CN213865387U - Carbon disulfide production system - Google Patents
Carbon disulfide production system Download PDFInfo
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- CN213865387U CN213865387U CN202022929693.6U CN202022929693U CN213865387U CN 213865387 U CN213865387 U CN 213865387U CN 202022929693 U CN202022929693 U CN 202022929693U CN 213865387 U CN213865387 U CN 213865387U
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Abstract
Carbon disulfide production system belongs to carbon disulfide production technical field, especially relates to a carbon disulfide production system. The utility model provides a carbon disulfide production system that work effect is good. The utility model discloses a synthetic part of carbon disulfide, carbon disulfide separation purification part, carbon disulfide warehousing and transportation part and torch are congealed liquid and are retrieved the part, and its characterized in that carbon disulfide synthesis part, carbon disulfide separation purification part, carbon disulfide warehousing and transportation part link to each other in proper order, and the torch is congealed the input port of liquid recovery part and is linked to each other with the output port of carbon disulfide separation purification part, the synthetic output port of carbon disulfide respectively.
Description
Technical Field
The utility model belongs to the technical field of the carbon disulfide production, especially, relate to a carbon disulfide production system.
Background
Carbon disulfide is an inorganic substance, a common solvent and a colorless liquid, and can dissolve sulfur simple substances. Carbon disulfide can be used for manufacturing rayon, pesticides, accelerators and the like, and can also be used as a solvent. The existing carbon disulfide production system still needs to be further improved.
SUMMERY OF THE UTILITY MODEL
The utility model discloses just to above-mentioned problem provides a carbon disulfide production system that work effect is good.
For realizing above-mentioned purpose, the utility model discloses a following technical scheme, the utility model discloses a synthetic part of carbon disulfide, carbon disulfide separation purification part, carbon disulfide warehousing and transportation part and torch are congealed liquid and are retrieved the part, and synthetic part of its characterized in that carbon disulfide, carbon disulfide separation purification part, carbon disulfide warehousing and transportation part link to each other in proper order, and the torch is congealed the input port of liquid and is retrieved the input port of part and is linked to each other with the output port of carbon disulfide separation purification part, the synthetic partial output port of carbon disulfide respectively.
As a preferred scheme, the carbon disulfide synthesis part of the utility model comprises a sulfur melting tank, the upper end of the sulfur melting tank is provided with a solid sulfur inlet, the lower end outlet of the sulfur melting tank is connected with a first inlet at the upper end of a pre-coating tank stirrer, a second inlet at the upper end of the pre-coating tank stirrer is connected with an outlet at the lower end of an air stripping tower, the outlet of the pre-coating tank stirrer is connected with an inlet at the upper end of a sulfur filter through a pre-coating tank delivery pump, the lower end outlet of the sulfur filter is connected with a first inlet at the upper end of a liquid sulfur tank, a second inlet at the upper end of the liquid sulfur tank is connected with an outlet of a sulfur recovery unit, the outlet of the liquid sulfur tank is connected with a sulfur inlet of raw materials of a reaction furnace through a liquid sulfur delivery pump, the inlet of the raw materials of the reaction furnace is connected with a purified gas outlet of a pressure swing adsorption device PSA, the inlet of the raw materials of the PSA raw materials is connected with a natural gas outlet of a natural gas buffer tank, the inlet of the natural gas buffer tank is connected with a transmission pipeline of the natural gas recovery tail gas treatment unit, the PSA desorption gas outlet is respectively connected with a fuel gas main pipe and a sulfur recovery port of the reaction furnace;
the outlet of the reaction furnace is connected with the inlet of the reactor, the outlet of the reactor is connected with the inlet of the sulfur condenser, the water inlet of the sulfur condenser is connected with the boiler water supply BFW interface, the steam outlet of the sulfur condenser is connected with the low-pressure steam SL interface, the outlet of the sulfur condenser is connected with the inlet of the sulfur condensate receiver, the boiler sewage outlet of the sulfur condenser is connected with the inlet of the boiler sewage discharge barrel, and the water inlet of the boiler sewage discharge barrel is connected with the circulating water backwater CW port.
As another preferred scheme, the export of the sulfur condenser is connected with the import of the sulfur-containing gas separation tank through a valve.
As another preferred scheme, the low pressure steam SL interface of the present invention is a 0.35MPa low pressure steam SL interface.
As another preferred scheme, the utility model discloses a boiler blow-off bucket's outlet connects the floor drain through the funnel.
As another preferred scheme, the utility model discloses a carbon disulfide separation purification part includes sulphur condensate receiver, and the import of sulphur condensate receiver connects the export of sulphur condenser, and the export of sulphur condensate receiver upper end links to each other with desulfurizing tower import, flash distillation carbon disulfide transfer pump export respectively, and the reboiler reentry mouth of desulfurizing tower connects the export of desulfurizing tower reboiler, and the import of desulfurizing tower reboiler links to each other with desulfurizing tower lower extreme export, sulphur condensate receiver lower extreme export, flash tank import respectively;
an outlet at the upper end of the desulfurizing tower is connected with an inlet of a carbon disulfide rectification feeding separation tank through a desulfurizing tower condenser, an outlet at the lower end of the carbon disulfide rectification feeding separation tank is respectively connected with an upper liquid phase feed inlet of the carbon disulfide rectification tower and an upper reflux port of the desulfurizing tower through a desulfurizing tower reflux pump, an upper gas phase feed inlet of the carbon disulfide rectification tower is connected with an upper outlet of the carbon disulfide rectification feeding separation tank, a lower outlet of the carbon disulfide rectification tower is respectively connected with a lower inlet of the carbon disulfide rectification tower, an inlet of a carbon disulfide finished product cooler and an upper outlet of the carbon disulfide rectification tower, and an outlet of the carbon disulfide finished product cooler is connected with a carbon disulfide shift tank through a carbon disulfide finished product subcooler;
the upper end gas phase outlet of the carbon disulfide refining tower is respectively connected with the upper end outlet of the flash tank and the inlet of the flash carbon disulfide condenser, the outlet of the flash carbon disulfide condenser is connected with the material inlet of the flash carbon disulfide receiving tank through a water separator, the material inlet of the flash carbon disulfide receiving tank is connected with the lower end outlet of the carbon disulfide refining tower through a jacket cooler, the upper end outlet of the flash carbon disulfide receiving tank is connected with a sulfur-free gas separation tank, and the upper end unqualified product return port of the flash carbon disulfide receiving tank is connected with the outlet of a carbon disulfide emergency pump; an outlet at the lower end of the flash evaporation carbon disulfide receiving tank is connected with an inlet of a flash evaporation carbon disulfide transfer pump;
an outlet at the lower end of the flash tank is connected with an inlet of a stripping tower, an outlet at the upper end of the stripping tower is connected with a sulfur removal and recovery interface, a sulfur outlet at the lower part of the stripping tower is connected with a sulfur recovery interface, and an outlet at the lower end of the stripping tower is connected with a precoating tank interface;
an outlet at the upper end of the carbon disulfide rectifying tower is respectively connected with a sulfur removal and recovery interface and an inlet of the sulfur-free gas separation tank.
