CN112843983A - Recovery process of carbon disulfide in viscose fiber production - Google Patents
Recovery process of carbon disulfide in viscose fiber production Download PDFInfo
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- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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- C01B32/00—Carbon; Compounds thereof
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Abstract
The invention discloses a recovery process of carbon disulfide in viscose fiber production, which is used for recovering CS (carbon disulfide) generated in the production process of viscose staple fiber2And H2S mixed gas is washed by alkali to remove H2After S, the active carbon is absorbed and recoveredCS2The secondary adsorption tank is arranged to further adsorb waste gas, high-standard discharge is realized, alkaline waste water generated by the tertiary alkaline washing tank enters from the upper part of the conversion device, is mixed with acidic waste water from a spinning workshop, and is subjected to full reaction through a plurality of baffle plates under the aeration action of compressed air below, and separated H2The S gas is removed from the acid making device under the action of negative pressure, after neutralization reaction, the neutralized liquid enters the physicochemical pool, lime is added for physicochemical reaction, and finally the neutralized liquid enters the biochemical pool for treatment and then is discharged after reaching the standard.
Description
Technical Field
The invention relates to the field of energy conservation and environmental protection, in particular to a recovery process of carbon disulfide in viscose fiber production.
Background
The adsorption method is used for treating waste gas in viscose production, namely the activated carbon is used for treating CS in the waste gas under specific conditions2Adsorbing and desorbing CS by steam2Desorbing from activated carbon, condensing and recovering the recovered CS2Then put into viscose production, the CS recovered by the method2The quality of the product completely reaches the commercial product CS2The quality of (2). The whole adsorption-desorption-re-adsorption-re-desorption is a physical circulation process due to H in the waste gas2S can poison the activated carbon, can quickly reduce the activity and the service life of the activated carbon, thereby seriously affecting the CS of the activated carbon2The adsorption efficiency of (2) or even the adsorption cannot be carried out, so that the CS is recovered by the adsorption method2Process configuration H2And the step of S removal, namely the step of alkali washing and washing, and in addition, according to the use condition of the prior waste gas treatment, the exhaust emission concentration is about 200ppm and can not meet the environmental protection requirement, so the invention is provided with a secondary adsorption tank for further adsorbing the waste gas and then discharging the waste gas at a high standard.
CS produced in the production process of viscose staple fiber2And H2S mixed gas is washed by alkali to remove H2After S, the CS is recovered by active carbon adsorption2NaOH solution and H in three alkaline washes2After S reaction, a large amount of alkali wastewater is generated, and the components of the wastewater comprise 10-30% of NaHS and 2-4% of Na2S belongs to strong alkali property, and if the S is directly discharged to a whole plant wastewater treatment system, the S causes serious burden of wastewater treatment and increases the cost. Therefore, two treatment methods are generally adopted for the alkali wastewaterThe formula (I): (1) setting an evaporation concentration system for tabletting; (2) set up H2The S gas conversion system is used for treating alkaline wastewater, and NaHS solution reacts with acid to remove H2And S gas is merged into a combustion acid making device.
Collected low concentrations of NaHS and Na2The alkaline waste water of S, if the tablet is produced, consumes a large amount of steam for evaporation concentration, and is extremely uneconomical; if the acid is prepared, fresh acid is consumed, which is not economical; in addition, the tows generated from the spinning machine can be finished products through a series of procedures of drafting, cutting, washing, desulfurizing, bleaching, oiling, drying, weighing and packaging, and a large amount of acidic wastewater can be generated in the process of washing, and under the general condition, the amount of acidic wastewater in a viscose staple fiber production plant>The alkaline waste water amount is utilized, a set of device is designed by utilizing the characteristic, and H is removed by utilizing the neutralization reaction of the acidic waste water generated in the spinning workshop and the alkaline waste water generated in the waste gas treatment workshop2And S gas is merged into a combustion acid making device, so that the aim of saving fresh acid is fulfilled.
Disclosure of Invention
In order to solve the problems, the invention discloses a recovery process of carbon disulfide in viscose fiber production, which has the advantages of simple process, convenient operation, high waste gas recovery rate, waste liquid reduction, waste material recycling, resource saving, high efficiency, environmental protection and high emission standard.
