阅读说明：本技术 二硫化碳分离提纯系统 (Carbon disulfide separation purification system ) 是由 李晓亮 于 2020-12-09 设计创作，主要内容包括：二硫化碳分离提纯系统属于二硫化碳生产技术领域,尤其涉及一种二硫化碳分离提纯系统。本发明提供一种工作效果好的二硫化碳分离提纯系统。本发明包括硫冷凝液接收器,硫冷凝液接收器的进口接硫冷凝器的出口,硫冷凝液接收器上端出口分别与脱硫塔进口、闪蒸二硫化碳输送泵出口相连,脱硫塔的再沸器返回口接脱硫塔再沸器的出口,脱硫塔再沸器的进口分别与脱硫塔下端出口、硫冷凝液接收器下端出口、闪蒸罐进口相连。(Carbon disulfide separation and purification system belongs to carbon disulfide production technical field, especially relates to a carbon disulfide separation and purification system. The invention provides a carbon disulfide separation and purification system with a good working effect. The system comprises a sulfur condensate receiver, wherein 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 transfer pump, a reboiler return port of the desulfurizing tower is connected with an outlet of a reboiler of the desulfurizing tower, and an 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.)

1. The carbon disulfide separation and purification system is characterized by comprising a sulfur condensate receiver, wherein the inlet of the sulfur condensate receiver is connected with the outlet of a sulfur condenser, the outlet at the upper end of the sulfur condensate receiver is respectively connected with the inlet of a desulfurizing tower and the outlet of a flash evaporation carbon disulfide conveying pump, the reboiler return port of the desulfurizing tower is connected with the outlet of a reboiler of the desulfurizing tower, and the inlet of the reboiler of the desulfurizing tower is respectively connected with the outlet at the lower end of the desulfurizing tower, the outlet at the lower end of the sulfur condensate receiver and the inlet of a flash;

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 a sulfur-free gas separation tank;

the process gas condensed by the condenser enters a sulfur condensate receiver, and gas and liquid phases are separated;

the liquid phase separated by the sulfur condensate receiver is gathered in a separation tank, and the liquid sulfur and the sulfur from the desulfurizing tower (A-402) enter a flash tank (A408); CS₂Is flashed off, and the flashed product contains trace CS₂And H₂Allowing sulfur of the S to enter a stripping tower for stripping by virtue of self-flow, allowing liquid sulfur at the bottom of the stripping tower to flow into a precoating tank by virtue of gravity, and allowing gas at the top of the stripping tower to still return to a sulfur recovery system; the gas phase coming out of the top of the flash tank (A-408) enters a flash CS₂A 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).

2. The carbon disulfide separation and purification system according to claim 1, wherein a steam inlet of the reboiler of the desulfurization tower is connected with a 0.8MPa medium pressure steam SM interface, and a liquid outlet of the reboiler of the desulfurization tower is connected with a medium pressure condensate SCM interface.

3. The carbon disulfide separation and purification system according to claim 1, wherein the water inlet and outlet of the condenser of the desulfurization tower are connected with a circulating water CW port.

4. The carbon disulfide separation and purification system according to claim 1, wherein an overhead carbon disulfide rectification tower condenser is arranged at the upper end of the carbon disulfide rectification tower, and a water inlet and a water outlet of the carbon disulfide rectification tower condenser are connected with a chilled water interface GW 2.

5. The carbon disulfide separation and purification system according to claim 1, wherein the reboiler return port at the lower part of the carbon disulfide rectification tower is connected with the outlet at the lower end of the carbon disulfide rectification tower through a reboiler of the carbon disulfide rectification tower, the steam inlet of the reboiler of the carbon disulfide rectification tower is connected with a 0.8MPa low-pressure steam SM interface, and the condensate outlet of the reboiler of the carbon disulfide rectification tower is connected with a medium-pressure condensate interface SCM.

6. The carbon disulfide separation and purification system of claim 1, wherein the reboiler return port at the lower part of the carbon disulfide refining tower is connected with the outlet at the lower end of the carbon disulfide refining tower through a reboiler of the carbon disulfide refining tower, the steam inlet of the reboiler of the carbon disulfide refining tower is connected with a 0.35MPa low-pressure steam SL interface, and the condensate outlet of the reboiler of the carbon disulfide refining tower is connected with a low-pressure condensate SCL interface.

7. The carbon disulfide separation and purification system according to claim 1, wherein 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.

8. The carbon disulfide separation and purification system according to claim 1, wherein an overhead carbon disulfide refining tower condenser is arranged at the upper end of the carbon disulfide refining tower, and the water inlet and the water outlet of the carbon disulfide refining tower condenser are connected with a circulating water CW port.

9. The carbon disulfide separation and purification system of claim 1, wherein the water inlet of the flash carbon disulfide condenser is connected with a circulating water CW port.

10. The carbon disulfide separation and purification system according to claim 1, wherein the water inlet and outlet of the jacketed pipe cooler are connected with a circulating water CW port.

Technical Field

The invention belongs to the technical field of carbon disulfide production, and particularly relates to a carbon disulfide separation and purification 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 separation and purification system is still to be further improved.

Disclosure of Invention

The invention aims at the problems and provides a carbon disulfide separation and purification system with good working effect.

