CN221107027U - Energy-saving carbon disulfide continuous rectification system - Google Patents
Energy-saving carbon disulfide continuous rectification system Download PDFInfo
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- CN221107027U CN221107027U CN202323123811.4U CN202323123811U CN221107027U CN 221107027 U CN221107027 U CN 221107027U CN 202323123811 U CN202323123811 U CN 202323123811U CN 221107027 U CN221107027 U CN 221107027U
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- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 title claims abstract description 159
- 238000004821 distillation Methods 0.000 claims abstract description 108
- 239000012043 crude product Substances 0.000 claims abstract description 20
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000010992 reflux Methods 0.000 claims abstract description 15
- 239000011593 sulfur Substances 0.000 claims abstract description 15
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 15
- QGJOPFRUJISHPQ-NJFSPNSNSA-N carbon disulfide-14c Chemical compound S=[14C]=S QGJOPFRUJISHPQ-NJFSPNSNSA-N 0.000 claims abstract description 7
- 238000003860 storage Methods 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 50
- 238000012856 packing Methods 0.000 claims description 17
- 238000007789 sealing Methods 0.000 claims description 15
- 239000000498 cooling water Substances 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 9
- 239000012071 phase Substances 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 3
- 239000007791 liquid phase Substances 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 210000001503 joint Anatomy 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 8
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 238000007670 refining Methods 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 30
- 238000000926 separation method Methods 0.000 description 12
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 11
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 11
- 239000000463 material Substances 0.000 description 10
- 238000001816 cooling Methods 0.000 description 9
- 230000000694 effects Effects 0.000 description 6
- 239000006260 foam Substances 0.000 description 6
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- 239000000047 product Substances 0.000 description 5
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- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 230000017525 heat dissipation Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 229920000298 Cellophane Polymers 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000000110 cooling liquid Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 239000013527 degreasing agent Substances 0.000 description 1
- 238000005237 degreasing agent Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
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- 239000007792 gaseous phase Substances 0.000 description 1
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- 229910010272 inorganic material Inorganic materials 0.000 description 1
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- 238000011031 large-scale manufacturing process Methods 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model provides an energy-saving continuous rectification system for carbon disulfide, which belongs to the technical field of carbon disulfide production and comprises the following components: CS 2 crude product tank, primary distillation tower and rectifying tower, the rectifying tower is equipped with top condenser; the tube side inlet of the tower top condenser is connected with the tower top outlet of the rectifying tower, the tube side outlet of the tower top condenser is connected with the buffer tank, the shell side inlet of the tower top condenser is connected with the CS 2 crude product tank outlet through a magnetic pump, and the shell side outlet of the tower top condenser is connected with the primary tower inlet; the bottom of the primary distillation tower is provided with a reboiler for providing a heat source of the primary distillation tower, and the bottom of the primary distillation tower is connected with a feed inlet of the rectifying tower through a rectifying feed pump; the buffer tank is connected with a reflux port of the rectifying tower and is connected with a CS 2 fine tank through a pipeline; the outlet of the tower bottom of the rectifying tower is connected with a sulfur storage tank. The system realizes continuous rectification of the carbon disulfide, has high rectification efficiency, convenient operation and high automation degree, and reduces the circulating water consumption and the refrigerating capacity of the system and the energy consumption required by CS 2 refining.
Description
Technical Field
The utility model relates to the technical field of carbon disulfide production, in particular to an energy-saving carbon disulfide continuous rectification system.
Background
Carbon disulfide is an inorganic compound, is colorless liquid, is a common solvent, and can dissolve elemental sulfur. Besides being used as a solvent, carbon disulfide is mainly used as a raw material for manufacturing cellophane and artificial fibers, an agricultural pesticide and an intermediate of an ore floatation agent, and can also be used as an aviation accelerator, a rubber vulcanization accelerator, an anticorrosive agent for equipment and pipelines in an ammonia treatment system, a wool degreasing agent, a clothes stain remover, a parting agent for paint and varnish, an aviation fuel additive and the like.