In order to achieve the above object, the present invention provides a carbon disulfide recovery process in viscose fiber production, which is characterized by comprising the following steps:
(1) conveying the produced waste gas to a tertiary alkaline washing tank by an alkaline washing fan, and reacting the sprayed NaOH aqueous solution with the produced waste gas to remove H2S, discharging waste alkaline water discharged from the tertiary alkaline washing tank to a conversion system, passing waste gas discharged from the tertiary alkaline washing tank through a washing tower, then entering a separator and a cooler to separate moisture, and then conveying the waste alkaline water to a primary adsorption tank through a waste gas fan; h in the waste gas conveyed to the primary adsorption tank2The concentration of S is lower than 10 ppm;
H2S+2NaOH = Na2S+2H2O；
H2S+Na2S = 2NaHS；
(2) adsorbing CS in the exhaust gas discharged in the step (1) by a primary adsorption tank2After saturation of adsorption, first pass through N2Purging O in primary adsorption tank2Then introducing steam to the adsorbed CS2Performing desorption, the desorbed CS2Steam and condensed water enter the evaporating pot together;
(3) conveying the waste gas discharged after the absorption in the primary absorption tank in the step (2) to a secondary absorption tank and then discharging the waste gas to an exhaust tower, and after the secondary absorption tank is saturated in absorption, passing through N2Purging O in secondary adsorption tank2Then introducing steam to the adsorbed CS2Performing desorption, the desorbed CS2Steam and condensed water enter an evaporating pot together to obtain CS containing water vapor2Steam;
(4) the CS containing water vapor obtained in the step (2) and the step (3)2The steam enters the first condenser, most of the water vapor and CS2Cooling the steam into liquid, passing through a gas-liquid separator, and collecting uncooled CS containing water vapor2The steam enters a safety tank and is circulated into a primary absorption tank again, and the primary absorption tank contains liquid CS2The water enters a second condenser to be further cooled into a liquid state;
(5) layering the mixed liquid condensed in the step (3) by a specific gravity separator, and then CS2Further cooling in an after-cooler, and metering to enter CS2A storage tank.
Further, the primary adsorption tank and the secondary adsorption tank are independent DCS programs, activated carbon is filled in the primary adsorption tank and the secondary adsorption tank, the secondary adsorption tank comprises 3 adsorption tanks, and the total air volume of the secondary adsorption tank is 70000m3/h。
Further, change system includes conversion equipment in step (1), conversion equipment connects spent acid holding vessel and spent acid holding vessel, the wash bowl is connected to the inlet of spent acid holding vessel, the cubic alkali wash tank is connected to the inlet of spent alkali holding vessel, all be equipped with filter mechanism in spent acid holding vessel and the spent alkali holding vessel, conversion equipment is connected to the liquid outlet of spent acid holding vessel and the liquid outlet of spent alkali holding vessel, conversion equipment is inside to be equipped with a plurality of baffling boards and a plurality of aeration mechanism, the baffling board transversely sets up or vertically sets up, still be equipped with the liquid level detector in the conversion equipment, gas dispersion pond is connected to conversion equipment, be equipped with aeration mechanism in the gas dispersion pond, the physicochemical reaction pond is connected to the gas dispersion pond, biochemical reaction pond is connected to the physicochemical reaction pond.
Further, conversion equipment includes the barrel, and the barrel top is equipped with waste alkali lye import, waste acid liquid import, gas vent, observation hole and manometer, and the barrel bottom is equipped with the liquid outlet, waste acid liquid access connection house steward, house steward connect a plurality of branch pipes, are equipped with the shower nozzle on the branch pipe, and the barrel is inside to be equipped with a plurality of baffling boards, and the inner wall of barrel is connected to baffling board one end, and another tip all is equipped with the overflow board, and aeration mechanism is all connected to the lower surface of baffling board, is equipped with a plurality of T type aeration holes in the aeration mechanism, T type aeration hole runs through the baffling board, and the barrel side is equipped with a plurality of imports and exports, and the baffl.
Further, a plurality of pH detectors are arranged inside the cylinder, and the pH detectors are arranged above and below the baffle plate.
Further, filtering mechanism includes filter and slag notch, the filter is arranged in spent acid holding vessel or waste alkali holding vessel to one side, the filter lower extreme is equipped with the recess, is equipped with the filter cell in the recess, filter cell one end upper portion is equipped with the opening, the retainer plate is connected to the other end of filter cell, and the retainer plate is arranged in between slag notch and the sealed lid, sealed covering is equipped with bracing piece both ends and connects the hydraulic stem, be equipped with liquid level detector and pH detector in spent acid holding vessel and the spent acid holding vessel.
