CN114195102A - Method and device for refining sulfur from desulfurized sulfur paste - Google Patents
Method and device for refining sulfur from desulfurized sulfur paste Download PDFInfo
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- CN114195102A CN114195102A CN202111624156.3A CN202111624156A CN114195102A CN 114195102 A CN114195102 A CN 114195102A CN 202111624156 A CN202111624156 A CN 202111624156A CN 114195102 A CN114195102 A CN 114195102A
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 460
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 421
- 239000011593 sulfur Substances 0.000 title claims abstract description 421
- 238000000034 method Methods 0.000 title claims abstract description 23
- 238000007670 refining Methods 0.000 title claims abstract description 19
- 238000005406 washing Methods 0.000 claims abstract description 62
- 239000002002 slurry Substances 0.000 claims abstract description 59
- 238000004537 pulping Methods 0.000 claims abstract description 45
- 238000002844 melting Methods 0.000 claims abstract description 41
- 230000008018 melting Effects 0.000 claims abstract description 41
- 238000007738 vacuum evaporation Methods 0.000 claims abstract description 36
- 238000002425 crystallisation Methods 0.000 claims abstract description 27
- 230000008025 crystallization Effects 0.000 claims abstract description 27
- 239000000047 product Substances 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims description 304
- 239000007789 gas Substances 0.000 claims description 136
- 239000005416 organic matter Substances 0.000 claims description 39
- 238000009833 condensation Methods 0.000 claims description 38
- 230000005494 condensation Effects 0.000 claims description 38
- 239000002893 slag Substances 0.000 claims description 38
- 238000000926 separation method Methods 0.000 claims description 34
- 238000004821 distillation Methods 0.000 claims description 31
- 238000000354 decomposition reaction Methods 0.000 claims description 29
- 238000003860 storage Methods 0.000 claims description 27
- 238000007599 discharging Methods 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 13
- 238000005192 partition Methods 0.000 claims description 11
- 239000000706 filtrate Substances 0.000 claims description 10
- 150000003839 salts Chemical group 0.000 claims description 10
- 239000012266 salt solution Substances 0.000 claims description 9
- 239000002245 particle Substances 0.000 claims description 8
- 239000005864 Sulphur Substances 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 6
- 239000002351 wastewater Substances 0.000 claims description 6
- 238000005086 pumping Methods 0.000 claims description 5
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 4
- 238000000859 sublimation Methods 0.000 claims description 4
- 230000008022 sublimation Effects 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 3
- 239000011343 solid material Substances 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 2
- 239000012141 concentrate Substances 0.000 claims 1
- 229910001873 dinitrogen Inorganic materials 0.000 claims 1
- 238000006477 desulfuration reaction Methods 0.000 abstract description 12
- 230000023556 desulfurization Effects 0.000 abstract description 11
- 238000009279 wet oxidation reaction Methods 0.000 abstract description 6
- 239000006227 byproduct Substances 0.000 abstract description 2
- 238000004939 coking Methods 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract description 2
- 239000003245 coal Substances 0.000 abstract 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 239000002994 raw material Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 3
- 238000010079 rubber tapping Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- QIGBRXMKCJKVMJ-UHFFFAOYSA-N Hydroquinone Chemical compound OC1=CC=C(O)C=C1 QIGBRXMKCJKVMJ-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 125000001741 organic sulfur group Chemical group 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- BDHFUVZGWQCTTF-UHFFFAOYSA-M sulfonate Chemical compound [O-]S(=O)=O BDHFUVZGWQCTTF-UHFFFAOYSA-M 0.000 description 1
- 150000003463 sulfur Chemical class 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/0232—Purification, e.g. degassing
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/0221—Melting
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/0226—Vaporising or superheating
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/027—Recovery of sulfur from material containing elemental sulfur, e.g. luxmasses or sulfur containing ores; Purification of the recovered sulfur
Abstract
The invention discloses a method and a device for refining sulfur from desulfurized sulfur paste, wherein a sulfur paste pulping tank is connected with wet-process desulfurized sulfur paste through a first pipeline and is communicated with a sulfur paste concentration filter through a second pipeline; the sulfur pulp concentration filter is communicated with the sulfur pulp buffer tank through a third pipeline, the sulfur pulp concentration filter is communicated with the vacuum evaporation crystallization tank through a tenth pipeline, and the sulfur pulp concentration filter is communicated with the tail gas washing tower through a twentieth pipeline; the slurry of the sulfur slurry buffer tank is communicated with the sulfur melting kettle through a fourth pipeline; the invention adopts the sulfur melting and sublimating combined sulfur paste refining sulfur device, the sulfur product obtained by refining and recycling the sulfur paste reaches the excellent grade of industrial sulfur, and meanwhile, the whole sulfur paste refining sulfur device realizes automation, continuity and no secondary pollution, and is particularly suitable for treating a large amount of sulfur paste by-products of a wet oxidation desulfurization device in the fields of coal coking gas, petrochemical gas and the like.
Description
Technical Field
The invention relates to a method and a device for refining sulfur, in particular to a method and a device for refining sulfur from desulfurized sulfur paste, belonging to the technical field of chemical industry.
Background
At present, domestic petrochemical, metallurgical and coking enterprises need to carry out desulfurization treatment on raw materials in order to improve the quality of products. Generally, chemical enterprises with the latent sulfur content of less than 30t/d in raw materials are equipped with wet oxidation desulfurization equipment, wherein the complex iron wet oxidation desulfurization method gradually replaces the traditional HPF (hydroquinone, PDS-phthalocyancobalt sulfonate, FeSO)4Composite catalyst) desulfurization process becomes the mainstream desulfurization process. H by complex iron wet oxidation desulfurization2The reaction selectivity of S is over 99 percent at most, so compared with the traditional HPF device, the amount of the secondary salt generated is greatly reduced, no wastewater discharge is realized, and the advantages of economic operation cost, low investment, simple process and the like are favored by domestic chemical enterprises.