At present, most enterprises adopt a semicoke method to produce carbon disulfide, namely semi-coke and sulfur are used as production raw materials, sulfur is gasified at high temperature and chemically reacts with carbon element to produce carbon disulfide, and meanwhile, waste gas such as hydrogen sulfide, carbon monoxide and the like and impurities such as sulfur, carbon and the like can be produced as byproducts. And removing sulfur from the generated carbon disulfide to obtain a crude product, and rectifying to remove impurities in the crude product carbon disulfide to obtain a refined carbon disulfide finished product. If batch rectification is adopted in carbon disulfide refining, the problems of low separation efficiency, high energy consumption, inconvenient operation and low automation degree are solved. Therefore, when the domestic carbon disulfide rectification technology is applied to large-scale production, the double-tower continuous rectification separated by hydrogen sulfide removal and desulfurization and sulfoacid is mainly adopted, but the prior art still has the following problems: the traditional rectifying system is generally used for achieving the refining purpose, energy conservation is less considered, each tower is provided with a steam heating reboiler or a jacket, each tower top air outlet is provided with a circulating water cooling condenser, the consumption of steam and circulating cooling water is large, the energy consumption level is always high, the heat of materials at the tower top of the rectifying tower is often not comprehensively recovered and utilized, and energy waste is caused. Therefore, a rectification system capable of reducing energy consumption is needed to achieve the purpose of energy saving.
Disclosure of utility model
The utility model provides an energy-saving carbon disulfide continuous rectification system which is used for solving the problems of heat not comprehensively recycled and energy waste caused by higher consumption of steam and circulating cooling water and higher energy consumption level of the existing rectification system.
The utility model provides an energy-saving carbon disulfide continuous rectification system, which has the technical key points that: CS 2 crude product tank, primary distillation tower and rectifying tower, the rectifying tower is equipped with top condenser; the tube side inlet of the tower top condenser is connected with the tower top outlet of the rectifying tower, the tube side outlet of the tower top condenser is connected with the buffer tank, the shell side inlet of the tower top condenser is connected with the CS 2 crude product tank outlet through a magnetic pump, and the shell side outlet of the tower top condenser is connected with the primary tower inlet; the bottom of the primary distillation tower is provided with a reboiler for providing a heat source of the primary distillation tower, and the bottom of the primary distillation tower is connected with a feed inlet of the rectifying tower through a rectifying feed pump; the buffer tank is connected with a reflux port of the rectifying tower and is connected with a CS 2 fine tank through a pipeline; the outlet of the tower bottom of the rectifying tower is connected with a sulfur storage tank.
Further, a tower top exhaust port on a tower top end enclosure of the primary distillation tower is connected with the Claus furnace through a pipeline; the primary distillation tower is provided with a built-in tower top cooler, and the tower top cooler is arranged below a tower top head of the primary distillation tower; the shell of the tower top cooler has the same diameter as the primary distillation tower body, and is in sealing connection with the primary distillation tower body through a top plate and a bottom plate, and the side wall of the shell is communicated with a cooling water inlet and a cooling water outlet; a plurality of heat exchange tubes are arranged in the shell along the axial direction of the primary distillation tower body, a plurality of return tubes are arranged around the heat exchange tubes, and the heat exchange tubes and the return tubes penetrate through the top plate and the bottom plate to be communicated with the primary distillation tower body up and down of the shell; an arch cover is arranged above the top plate, a plurality of air outlets are arranged on the arch cover, and a plurality of liquid discharging holes are reserved between the arch cover and the inner wall of the primary distillation tower body.
Further, the pipe orifice of the heat exchange pipe extends upwards to be higher than the top plate of the shell; the air outlet hole on the arch cover and the pipe orifice of the heat exchange pipe are arranged in a staggered way; the liquid outlet hole is aligned with the return pipe in the vertical direction.
Further, an extension spring is arranged in the return pipe, the upper end of the extension spring is connected with a fixing frame fixedly arranged in the return pipe, the lower end of the extension spring is connected with a sealing cover, and the sealing cover is abutted with the lower end of the return pipe through the extension spring.
Further, a downward-inclined guide plate is arranged below the return pipe, the upper inclined end of the guide plate is fixedly connected to the inner wall of the primary distillation tower body, and the lower inclined end of the guide plate faces the central position of the primary distillation tower body.