Further, the conversion system comprises the following steps:
(1) conveying the waste alkaline water to a waste alkaline storage tank, filtering, and storing the waste alkaline water filtrate in the waste alkaline storage tank;
(2) conveying the waste acid water to a waste acid storage tank, and storing the filtrate of the filtered waste acid water in the waste acid storage tank;
(3) conveying the waste alkali water filtrate obtained in the step (1) to a waste alkali liquid inlet of a conversion device, and allowing the waste alkali water filtrate to flow intoConveying the waste acid water filtrate obtained in the step (2) to a waste acid liquid inlet of the conversion device on a baffle plate, spraying the waste acid water filtrate to the waste alkali water filtrate on the baffle plate through a branch pipe, discharging compressed air from a T-shaped aeration hole by an aeration mechanism, aerating the waste alkali water filtrate and the waste acid water filtrate, then flowing into the baffle plate below, aerating again until the compressed air flows to the bottom of the conversion device, and separating out H2S, discharging the gas from an exhaust port to an acid making device under the action of negative pressure to obtain a neutralized liquid;
(4) conveying the neutralized liquid obtained in the step (3) to a gas dispersing pool, aerating again, and separating out H2S, discharging to an acid making device under the action of negative pressure;
(5) and (4) sequentially feeding the neutralization solution obtained in the step (4) into a physicochemical reaction tank and a biochemical tank, and discharging after reaching the standard.
Further, the alkaline waste water in the step (1) is alkaline waste water generated in a tertiary alkaline washing tank in a carbon disulfide recovery process in viscose fiber production, and the alkaline waste water comprises NaHS and Na2S, the concentration of NaHS is 10-30%, and Na is2The concentration of S is 2-4%, the waste acid water in the step (2) is waste acid water generated in a tow washing tank in the spinning process, and the concentration of H + in the waste acid water is 3500mg/L of 2000-3500 mg/L.
Further, the aeration time in the step (3) is 0.5 to 12 hours, and the aeration time in the step (4) is 0.5 to 6 hours.
Compared with the prior art, the invention has the following advantages and beneficial effects:
(1) the invention adopts the secondary adsorption tank to further adsorb the waste gas discharged by the primary adsorption tank, meets the environmental protection requirement and improves the emission standard.
(2) The invention enters low-concentration alkaline wastewater generated by waste gas treatment from the upper part of the conversion device, is mixed with acidic wastewater from a spinning workshop, and then passes through a plurality of baffle plates to fully react the acidic and alkaline wastewater under the aeration action of compressed air at the lower part, so that separated H2The S gas is removed to prepare acid under the action of negative pressure, after neutralization reaction, the neutralized liquid enters a physicochemical pool, lime is added to carry out physicochemical reaction, and finally the neutralized liquid enters a biochemical pool to be treatedThe method has the advantages of simple process, convenient operation, reutilization of waste liquid, waste material utilization, resource saving, high efficiency and environmental protection.
(3) According to the invention, the filter plates are arranged in the waste acid storage tank and the waste alkali storage tank, the lower end of each filter plate is provided with the groove, the filter tank is arranged in the groove, the upper part of one end of the filter tank is provided with the opening, the other end of the filter tank is connected with the fixing ring, the fixing ring is arranged between the slag outlet and the sealing cover, the sealing cover is provided with the supporting rod, the two ends of the supporting rod are connected with the hydraulic rod, so that filter residues are automatically deposited in the filter tank, and the hydraulic rod is controlled to move the sealing cover, so.