However, regardless of the traditional HPF desulfurization process or the complex iron wet oxidation desulfurization process, the sulfur paste produced by the desulfurization process is a difficult-to-sell waste due to low sulfur content (40-60 wt%), and complex other components (water, sulfur salts, oil, catalysts, solid particles and other impurities). The general enterprises adopt a direct abandonment mode, thereby not only causing pollution to the environment, but also wasting sulfur resources therein. In addition, some enterprises adopt conventional refined molten sulfur but can not obtain qualified sulfur required by national standards, and the semi-finished sulfur still has no market. If the part of sulfur can be refined and extracted through a reasonable process, the requirement of the prior art on the sulfur can be met, and meanwhile, the preparation cost of the sulfur is greatly reduced by adopting the sulfur paste as an extraction raw material. Not only the enterprise can not worry about the production, but also the extra sales revenue can be obtained.
Disclosure of Invention
The invention aims to solve the technical problem that the sulfur extraction device in the prior art cannot realize the deep removal of oil, water, gas, salt and slag which cause unexpected sulfur generation in the desulfurized sulfur paste, so that the prepared sulfur product has high impurity content and is unqualified, and further provides a refined sulfur device for obtaining high-quality sulfur from the desulfurized sulfur paste.
The sulfur paste raw material can adopt the filtered liquid and the water after the separated clear liquid is crystallized after the sulfur is melted as the circulating slurry preparation, thereby saving the public works.
In order to achieve the purpose, the method and the device for refining the sulfur from the desulfurized sulfur paste comprise a sulfur paste preparation tank, a sulfur paste concentration filter, a sulfur paste buffer tank, a sulfur melting kettle, a liquid sulfur buffer tank, an organic matter decomposition kettle, a liquid sulfur distillation kettle, a refined liquid sulfur storage tank, a vacuum evaporation crystallization tank, a vacuumizing gas condensation liquid separation tank and a tail gas washing tower.
The solid material inlet of the sulfur paste pulping tank is communicated with a wet desulphurization device outside the battery compartment through a first pipeline; the slurry outlet of the sulfur paste pulping tank is communicated with the sulfur slurry concentration filter through a second pipeline; a first liquid outlet of the sulfur pulp concentration filter is communicated with a sulfur pulp buffer tank through a third pipeline, a second liquid outlet of the sulfur pulp concentration filter is communicated with a vacuum evaporation crystallization tank through a tenth pipeline, and a third liquid outlet of the sulfur pulp concentration filter is communicated with a tail gas washing tower through a twentieth pipeline; the slurry outlet of the sulfur slurry buffer tank is communicated with the sulfur melting kettle through a fourth pipeline; the first liquid outlet of the sulfur melting kettle is communicated with the liquid sulfur inlet of the liquid sulfur buffer tank through a fifth pipeline, and the second liquid outlet of the sulfur melting kettle is communicated with the vacuum evaporation crystallization tank through an eleventh pipeline; the liquid sulfur outlet of the liquid sulfur buffer tank is communicated with the organic matter decomposition kettle through a sixth pipeline; the first liquid outlet of the organic matter decomposition kettle is communicated with the liquid sulfur distillation kettle through a seventh pipeline; the first gas outlet of the liquid sulfur distillation kettle is communicated with a refined liquid sulfur storage tank through an eighth pipeline; and the liquid sulfur outlet of the refined liquid sulfur storage tank is communicated with the slicing machine through a ninth pipeline.
Further, the device also comprises a vacuum evaporation crystallization tank, a vacuumizing gas condensation liquid separation tank and a tail gas washing tower; the gas outlet of the vacuum evaporation crystallization tank is communicated with the vacuumizing gas condensation liquid separation tank through a twelfth pipeline; the gas outlet of the vacuumizing gas condensation and separation liquid tank is communicated with the tail gas washing tower through a thirteenth pipeline, the first liquid outlet of the vacuumizing gas condensation and separation liquid tank is communicated with the sulfur paste pulping tank through a sixteenth pipeline, and the second liquid outlet of the vacuumizing gas condensation and separation liquid tank is communicated with a clean water tank outside the boundary area through a twenty-four pipeline; the gas outlet of the organic matter decomposition kettle is communicated with the tail gas washing tower through a fourteenth pipeline; and a gas outlet of the tail gas washing tower is communicated with the outside incinerator through a twenty-third pipeline.
Further, a partition plate in the liquid sulfur buffer tank divides the liquid sulfur buffer tank into a liquid sulfur buffer zone and a slag discharging zone, and a liquid sulfur outlet of the liquid sulfur buffer zone of the liquid sulfur buffer tank is communicated with a sulfur inlet of the organic matter decomposition kettle sequentially through a liquid sulfur pump inlet pipeline, a liquid sulfur filter, a liquid sulfur pump and a sixth pipeline; the slag discharging outlet of the sulfur melting kettle is communicated with the slag discharging area of the liquid sulfur buffer tank through a seventeenth pipeline; and a slag discharge outlet of the liquid sulfur distillation kettle is communicated with a slag discharge area of the liquid sulfur buffer tank through an eighteenth pipeline.
Further, a sublimed sulfur gas outlet of the liquid sulfur distillation kettle is communicated with a refined liquid sulfur storage tank sequentially through a twenty-fifth pipeline, a sublimed sulfur cooler and an eighth pipeline; the non-condensable gas outlet of the sublimed sulfur cooler is communicated with the tail gas washing tower through a nineteenth pipeline; and a liquid sulfur outlet of the refined liquid sulfur storage tank is communicated with the slicing machine sequentially through a refined liquid sulfur pump inlet pipeline, a refined liquid sulfur pump and a ninth pipeline.
Further, a flash steam outlet of the vacuum evaporation crystallization tank is communicated with the vacuum pumping gas condensation liquid separation tank sequentially through a twenty-sixth pipeline, a flash steam condenser and a twelfth pipeline; and the gas outlet pipeline of the vacuumizing gas condensation separation liquid tank is communicated with the tail gas washing tower sequentially through a thirteenth pipeline, a vacuum pump and a vacuum pump exhaust pipeline.
Further, a first liquid outlet of the tail gas washing tower is communicated with a spraying liquid inlet of the tail gas washing tower sequentially through a washing circulating pump inlet pipeline, a washing circulating pump and a twenty-first pipeline; the liquid outlet of the washing circulating pump is communicated with the sulfur paste pulping tank through a twenty-two pipeline; and a gas outlet of the tail gas washing tower is connected and communicated with the incinerator outside the battery limits sequentially through an induced draft fan inlet pipeline, an induced draft fan and a twenty-third pipeline.