As another kind of preferred scheme, desulfurizing tower reboiler's steam inlet connects 0.8MPa middling pressure steam SM interface, and desulfurizing tower reboiler's liquid outlet connects middling pressure condensate interface SCM.
As another preferred scheme, the utility model discloses a desulfurizing tower condenser's inlet outlet connects circulating water CW mouth.
As another kind of preferred scheme, carbon disulfide rectifying column upper end is provided with overhead type carbon disulfide rectifying column condenser, and the inlet outlet of carbon disulfide rectifying column condenser links to each other with refrigerated water interface GW 2.
As another kind of preferred scheme, carbon disulfide rectifying column lower part reboiler returns the mouth and connects carbon disulfide rectifying column lower extreme export through carbon disulfide rectifying column reboiler, and the steam inlet of carbon disulfide rectifying column reboiler connects 0.8MPa low pressure steam SM interface, and the condensate export of carbon disulfide rectifying column reboiler connects middling pressure condensate interface SCM.
As another kind of preferred scheme, carbon disulfide refining tower lower part reboiler returns the mouth and connects carbon disulfide refining tower lower extreme export through carbon disulfide refining tower reboiler, and carbon disulfide refining tower reboiler's steam inlet connects 0.35MPa low pressure steam SL interface, and carbon disulfide rectifying column reboiler's condensate export connects low pressure condensate SCL interface.
As another kind of preferred scheme, carbon disulfide finished product cooler's inlet outlet connects circulating water CW mouth, and carbon disulfide finished product subcooler's inlet outlet connects refrigerated water interface GW 2.
As another kind of preferred scheme, carbon disulfide refining tower upper end is provided with overhead carbon disulfide refining tower condenser, and the inlet outlet of carbon disulfide refining tower condenser connects circulating water CW mouth.
As another preferred scheme, the water inlet of flash distillation carbon disulfide condenser connects circulating water CW mouth.
As another preferred scheme, the utility model discloses the inlet outlet of double-pipe type cooler connects circulating water CW mouth.
As another preferred scheme, the utility model discloses a set up a few font pipelines between gas stripping tower lower extreme export and the groove interface of precoating.
As another preferred scheme, carbon disulfide warehousing and transportation part includes the sewage strip tower, the import of sewage strip tower links to each other with 0.35MPa low pressure steam SL interface, nitrogen gas interface N respectively, the export of sewage strip tower upper end connects gaseous collection tank middle part import, gaseous collection tank upper end export connects sulphur and retrieves the interface, gaseous collection tank lower extreme export water receiving seal basin gas condensate return mouth, the first entry of water seal basin loops through water seal water strip aftercooler, water seal water strip preheater connects sewage strip tower lower extreme export, the water seal water export of water seal water strip preheater connects sewage strip tower upper portion water seal water inlet, the water seal water import of water seal strip water strip preheater links to each other with strip water pump export, water seal water circulation pump export, carbon disulfide storage tank import, carbon disulfide class product jar import respectively, strip water pump import links to each other with water seal basin middle part export respectively, The outlet of the waste water collecting tank is connected, and the water outlet of the waste water collecting tank is connected with a drainage ditch;
a first inlet of the wastewater collection tank is connected with an overflow port of a water-sealed water tank, a fresh water inlet of the water-sealed water tank is connected with production water IW, a second inlet of the water-sealed water tank is respectively connected with a water-sealed water overflow port of the carbon disulfide regular production tank and a water-sealed water overflow port of the carbon disulfide storage tank, and a water-sealed water outlet of the water-sealed water tank is connected with an inlet of a water-sealed water circulating pump;
a second inlet of the wastewater collection tank is respectively connected with a cleaning water outlet of a carbon disulfide shift production tank and a cleaning water outlet of a carbon disulfide storage tank, a carbon disulfide inlet of the carbon disulfide shift production tank is connected with an outlet of a carbon disulfide finished product subcooler, a carbon disulfide outlet of the carbon disulfide shift production tank is respectively connected with an inlet of a carbon disulfide emergency pump, an inlet of a carbon disulfide conveying and loading pump and an inlet of a carbon disulfide storage tank, and an outlet of the carbon disulfide emergency pump is connected with an inlet of a flash evaporation carbon disulfide receiving tank;
carbon disulfide is carried and the car loading pump export links to each other with carbon disulfide storage tank carbon disulfide import, tank car import respectively.
As another preferred scheme, the utility model discloses the inlet outlet of cold ware is connect circulating water CW mouth after the water seal water strip.
As another preferred scheme, the tank car of the utility model is arranged on the upper end of the partition fence at the upper end of the water collecting tank, and the nitrogen inlet of the tank car is connected with nitrogen N2.
As another kind of preferred scheme, the water seal basin divide into four and separates the pond, four separate the pond and set up overflow water mouth on upper portion respectively, the first entry and the second entry setting of water seal basin separate the pond upper end at first, and water seal basin air stripping is congealed water and is returned the mouth and set up at first separate the pond and extend to first separate the pond lower part through the pipeline, and water seal basin middle part export setting separates the pond middle part at first.
