles in the salt solution, avoid blockage of pipelines, improve the treatment efficiency in the incineration acid production stage, and enable the reaction in the incineration stage to be more complete.
It should be understood by those skilled in the art that the present invention may be embodied in many other specific forms without departing from the spirit or scope of the invention. Although an embodiment of the present invention has been described, it is understood that the present invention should not be limited to this embodiment, but variations and modifications can be made by one skilled in the art within the spirit and scope of the invention as defined in the appended claims.
Claims (10)
1. The utility model provides a raw materials pretreatment system of desulfurization waste liquid, crude salt incineration system acid which characterized in that, is including the enrichment facility that is used for desulfurization waste liquid concentrated for the salt device that dissolves of crude salt, and buffer tank, enrichment facility's solution output with the buffer tank is connected, the solution output of dissolving the salt device with the buffer tank is connected, the buffer tank is including being used for maintaining the internal solution temperature of jar at 40 ~ 95 ℃ heating device, enrichment facility arrives on the pipeline of buffer tank and dissolve the salt device and arrive all be provided with gravity settling chamber and filter on the pipeline of buffer tank, the solution output of buffer tank is connected with the pipeline to burning the workshop section.
2. The system for pretreating raw materials for producing acid by incinerating desulfurization waste liquid and crude salt according to claim 1, wherein the concentration device comprises a concentration tower, a heater and a first circulating pump, the first circulating pump is connected with the bottom of the concentration tower and conveys the solution to the heater, the heater is connected with the upper part of the concentration tower, saturated steam at 140-200 ℃ is introduced into the heater, and the output end of the first circulating pump is further connected with the buffer tank.
3. The system for pretreating a raw material for producing acid by incinerating desulfurization waste liquid and crude salt according to claim 2, wherein the concentration device further comprises a vacuum pump, the vacuum pump is connected to the top end of the concentration tower, and a cooler is further arranged on the pipelines of the concentration tower and the vacuum pump.
4. The system for pretreating a raw material for producing acid by incinerating a desulfurized waste liquid and crude salt according to claim 1, wherein the final temperature of the salt solution in said concentration device is not more than 110 ℃.
5. The system for pretreating raw materials of desulfurization waste liquid and crude salt incineration acid according to claim 1, wherein the desulfurization waste liquid and the crude salt reach a salt mass fraction of 50-90% in a concentration device and a salt dissolving device, respectively, and enter the buffer tank.
6. The system for pretreating raw materials for producing acid by incinerating desulfurized waste liquid and crude salt according to claim 1, wherein the salt dissolving device comprises a salt dissolving reactor and a second circulating pump, an inlet end of the second circulating pump is connected with the bottom of the salt dissolving reactor, an outlet end of the second circulating pump is connected with the upper end of the salt dissolving reactor, an outlet end of the second circulating pump is further connected with the buffer tank, and the salt dissolving reactor comprises a heating device for maintaining the temperature of the solution at 40-95 ℃.
7. The system for pretreating desulfurization waste liquid and raw materials for producing acid by incinerating crude salt according to claim 1, wherein a differential pressure gauge is further connected to the concentration device and the salt dissolving device respectively.
8. The system for pretreating raw materials of desulfurization waste liquid and crude salt incineration acid according to claim 1, wherein a stirrer is arranged in the buffer tank, and a third circulating pump is connected to the buffer tank and is used for connecting the bottom and the upper part of the buffer tank for solution circulation.
9. A method for using the desulfurization waste liquid and raw salt incineration acid-making raw material pretreatment system according to any one of claims 1 to 8, characterized by comprising the steps of:
conveying the salt-rich solution after the desulfurization waste liquid is concentrated to a set concentration in a concentration device into a buffer tank;
conveying the crude salt solution obtained after the crude salt is dissolved to a set concentration in a salt dissolving device into a buffer tank;
and feeding the salt-rich solution and the crude salt solution into the buffer tank after passing through a gravity settling chamber and a filter, and maintaining the temperature of the solution in the buffer tank to be 40-95 ℃.