Further, the seventh pipeline is provided with a temperature communication switch valve; and a pressure control valve is arranged on the eleventh pipeline.
Further, the nitrogen distributor at the bottom of the organic sulfur decomposition kettle is connected with a system pipeline through a nitrogen inlet pipeline.
Further, the jacket layer of the sulfur melting kettle is heated by steam; the jacket layers of the organic matter decomposition kettle and the liquid sulfur distillation kettle are heated by heat conduction oil; the sublimed sulfur cooler is cooled by steam; and the flash steam condenser and the slicing machine are cooled by circulating water.
Further, the liquid sulfur buffer tank and the refined liquid sulfur storage tank are heated by steam tracing; the liquid sulfur pump and the refined liquid sulfur pump are heated by steam tracing; the liquid sulfur-containing pipelines such as the fifth pipeline, the sixth pipeline, the seventh pipeline, the eighth pipeline and the ninth pipeline are subjected to steam heat tracing; and the seventeenth pipeline and the eighteenth pipeline of the slag discharge pipeline are heated by steam.
Furthermore, the seventeenth pipeline and the eighteenth pipeline of the slag discharge pipeline are communicated with a low-level inlet of a slag discharge zone of the liquid sulfur buffer tank, so that a small amount of liquid sulfur carried in slag conveniently overflows to the liquid sulfur zone through the partition plate.
Further, the organic matter decomposition kettle and the liquid sulfur distillation kettle are arranged in a high-low position from top to bottom, and the liquid sulfur in the organic matter decomposition kettle overflows to the low-level liquid sulfur distillation kettle through the high position; the sublimed sulfur cooler and the refined liquid sulfur storage tank are arranged in a high-low position from top to bottom, and the liquid sulfur condensed from the sublimed sulfur flows into the refined liquid sulfur storage tank in a low position through potential difference; the sulfur slurry concentration filter and the sulfur slurry buffer tank are arranged at the upper and lower high and low positions, and the concentrated slurry automatically flows to the low-position sulfur slurry buffer tank through the high position; the flash evaporation steam condenser and the vacuumizing gas condensation liquid separation tank are arranged in a high position and a low position, and liquid condensed by the cooler flows into the vacuumizing gas condensation liquid separation tank in a relatively low position through potential difference; the vacuumizing gas condensation liquid separation tank and the sulfur paste pulping tank are arranged at the upper and lower positions, and liquid in the high-position vacuumizing gas condensation liquid separation tank flows to the low-position sulfur paste pulping tank through a height difference.
Also provides a method for refining sulfur from the desulfurized sulfur paste and a device implementing method, which are concretely as follows:
1) sulphur paste pulping, concentrating and filtering
Conveying crude sulfur paste from a wet desulphurization device to a receiving inlet of a sulfur paste pulping tank through a first pipeline, stirring the sulfur paste and condensed water from a sixteenth pipeline of a vacuum evaporation concentration unit in the sulfur paste pulping tank for pulping, conveying pulping liquid to a sulfur slurry concentration filter through a second pipeline by a pulping pump, conveying the filtered concentrated slurry to a sulfur slurry buffer tank through a third pipeline, conveying a large part of clean filtrate to a vacuum evaporation crystallization tank through a tenth pipeline to obtain concentrated salt solution, and conveying a small part of filtrate to a tail gas washing tower through a twentieth pipeline to serve as supplementary liquid.
2) Refining by melting sulphur and sublimation
The sulfur slurry is pumped from a slurry outlet of a sulfur slurry buffer tank and is sent into a sulfur melting kettle through a fourth pipeline, the sulfur slurry in the sulfur melting kettle is heated to 130-160 ℃ by a steam jacket, clear liquid separated from the upper layer of the sulfur melting kettle is sent to a vacuum evaporation crystallization tank through an eleventh pipeline and a pressure control valve for concentrating, crystallizing and separating secondary salt, liquid sulfur discharged from the lower layer of the sulfur melting kettle is sent to a liquid sulfur zone of a liquid sulfur buffer tank through a fifth pipeline, slag discharged from the lower layer is sent to a slag discharging zone of the liquid sulfur buffer tank through a seventeenth pipeline, liquid sulfur contained in the slag discharging zone overflows to the liquid sulfur buffer zone through a partition plate in the liquid sulfur buffer tank, the liquid sulfur is pumped from the liquid sulfur zone of the liquid sulfur buffer tank and is pumped into an organic matter decomposing kettle through a liquid sulfur filter and a sixth pipeline, the liquid sulfur in the organic matter decomposing kettle is heated by a heat-conducting oil jacket, most of oil gas and organic matter are sent to a tail gas washing tower through a fourteenth pipeline by nitrogen blown from the bottom of the organic matter decomposing kettle, heating liquid sulfur in the organic matter decomposition kettle to 300-330 ℃, then electrically communicating with a switch valve on a seventh pipeline to enable the heated liquid sulfur to automatically flow to a low-level liquid sulfur distillation kettle through the seventh pipeline, heating the liquid sulfur in the liquid sulfur distillation kettle to 445-460 ℃ by adopting a heat conduction oil jacket to obtain sublimed sulfur gas, mixing sublimed sulfur vapor with other gases in the kettle, discharging the mixture out of the kettle through an eighth pipeline to enter a sublimed sulfur cooler, discharging residual residues in the liquid sulfur distillation kettle into a liquid sulfur buffer tank slag discharging area through an eighteenth pipeline, condensing the sublimed sulfur vapor by adopting 150-180 ℃ steam in the sublimed sulfur cooler, flowing the condensed liquid sulfur into a low-level refined liquid sulfur storage tank through a high level difference, sending other non-condensable gases and gaseous organic matters to a tail gas washing tower through a nineteenth pipeline, pumping refined liquid sulfur from an outlet of the refined liquid sulfur storage tank by a refined liquid sulfur pump, sending the refined liquid sulfur into a slicing machine through a ninth pipeline to prepare finished product sulfur, the sulfur content of the product is more than or equal to 99.95 wt%.