Further, the heat exchange tube is a straight tube or a spiral tube.
Further, a silk screen foam remover is arranged in the primary distillation tower, and the silk screen foam remover is arranged between the arch cover and the head of the top of the primary distillation tower.
Further, the primary distillation tower and the rectifying tower are all filled with stainless steel ripple; the packing of the primary distillation tower is divided into an upper packing region and a lower packing region, and a primary distillation tower inlet is arranged on the primary distillation tower body between the upper packing region and the lower packing region.
Further, the reboiler of the primary distillation tower adopts any one of kettle type, thermosiphon type, jacket type and built-in indirect heating reboiler.
Further, a recooler is arranged between the top exhaust port of the primary distillation tower and the Claus furnace, a tube side inlet of the recooler is connected with the top exhaust port, a tube side gas phase outlet of the recooler is connected with the Claus furnace, and a tube side liquid phase outlet of the recooler is connected with the CS 2 fine tank.
The energy-saving continuous rectification system for carbon disulfide provided by the utility model realizes continuous rectification of carbon disulfide, has high rectification efficiency, convenient operation and high degree of automation, separates excessive sulfur and byproduct hydrogen sulfide in CS 2 crude products, and obtains pure carbon disulfide products with purity of more than 98.5%. The system realizes hydrogen sulfide removal under micro-high pressure, realizes rectification separation under normal pressure, realizes heat coupling through mutual cooperation among devices, furthest recovers waste heat in the system on the premise of ensuring the quality of carbon disulfide products, utilizes materials at the top of a rectification tower to preheat CS 2 crude products, reduces the consumption of heating steam of a reboiler of a primary distillation tower, reduces the consumption and refrigerating capacity of circulating water of the system, simultaneously does not need the reboiler of the rectification tower, further reduces the energy consumption required by CS 2 refining, solves the problem of higher energy consumption in the existing carbon disulfide rectification process, utilizes heat energy step by step, saves a large amount of heating water steam and circulating water for cooling, saves production cost, and is suitable for large-scale continuous production.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions of the prior art, the following description will briefly explain the drawings used in the embodiments or the description of the prior art, and it is obvious that the drawings in the following description are some embodiments of the present utility model, and other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural diagram of an energy-saving continuous rectification system for carbon disulfide according to an embodiment of the present utility model;
FIG. 2 is a schematic diagram of an overhead cooler according to an embodiment of the present utility model;
FIG. 3 is a schematic view in the direction A-A of FIG. 2;
Fig. 4 is a schematic structural diagram of an energy-saving carbon disulfide continuous rectification system according to another embodiment of the present utility model.
Reference numerals illustrate: 1-CS 2 crude product tank, 2-primary distillation tower, 3-rectifying tower, 4-CS 2 fine product tank, 5-sulfur storage tank, 6-Claus furnace, 11-magnetic pump, 21-reboiler, 22-rectifying feed pump, 23-overhead gas outlet, 24-overhead cooler, 25-arch cover, 26-deflector, 27-wire mesh foam remover, 28-recooler, 31-overhead condenser, 32-buffer tank, 241-top plate, 242-bottom plate, 243-cooling water inlet, 244-cooling water outlet, 245-heat exchange tube, 246-return tube, 247-extension spring, 248-sealing cover, 251-gas outlet and 252-liquid outlet.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present utility model more clear, the technical solutions in the embodiments of the present utility model will be clearly and completely described below, and it is apparent that the described embodiments are some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are also within the scope of the utility model.