As another preferred scheme, the wastewater collection tank of the utility model is provided with a first partition wall and a second partition wall along the length direction of the wastewater collection tank, the lower end of the first partition wall is connected with the lower end of the wastewater collection tank, and the upper end of the first partition wall is spaced from the upper end of the wastewater collection tank; the upper end of the second partition wall is connected with the upper end of the wastewater collecting tank, and the lower end of the first partition wall is spaced from the lower end of the wastewater collecting tank;
an outlet of the wastewater collection tank is formed in the front upper side wall of a first interval in front of the first partition wall, a water outlet of the wastewater collection tank is formed in the front lower side wall of the first interval in front of the first partition wall, a first inlet and a second inlet of the wastewater collection tank are formed in the upper end of a third interval in the rear of the second partition wall, and a second interval is formed between the first partition wall and the second partition wall.
As another preferred scheme, the utility model discloses first partition wall upper end is higher than the lower extreme of second partition wall.
As another preferred scheme, the torch condensate recovery part of the utility model comprises a sulfur-free gas separation tank and a condensate tank, wherein the inlet of the sulfur-free gas separation tank is respectively connected with the outlet of the flash evaporation carbon disulfide receiving tank and the outlet of the carbon disulfide rectifying tower, the outlet of the sulfur-free gas separation tank is connected with the sulfur-free gas inlet of the torch sealing tank, the sulfur-containing gas inlet of the torch sealing tank is connected with the outlet of the sulfur-containing gas separation tank, and the inlet of the sulfur-containing gas separation tank is connected with the outlet of the sulfur condenser;
a liquid inlet of the condensate tank is connected with a low-pressure condensate SCL interface, a medium-pressure condensate inlet of the condensate tank is connected with an outlet at the lower end of the condensate flash tank, a liquid inlet at the upper part of the condensate flash tank is connected with a medium-pressure condensate interface SCM, and an outlet at the upper end of the condensate flash tank is connected with a 0.35MPa low-pressure steam SL interface;
an outlet at the upper end of the condensate tank is connected with a condensate inlet after the upper part of the condensate tank is flashed through a condensate flash condenser, and an outlet at the lower end of the condensate tank is connected with a deaerator through a condensate delivery pump.
Secondly, condensate flash evaporation condenser's inlet outlet connects circulating water CW mouth.
Additionally, the lower head part of the sulfur-free gas separation tank is provided with a jacket, the barrel and the lower head part of the torch sealing tank are provided with a jacket, and the barrel and the lower head part of the sulfur-containing gas separation tank are provided with a jacket.
The utility model has the advantages of.
The utility model discloses the synthetic partial reaction production carbon disulfide of carbon disulfide, carbon disulfide purification part obtains pure carbon disulfide product, and carbon disulfide stores up the storage and the transportation of the partial carbon disulfide of being convenient for of fortune, and torch condensate recovery part is retrieved the condensate, practices thrift the environmental protection. The utility model discloses a mutually supporting of each part does benefit to reliable, the high-efficient production of carbon disulfide.
Drawings
The present invention will be further described with reference to the accompanying drawings and the following detailed description. The scope of protection of the present invention is not limited to the following description.
Figure 1 is a schematic structural diagram of the carbon disulfide synthesis part of the present invention.
Figure 2 is the structure schematic diagram of the carbon disulfide separation and purification part of the utility model.
Figure 3 is the structure schematic diagram of the carbon disulfide storage and transportation part of the invention.
FIG. 4 is a schematic structural view of the recovery part of the flare condensate of the present invention.
Fig. 5 and 6 are partially enlarged views of fig. 1.
Fig. 7 and 8 are partially enlarged views of fig. 2.
Fig. 9 and 10 are partially enlarged views of fig. 3.
Fig. 11 and 12 are partially enlarged views of fig. 4.
Detailed Description
As shown in the figure, the utility model discloses a synthetic part of carbon disulfide, carbon disulfide separation purification part, carbon disulfide warehousing and transportation part and torch are congealed liquid and are retrieved the part, and synthetic part of carbon disulfide, carbon disulfide separation purification part, carbon disulfide warehousing and transportation part link to each other in proper order, and the torch is congealed liquid and is retrieved the input port of part and is linked to each other with the output port of carbon disulfide separation purification part, the synthetic output port of carbon disulfide respectively.
The carbon disulfide synthesis part comprises a sulfur melting tank, a solid sulfur inlet is arranged at the upper end of the sulfur melting tank, a lower end outlet of the sulfur melting tank is connected with a first inlet at the upper end of a pre-coating tank stirrer, a second inlet at the upper end of the pre-coating tank stirrer is connected with a lower end outlet of a gas stripping tower, an outlet of the pre-coating tank stirrer is connected with an upper end inlet of a sulfur filter through a pre-coating tank conveying pump, a lower end outlet of the sulfur filter is connected with a first inlet at the upper end of a liquid sulfur tank, a second inlet at the upper end of the liquid sulfur tank is connected with an outlet of a sulfur recovery unit, an outlet of the liquid sulfur tank is connected with a raw material sulfur inlet of a reaction furnace through a liquid sulfur conveying pump, a raw material gas inlet of the reaction furnace is connected with a purified gas outlet of a natural gas pressure swing adsorption device (PSA), a natural gas inlet is connected with a natural gas outlet of a natural gas buffer tank, an inlet of the natural gas buffer tank is connected with a transmission pipeline of raw material natural gas, a natural gas outlet of the natural gas recovery tail gas treatment unit, a desorbed gas outlet is respectively connected with a fuel gas main pipe of the reaction furnace, The sulfur recovery port is connected;
the outlet of the reaction furnace is connected with the inlet of the reactor, the outlet of the reactor is connected with the inlet of the sulfur condenser, the water inlet of the sulfur condenser is connected with the boiler water supply BFW interface, the steam outlet of the sulfur condenser is connected with the low-pressure steam SL interface, the outlet of the sulfur condenser is connected with the inlet of the sulfur condensate receiver, the boiler sewage outlet of the sulfur condenser is connected with the inlet of the boiler sewage discharge barrel, and the water inlet of the boiler sewage discharge barrel is connected with the CW port.
And the outlet of the sulfur condenser is connected with the inlet of the sulfur-containing gas separation tank through a valve.
The low-pressure steam SL interface is a 0.35MPa low-pressure steam SL interface.
The water outlet of the boiler blow-off barrel is connected with a floor drain through a funnel.