3) Vacuum evaporation crystallization of waste water
Clean filtrate from a sulfur slurry concentration filter and clear liquid from a sulfur melting kettle both enter a vacuum evaporation crystallizing tank, the vacuum evaporation crystallizing tank realizes salt solution flash evaporation by virtue of vacuum pumping to obtain concentrated salt solution, liquid obtained by condensation of flash steam in a flash steam condenser flows into a vacuumizing gas condensation liquid tank through a twelfth pipeline, most of liquid discharged from the vacuumizing gas condensation liquid tank returns to a sulfur paste pulping tank through a sixteenth pipeline to realize continuous pulping, the other small part of liquid is discharged to a clear water tank outside a boundary region through a twenty fourth pipeline, and exhaust gas of a vacuum pump is sent to a tail gas washing tower through a thirteenth pipeline.
4) Exhaust gas purification
Three strands of non-condensable gas and gaseous organic matters from the organic matter decomposition kettle, the sublimed sulfur cooler and the vacuum exhaust gas enter the tail gas washing tower to be washed by countercurrent contact with clean washing liquid sent by a twenty-first pipeline at the outlet of the washing circulating pump, sulfur particles and a small amount of salt particles contained in the tail gas are removed, and the washed tail gas enters the draught fan through a fifteenth pipeline and is discharged to the incinerator through a twenty-third pipeline.
Compared with the prior art, the invention has the following advantages:
1. the device adopts a combined process of sulfur melting and sublimation, deep removal and separation are carried out on four phases of oil, water, salt and solid slag contained in the sulfur paste, the sulfur content of the sulfur solid obtained by refining the sulfur paste is more than or equal to 99.95 wt%, the superior grade in the industrial sulfur GB/T2449.1-2014 standard is reached, the resource and harmless treatment of the sulfur solid waste completely meets the requirements of national industrial policies, and extra income is brought to enterprises. Is particularly suitable for treating a large amount of sulfur paste which is a byproduct of a wet oxidation desulfurization device in the fields of coke gas, petrochemical gas and the like.
2. The device can realize the automatic, continuous and pollution-free industrial sulfur process of pulping from sulfur paste, filtering, concentrating, separating molten sulfur, distilling, vaporizing, condensing, curing, slicing and packaging, is controlled by a PLC system, and has no harmful gas leakage in the closed production process. The problems of low treatment efficiency, high manual operation intensity, low product purity and serious pollution of the conventional desulfurization sulfur paste are solved.
3. The device of the invention adopts the crystallization liquid of the filtrate and the sulfur melting clear liquid as the sulfur paste pulping liquid for recycling, thereby saving the consumption of public works.
Drawings
FIG. 1 is a schematic flow chart of the method and apparatus for refining sulfur from desulfurized sulfur paste according to the present invention.
Detailed Description
The invention is described in further detail below with reference to the figures and the specific embodiments.
As shown in figure 1, the device for refining sulfur from desulfurized sulfur paste comprises a sulfur paste slurrying tank 11 with a stirrer assembly 24, a sulfur paste concentration filter 12, a sulfur paste buffer tank 13 with a stirrer assembly 25, a sulfur melting kettle 14, a sulfur paste buffer tank 15, an organic matter decomposing kettle 16, a liquid sulfur distillation kettle 17, a liquid sulfur filter 18, a refined liquid sulfur storage tank 19, a slicing machine 20, an exhaust gas washing tower 21 with a filler 30, a vacuum evaporation crystallization tank 22 in a vacuum evaporation crystallization unit, a flash steam condenser 156, a vacuumizing gas condensation separation tank 23 and a vacuum pump 157. Wherein, a partition 26 is arranged in the liquid sulfur buffer tank 15 to divide the liquid sulfur buffer tank 15 into a liquid sulfur zone 15A and a slag discharging zone 15B. The sulfur slurry concentration filter 12 is arranged above the sulfur slurry buffer tank 13 and is connected with the sulfur slurry buffer tank through a third pipeline 1103; the organic matter decomposition kettle 16 is arranged above the liquid sulfur distillation kettle 17 and is connected with the liquid sulfur distillation kettle 17 through a seventh pipeline 1107; the sublimed sulfur cooler 154 is arranged above the refined liquid sulfur storage tank 19 and connected with the refined liquid sulfur storage tank through an eighth pipeline 1108; the flash steam condenser 156 is connected with the twelfth pipeline 1112 above the vacuumizing gas condensation separation tank 23; the vacuumizing air condensation separation liquid tank 23 is arranged above the sulfur paste pulping tank 11 and is connected with the sulfur paste pulping tank through a sixteenth pipeline 1116; the seventeenth pipeline 1117 and the eighteenth pipeline 1118 are communicated with the low-level inlet 15C of the slag discharging zone 15B of the liquid sulfur buffer slot 15, and a small amount of liquid sulfur carried in the slag discharging zone 15B overflows to the liquid sulfur zone 15A through the partition plate 26.
A solid material inlet 11a of the sulfur paste pulping tank 11 is connected with the sulfur paste from the wet desulphurization device through a first pipeline 1101, and a first liquid outlet 11b of the sulfur paste pulping tank 11 is communicated with the sulfur paste concentration filter 12 through a sulfur paste inlet pipeline 1511, the pulping pump 151 and a second pipeline 1102 in sequence; a first liquid outlet 12a of the sulfur slurry concentration filter 12 is communicated with the sulfur slurry buffer tank 13 through a third pipeline 1103, a second liquid outlet 12b of the sulfur slurry concentration filter 12 is communicated with the vacuum evaporation crystallization tank 22 through a tenth pipeline 1110, and the other pipeline 1120 of the second liquid outlet 12b of the sulfur slurry concentration filter 12 is communicated with the tail gas washing tower 21; the liquid outlet 13a of the sulfur slurry buffer tank 13 is communicated with the sulfur melting kettle 14 through an inlet pipeline 1521 of the sulfur slurry pump 152, the sulfur slurry pump 152 and a fourth pipeline 1104 in sequence; a first liquid outlet 14a of the sulfur melting kettle 14 is communicated with the vacuum evaporation crystallizer 22 through an eleventh pipeline 1111, a second liquid outlet 14B of the sulfur melting kettle 14 is communicated with a liquid sulfur zone 15A of the sulfur slurry buffer slot 15 through a fifth pipeline 1105, and the other pipeline 1117 of the second liquid outlet 14B of the sulfur melting kettle 14 is communicated with a slag tapping zone 15B of the sulfur slurry buffer slot 15; a liquid outlet 15A of the liquid sulfur zone 15A of the sulfur slurry buffer tank 15 is communicated with the organic matter decomposition kettle 16 through an inlet pipeline 1531 of the liquid sulfur pump 153, the liquid sulfur filter 18, the liquid sulfur pump 153 and a sixth pipeline 1106 in sequence; a liquid outlet 16a of the organic matter decomposition kettle 16 is communicated with the liquid sulfur distillation kettle 17 through a seventh pipeline 1107, and a gas outlet 16b of the organic matter decomposition kettle 16 is communicated with the tail gas washing tower 21 through a fourteenth pipeline 1114; a liquid outlet 17a of the liquid sulfur distillation kettle 17 is communicated with a slag tapping zone 15B of the liquid sulfur buffer slot 15 through an eighteenth pipeline 1118; the gas outlet 17b of the liquid sulfur distillation kettle 17 is communicated with the refined liquid sulfur storage tank 19 through a twenty-fifth pipeline 1125, the sublimed sulfur cooler 154 and an eighth pipeline 1108 in turn; a liquid outlet 19a of the refined liquid sulfur storage tank 19 is communicated with the slicing machine 20 through an inlet pipeline 1551 of the refined liquid sulfur pump 155, the refined liquid sulfur pump 155 and a ninth pipeline 1109 in sequence; the outlet 20a of the slicer 20 is provided with a sulfur pellet line 2011.