In order to achieve the purpose, the invention adopts the following technical scheme that the device comprises a sulfur condensate receiver, wherein the inlet of the sulfur condensate receiver is connected with the outlet of a sulfur condenser, the outlet at the upper end of the sulfur condensate receiver is respectively connected with the inlet of a desulfurizing tower and the outlet of a flash evaporation carbon disulfide conveying pump, the reboiler return port of the desulfurizing tower is connected with the outlet of a reboiler of the desulfurizing tower, and the inlet of the reboiler of the desulfurizing tower is respectively connected with the outlet at the lower end of the desulfurizing tower, the outlet at the lower end of the sulfur condensate receiver and the inlet;

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 a preferable scheme, 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.

As another preferred scheme, the water inlet and the water outlet of the condenser of the desulfurizing tower are connected with a circulating water CW port.

As another preferred scheme, the upper end of the carbon disulfide rectifying tower is provided with an overhead carbon disulfide rectifying tower condenser, and a water inlet and a water outlet of the carbon disulfide rectifying tower condenser are connected with a chilled water interface GW 2.

As another preferred scheme, a reboiler return port at the lower part of the carbon disulfide rectifying tower is connected with an outlet at the lower end of the carbon disulfide rectifying tower through a reboiler of the carbon disulfide rectifying tower, a steam inlet of the reboiler of the carbon disulfide rectifying tower is connected with a 0.8MPa low-pressure steam SM interface, and a condensate outlet of the reboiler of the carbon disulfide rectifying tower is connected with a medium-pressure condensate interface SCM.

As another preferred scheme, a reboiler return port at the lower part of the carbon disulfide refining tower is connected with an outlet at the lower end of the carbon disulfide refining tower through a reboiler of the carbon disulfide refining tower, a steam inlet of the reboiler of the carbon disulfide refining tower is connected with a 0.35MPa low-pressure steam SL interface, and a condensate outlet of the reboiler of the carbon disulfide refining tower is connected with a low-pressure condensate SCL interface.

As another preferred scheme, 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.

As another preferred scheme, the upper end of the carbon disulfide refining tower is provided with an overhead carbon disulfide refining tower condenser, and the water inlet and the water outlet of the carbon disulfide refining tower condenser are connected with a circulating water CW port.

As another preferred scheme, the water inlet of the flash evaporation carbon disulfide condenser is connected with a circulating water CW port.

And secondly, the water inlet and the water outlet of the double-pipe type cooler are connected with a circulating water CW port.

In addition, a zigzag pipeline is arranged between the outlet at the lower end of the stripping tower and the interface of the pre-coating groove.

The invention has the beneficial effects.

The device of the invention does not have storage equipment and a delivery pipeline for the liquid hydrogen sulfide, thereby increasing the safety of the device. 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.

Drawings

The invention is further described with reference to the following figures and detailed description. The scope of the invention is not limited to the following expressions.

Figure 1 is a schematic diagram of a portion of the carbon disulfide synthesis of the present invention.

Figure 2 is a schematic structural diagram of a carbon disulfide separation and purification part of the invention.

Figure 3 is a schematic structural diagram of a part of carbon disulfide storage and transportation of the invention.

FIG. 4 is a schematic structural diagram of a recovery part of the flare condensate.

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 carbon disulfide separation and purification system can be applied to a carbon disulfide production system, the carbon disulfide production system comprises a carbon disulfide synthesis part, a carbon disulfide separation and purification part (namely, the carbon disulfide separation and purification system of the invention), a carbon disulfide storage and transportation part and a torch condensation liquid recovery part, 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 condensation liquid 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.

The carbon disulfide synthesis part of the invention produces carbon disulfide through reaction, the carbon disulfide purification part obtains a pure carbon disulfide product, the carbon disulfide storage and transportation part is convenient for the storage and transportation of the carbon disulfide, and the torch condensate recovery part recovers the condensate, thereby saving and protecting the environment. The invention is beneficial to the reliable and high-efficiency production of the carbon disulfide by the mutual matching of all parts.

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, 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 carbon disulfide synthesis part of the invention is the purification of the raw materials of sulfur and natural gas, and the carbon disulfide is produced by reaction in a reaction furnace and a 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;

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.

The carbon disulfide rectifying tower and the carbon disulfide refining tower of the carbon disulfide separation and purification part 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.

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.

Post-condensation processThe stream enters 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 provided with carbon disulfide containing impurities, and the carbon disulfide enters a flash evaporation CS after being cooled by a jacketed pipe type cooler₂And 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 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, 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 enter into in the groove all is by the interval entering groove of third in, if there is the material to reveal, because material proportion is greater than water, the material can deposit and collect in the interval of third and second 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 CS₂Collected in one of three carbon disulfide shift tanks (T-501A/B/C), which were used alternately, each of which could store approximately 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 easy volatilization, so it is needed to be sealed by waterAnd (4) storing. 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.

In the running process of the carbon disulfide storage and transportation device, the water-sealed water of the storage tank contains carbon disulfide, the carbon disulfide in the water can react to generate hydrogen sulfide after long-time running, and the hydrogen sulfide can be dissolved into the carbon disulfide product, so that the product quality of the carbon disulfide is influenced. 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 recovery part of the torch condensate, a sulfur-containing gas separation tank and a sulfur-free gas separation tank are respectively arranged in front of a torch sealing tank to separate liquid possibly contained in the discharged gas, and meanwhile, a tank body is provided with a jacket and discharges the collected liquid after vaporization; 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 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 be modified or substituted equally to achieve the same technical effects; as long as the use requirements are met, the method is within the protection scope of the invention.