The utility model discloses carbon disulfide synthesis part is the purification of raw materials sulphur and natural gas to reaction production carbon disulfide in reacting furnace and reactor. The sulfur filter is arranged to remove impurities in the sulfur and the heavy components in the natural gas are removed by the natural gas purification device (PSA device), so that the operation period and the service life of the furnace tube in the reaction furnace are prolonged. The filtered sulfur enters a reaction furnace for reaction, so that mechanical impurities can be prevented from entering the reaction furnace and the reactor; the natural gas purified by the PSA device is separated from heavy components in the natural gas, so that the heavy components in the natural gas can be prevented from being cracked in the reaction furnace to form carbon deposition, and the running time of the reaction furnace is prolonged.
The carbon disulfide separation and purification part comprises a sulfur condensate receiver, an inlet of the sulfur condensate receiver is connected with an outlet of a sulfur condenser, an outlet at the upper end of the sulfur condensate receiver is respectively connected with an inlet of a desulfurizing tower and an outlet of a flash-evaporation carbon disulfide conveying pump, a reboiler return port of the desulfurizing tower is connected with an outlet of a reboiler of the desulfurizing tower, and the inlet of the reboiler of the desulfurizing tower is respectively connected with an outlet at the lower end of the desulfurizing tower, an outlet at the lower end of the sulfur condensate receiver and an inlet of a flash tank;
an outlet at the upper end of the desulfurizing tower is connected with an inlet of a carbon disulfide rectification feeding separation tank through a desulfurizing tower condenser, an outlet at the lower end of the carbon disulfide rectification feeding separation tank is respectively connected with an upper liquid phase feed inlet of the carbon disulfide rectification tower and an upper reflux port of the desulfurizing tower through a desulfurizing tower reflux pump, an upper gas phase feed inlet of the carbon disulfide rectification tower is connected with an upper outlet of the carbon disulfide rectification feeding separation tank, a lower outlet of the carbon disulfide rectification tower is respectively connected with a lower inlet of the carbon disulfide rectification tower, an inlet of a carbon disulfide finished product cooler and an upper outlet of the carbon disulfide rectification tower, and an outlet of the carbon disulfide finished product cooler is connected with a carbon disulfide shift tank through a carbon disulfide finished product subcooler;
the upper end gas phase outlet of the flash carbon disulfide refining tower is respectively connected with the upper end outlet of the flash tank and the inlet of the flash carbon disulfide condenser, the outlet of the flash carbon disulfide condenser is connected with the material inlet of the flash carbon disulfide receiving tank through a water separator, the material inlet of the flash carbon disulfide receiving tank is connected with the lower end outlet of the carbon disulfide refining tower through a jacket cooler (the jacket cooler is used for circulating process materials in an inner pipe, the process materials are introduced into a jacket to cool the process materials in the inner pipe), the upper end outlet of the flash carbon disulfide receiving tank is connected with the sulfur-free gas separation tank, and the upper end unqualified product return port of the flash carbon disulfide receiving tank is connected with the outlet of the carbon disulfide emergency pump; an outlet at the lower end of the flash evaporation carbon disulfide receiving tank is connected with an inlet of a flash evaporation carbon disulfide transfer pump;
an outlet at the lower end of the flash tank is connected with an inlet of a stripping tower, an outlet at the upper end of the stripping tower is connected with a sulfur removal and recovery interface, a sulfur outlet at the lower part of the stripping tower is connected with a sulfur recovery interface, and an outlet at the lower end of the stripping tower is connected with a precoating tank interface;
an outlet at the upper end of the carbon disulfide rectifying tower is respectively connected with a sulfur removal and recovery interface and an inlet of the sulfur-free gas separation tank.
And a steam inlet of the reboiler of the desulfurizing tower is connected with a 0.8MPa medium-pressure steam SM interface, and a liquid outlet of the reboiler of the desulfurizing tower is connected with a medium-pressure condensate interface SCM.
And the water inlet and the water outlet of the condenser of the desulfurizing tower are connected with a circulating water CW port.
And an overhead carbon disulfide rectifying tower condenser is arranged at the upper end of the carbon disulfide rectifying tower, and a water inlet and a water outlet of the carbon disulfide rectifying tower condenser are connected with a chilled water interface GW 2.
Carbon disulfide rectifying column reboiler return opening connects carbon disulfide rectifying column lower extreme export through carbon disulfide rectifying column reboiler, and the steam inlet of carbon disulfide rectifying column reboiler connects 0.8MPa low pressure steam SM interface, and the condensate export of carbon disulfide rectifying column reboiler connects middling pressure condensate interface SCM.
Carbon disulfide refining tower lower part reboiler returns the mouth and connects carbon disulfide refining tower lower extreme export through carbon disulfide refining tower reboiler, and carbon disulfide refining tower reboiler's steam inlet connects 0.35MPa low pressure steam SL interface, and carbon disulfide rectifying column reboiler's condensate export connects low pressure condensate SCL interface.
And the water inlet and outlet of the carbon disulfide finished product cooler are connected with a circulating water CW port, and the water inlet and outlet of the carbon disulfide finished product subcooler are connected with a chilled water interface GW 2.
And an overhead carbon disulfide refining tower condenser is arranged at the upper end of the carbon disulfide refining tower, and a water inlet and a water outlet of the carbon disulfide refining tower condenser are connected with a circulating water CW port.
And a water inlet of the flash evaporation carbon disulfide condenser is connected with a circulating water CW port.
And the water inlet and the water outlet of the jacketed pipe cooler are connected with a circulating water CW port.
A n-shaped pipeline (the n-shaped pipeline is used for liquid seal to prevent gas-phase media in the gas stripping tower from leaking out through a sulfur pipeline) is arranged between the outlet at the lower end of the gas stripping tower and the interface of the pre-coating groove.
As shown in fig. 2, the carbon disulfide separation purification: the process gas condensed from the condenser enters a sulfur condensate receiver (a-206). Here, the gas phase and the liquid phase are separated.
The liquid phase separated by the sulfur condensate receiver (a-206) is collected at the bottom of the knockout drum. The liquid sulfur and sulfur from the bottom of the desulfurizing tower (A-402) enter a flash evaporation tank (A408). The pressure in the flash tank is slightly positive, due to the pressure drop, CS2Is flashed off, and the flashed product contains trace CS2And H2And (3) stripping sulfur entering a stripping tower of the sulfur recovery system by self-flowing, wherein liquid sulfur at the bottom of the stripping tower flows into the precoating tank by gravity, and gas at the top of the stripping tower still returns to the sulfur recovery system. The gas phase coming out of the top of the flash tank (A-408) enters a flash CS2And a condenser (H-404) cooled by circulating water. The condensed liquid is inspected by a water separator (A-409) and finally collected in a flash evaporation CS2In the receiving tank (A-403), the flash evaporation CS2The delivery pump (P-401A/B) is driven into the desulfurizing tower (A-402).