In addition, a gas outlet 22a of the vacuum evaporation crystallization tank 22 is communicated with the vacuumizing gas condensation separation liquid tank 23 sequentially through a twenty-sixth pipeline 1126, the flash steam condenser 156 and a twelfth pipeline 1112, and a liquid outlet 22b of the vacuum evaporation crystallization tank 22 is provided with a concentrated salt liquid pipeline 2211; a liquid outlet 23a of the vacuumizing gas condensation separation liquid tank 23 is communicated with the sulfur paste pulping tank 11 through a sixteenth pipeline 1116, the other pipeline 1124 of the liquid outlet 23a of the vacuumizing gas condensation separation liquid tank 23 is communicated with the tail gas washing tower 21, and a gas outlet 23b of the vacuumizing gas condensation separation liquid tank 23 is communicated with the tail gas washing tower 21 through an inlet pipeline 1571 of a vacuum pump 157, the vacuum pump 157 and a thirteenth pipeline 1113 in sequence; the non-condensable gas outlet 154a of the sublimed sulfur cooler 154 is communicated with the tail gas washing tower 21 through a nineteenth pipeline 1119; the liquid outlet 21a of the tail gas washing tower 21 is communicated with the liquid inlet 21b of the tail gas washing tower 21 through a washing circulating pump 158 inlet pipeline 1581, a washing circulating pump 158 and a twenty-first pipeline 1121 in sequence, and the gas outlet 21c of the tail gas washing tower 21 is communicated with the external incinerator through a fifteenth pipeline 1115, an induced draft fan 159 and a twenty-third pipeline 1123 in sequence.
In addition, the outlet 158a of the washing and circulating pump 158 is communicated with the sulfur paste making tank 11 through another pipeline 1122 so as to return the washed sulfur particles to be filtered again; the tail gas scrubber 21 is provided with random packing 30 and a wire mesh demister assembly 31.
In addition, a seventh pipeline 1107 for communicating the organic matter decomposition kettle 16 with the liquid sulfur distillation kettle 17 is provided with a switch valve 28 communicated with the temperature, and the switch valve 28 is communicated after the temperature of the liquid sulfur in the organic matter decomposition kettle 16 is heated to the set temperature of 300-330 ℃ so as to allow the heated liquid sulfur to automatically flow to the liquid sulfur distillation kettle 17; a pressure control valve 27 is arranged on an eleventh pipeline 1111 at the clear liquid outlet of the sulfur melting kettle 14 and is used for maintaining the pressure of the sulfur melting kettle 14 to be more than 0.6 MPaG.
In addition, the bottom of the organic sulfur decomposition kettle 16 is provided with a nitrogen distributor 29 for rapidly extracting most of oil gas and organic matters contained in the liquid sulfur by injecting nitrogen.
In addition, the jacket layer 14A of the sulfur melting kettle 14 is heated by steam; the jacket layer 16A of the organic matter decomposition kettle 16 adopts a heat conduction oil medium to realize heating and temperature rise; the jacket layer 17A of the liquid sulfur distillation kettle 17 adopts a heat-conducting oil medium to realize heating and temperature rise; the sublimed sulfur cooler 154 realizes condensation through a steam medium at 150-180 degrees; the flash steam condenser 156 condenses flash steam by circulating water; the slicing machine 20 realizes the cooling of the liquid sulfur by circulating water, the cooled solid sulfur is cut into flaky sulfur by the slicing machine 20, and the formed flaky sulfur is bagged and transported outside.
In addition, the seventeenth pipeline 1117 and the eighteenth pipeline 1118 are communicated with the low-level inlet 15B of the slag discharging zone 15B of the liquid sulfur buffer slot 15, so that a small amount of liquid sulfur carried in the slag can overflow to the liquid sulfur zone 15A through the partition plate 26.
The method for refining the sulfur from the desulfurized sulfur paste specifically comprises the following steps:
1) sulphur paste pulping, concentrating and filtering
The method comprises the steps of conveying crude sulfur paste from a wet desulphurization device to a receiving inlet 11a of a sulfur paste pulping tank 11 through a first pipeline 1101, stirring and pulping condensed water from a sixteenth pipeline 1116 of a sulfur paste and wastewater vacuum evaporation concentration unit in the sulfur paste pulping tank 11, conveying pulping liquid to a sulfur slurry concentration filter 12 through a second pipeline 1102 through a pulping pump 151, filtering the concentrated slurry to a sulfur slurry buffer tank 13 through a third pipeline 1103, conveying most of clean filtrate to a vacuum evaporation crystallization tank 22 through a tenth pipeline 1110 to obtain concentrated salt solution, and conveying a small part of filtrate to an exhaust washing tower 20 through a twentieth pipeline 1120 to serve as make-up liquid.