Drawings
FIG. 1 is a schematic view of the process of the present invention;
FIG. 2 is a schematic process flow diagram of the conversion system of the present invention;
FIG. 3 is a schematic structural diagram of the conversion device of the present invention;
FIG. 4 is a schematic structural diagram of a spent caustic storage tank according to the present invention;
description of reference numerals:
1. a spent caustic storage tank; 2. a spent acid storage tank; 3. a conversion device; 4. a gas dispersing pool; 5. a physicochemical reaction tank; 6. a biochemical pool; 7. a delivery pump; 8. a battery valve; 301. a barrel; 302. waste alkali liquor inlet; 303. a waste acid liquor inlet; 304. a header pipe; 305. an exhaust port; 306. an observation hole; 307. a pressure gauge; 308. a spray head; 309. a branch pipe; 310. a liquid level detector; 311. an overflow plate; 312. a baffle plate; 313. t-shaped aeration holes; 314. an aeration mechanism; 315. a pH detector; 316. a liquid outlet; 317. an inlet; 318. a U-shaped pipe; 319. an outlet; 101. a liquid inlet of a waste alkali storage tank; 102. a liquid outlet of the spent caustic storage tank; 103. an opening; 104. a hydraulic lever; 105. a stationary ring; 106. a groove; 107. a filter plate; 108. a support bar; 109. a filter cell; 110. a sealing cover; 9, an alkaline washing fan; 10. a third alkaline washing tank; 11. a washing tower; 12. a dirty air blower; 13. a primary adsorption tank; 14. adsorbing grass for the second time; 15. an exhaust column; 16. an evaporator tank; 17. a safety tank; 18. a first condenser and a second condenser; 19. a gas-liquid separator; 20. a specific gravity separator; 21. an aftercooler; 22. CS2A storage tank; 23An acid making device; 24. a conversion system; 25. producing foul gas.
Detailed Description
The present invention will be further illustrated with reference to the accompanying drawings and specific embodiments, which are to be understood as merely illustrative of the invention and not as limiting the scope of the invention. It should be noted that the terms "front," "back," "left," "right," "upper" and "lower" used in the following description refer to directions in the drawings, and the terms "inner" and "outer" refer to directions toward and away from, respectively, the geometric center of a particular component.
Example 1
A recovery process of carbon disulfide in viscose fiber production comprises the following steps:
(1) the alkaline washing fan 9 conveys the production waste gas 25 to a tertiary alkaline washing tank 10, and the sprayed NaOH aqueous solution reacts with the production waste gas 25 to remove H2S, discharging waste alkaline water discharged from the tertiary alkaline washing tank 10 to a conversion system 24, passing waste gas discharged from the tertiary alkaline washing tank 10 through a washing tower 11, then entering a separator and a cooler to separate moisture, and then passing through a waste gas fan 12 to be conveyed to a primary adsorption tank 13; h in the exhaust gas sent to the primary adsorption tank 132The concentration of S is 8 ppm;
H2S+2NaOH = Na2S+2H2O；
H2S+Na2S = 2NaHS；
(2) the primary adsorption tank 13 adsorbs CS in the exhaust gas discharged in the step (1)2After saturation of adsorption, first pass through N2Purging O in the primary absorption tank 132Then introducing steam to the adsorbed CS2Performing desorption, the desorbed CS2The steam and the condensed water enter the evaporating pot 16 together;
(3) conveying the waste gas discharged from the primary adsorption tank 13 in the step (2) to a secondary adsorption tank 14, then discharging the waste gas to an exhaust tower 15, and after the secondary adsorption tank 14 is saturated in adsorption, passing through N2Purging O in the secondary absorption tank 142Then introducing steam to the adsorbed CS2Performing desorption, the desorbed CS2The steam and the condensed water enter the evaporating pot 16 together;
（4）the CS containing water vapor obtained in the step (2) and the step (3)2The steam enters the first of the first and second condensers 18, mostly water vapor and CS2The steam is cooled to a liquid state, and the uncooled CS containing the water vapor is passed through a gas-liquid separator 192The steam enters the safety tank 17 and is recycled into the primary absorption tank 13 again, containing the liquid CS2The water is further cooled to a liquid state in a second condenser of the first and second condensers 18;
(5) layering the mixed liquid condensed in the step (3) by a specific gravity separator 20, and then CS2Enters the after-cooler 21 for further cooling and then enters the CS after being measured2A storage tank 22.
The primary adsorption tank 13 and the secondary adsorption tank 14 are independent DCS programs, activated carbon is filled in both the primary adsorption tank 13 and the secondary adsorption tank 14, the secondary adsorption tank 14 comprises 3 adsorption tanks, and a process flow chart is shown in figure 1.