Referring to fig. 1, an energy-saving continuous rectification system for carbon disulfide of the present utility model comprises: CS 2 crude product tank 1, primary distillation tower 2 and rectifying tower 3, rectifying tower 3 is provided with top condenser 31; the tube side inlet of the tower top condenser 31 is connected with the tower top outlet of the rectifying tower 3, the tube side outlet of the tower top condenser 31 is connected with the buffer tank 32, the shell side inlet of the tower top condenser 31 is connected with the outlet of the CS 2 crude product tank 1 through the magnetic pump 11, and the shell side outlet of the tower top condenser 31 is connected with the inlet of the primary distillation tower 2; the bottom of the primary distillation tower 2 is provided with a reboiler 21 for providing a heat source of the primary distillation tower 2, and the bottom of the primary distillation tower 2 is connected with a feed inlet of the rectifying tower 3 through a rectifying feed pump 22; the buffer tank 32 is connected with a reflux port of the rectifying tower 3 and is connected with the CS 2 fine tank 4 through a pipeline; the outlet of the tower kettle of the rectifying tower 3 is connected with a sulfur storage tank 5.
As shown in fig. 1, 2 and 3, the top vent 23 on the top end of the primary distillation column 2 is connected to the claus furnace 6 by a pipeline; the primary distillation tower 2 is provided with a built-in tower top cooler 24, and the tower top cooler 24 is arranged below a tower top head of the primary distillation tower 2; the shell of the tower top cooler 24 has the same diameter as the tower body of the primary distillation tower 2, is in sealing connection with the tower body of the primary distillation tower 2 through a top plate 241 and a bottom plate 242, and is communicated with a cooling water inlet 243 and a cooling water outlet 244 on the side wall of the shell; a plurality of heat exchange pipes 245 are arranged in the shell along the axial direction of the tower body of the primary distillation tower 2, a plurality of return pipes 246 are arranged around the heat exchange pipes 245, and the heat exchange pipes 245 and the return pipes 246 penetrate through the top plate 241 and the bottom plate 242 to be communicated with the tower body of the primary distillation tower 2 up and down the shell; an arched cover 25 is arranged above the top plate 241, a plurality of air outlets 251 are arranged on the arched cover 25, and a plurality of liquid discharging holes 252 are reserved between the arched cover 25 and the inner wall of the tower body of the primary distillation tower 2.
The normal-temperature CS 2 crude product from a CS 2 crude product tank 1 is preheated by a refined CS 2 hot material discharged from the top of a rectifying tower 3, and the preheated CS 2 crude product enters a micro-high-pressure primary distillation tower 2 for primary rectifying separation. The primary distillation tower 2 uses a reboiler 21 to provide heat, so that the temperature of the tower bottom of the primary distillation tower 2 is controlled to be not lower than 60 ℃, gas in the primary distillation tower 2 is sent to the tower top, after the carbon disulfide forming liquid is totally refluxed under the cooling of a built-in tower top cooler 24, uncooled hydrogen sulfide gas is discharged to the Claus furnace 6 for treatment through the tower top. The bottom liquid of the primary distillation tower 2 mainly contains carbon disulfide and unreacted sulfur, the carbon disulfide is sent into the rectifying tower 3 through the rectifying feed pump 22 for secondary rectifying separation, the feeding temperature in the rectifying tower 3 is higher, and the carbon disulfide is basically gasified and discharged through the top of the tower after entering the rectifying tower 3 with normal pressure from the micro-high pressure primary distillation tower 2, so that the rectifying tower 3 does not need to be provided with a reboiler, and the sulfur with higher boiling point is discharged from the bottom of the rectifying tower 3 in a liquid form. After being discharged from the top of the rectifying tower 3, the carbon disulfide gas is liquefied by heat dissipation through the top condenser 31, the liquid part is used for reflux of the rectifying tower 3, and the liquid part is sent to the CS 2 fine tank 4, so that the carbon disulfide with the purity of more than 98.5% is obtained.
The built-in tower top cooler 24 is used at the tower top of the primary distillation tower 2 for cooling light components such as hydrogen sulfide, carbon disulfide and the like by utilizing low-temperature circulating water, so that the installation space of equipment can be saved, and the liquid reflux conveying time and the pipeline cost can be reduced. The CS 2 crude product is preheated by utilizing the material at the top of the rectifying tower 3, so that the consumption of heating steam of the reboiler 21 of the primary distillation tower 2 can be reduced, the preheating recovery of the system is realized, the use of circulating water by the condenser 31 at the top of the tower can be avoided, the consumption and the refrigerating capacity of the circulating water of the system are reduced, and the energy-saving and consumption-reducing effects are remarkable. And the rectifying tower 3 does not need a reboiler, but utilizes the heat of the tower bottom material of the primary tower 2 to carry out rectifying separation, thereby obviously reducing the energy consumption of the rectifying tower 3. The system comprehensively utilizes the heat of the materials at the top and the bottom of the primary distillation tower 2 and the rectifying tower 3 step by step, saves a great amount of heating steam and cooling circulating water, and reduces the consumption of the heating steam and the circulating cooling water to 1/3 to 1/2 of the conventional rectifying process, thereby achieving the purposes of energy conservation and consumption reduction.