2) Refining by melting sulphur and sublimation
The sulfur slurry is pumped out from a slurry outlet 13a of a sulfur slurry buffer groove 13 by a sulfur slurry pump 152 and is sent into a sulfur melting kettle 14 through a fourth pipeline 1104, the sulfur slurry in the sulfur melting kettle 14 is heated to 130-160 ℃ by a steam jacket 14A, clear liquid separated from the upper layer of the sulfur melting kettle 14 is sent to a vacuum evaporation crystallizer 22 for concentration, crystallization and separation of secondary salt through an eleventh pipeline 1111 and a pressure control valve 27, liquid sulfur discharged from the lower layer of the sulfur melting kettle 14 is sent to a liquid sulfur zone 15A of a 1105 liquid sulfur buffer groove 15 through a fifth pipeline, slag discharged from the lower layer is sent to a slag discharging zone 15B of the liquid sulfur buffer groove 15 through a seventeenth pipeline 1117, liquid sulfur contained in the slag discharging zone overflows to the liquid sulfur buffer groove 15A through a partition plate 26 in the liquid sulfur buffer groove 15, the liquid sulfur is pumped out from the liquid sulfur zone 15A of the liquid sulfur buffer groove 15 and is pumped into an organic matter decomposing kettle 16 through a liquid sulfur filter 18 and a sixth pipeline 1106, the liquid sulfur in the organic matter decomposing kettle 16 is heated by the jacket 16A, and most of the oil gas and the organic matter are blown into a nitrogen decomposing kettle 16 through a gas stripping pipeline 114 Sending the sulfur to a tail gas washing tower 20, heating the liquid sulfur in the organic matter decomposition kettle 16 to 300-330 ℃, electrically communicating the switch valve 28 on a seventh pipeline 1107 to allow the heated liquid sulfur to automatically flow to a low-level liquid sulfur distillation kettle 17 through the seventh pipeline 1107, heating the liquid sulfur in the liquid sulfur distillation kettle 17 to 445-460 ℃ by using a heat conduction oil jacket 17A to obtain sublimed sulfur gas, mixing the sublimed sulfur vapor with other gases in the kettle, discharging the mixture out of the liquid sulfur distillation kettle 17 through a twenty-fifth pipeline 1125 to enter a sublimed sulfur cooler 154, discharging the residue in the liquid sulfur distillation kettle 17 into a liquid sulfur buffer slot 15 slag tapping zone 15B through an eighteenth pipeline 1118, condensing the sublimed sulfur vapor by using 150-180 ℃ steam in the sublimed sulfur cooler 154, flowing the condensed liquid sulfur into a low-level refined liquid sulfur storage tank 19 through an eighth pipeline 1108, and sending other non-condensable gases and gaseous organic matters to the tail gas washing tower 21 through a nineteenth pipeline 1119, refined liquid sulfur is pumped out from an outlet of a refined liquid sulfur storage tank 19 by a refined liquid sulfur pump 155 and is sent into a slicing machine 20 through a ninth pipeline 1109 to be sliced into finished product sulfur, and the sulfur content of the product is more than or equal to 99.95 wt%.
3) Vacuum evaporation and concentration of waste water
Clean filtrate from the sulfur slurry concentration filter 12 and clear liquid from the sulfur melting kettle 14 both enter the vacuum evaporation crystallizing tank 22, the vacuum evaporation crystallizing tank 22 is vacuumized by the vacuum pump 157 to realize salt solution flash evaporation to obtain concentrated salt solution, liquid condensed by flash steam condenser 156 of flash steam flows into the vacuum air condensation separation liquid tank 23 through the twelfth pipeline 1112, most of liquid discharged from the vacuum air condensation separation liquid tank 23 returns to the sulfur paste pulping tank 11 through the sixteenth pipeline 1116 to realize continuous pulping, the other small part is discharged to a clear water tank outside the boundary region through the twenty-fourth pipeline 1124, and gas discharged by the vacuum pump 156 is sent to the tail gas washing tower 21 through the thirteenth pipeline 1113.
4) Exhaust gas purification
Three strands of non-condensable gas and gaseous organic matters discharged from the organic matter decomposition kettle 16, the sublimed sulfur cooler 154 and the vacuum pump 157 enter the tail gas washing tower 21 to be in countercurrent contact with clean washing liquid sent by a twenty-first pipeline 1121 at the outlet of the washing circulating pump 158 for washing, sulfur particles and a small amount of salt particles contained in the tail gas are removed, and the washed tail gas enters the induced draft fan 159 through a fifteenth pipeline 1115 and is discharged to the incinerator through a twenty-third pipeline 1123.
Claims (10)
1. A device for refining sulfur from desulfurized sulfur paste comprises a sulfur paste preparation tank (11), a sulfur paste concentration filter (12), a sulfur paste buffer tank (13), a sulfur melting kettle (14), a liquid sulfur buffer tank (15), an organic matter decomposition kettle (16), a liquid sulfur distillation kettle (17), a refined liquid sulfur storage tank (19), a vacuum evaporation crystallization tank (22), a vacuumizing gas condensation separation tank (23) and a tail gas washing tower (21);
a solid material inlet (11a) of the sulfur paste pulping tank (11) is communicated with a wet desulphurization device outside a battery compartment through a first pipeline (1101); the slurry outlet of the sulfur paste pulping tank (11) is communicated with the sulfur slurry concentration filter (12) through a second pipeline (1102); a first liquid outlet (12a) of the sulfur pulp concentration filter (12) is communicated with a sulfur pulp buffer tank (13) through a third pipeline (1103), a second liquid outlet (12b) of the sulfur pulp concentration filter (12) is communicated with a vacuum evaporation crystallization tank (22) through a tenth pipeline (1110), and the other path of the outlet (12b) of the sulfur pulp concentration filter (12) is communicated with an exhaust gas washing tower (21) through a twentieth pipeline (1120); the slurry outlet (13a) of the sulfur slurry buffer tank (13) is communicated with the sulfur melting kettle (14) through a fourth pipeline (1104); a first liquid outlet (14a) of the sulfur melting kettle (14) is communicated with the liquid sulfur buffer tank (15) through a fifth pipeline (1105), and a second liquid outlet (14b) of the sulfur melting kettle (14) is communicated with the vacuum evaporation crystallization tank (22) through an eleventh pipeline (1111); the liquid sulfur outlet (15a) of the liquid sulfur buffer tank (15) is communicated with the organic matter decomposition kettle (16) through a sixth pipeline (1106); a first liquid outlet (16a) of the organic matter decomposition kettle (16) is communicated with a liquid sulfur distillation kettle (17) through a seventh pipeline (1107); a first gas outlet (17b) of the liquid sulfur distillation kettle (17) is communicated with a refined liquid sulfur storage tank (19) through an eighth pipeline (1108); and a liquid sulfur outlet (19a) of the refined liquid sulfur storage tank (19) is communicated with a slicing machine (20) through a ninth pipeline (1109).