Example 2
According to the use condition of the previous waste gas treatment of Jilin chemical fiber company Limited, the exhaust emission concentration is about 200ppm and can not meet the environmental protection requirement, the secondary adsorption process is adopted, the treated exhaust is sent to an exhaust tower, the exhaust emission concentration is 50ppm, and the environmental protection requirement is met; the scheme is as follows:
considering comprehensive treatment of tail gas in combination with site area, investment cost, operation stability and operation convenience, tail gas of a single line is introduced into 3 absorption tanks of a secondary absorption tank 14, the total air volume of secondary absorption is designed to be 70000 m/h, the air volume of a single absorption tank is designed to be 35000 m/h, 1 of the 3 absorption tanks is in a normal absorption working state, 1 is in an air inlet state, and 1 is in a standby state; the increased 3 absorption tanks of this secondary adsorption will be shared with the condensing system of the primary adsorption tank 13 to reduce investment and floor space.
The first adsorption tank 13 normally has a tail gas exceeding the emission standard, namely the tank time with the longest air intake time, in order to ensure the tail gas emission to reach the standard, the tail gas of the tank time with the longest air intake time is replaced into the second adsorption tank 14, the valve for exhausting the tail gas to the exhaust tower is automatically closed, and the valve for entering the second adsorption tank 14 is automatically opened.
After the analysis of any absorption tank in the primary absorption tank 13 is completed, a time interval of about 40 minutes is provided, so that the secondary absorption tank 14 can be completely analyzed by using the time interval after being saturated, the normal operation of the primary absorption tank 13 is not influenced, and the primary absorption tank 13 and the secondary absorption tank 14 are independent DCS programs.
Example 3: a process for recovering carbon disulfide from viscose production, conversion system 24 comprising the steps of:
(1) conveying alkaline waste water generated by a tertiary alkaline washing tank in the viscose fiber production process to an alkaline waste storage tank 1, filtering, storing filtrate of alkaline waste water in the alkaline waste storage tank 1, wherein the concentration of NaHS in the alkaline waste water is 22% and Na2The concentration of S is 2%;
(2) conveying waste acid water generated by a tow washing tank in a spinning process to a waste acid storage tank 2, and storing a filtered waste acid water filtrate in the waste acid storage tank 2, wherein the concentration of H & lt + & gt in the waste acid water is 3000 mg/L;
(3) conveying the waste alkali water filtrate obtained in the step (1) to a waste alkali liquid inlet 302 of a conversion device 3, flowing into a baffle plate 312, conveying the waste acid water filtrate obtained in the step (2) to a waste acid liquid inlet 303 of the conversion device 3, spraying the waste alkali water filtrate on the baffle plate 312 through a branch pipe 309, discharging compressed air from a T-shaped aeration hole 313 by an aeration mechanism 314, aerating the waste alkali water filtrate and the waste acid water filtrate, then flowing onto the baffle plate 312 below, aerating again until the waste alkali water filtrate flows to the bottom of the conversion device 3, continuing aerating the waste alkali water filtrate at a liquid level detector 310 for 1 hour, and separating out H2S, discharging the gas from an exhaust port to an acid making device under the action of negative pressure to obtain a neutralized liquid;
(4) conveying the neutralized liquid obtained in the step (3) to a gas diffusion pool 4, aerating for 1 hour again, and separating out H2S, discharging to an acid making device under the action of negative pressure;
(5) and (4) sequentially feeding the neutralization solution obtained in the step (4) into a physicochemical reaction tank 5 and a biochemical tank 6, and discharging after reaching the standard.
The treatment method for recycling the low-concentration alkaline wastewater from the waste gas has the advantages of simple process, convenient operation, reutilization of waste liquid, waste change into valuable, improvement of emission standard, resource saving, high efficiency and environmental protection.
Example 4: as shown in fig. 2 to 4, the conversion system 24 includes a waste acid storage tank 2, a waste alkali storage tank 1 and a conversion device 3, a liquid inlet of the waste acid storage tank 2 is connected to a washing tank, a liquid inlet 101 of the waste alkali storage tank is connected to an alkali washing tank, a first filtering mechanism is disposed in the waste acid storage tank 2, a second filtering mechanism is disposed in the waste alkali storage tank 1, a liquid outlet of the waste acid storage tank and a liquid outlet 102 of the waste alkali storage tank are connected to the conversion device 3, the volume of the conversion device 3 is larger than the sum of the volumes of the waste acid storage tank 2 and the waste alkali storage tank 1, a baffle 312 and an aeration device 314 are disposed in the conversion device 3, the baffle 312 is disposed horizontally or longitudinally, a liquid level detector 310 and a plurality of pH detectors 315 are further disposed in the conversion device 3, the pH detectors 315 are disposed between the baffles 312, the conversion device 3 is connected to a gas diffusion pool 4, an aeration mechanism 314 is disposed in the, the physicochemical reaction tank 5 is connected with the biochemical tank 6, the connection is realized through a pipeline, a delivery pump 7 and a battery valve 8 are arranged on the pipeline, and the battery valve 8, the delivery pump 7, the pH detector 315 and the liquid level detector 310 are in communication connection.