The gaseous phase from the sulphur condensate receiver (A-206) is passed to a desulphurisation column (A-402) where sulphur is further separated and collected at the bottom of the column. And (4) conveying the sulfur at the bottom of the tower to a flash evaporation tank for flash evaporation.
The heat for the reboiler (H-403) is provided by medium pressure steam.
The superheated gas at the top of the desulfurizing tower (A-402) enters a desulfurizing tower condenser (H-202) and is partially condensed by cooling water.
The condensed process stream is passed to H2And carrying out gas-liquid separation in the S distillation feed separator. The liquid passes through a reflux pump (P-201A/B) of the desulfurizing tower, wherein one part of the liquid is used as reflux of the desulfurizing tower, and the other part of the liquid is used as CS2Liquid phase feed to the rectification column. Direct gas phase into CS2A rectifying tower.
CS2The rectifying column (A-401) receives H2S and CS2Gas phase mixture, pure CS is produced at the bottom of the tower2And acid gas is produced at the tower top. CS2The heat required by the bottom of the rectifying tower is provided by a reboiler (H-401), and a built-in condenser is arranged at the top of the rectifying tower. CS2Rectifying column condenser (H-402) as CS2Part of a distillation column (a-401), installed at the top of the column, uses a cooling medium which is glycol cooling liquid from a refrigeration system. CS2The top of the rectifying tower (A-401) produces H2And conveying the S gas to a sulfur recovery and sulfur production furnace. When the system is in fire or leaks, it is vented to the flare system.
CS2The rectifier reboiler (H-401) is provided by medium pressure steam.
CS2The bottom of the rectification column (A-401) is pure CS2And (5) producing the product. Since there is a certain pressure in the column, no pump, CS, is required2Can be sent to the CS2Product cooler (H-405) and CS2After being cooled by a finished product subcooler (H-406), the finished product is sent to CS2A shift production tank (T-501A/B/C).
CS2The finished product subcooler uses glycol chilled water as a cooling medium.
Normally, CS at the bottom of A-4012Through CS2Cooler (H-405) and CS2And a finished product subcooler (H-406) for cooling, and then conveying to a shift production tank for storage. When the A-401 tower bottom product is unqualified or a refined product of carbon disulfide is needed, the A-401 tower bottom product (CS)2) Sent to a carbon disulfide refining column (A-410).
The bottom of the carbon disulfide refining tower is disulfide containing impuritiesCarbon, cooled by jacketed pipe cooler and then enters flash evaporation CS2And the receiving tank (A-403) is conveyed back to the desulfurizing tower for re-rectification. The jacketed pipe cooler uses circulating cooling water as a cooling medium.
Qualified carbon disulfide products treated by the carbon disulfide refining tower pass through a condenser (H-411) of the carbon disulfide refining tower at the top of the tower, come out from the upper part of the tower, and pass through CS2Cooler (H-405) and CS2And a finished product subcooler (H-406) for cooling, and then conveying to a shift production tank for storage.
The process gas which is not cooled down at the top of the carbon disulfide refining tower enters a flash evaporation CS2A condenser (H-404) which enters a flash evaporation CS after being cooled2And the receiving tank (A-403) is conveyed back to the desulfurizing tower for re-rectification.
A carbon disulfide refining tower reboiler (H-410) is arranged at the bottom of the A-410, and low-pressure steam is used as a heat source. The top of the carbon disulfide refining tower is provided with a condenser (H-411) of a carbon disulfide refining tower, and circulating cooling water is used as a cooling medium.
The carbon disulfide rectifying tower and the carbon disulfide refining tower of the carbon disulfide separation and purification part of the utility model adopt internal reflux, and the condenser is arranged in an overhead type; the equipment investment is reduced, and the operating cost of the device is also reduced. The device is not provided with a storage device and a delivery pipeline for liquid hydrogen sulfide, so that the safety of the device is improved. And separating excessive sulfur and a byproduct hydrogen sulfide in the carbon disulfide product to obtain a pure carbon disulfide product. The carbon disulfide refining tower is arranged, so that light and heavy impurities of qualified varieties of carbon disulfide can be further removed, and a carbon disulfide refined product is obtained.
The carbon disulfide storage and transportation part comprises a sewage stripping tower, the inlet of the sewage stripping tower is respectively connected with a 0.35MPa low-pressure steam SL interface and a nitrogen interface N, the upper end outlet of the sewage stripping tower is connected with the middle inlet of a gas collection tank, the upper end outlet of the gas collection tank is connected with a sulfur recovery interface, the lower end outlet of the gas collection tank is connected with a water seal water tank gas condensate return port, the first inlet of the water seal water tank is sequentially connected with a water seal water stripping aftercooler and a water seal water stripping preheater through a water seal water stripping lower end outlet of the sewage stripping tower, the water seal water outlet of the water seal water stripping preheater is connected with the upper water seal water inlet of the sewage stripping tower, the water seal water inlet of the water seal water stripping preheater is respectively connected with a stripping water pump outlet, a water seal water circulating pump outlet, a carbon disulfide storage tank inlet and a carbon disulfide shift tank inlet (the water seal water circulating pump outlet conveys water seal water to the carbon disulfide storage tank inlet and the water seal water inlet of the carbon disulfide shift tank, and the outlet of the stripping water pump conveys water in the water-sealed water tank and the wastewater collecting tank to the stripping tower. Meanwhile, an outlet pipeline of the water-seal water circulating pump is communicated with an outlet pipeline of the stripping water pump, and the water-seal water in the water-seal water tank can be conveyed to the stripping tower through the water-seal water circulating pump;
a first inlet of the wastewater collection tank is connected with an overflow port of a water-sealed water tank, a fresh water inlet of the water-sealed water tank is connected with production water IW, a second inlet of the water-sealed water tank is respectively connected with a water-sealed water overflow port of the carbon disulfide regular production tank and a water-sealed water overflow port of the carbon disulfide storage tank, and a water-sealed water outlet of the water-sealed water tank is connected with an inlet of a water-sealed water circulating pump;
a second inlet of the wastewater collection tank is respectively connected with a cleaning water outlet of a carbon disulfide shift production tank and a cleaning water outlet of a carbon disulfide storage tank, a carbon disulfide inlet of the carbon disulfide shift production tank is connected with an outlet of a carbon disulfide finished product subcooler, a carbon disulfide outlet of the carbon disulfide shift production tank is respectively connected with an inlet of a carbon disulfide emergency pump, an inlet of a carbon disulfide conveying and loading pump and an inlet of a carbon disulfide storage tank, and an outlet of the carbon disulfide emergency pump is connected with an inlet of a flash evaporation carbon disulfide receiving tank;
carbon disulfide is carried and the car loading pump export links to each other with carbon disulfide storage tank carbon disulfide import, tank car import respectively.