2. The apparatus according to claim 1, wherein the apparatus further comprises: the gas outlet (22a) of the vacuum evaporation crystallization tank (22) is communicated with the vacuumizing gas condensation liquid separation tank (23) through a twelfth pipeline (1112); a gas outlet (23a) of the vacuumizing gas condensation liquid separation tank (23) is communicated with the tail gas washing tower (21) through a thirteenth pipeline (1113), a first liquid outlet (23b) of the vacuumizing gas condensation liquid separation tank (23) is communicated with the sulfur paste pulping tank (11) through a sixteenth pipeline (1116), and the other path of liquid of the vacuumizing gas condensation liquid separation tank (23) is communicated with a clean water tank outside a boundary area through a twenty-four pipeline (1124); the gas outlet (16b) of the organic matter decomposition kettle (16) is communicated with the tail gas washing tower (21) through a fourteenth pipeline (1114); and a gas outlet (21c) of the tail gas washing tower (21) is communicated with an incinerator outside a battery limit area through a twenty-third pipeline (1115).
3. The apparatus according to claim 1, wherein the apparatus further comprises: a partition plate (26) is arranged in the liquid sulfur buffer tank (15), the partition plate (26) divides the liquid sulfur buffer tank (15) into a liquid sulfur buffer area (15A) and a slag discharging area (15B), and a liquid sulfur outlet (15A) of the liquid sulfur buffer area (15A) of the liquid sulfur buffer tank (15) is communicated with the organic matter decomposition kettle (16) through an inlet pipeline (1531) of a liquid sulfur pump (153), a liquid sulfur filter (18), the liquid sulfur pump (153) and a sixth pipeline (1106) in sequence; a slag discharge outlet (14B) of the sulfur melting kettle (14) is communicated with a slag discharge area (15B) of the liquid sulfur buffer tank (15) through a seventeenth pipeline (1117); and a slag discharge outlet (17a) of the liquid sulfur distillation kettle (17) is communicated with a slag discharge area (15B) of the liquid sulfur buffer tank (15) through an eighteenth pipeline (1118).
4. The apparatus according to claim 1, wherein the apparatus further comprises: the outlet (17b) of the sublimed sulfur gas of the liquid sulfur distillation kettle (17) is communicated with the refined liquid sulfur storage tank (19) through a twenty-fifth pipeline (1125), a sublimed sulfur cooler (154) and an eighth pipeline (1108) in sequence; the non-condensable gas outlet (154a) of the sublimed sulfur cooler (154) is communicated with the tail gas washing tower (21) through a nineteenth pipeline (1119); and a liquid sulfur outlet (19a) of the refined liquid sulfur storage tank (19) is communicated with the slicing machine (20) through an inlet pipeline (1551) of the refined liquid sulfur pump (155), the refined liquid sulfur pump (155) and a ninth pipeline (1109) in sequence.
5. The apparatus according to claim 1 or 2, wherein: the flash steam outlet (22a) of the vacuum evaporation crystallization tank (22) is communicated with the vacuum pumping gas condensation liquid separation tank (23) through a twenty-sixth pipeline (1126), a flash steam condenser (156) and a twelfth pipeline (1112) in sequence; and a gas outlet (23b) of the vacuumizing gas condensation liquid separation tank (23) is communicated with the tail gas washing tower (21) through an inlet pipeline (1571) of a vacuum pump (23), a vacuum pump (157) and a thirteenth pipeline (1113) in sequence.
6. The apparatus according to claim 1 or 2, wherein: a first liquid outlet (21a) of the tail gas washing tower (21) is communicated with a spraying liquid inlet (21b) of the tail gas washing tower (21) through a washing circulating pump inlet pipeline (1581), a washing circulating pump (158) and a twenty-first pipeline (1121) in sequence; the liquid outlet (158a) of the washing circulating pump (158) is communicated with the sulfur paste pulping tank (11) through a twenty-two pipeline (1122); and a gas outlet (21c) of the tail gas washing tower (21) is communicated with an incinerator outside a battery compartment sequentially through an induced draft fan inlet pipeline (1115), an induced draft fan (158) and a twenty-third pipeline (1123).
7. The apparatus according to claim 1, wherein the apparatus further comprises: the liquid sulfur buffer tank (15) and the refined liquid sulfur storage tank (19) are heated by steam; the liquid sulfur pump (153) and the refined liquid sulfur pump (155) are heated by steam; liquid sulfur-containing pipelines such as the fifth pipeline (1105), the sixth pipeline (1106), the seventh pipeline (1107), the eighth pipeline (1108) and the ninth pipeline (1109) are subjected to steam tracing; and the seventeenth pipeline (1117) and the eighteenth pipeline (1118) of the slag discharge pipeline are subjected to steam heat tracing.
8. The apparatus according to claim 3, wherein the apparatus further comprises: and a seventeenth pipeline (1117) and an eighteenth pipeline (1118) of the slag discharge pipeline are communicated with a low-level inlet (15B) of a slag discharge area (15B) of the liquid sulfur buffer tank (15), so that a small amount of liquid sulfur carried in slag can overflow to the liquid sulfur area (15A) through a partition plate (26).