The conversion device 3 comprises a cylinder 301, the top of the cylinder 301 is provided with a waste alkali liquid inlet 302, a waste acid liquid inlet 303, an exhaust port 305, an observation hole 306 and a pressure gauge 307, the bottom of the cylinder 301 is provided with a liquid outlet 316, the waste acid liquid inlet 303 is connected with a main pipe 304, the main pipe 304 is connected with a plurality of branch pipes 309, the branch pipes 309 are provided with spray heads 308, the inside of the cylinder 301 is provided with a plurality of baffle plates 312, one end of each baffle plate 312 is connected with the inner wall of the cylinder 301, the other end of each baffle plate 312 is provided with an overflow plate 311, the lower surfaces of the baffle plates 312 are connected with an aeration mechanism 314, the aeration mechanism 314 is provided with a plurality of T-shaped aeration holes 313, the T-shaped aeration holes 313 penetrate through the baffle plates 312, the side surface of the cylinder 301 is provided with.
The inside pH detector 315 that is equipped with of barrel 301, pH detector 315 set up in the top and the below of baffling board 312, and the pH of waste liquid between each baffling board 312 is monitored in real time, just can discharge when upper and lower pH is up to standard and even, improves discharge standard.
The top parts of the waste alkali storage tank 1 and the waste acid storage tank 2 are respectively provided with an observation hole 306 and a pressure gauge 307, the filtering mechanism comprises a filtering plate 107 and a slag outlet, the filtering plate 107 is obliquely arranged in the waste acid storage tank 2, the lower end of the filtering plate 107 is provided with a groove 106, a filtering tank 109 is arranged in the groove 106, the upper part of one end of the filtering tank 109 is provided with an opening 103, the other end of the filtering tank 109 is connected with a fixing ring 105, the fixing ring 105 is arranged between the slag outlet and a sealing cover 110, the sealing cover 110 is provided with a supporting rod 108, two ends of the supporting rod 108 are connected with a hydraulic rod 104; when the value of the pressure gauge 307 becomes high, the adjusting hydraulic rod 104 drives the sealing cover 110 to open, the filter tank 109 is taken out through the fixing ring 105, and the filter tank 109 is cleaned and then installed again for use.
Be equipped with liquid level detector 310 real-time supervision liquid level in the filter house, when the liquid level exceeded liquid level detector 310, just carried spent acid filtrate and waste alkali filtrate to conversion equipment 3 and carried out neutralization reaction.
The technical means disclosed in the invention scheme are not limited to the technical means disclosed in the above embodiments, but also include the technical scheme formed by any combination of the above technical features. It should be noted that those skilled in the art can make various improvements and modifications without departing from the principle of the present invention, and such improvements and modifications are also considered to be within the scope of the present invention.