And the water inlet and the water outlet of the water-sealed water stripping aftercooler are connected with a circulating water CW port.
The tank car sets up on the jube upper end of collecting the basin upper end (the tank car outside needs the spray water cooling when summer temperature is high, drenches the water that is collecting through collecting the basin under the car outside the transport tank), and the nitrogen gas import of tank car connects nitrogen gas N2 (the tank car carries out nitrogen seal after the carbon disulfide tank car loading).
The water seal basin divide into four and separates the pond, four separate the pond and set up overflow water mouth respectively on upper portion (make water seal water can separate the pond by first and begin one by one and separate pond overflow to next one), the first entry and the second entry setting of water seal basin separate the pond upper end at first, water seal basin air stripping is congealed water and is returned the mouth and set up at first separate the pond and extend to first separate the pond lower part through the pipeline (advance first separate bottom of the pool upwards again to the next interval, carry out the intensive cycle), water seal basin middle part export sets up at first separate middle part of the pond.
And (3) returning overflow water from the carbon disulfide shift tank T-501 and the carbon disulfide storage tank T-502 to the first separation tank, when water-sealed water needs to be stripped, opening a valve from the first separation tank to a stripping water pump P-504 to strip the returned overflow water, and taking the residual separation tank as a water source of a water-sealed water circulating pump P-503.
A first partition wall and a second partition wall are arranged in the wastewater collection tank along the length direction of the wastewater collection tank, the lower end of the first partition wall is connected with the lower end of the wastewater collection tank, and the upper end of the first partition wall is spaced from the upper end of the wastewater collection tank; the upper end of the second partition wall is connected with the upper end of the wastewater collecting tank, and the lower end of the first partition wall is spaced from the lower end of the wastewater collecting tank;
an outlet of the wastewater collection tank is formed in the front upper side wall of a first interval in front of the first partition wall, a water outlet of the wastewater collection tank is formed in the front lower side wall of the first interval in front of the first partition wall, a first inlet and a second inlet of the wastewater collection tank are formed in the upper end of a third interval in the rear of the second partition wall, and a second interval is formed between the first partition wall and the second partition wall. Set up the partition wall, with dividing into the triplex in the pond, all water that get into in the inslot all is by the third interval entering groove in, if there is the material to leak, because material proportion is greater than water, the material can deposit and collect in the third interval and the second interval to can not get into first interval and discharge outside the pond.
The upper end of the first partition wall is higher than the lower end of the second partition wall. Floating objects that may fall into the third interval are prevented from entering the first interval.
As shown in fig. 3, carbon disulfide is stored and transported: produced CS2Is collected in one of three carbon disulfide shift tanks (T-501A/B/C)Three shift pots are used alternately, and each shift pot can store about 8 hours of production.
CS in regular labor pot2An assay is required before sending to the carbon disulfide storage tank (T-502A/B/C). If the analyzed product has unqualified quality, the product can pass through CS2Flash CS with emergency pump (P-502) return to process system2In the collection tank (A-403). Three CS stations2In the conveying and loading pump (P-501A/B/C), the P-501A/B can be used for conveying the CS in the regular production tank2To a carbon disulfide storage tank (T-502A/B/C), and P501B/C can be used for CS2The truck-mounted, that is P-501B can be used as a backup pump for the P-501A and P-501C pumps.
Due to CS2Has high vapor pressure and is easy to volatilize, so the water-sealed storage is needed. The water-sealed water is pumped into the CS by a water-sealed water circulating pump (P-503A/B)2Storage tank for water in CS2The storage tank and the water-sealed water tank (T-503) are circulated. When CS is used2When the water enters the storage tank, the excessive water-sealed water flows into the water-sealed water tank (T-503) through the overflow port.
After long-time operation, trace H2S is generated in the water seal water tank (T-503) and the wastewater collection tank (T-504), the water seal water is sent to a water seal water preheater (H-501) through a stripping water pump (P-504A/B) and is preheated by the stripped water seal water, and then the water seal water enters a stripping tower (A-501) for stripping. And discharging qualified water-sealed water after stripping from the bottom of the tower, cooling the water-sealed water twice by a water-sealed water preheater (H-501) and a water-sealed water stripping aftercooler (H-502), and returning the water-sealed water to a water-sealed water tank (T-503).
The water-sealed water preheater (H-501) uses water-sealed water delivered by a stripping water pump as a cooling medium, and the water-sealed water stripping aftercooler (H-502) uses circulating cooling water as a cooling medium.
The water vapor and the nitrogen are mixed and then enter from the bottom of the tower, the trace H2S in the water is stripped, and the stripped gas enters a gas collecting tank (A-502) to separate water drops which may be carried, and then enters a sulfur recovery unit. The water seal water collected in the gas collection tank returns to the water seal water tank (T-503).
The water-sealed water in the water-sealed water tank (T-503) can also be conveyed to the stripping tower (A-501) through a water-sealed water circulating water pump P-503.
And (3) discharging cleaning water generated during cleaning of the carbon disulfide shift tank (T-501A/B/C) and the carbon disulfide storage tank (T-502A/B/C) and overflow water generated by the water seal tank (T-503) into a wastewater collection tank (T-504).
CS2The loading platform is arranged near the storage tank and passes through the CS2The loading pump is loaded into the transport tank. After the CS2 product is filled, the transportation tank is filled with nitrogen for nitrogen sealing.