9. The apparatus according to claim 1, wherein the apparatus further comprises: the organic matter decomposition kettle (16) and the liquid sulfur distillation kettle (17) are arranged in a vertical high-low position, and liquid sulfur in the organic matter decomposition kettle (16) overflows to the low-level liquid sulfur distillation kettle (17) through a high position; the sublimed sulfur cooler (154) and the refined liquid sulfur storage tank (19) are arranged in a high-low position, and the liquid sulfur condensed from the sublimed sulfur flows into the refined liquid sulfur storage tank (19) in a low position through a potential difference; the sulfur slurry concentration filter (12) and the sulfur slurry buffer tank (13) are arranged in a vertical high-low position, and the concentrated slurry automatically flows to the low-position sulfur slurry buffer tank (13) through the high position; the flash steam condenser (156) and the vacuumizing gas condensation liquid separation tank (23) are arranged at the upper and lower positions, and condensed liquid flows into the vacuumizing gas condensation liquid separation tank (23) at the relatively lower position through a potential difference; the vacuumizing gas condensation liquid separation tank (23) and the sulfur paste pulping groove (11) are arranged in a vertical high-low position mode, and liquid in the high-position vacuumizing gas condensation liquid separation tank (23) flows to the low-position sulfur paste pulping groove (11) through a height difference.
10. A method for refining sulfur from desulfurized sulfur paste comprises the following steps:
1) sulphur paste pulping, concentrating and filtering
Conveying crude sulfur paste from a wet desulphurization device to a receiving inlet (11a) of a sulfur paste pulping tank (11) through a first pipeline (1101), stirring and pulping condensed water from a sixteenth pipeline (1116) of a sulfur paste and wastewater vacuum evaporation concentration unit in the sulfur paste pulping tank (11), conveying the pulping liquid to a sulfur slurry concentration filter (12) through a second pipeline (1102) through a pulping pump (151), filtering the concentrated slurry, conveying the concentrated slurry to a sulfur slurry buffer tank (13) through a third pipeline (1103), conveying the majority of clean filtrate to a vacuum evaporation crystallization tank (22) through a tenth pipeline (1110) to obtain concentrated salt solution, and conveying a small part of the filtrate to a tail gas washing tower (20) through a twentieth pipeline (1120) to be used as make-up liquid;
2) refining by melting sulphur and sublimation
The sulfur slurry is pumped out from a slurry outlet (13a) of a sulfur slurry buffer groove (13) by a sulfur slurry pump (152) and is sent into a sulfur melting kettle (14) through a fourth pipeline (1104), the sulfur slurry in the sulfur melting kettle (14) is heated to 130-160 ℃ by a steam jacket (14A), clear liquid separated from the upper layer of the sulfur melting kettle (14) is sent to a vacuum evaporation crystallization tank (22) through an eleventh pipeline (1111) and a pressure control valve (27) to concentrate, crystallize and separate secondary salt, liquid sulfur discharged from the lower layer of the sulfur melting kettle (14) is sent to a liquid sulfur region (15A) of a liquid sulfur buffer groove (15) through a fifth pipeline (1105), slag discharged from the lower layer is sent to a slag discharging region (15B) of the liquid sulfur buffer groove (15) through a seventeenth pipeline (1117), liquid sulfur contained in the slag discharging region overflows to the liquid sulfur buffer region (15A) through a partition plate (26) in the liquid sulfur buffer groove (15), and the liquid sulfur is pumped into the liquid sulfur buffer groove (15A) from the liquid sulfur buffer groove (15A) and is sent into a liquid sulfur filter (1106), liquid sulfur in the organic matter decomposing kettle (16) is heated by a heat conducting oil jacket (16A), most of oil gas and organic matter are lifted by nitrogen gas blown from the bottom of the organic matter decomposing kettle (16) and sent to a tail gas washing tower (20) through a fourteenth pipeline (114), the liquid sulfur in the organic matter decomposing kettle (16) is electrically communicated with a switch valve (28) on a seventh pipeline (1107) after being heated to 300-330 ℃, the heated liquid sulfur flows to a low-level liquid sulfur distilling kettle (17) through the seventh pipeline (1107), the liquid sulfur in the liquid sulfur distilling kettle (17) is heated to 445-460 ℃ by the heat conducting oil jacket (17A) to obtain sublimed sulfur gas, the sublimed sulfur vapor and other gases in the kettle are mixed and discharged out of the liquid sulfur distilling kettle (17) through a pipeline (1701) to enter a sublimed sulfur cooler (154), and residues remained in the liquid sulfur distilling kettle (17) are discharged into a liquid sulfur buffer zone (15B) through an eighteen pipeline (1118), the sublimed sulfur cooler (154) condenses sublimed sulfur vapor by adopting 150-180 ℃ steam, the condensed liquid sulfur flows into a low-level refined liquid sulfur storage tank (19) through an eighth pipeline (1108), other non-condensable gases and gaseous organic matters are sent to a tail gas washing tower (21) through a nineteenth pipeline (1119), the refined liquid sulfur is pumped out from an outlet of the refined liquid sulfur storage tank (19) by a refined liquid sulfur pump (155) and sent into a slicing machine (20) through a ninth pipeline (1109) to be sliced into finished product sulfur, and the sulfur content of the product is more than or equal to 99.95 wt%;
3) vacuum evaporation and concentration of waste water
Clean filtrate from a sulfur slurry concentration filter (12) and clear liquid from a sulfur melting kettle (14) both enter a vacuum evaporation crystallization tank (22), the vacuum evaporation crystallization tank (22) realizes salt solution flash evaporation by virtue of vacuum pumping of a vacuum pump (157), concentrated salt solution is obtained, liquid condensed by flash steam through a flash steam condenser (156) flows into a vacuum gas condensation liquid tank (23) through a twelfth pipeline (1112), most of liquid discharged from the vacuum gas condensation liquid tank (23) returns to a sulfur paste pulping tank (11) through a sixteenth pipeline (1116) to realize continuous pulping, the other small part of liquid is discharged to a clear water tank outside a boundary region through a twenty-four pipeline (1124), and gas discharged from the vacuum pump 156 is sent to a tail gas washing tower (21) through a thirteenth pipeline (1113);
4) exhaust gas purification
Three strands of non-condensable gas and gaseous organic matters discharged from the organic matter decomposition kettle (16), the sublimed sulfur cooler (154) and the vacuum pump (157) enter the tail gas washing tower (21) to be washed by countercurrent contact with clean washing liquid sent by a twenty-first pipeline (1121) at the outlet of the washing circulating pump (158), sulfur particles and a small amount of salt particles contained in tail gas are removed, and the washed tail gas enters the induced draft fan (159) through a fifteenth pipeline (1115) and is discharged to the incinerator through a twenty-third pipeline (1123).
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