Further, as shown in fig. 2, the nozzles of the heat exchange tubes 245 extend upwardly above the top plate 241 of the housing; the air outlet holes 251 on the arch cover 25 are arranged in a dislocation manner with the pipe orifices of the heat exchange pipes 245; the hold-down hole 252 is vertically aligned with the return tube 246. The tower top material cooled by the tower top cooler 24 is divided into gas and liquid, the gas is discharged to the tower top end socket through the gas outlet hole 251 on the arch cover 25, the gas outlet hole 251 which is arranged in a staggered way with the pipe orifice of the heat exchange pipe 245 can prevent the liquid falling from the tower top end socket from directly entering the heat exchange pipe 245, and the liquid flows through the liquid outlet hole 252 along the arch cover 25 and enters the reflux pipe 246 to flow back into the tower body of the primary distillation tower 2. The mouth of pipe of heat exchange tube 245 exceeds roof 241 can make the liquid after the cooling can not flow back to heat exchange tube 245 in, but flows back through back flow 246, also makes the gas in the heat exchange tube 245 rise smoothly and can not receive the hindrance, promotes cooling efficiency.
Further, a tension spring 247 is provided in the return pipe 246, an upper end of the tension spring 247 is connected to a fixing frame fixed in the return pipe 246, a lower end of the tension spring 247 is connected to a seal cover 248, and the seal cover 248 is abutted to a lower end of the return pipe 246 by the tension spring 247. The fixing frame in the return pipe is only used to fix the tension spring 247 without closing the return pipe 246, and thus the fixing frame may be in a shape of a cross, or the like, and is not particularly limited herein. When no liquid flows back, the lower end part of the return pipe 246 is blocked by the sealing cover 248 under the action of the tension spring 247, and at the moment, the gas below cannot rise through the return pipe 246, and can only rise through the heat exchange pipe 245 of the tower top cooler 24 to be cooled, so that the cooling efficiency is improved, and the loss caused by entrainment of carbon disulfide out of the primary distillation tower 2 is avoided. The cooled overhead material is separated into gas and liquid, the liquid falls through a return pipe 246, the liquid flowing into the return pipe 246 is collected on a sealing cover 248, when the weight of the liquid reaches a certain value (such as reaching or exceeding the initial tension of a tension spring 247), the tension spring 247 stretches downwards due to the pressure of the liquid, the sealing cover 248 is separated from the lower end part of the return pipe 246, the liquid falls from a gap to the rectifying process of the reflux and regasification in the tower body of the primary distillation tower 2, the pressure is reduced after the liquid falls, and the sealing cover 248 is reset under the action of the tension spring 247, so that the lower end part of the return pipe 246 is reclosed.
Further, a downward-inclined guide plate 26 is arranged below the return pipe 246, the inclined upper end of the guide plate 26 is fixedly connected to the inner wall of the tower body of the primary distillation tower 2, and the inclined lower end of the guide plate 26 faces to the central position of the tower body of the primary distillation tower 2. The reflux pipe 246 is arranged at the position of the tower body of the primary distillation tower 2 close to the inner wall, so that the reflux liquid is more uniformly distributed on the filler, the deflector 26 is arranged below the reflux pipe 246 and can guide the liquid to the central position of the tower body of the primary distillation tower 2, the mixing degree and the heat exchange effect between the ascending air flow and the falling liquid are improved, and the separation efficiency and the rectifying effect are ensured.