10. The method for pretreating desulfurization waste liquid and raw materials for producing acid by incinerating crude salt according to claim 9, wherein the treatment process of the desulfurization waste liquid and the crude salt in the concentration device and the salt dissolving device respectively comprises the following steps:
controlling the end point temperature of the salt solution in the concentration device not to exceed 110 ℃;
and maintaining the temperature of the solution in the salt dissolving device at 40-95 ℃.
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009028573A (en) * | 2007-07-24 | 2009-02-12 | Nippon Steel Engineering Co Ltd | Apparatus and method for treating desulphurization waste liquid |
| CN105731681A (en) * | 2014-12-11 | 2016-07-06 | 中国石油天然气股份有限公司 | Treatment apparatus and treatment process for catalytic cracking flue gas desulfurization waste liquid |
| CN107352679A (en) * | 2017-07-11 | 2017-11-17 | 河南中鸿集团煤化有限公司 | A kind of doctor solution salt extraction technique and its device |
| CN210584388U (en) * | 2019-07-19 | 2020-05-22 | 中冶焦耐(大连)工程技术有限公司 | System for preparing sulfur slurry by treating coking sulfur foam through gravity settling separation method |
| CN111517338A (en) * | 2020-03-31 | 2020-08-11 | 临涣焦化股份有限公司 | Dechlorination process for solid product of desulfurization waste liquid salt extraction device |
| CN112093779A (en) * | 2020-09-18 | 2020-12-18 | 南京合工智能环保研究院有限公司 | Acid preparation system and acid preparation process |
| CN112125319A (en) * | 2020-09-01 | 2020-12-25 | 太原理工大学 | Process for recovering all components of desulfurization waste liquid |
| CN112794290A (en) * | 2021-02-26 | 2021-05-14 | 中冶焦耐(大连)工程技术有限公司 | Process and system for treating low-quality sulfur and secondary salt waste liquid produced by coke oven gas desulfurization |
| CN214780762U (en) * | 2021-02-26 | 2021-11-19 | 中冶焦耐(大连)工程技术有限公司 | System for treating low-quality sulfur and secondary salt waste liquid produced by coke oven gas desulfurization |
| CN114014468A (en) * | 2021-11-30 | 2022-02-08 | 中冶南方都市环保工程技术股份有限公司 | System and method applied to pretreatment of coke oven gas desulfurization waste liquid |
-
2022
- 2022-09-28 CN CN202211187715.3A patent/CN115488139B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009028573A (en) * | 2007-07-24 | 2009-02-12 | Nippon Steel Engineering Co Ltd | Apparatus and method for treating desulphurization waste liquid |
| CN105731681A (en) * | 2014-12-11 | 2016-07-06 | 中国石油天然气股份有限公司 | Treatment apparatus and treatment process for catalytic cracking flue gas desulfurization waste liquid |
| CN107352679A (en) * | 2017-07-11 | 2017-11-17 | 河南中鸿集团煤化有限公司 | A kind of doctor solution salt extraction technique and its device |
| CN210584388U (en) * | 2019-07-19 | 2020-05-22 | 中冶焦耐(大连)工程技术有限公司 | System for preparing sulfur slurry by treating coking sulfur foam through gravity settling separation method |
| CN111517338A (en) * | 2020-03-31 | 2020-08-11 | 临涣焦化股份有限公司 | Dechlorination process for solid product of desulfurization waste liquid salt extraction device |
| CN112125319A (en) * | 2020-09-01 | 2020-12-25 | 太原理工大学 | Process for recovering all components of desulfurization waste liquid |
| CN112093779A (en) * | 2020-09-18 | 2020-12-18 | 南京合工智能环保研究院有限公司 | Acid preparation system and acid preparation process |
| CN112794290A (en) * | 2021-02-26 | 2021-05-14 | 中冶焦耐(大连)工程技术有限公司 | Process and system for treating low-quality sulfur and secondary salt waste liquid produced by coke oven gas desulfurization |
| CN214780762U (en) * | 2021-02-26 | 2021-11-19 | 中冶焦耐(大连)工程技术有限公司 | System for treating low-quality sulfur and secondary salt waste liquid produced by coke oven gas desulfurization |
| CN114014468A (en) * | 2021-11-30 | 2022-02-08 | 中冶南方都市环保工程技术股份有限公司 | System and method applied to pretreatment of coke oven gas desulfurization waste liquid |
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