Claims (9)
1. A recovery process of carbon disulfide in viscose fiber production is characterized by comprising the following steps:
(1) conveying the produced waste gas to a tertiary alkaline washing tank by an alkaline washing fan, and reacting the sprayed NaOH aqueous solution with the produced waste gas to remove H2S, discharging waste alkaline water discharged from the tertiary alkaline washing tank to a conversion systemWaste gas discharged by the third alkaline washing tank passes through a washing tower, enters a separator and a cooler to separate moisture, and is conveyed to the primary adsorption tank through a dirty gas fan; h in the waste gas conveyed to the primary adsorption tank2The concentration of S is lower than 10 ppm;
H2S+2NaOH = Na2S+2H2O；
H2S+Na2S = 2NaHS；
(2) adsorbing CS in the exhaust gas discharged in the step (1) by a primary adsorption tank2After saturation of adsorption, first pass through N2Purging O in primary adsorption tank2Then introducing steam to the adsorbed CS2Performing desorption, the desorbed CS2Steam and condensed water enter the evaporating pot together;
(3) conveying the waste gas discharged after the absorption in the primary absorption tank in the step (2) to a secondary absorption tank and then discharging the waste gas to an exhaust tower, and after the secondary absorption tank is saturated in absorption, passing through N2Purging O in secondary adsorption tank2Then introducing steam to the adsorbed CS2Performing desorption, the desorbed CS2Steam and condensed water enter an evaporating pot together to obtain CS containing water vapor2Steam;
(4) the CS containing water vapor obtained in the step (2) and the step (3)2The steam enters the first condenser, most of the water vapor and CS2Cooling the steam into liquid, passing through a gas-liquid separator, and collecting uncooled CS containing water vapor2The steam enters a safety tank and is circulated into a primary absorption tank again, and the primary absorption tank contains liquid CS2The water enters a second condenser to be further cooled into a liquid state;
(5) layering the mixed liquid condensed in the step (3) by a specific gravity separator, and then CS2Further cooling in an after-cooler, and metering to enter CS2A storage tank.
2. The process of claim 1, wherein the primary adsorption tank and the secondary adsorption tank are independent DCS programs, and the primary adsorption tank and the secondary adsorption tank are filled with carbon disulfideThe secondary adsorption tank comprises 3 adsorption tanks with total air volume of 70000m3/h。
3. The recycling process of carbon disulfide in viscose fiber production according to claim 1, wherein the conversion system in step (1) comprises a conversion device, the conversion device is connected with a waste acid storage tank and a waste acid storage tank, a liquid inlet of the waste acid storage tank is connected with a rinsing tank, a liquid inlet of the waste alkali storage tank is connected with a tertiary alkaline washing tank, the waste acid storage tank and the waste alkali storage tank are respectively provided with a filtering mechanism, a liquid outlet of the waste acid storage tank and a liquid outlet of the waste alkali storage tank are connected with the conversion device, the conversion device is internally provided with a plurality of baffle plates and a plurality of aeration mechanisms, the baffle plates are transversely or longitudinally arranged, the conversion device is further internally provided with a liquid level detector, the conversion device is connected with a gas dispersion tank, the gas dispersion tank is internally provided with an aeration mechanism, the gas dispersion tank is connected with a physicochemical reaction tank, and.
4. The recycling process of carbon disulfide in viscose fiber production as recited in claim 3, wherein said conversion device comprises a barrel, the top of the barrel is provided with a waste lye inlet, a waste acid liquid inlet, an exhaust port, an observation hole and a pressure gauge, the bottom of the barrel is provided with a liquid outlet, said waste acid liquid inlet is connected with a main pipe, the main pipe is connected with a plurality of branch pipes, the branch pipes are provided with nozzles, the barrel is internally provided with a plurality of baffle plates, one end of each baffle plate is connected with the inner wall of the barrel, the other end of each baffle plate is provided with an overflow plate, the lower surfaces of the baffle plates are connected with an aeration mechanism, the aeration mechanism is provided with a plurality of T-shaped aeration holes, the T-shaped aeration holes penetrate through the baffle plates, the side of the barrel is provided with a plurality of inlets.
5. The process for recovering carbon disulfide in viscose fiber production according to claim 4, wherein a plurality of pH detectors are arranged inside the cylinder, and pH detectors are arranged above and below the baffle plate.
6. The recycling process of carbon disulfide in viscose fiber production according to claim 3, wherein said filter mechanism comprises a filter plate and a slag hole, said filter plate is disposed in a waste acid storage tank or a waste alkali storage tank, said filter plate has a groove at its lower end, a filter tank is disposed in the groove, an opening is disposed at the upper part of one end of the filter tank, a fixing ring is connected to the other end of the filter tank, the fixing ring is disposed between the slag hole and a sealing cover, a support rod is disposed on the sealing cover, two ends of the support rod are connected to hydraulic rods, and a liquid level detector and a pH detector are disposed in the waste acid storage tank and the waste acid storage tank.