Further, the heat exchange tube 245 is a straight tube or a spiral tube. The heat exchange tube 245 may be a straight tube or a spiral tube, and may be selected according to the actual processing amount. When the processing amount is large, the spiral pipe is preferable, the spiral pipe can increase the contact area of the gas and the cooling water, and prolong the residence time of the gas in the tower top cooler 24, so that the gas at the tower top of the primary distillation tower 2 is fully cooled, and the carbon disulfide is fully liquefied and refluxed, thereby avoiding loss caused by being discharged out of the Claus furnace 6.
Further, as shown in fig. 4, a wire mesh foam remover 27 is arranged in the primary distillation tower 2, and the wire mesh foam remover 27 is arranged between the arch cover 25 and the top head of the primary distillation tower 2. The liquid is entrained in the overhead gas cooled by the overhead cooler 24, and in order to prevent the carbon disulfide liquid from being entrained to the claus furnace 6 to cause loss, a wire mesh demister 27 is used for gas-liquid separation, so that the separation effect is enhanced.
Further, the primary distillation tower 2 and the rectifying tower 3 are all filled with stainless steel ripple; the packing of the primary distillation tower 2 is divided into an upper packing region and a lower packing region, and an inlet of the primary distillation tower 2 is arranged on a tower body of the primary distillation tower 2 between the upper packing region and the lower packing region. Compared with the common Raschig rings, the corrugated packing has larger specific surface area, higher heat efficiency and higher rectification efficiency, has small tower resistance and high separation efficiency, and is beneficial to improving the working efficiency and the rectification separation effect of the primary distillation tower 2 and the rectification tower 3.
Preferably, both the primary distillation tower 2 and the rectifying tower 3 are provided with reflux distributors, and redistributors are arranged between different filler areas, so that carbon disulfide liquid can be uniformly distributed on the filler of the filler areas, and the rectifying efficiency and the separating effect are improved.
Further, the reboiler 21 of the preliminary distillation tower 2 is any one of a kettle type, a thermosiphon type, a jacket type, and a built-in indirect heating reboiler 21. The reboiler 21 of the primary distillation tower 2 is heated by using steam as a heating medium, the tower pressure of the primary distillation tower 2 is controlled to be 0.1-0.5MPa, the tower bottom temperature is not lower than 60 ℃, preferably 60-80 ℃, and gases such as hydrogen sulfide, carbon monoxide and the like can be completely removed during primary distillation.
Further, as shown in fig. 4, a recooler 28 is provided between the top vent 23 of the primary distillation column 2 and the claus furnace 6, the tube side inlet of the recooler 28 is connected to the top vent 23, the tube side gas phase outlet of the recooler 28 is connected to the claus furnace 6, and the tube side liquid phase outlet of the recooler 28 is connected to the CS 2 fine tank 4. Most of the gas phase discharged from the top exhaust port 23 of the primary distillation tower 2 is hydrogen sulfide gas, but when the processing amount is large, carbon disulfide which is not cooled by the top cooler 24 may be entrained, so that the recooler 28 can be added according to actual working conditions to further cool the gas phase discharged from the primary distillation tower 2, and the cooling liquid is basically carbon disulfide and can be directly fed into the CS 2 fine tank 4.
Example 1
When the energy-saving continuous rectification system for carbon disulfide works specifically, a normal-temperature CS 2 crude product (containing hydrogen sulfide, carbon disulfide and impurities) from a CS 2 crude product tank 1 is preheated by a hot material CS 2 refined product discharged from the top of a rectifying tower 3 (the temperature of the material at the top of the rectifying tower 3 is 50-60 ℃ in general), and the preheated CS 2 crude product enters a micro-high-pressure primary distillation tower 2 for primary rectification separation. The primary distillation tower 2 uses a reboiler 21 to provide heat, so that the temperature of the tower bottom of the primary distillation tower 2 is controlled to be not lower than 60 ℃, gas in the primary distillation tower 2 is sent to the tower top, after the carbon disulfide forming liquid is totally refluxed under the cooling of a built-in tower top cooler 24, uncooled hydrogen sulfide gas is discharged to the Claus furnace 6 for treatment through the tower top.