The utility model discloses in the partial device operation of carbon disulfide warehousing and transportation process, storage tank water seal can contain carbon disulfide, and the carbon disulfide of long-time operation back aquatic can react and generate hydrogen sulfide, and hydrogen sulfide can dissolve into in the product carbon disulfide to influence carbon disulfide's product quality. Through the sewage strip tower that sets up, strip the water seal water in tank field, carbon disulfide and the hydrogen sulfide that desorption water seal water contains make water seal water cycle use, guaranteed product quality promptly, realized the waste water zero release again.
The torch condensate recovery part comprises a sulfur-free gas separation tank and a condensate tank, wherein an inlet of the sulfur-free gas separation tank is respectively connected with an outlet of the flash evaporation carbon disulfide receiving tank and an outlet of the carbon disulfide rectifying tower, an outlet of the sulfur-free gas separation tank is connected with a sulfur-free gas inlet of the torch sealing tank, a sulfur-containing gas inlet of the torch sealing tank is connected with an outlet of the sulfur-containing gas separation tank, and an inlet of the sulfur-containing gas separation tank is connected with an outlet of the sulfur condenser;
a liquid inlet of the condensate tank is connected with a low-pressure condensate SCL interface, a medium-pressure condensate inlet of the condensate tank is connected with an outlet at the lower end of the condensate flash tank, a liquid inlet at the upper part of the condensate flash tank is connected with a medium-pressure condensate interface SCM, and an outlet at the upper end of the condensate flash tank is connected with a 0.35MPa low-pressure steam SL interface;
an outlet at the upper end of the condensate tank is connected with a condensate inlet after the upper part of the condensate tank is flashed through a condensate flash condenser, and an outlet at the lower end of the condensate tank is connected with a deaerator through a condensate delivery pump.
And the water inlet and the water outlet of the condensate flash evaporation condenser are connected with a circulating water CW port.
The lower end enclosure part of the sulfur-free gas separation tank is provided with a jacket, the barrel body and the lower end enclosure part of the torch sealing tank are provided with jackets, and the barrel body and the lower end enclosure part of the sulfur-containing gas separation tank are provided with jackets.
The jacket can be used for heating, the jacket of the sulfur-containing gas separation tank prevents liquid sulfur from solidifying, and the jacket of the torch sealing tank prevents liquid from depositing. The jacket of the sulfur-free gas separation tank prevents liquefaction of the heavy components of the natural gas.
In the utility model, the separation tanks for sulfur-containing gas and sulfur-free gas are respectively arranged in front of the torch sealing tank to separate the liquid possibly contained in the exhaust gas, and the tank body is provided with a jacket to vaporize the collected liquid and then discharge the vaporized liquid; the medium-pressure steam condensate water firstly enters a condensate water flash tank, and 0.35MPa steam obtained by flash evaporation is sent to a low-pressure steam pipe network, so that heat energy is further saved.
It should be understood that the above detailed description of the present invention is only for illustrating the present invention and is not limited by the technical solutions described in the embodiments of the present invention, and those skilled in the art should understand that the present invention can still be modified or equivalently replaced to achieve the same technical effects; as long as the use requirement is satisfied, the utility model is within the protection scope.
Claims (5)
1. The carbon disulfide production system comprises a carbon disulfide synthesis part, a carbon disulfide separation and purification part, a carbon disulfide storage and transportation part and a torch condensate recovery part, and is characterized in that the carbon disulfide synthesis part, the carbon disulfide separation and purification part and the carbon disulfide storage and transportation part are sequentially connected, and an input port of the torch condensate recovery part is respectively connected with an output port of the carbon disulfide separation and purification part and an output port of the carbon disulfide synthesis part.
2. A carbon disulfide production system as recited in claim 1, wherein said carbon disulfide synthesis section includes a sulfur melting tank, a solid sulfur inlet is provided at an upper end of the sulfur melting tank, a lower outlet of the sulfur melting tank is connected to a first inlet at an upper end of a pre-coating tank stirrer, a second inlet at an upper end of the pre-coating tank stirrer is connected to a lower outlet of the stripper, an outlet of the pre-coating tank stirrer is connected to an upper inlet of a sulfur filter through a pre-coating tank transfer pump, a lower outlet of the sulfur filter is connected to a first inlet at an upper end of a liquid sulfur tank, a second inlet at an upper end of the liquid sulfur tank is connected to an outlet of the sulfur recovery unit, an outlet of the liquid sulfur tank is connected to a raw sulfur inlet of the reaction furnace through a liquid sulfur transfer pump, a raw material gas inlet of the reaction furnace is connected to a purified gas outlet of a natural gas pressure swing adsorption unit (PSA), a raw material gas inlet of the PSA is connected to a natural, the PSA desorption gas outlet is respectively connected with a fuel gas main pipe and a sulfur recovery port of the reaction furnace;
the outlet of the reaction furnace is connected with the inlet of the reactor, the outlet of the reactor is connected with the inlet of the sulfur condenser, the water inlet of the sulfur condenser is connected with the boiler water supply BFW interface, the steam outlet of the sulfur condenser is connected with the low-pressure steam SL interface, the outlet of the sulfur condenser is connected with the inlet of the sulfur condensate receiver, the boiler sewage outlet of the sulfur condenser is connected with the inlet of the boiler sewage discharge barrel, and the water inlet of the boiler sewage discharge barrel is connected with the circulating water backwater CW port.