7. The process for recovering carbon disulfide from viscose fiber production according to claim 1, wherein said conversion system comprises the steps of:
conveying the waste alkaline water to a waste alkaline storage tank, filtering, and storing the waste alkaline water filtrate in the waste alkaline storage tank;
conveying the waste acid water to a waste acid storage tank, and storing the filtrate of the filtered waste acid water in the waste acid storage tank;
conveying the waste alkali water filtrate obtained in the step (1) to a waste alkali liquid inlet of a conversion device, allowing the waste alkali water filtrate to flow into a baffle plate, conveying the waste acid water filtrate obtained in the step (2) to a waste acid liquid inlet of the conversion device, spraying the waste alkali water filtrate onto the baffle plate through a branch pipe, discharging compressed air from a T-shaped aeration hole by an aeration mechanism, aerating the waste alkali water filtrate and the waste acid water filtrate, allowing the waste alkali water filtrate and the waste acid water filtrate to flow into the lower baffle plate, aerating again until the waste alkali water filtrate flows to the bottom of the conversion device, and separating out H2S, discharging the gas from an exhaust port to an acid making device under the action of negative pressure to obtain a neutralized liquid;
conveying the neutralized liquid obtained in the step (3) to a gas dispersing pool, aerating again, and separating out H2S, discharging to an acid making device under the action of negative pressure;
and (4) sequentially feeding the neutralization solution obtained in the step (4) into a physicochemical reaction tank and a biochemical tank, and discharging after reaching the standard.
8. According to the rightThe process for recovering carbon disulfide in viscose fiber production according to claim 7, wherein the alkaline waste water in step (1) is alkaline waste water generated in a tertiary alkaline washing tank in the carbon disulfide recovery process in viscose fiber production, and the alkaline waste water comprises NaHS and Na2S, the concentration of NaHS is 10-30%, and Na is2The concentration of S is 2-4%, the waste acid water in the step (2) is waste acid water generated in a tow washing tank in the spinning process, and the concentration of H + in the waste acid water is 3500mg/L of 2000-3500 mg/L.
9. The process for recovering carbon disulfide in viscose fiber production according to claim 7, wherein the aeration time in step (3) is 0.5-12 hours, and the aeration time in step (4) is 0.5-6 hours.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114470827A (en) * | 2022-02-22 | 2022-05-13 | 宁夏彩源科技有限公司 | Production method and production system of clean thiocarbohydrazide |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4968622A (en) * | 1987-10-19 | 1990-11-06 | Waagner-Biro Aktiengesellschaft | Procedure for microbiologica transformation of sulphur containing harmful components in exhaust gases |
| CN101274203A (en) * | 2007-12-27 | 2008-10-01 | 唐山三友集团兴达化纤有限公司 | Method for removing carbon disulfide gas in production process of viscose fiber |
| CN206051718U (en) * | 2016-06-22 | 2017-03-29 | 成都丽雅纤维股份有限公司 | A kind of processing meanss of sulfur-containing waste water |
| CN206535411U (en) * | 2017-01-10 | 2017-10-03 | 北京三景环境科技发展有限公司 | A kind of waste gas tower purifier |
| CN207973645U (en) * | 2018-01-27 | 2018-10-16 | 广东欧沃环境科技有限公司 | A kind of organic waste water treating device |
-
2020
- 2020-12-31 CN CN202011630512.8A patent/CN112843983A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4968622A (en) * | 1987-10-19 | 1990-11-06 | Waagner-Biro Aktiengesellschaft | Procedure for microbiologica transformation of sulphur containing harmful components in exhaust gases |
| CN101274203A (en) * | 2007-12-27 | 2008-10-01 | 唐山三友集团兴达化纤有限公司 | Method for removing carbon disulfide gas in production process of viscose fiber |
| CN206051718U (en) * | 2016-06-22 | 2017-03-29 | 成都丽雅纤维股份有限公司 | A kind of processing meanss of sulfur-containing waste water |
| CN206535411U (en) * | 2017-01-10 | 2017-10-03 | 北京三景环境科技发展有限公司 | A kind of waste gas tower purifier |
| CN207973645U (en) * | 2018-01-27 | 2018-10-16 | 广东欧沃环境科技有限公司 | A kind of organic waste water treating device |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114470827A (en) * | 2022-02-22 | 2022-05-13 | 宁夏彩源科技有限公司 | Production method and production system of clean thiocarbohydrazide |
| CN114470827B (en) * | 2022-02-22 | 2023-09-22 | 宁夏彩源科技有限公司 | Production method and production system of clean thiocarbazide |
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