When the gas in the tower body of the primary distillation tower 2 flows through the tower top cooler 24, the gas flows upwards through the straight pipe type heat exchange pipe 245, exchanges heat with cooling water in the shell in the heat exchange pipe 245, and is discharged from the pipe orifice of the heat exchange pipe 245 of the high-position top plate 241. The cooled and liquefied liquid flows back downwards through the return pipe 246 around the heat exchange pipe 245, the liquid flowing in the return pipe 246 is firstly accumulated on the sealing cover 248, when the weight of the liquid in the return pipe 246 reaches a certain value (reaches or exceeds the initial tension of the tension spring 247), the tension spring 247 in the return pipe 246 stretches downwards due to the pressure of the liquid, the sealing cover 248 is separated from the lower end part of the return pipe 246, the liquid falls from a gap, is guided to the rectifying process of the reflux and regasification in the tower body of the primary distillation tower 2 through the guide plate 26, the pressure is reduced after the liquid falls, and the sealing cover 248 is reset under the action of the tension spring 247, so that the lower end part of the return pipe 246 is reclosed. Uncooled gas is exhausted upward through the outlet 251 in the dome 25 to the overhead vent 23. If the entrained liquid falls during the ascent, it will pool around the arch cover 25 along the arc to the liquid discharge holes 252, and finally fall directly into the return pipe 246 through the liquid discharge holes 252.
The bottom liquid of the primary distillation tower 2 mainly contains carbon disulfide and unreacted sulfur, the carbon disulfide is sent into the rectifying tower 3 through a rectifying feed pump 22 for secondary rectifying separation, the feeding temperature in the rectifying tower 3 is higher (more than 60 ℃), and the carbon disulfide is basically gasified and discharged through the top of the tower after entering the rectifying tower 3 with normal pressure from the micro-high pressure primary distillation tower 2, so that the rectifying tower 3 does not need to be provided with a reboiler, and the sulfur with higher boiling point is discharged into the sulfur storage tank 5 from the bottom of the rectifying tower 3 in a liquid form. After being discharged from the top of the rectifying tower 3, the carbon disulfide gas is liquefied by heat dissipation through the top condenser 31, the liquid part is used for reflux of the rectifying tower 3, and the liquid part is sent to the CS 2 fine tank 4, so that the carbon disulfide with the purity of more than 98.5% is obtained.
Example 2
On the basis of embodiment 1, embodiment 2 further includes: when the processing amount is large, the heat exchange tube 245 of the tower top cooler 24 uses a spiral tube, so that the gas at the tower top of the primary distillation tower 2 is fully cooled, and all the carbon disulfide is liquefied and refluxed, so that the loss caused by being discharged out of the Claus furnace 6 is avoided. Meanwhile, a silk screen foam remover 27 is additionally arranged between the arch cover 25 and the head of the top of the primary distillation tower 2, so that the loss caused by entrainment of carbon disulfide liquid to the Claus furnace 6 is prevented. The liquid falling through the wire mist eliminator 27 falls onto the dome 25, down the arcuate surface from the liquid discharge opening 252 into the return pipe 246.
And, set up the recooler 28 between overhead vent 23 and claus stove 6 of the primary distillation tower 2, further cool the gaseous phase that the primary distillation tower 2 discharges, the coolant liquid discharged from the tube side is basically carbon disulfide, can send CS 2 exquisite jar 4 directly, uncooled hydrogen sulfide gas is sent to claus stove 6 to handle, has avoided the loss of carbon disulfide.
Finally, it should be noted that the above embodiments are merely illustrative of the technical solution of the present utility model, and not limiting thereof; although the present utility model has been described in detail with reference to the foregoing embodiments, those skilled in the art may modify the technical solutions described in the foregoing embodiments or make equivalent substitutions for some or all of the technical features thereof, and these modifications or substitutions do not depart from the spirit of the technical solutions of the embodiments of the present utility model.