3. The carbon disulfide production system according to claim 1, wherein the carbon disulfide separation and purification portion comprises a sulfur condensate receiver, an inlet of the sulfur condensate receiver is connected with an outlet of the sulfur condenser, an outlet at the upper end of the sulfur condensate receiver is respectively connected with an inlet of the desulfurization tower and an outlet of the flash evaporation carbon disulfide transfer pump, a reboiler return port of the desulfurization tower is connected with an outlet of a reboiler of the desulfurization tower, and an inlet of the reboiler of the desulfurization tower is respectively connected with an outlet at the lower end of the desulfurization tower, an outlet at the lower end of the sulfur condensate receiver and an inlet of the flash evaporation tank;
an outlet at the upper end of the desulfurizing tower is connected with an inlet of a carbon disulfide rectification feeding separation tank through a desulfurizing tower condenser, an outlet at the lower end of the carbon disulfide rectification feeding separation tank is respectively connected with an upper liquid phase feed inlet of the carbon disulfide rectification tower and an upper reflux port of the desulfurizing tower through a desulfurizing tower reflux pump, an upper gas phase feed inlet of the carbon disulfide rectification tower is connected with an upper outlet of the carbon disulfide rectification feeding separation tank, a lower outlet of the carbon disulfide rectification tower is respectively connected with a lower inlet of the carbon disulfide rectification tower, an inlet of a carbon disulfide finished product cooler and an upper outlet of the carbon disulfide rectification tower, and an outlet of the carbon disulfide finished product cooler is connected with a carbon disulfide shift tank through a carbon disulfide finished product subcooler;
the upper end gas phase outlet of the carbon disulfide refining tower is respectively connected with the upper end outlet of the flash tank and the inlet of the flash carbon disulfide condenser, the outlet of the flash carbon disulfide condenser is connected with the material inlet of the flash carbon disulfide receiving tank through a water separator, the material inlet of the flash carbon disulfide receiving tank is connected with the lower end outlet of the carbon disulfide refining tower through a jacket cooler, the upper end outlet of the flash carbon disulfide receiving tank is connected with a sulfur-free gas separation tank, and the upper end unqualified product return port of the flash carbon disulfide receiving tank is connected with the outlet of a carbon disulfide emergency pump; an outlet at the lower end of the flash evaporation carbon disulfide receiving tank is connected with an inlet of a flash evaporation carbon disulfide transfer pump;
an outlet at the lower end of the flash tank is connected with an inlet of a stripping tower, an outlet at the upper end of the stripping tower is connected with a sulfur removal and recovery interface, a sulfur outlet at the lower part of the stripping tower is connected with a sulfur recovery interface, and an outlet at the lower end of the stripping tower is connected with a precoating tank interface;
an outlet at the upper end of the carbon disulfide rectifying tower is respectively connected with a sulfur removal and recovery interface and an inlet of the sulfur-free gas separation tank.
4. The carbon disulfide production system of claim 1, wherein the carbon disulfide storage and transportation portion comprises a wastewater stripping tower, an inlet of the wastewater stripping tower is respectively connected with a 0.35MPa low-pressure steam SL interface and a nitrogen interface N, an outlet at the upper end of the wastewater stripping tower is connected with an inlet at the middle part of a gas collection tank, an outlet at the upper end of the gas collection tank is connected with a sulfur recovery interface, an outlet at the lower end of the gas collection tank is connected with a water seal water tank gas condensate return port, a first inlet of the water seal water tank is sequentially connected with a water seal water stripping aftercooler and a water seal water stripping preheater through a water seal water stripping aftercooler and a lower outlet of the wastewater stripping tower, a water seal water outlet of the water seal water stripping preheater is connected with an upper water seal water inlet of the wastewater stripping tower, a water seal water inlet of the water stripping preheater is respectively connected with an outlet of a stripping water pump, an outlet of the water seal circulation pump, an inlet of the carbon disulfide storage tank and an inlet of a carbon disulfide shift product tank, and an inlet of the stripping water pump is respectively connected with an outlet at the middle part of the water seal water stripping tank, The outlet of the waste water collecting tank is connected, and the water outlet of the waste water collecting tank is connected with a drainage ditch;
a first inlet of the wastewater collection tank is connected with an overflow port of a water-sealed water tank, a fresh water inlet of the water-sealed water tank is connected with production water IW, a second inlet of the water-sealed water tank is respectively connected with a water-sealed water overflow port of the carbon disulfide regular production tank and a water-sealed water overflow port of the carbon disulfide storage tank, and a water-sealed water outlet of the water-sealed water tank is connected with an inlet of a water-sealed water circulating pump;
a second inlet of the wastewater collection tank is respectively connected with a cleaning water outlet of a carbon disulfide shift production tank and a cleaning water outlet of a carbon disulfide storage tank, a carbon disulfide inlet of the carbon disulfide shift production tank is connected with an outlet of a carbon disulfide finished product subcooler, a carbon disulfide outlet of the carbon disulfide shift production tank is respectively connected with an inlet of a carbon disulfide emergency pump, an inlet of a carbon disulfide conveying and loading pump and an inlet of a carbon disulfide storage tank, and an outlet of the carbon disulfide emergency pump is connected with an inlet of a flash evaporation carbon disulfide receiving tank;
carbon disulfide is carried and the car loading pump export links to each other with carbon disulfide storage tank carbon disulfide import, tank car import respectively.
5. The carbon disulfide production system according to claim 1, wherein the torch condensate recovery part comprises a sulfur-free gas separation tank and a condensate tank, an inlet of the sulfur-free gas separation tank is respectively connected with an outlet of the flash carbon disulfide receiving tank and an outlet of the carbon disulfide rectifying tower, an outlet of the sulfur-free gas separation tank is connected with an inlet of a torch seal tank which does not contain sulfur gas, a sulfur-containing gas inlet of the torch seal tank is connected with an outlet of the sulfur-containing gas separation tank, and an inlet of the sulfur-containing gas separation tank is connected with an outlet of a sulfur condenser;
a liquid inlet of the condensate tank is connected with a low-pressure condensate SCL interface, a medium-pressure condensate inlet of the condensate tank is connected with an outlet at the lower end of the condensate flash tank, a liquid inlet at the upper part of the condensate flash tank is connected with a medium-pressure condensate interface SCM, and an outlet at the upper end of the condensate flash tank is connected with a 0.35MPa low-pressure steam SL interface;
an outlet at the upper end of the condensate tank is connected with a condensate inlet after the upper part of the condensate tank is flashed through a condensate flash condenser, and an outlet at the lower end of the condensate tank is connected with a deaerator through a condensate delivery pump.
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| CN202022929693.6U CN213865387U (en) | 2020-12-09 | 2020-12-09 | Carbon disulfide production system |
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| CN202022929693.6U CN213865387U (en) | 2020-12-09 | 2020-12-09 | Carbon disulfide production system |
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Effective date of registration: 20211118 Address after: No.8 Tiexi Road, Taizihe District, Liaoyang City, Liaoning Province Patentee after: LIAOYANG RUIXING CHEMICAL Co.,Ltd. Address before: 138000 chemical industry park, Changling Ring Industrial Zone, Changling County, Songyuan City, Jilin Province Patentee before: Jilin Sanyuan Chemical Co.,Ltd. |