Claims (9)
1. An energy-efficient continuous rectification system for carbon disulfide, comprising: CS 2 crude product tank, primary distillation tower and rectifying tower, the rectifying tower is equipped with overhead condenser; the tube side inlet of the tower top condenser is connected with the tower top outlet of the rectifying tower, the tube side outlet of the tower top condenser is connected with the buffer tank, the shell side inlet of the tower top condenser is connected with the CS 2 crude product tank outlet through a magnetic pump, and the shell side outlet of the tower top condenser is connected with the primary distillation tower inlet; the bottom of the primary distillation tower is provided with a reboiler for providing a heat source of the primary distillation tower, and the bottom of the primary distillation tower is connected with a feed inlet of the rectifying tower through a rectifying feed pump; the buffer tank is connected with a reflux port of the rectifying tower and is connected with a CS 2 fine tank through a pipeline; the tower kettle outlet of the rectifying tower is connected with a sulfur storage tank;
The top exhaust port on the top head of the primary distillation tower is connected with the Claus furnace through a pipeline; the primary distillation tower is provided with a built-in tower top cooler, and the tower top cooler is arranged below a tower top head of the primary distillation tower; the shell of the tower top cooler is the same as the primary distillation tower in diameter and is in sealing connection with the primary distillation tower through a top plate and a bottom plate, and the side wall of the shell is communicated with a cooling water inlet and a cooling water outlet; a plurality of heat exchange pipes are arranged in the shell along the axial direction of the primary distillation tower body, a plurality of return pipes are arranged around the heat exchange pipes, and the heat exchange pipes and the return pipes penetrate through the top plate and the bottom plate to be communicated with the primary distillation tower body up and down of the shell; an arch cover is arranged above the top plate, a plurality of air outlets are formed in the arch cover, and a plurality of liquid discharging holes are reserved between the arch cover and the inner wall of the primary distillation tower body.
2. The energy efficient continuous rectification system for carbon disulfide of claim 1, wherein the orifice of said heat exchange tube extends upwardly above said top plate of said housing; the air outlet holes on the arch cover and the pipe orifice of the heat exchange pipe are arranged in a staggered manner; the weep hole is vertically aligned with the return tube.
3. The energy-saving type carbon disulfide continuous rectification system of claim 1, wherein an extension spring is arranged in the return pipe, the upper end of the extension spring is connected with a fixing frame fixedly arranged in the return pipe, the lower end of the extension spring is connected with a sealing cover, and the sealing cover is in butt joint with the lower end of the return pipe through the extension spring.
4. The energy-saving continuous rectification system for carbon disulfide as claimed in claim 1, wherein a deflector which is inclined downwards is arranged below the reflux pipe, the inclined upper end of the deflector is fixedly connected to the inner wall of the primary distillation tower body, and the inclined lower end of the deflector faces the central position of the primary distillation tower body.
5. The continuous rectification system for carbon disulfide of any one of claims 1 to 4, wherein said heat exchange tube is a straight tube or a spiral tube.
6. The energy-saving continuous rectification system for carbon disulfide of claim 1, wherein a wire mesh demister is arranged in the primary distillation tower and is arranged between the arch cover and the top head of the primary distillation tower.
7. The energy-saving carbon disulfide continuous rectification system as claimed in claim 1, wherein the primary distillation tower and the rectification tower are respectively provided with stainless steel corrugated packing; the packing of the primary distillation tower is divided into an upper packing region and a lower packing region, and the inlet of the primary distillation tower is arranged on the primary distillation tower body between the upper packing region and the lower packing region.
8. The continuous rectification system of energy-efficient carbon disulfide of claim 1, wherein said reboiler of primary distillation column is any one of a kettle type, a thermosiphon type, a jacket type, and a built-in indirect heating reboiler.
9. The energy-efficient continuous rectification system for carbon disulfide of claim 1, wherein a recooler is arranged between an overhead vent of the primary distillation column and the claus furnace, a tube side inlet of the recooler is connected with the overhead vent, a tube side gas phase outlet of the recooler is connected with the claus furnace, and a tube side liquid phase outlet of the recooler is connected with the CS 2 fine tank.
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| CN202323123811.4U CN221107027U (en) | 2023-11-20 | 2023-11-20 | Energy-saving carbon disulfide continuous rectification system |
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| CN202323123811.4U CN221107027U (en) | 2023-11-20 | 2023-11-20 | Energy-saving carbon disulfide continuous rectification system |
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