CN216738134U

CN216738134U - Phthalic anhydride waste recovery system

Info

Publication number: CN216738134U
Application number: CN202123181799.3U
Authority: CN
Inventors: 骆智青
Original assignee: Individual
Current assignee: Individual
Priority date: 2021-12-17
Filing date: 2021-12-17
Publication date: 2022-06-14
Anticipated expiration: 2031-12-17

Abstract

The utility model discloses a phthalic anhydride waste recovery system, which comprises a dissolving unit, a vacuum pump, a rectifying unit and a phthalic anhydride condensation recovery unit which are connected in sequence, wherein the bottoms of the dissolving unit and the rectifying unit are respectively connected with a residue recovery tank, a water crushing tank, a solid-liquid centrifuge and a cooling kettle in sequence, and the cooling kettle is connected with an oxidative cracking unit; more than 99 percent of phthalic anhydride waste can be recycled, and the environment is not polluted by solid waste; secondly, the final residue is calcined, the generated gas is filtered in multiple stages, and the gas discharged into the air has no pollution to the environment.

Description

Phthalic anhydride waste recovery system

Technical Field

The utility model belongs to the technical field of chemical waste recovery equipment, a phthalic anhydride waste recovery system is related to.

Background

Phthalic anhydride is an important chemical raw material and is used for preparing a plasticizer, but a large amount of phthalic anhydride waste is generated in the production process, and the phthalic anhydride waste contains 95% of phthalic anhydride, 3% of tar and 2% of insoluble substances through detection, so that the phthalic anhydride waste and the environmental pollution are caused when the phthalic anhydride waste is directly discharged.

SUMMERY OF THE UTILITY MODEL

The utility model aims at providing a phthalic anhydride waste recycling system can retrieve the phthalic anhydride in the phthalic anhydride waste material to carry out purification treatment to the waste material that produces, prevent that chemical waste material from producing the pollution to the environment.

The utility model discloses phthalic anhydride waste recovery system, including dissolving unit, vacuum pump, rectification unit, phthalic anhydride condensation recovery unit that connect gradually, dissolve unit, rectification unit bottom and all connect gradually residue accumulator, water garrulous groove, solid-liquid centrifuge, cooling kettle, the oxidative cracking unit is connected to the cooling kettle.

The utility model discloses a characteristics still lie in:

the oxidative cracking unit comprises a crushing system connected with a cooling kettle, and the crushing system is sequentially connected with a feeding device, a combustion system, a heat-conducting oil furnace, a quench tower, a dry spraying tower, a bag-type dust remover, an induced draft fan, an SCR denitration system, a spray washing tower and a wet electric precipitator.

The combustion system comprises a primary combustion chamber connected with the feeding device, the primary combustion chamber is connected with a secondary combustion chamber, and the secondary combustion chamber is connected with the heat-conducting oil furnace.

The primary combustion chamber and the secondary combustion chamber are respectively connected with a combustion-supporting system and a slag discharging system.

The heat-conducting oil furnace is connected with a urea spray gun joint, and the heat-conducting oil in the heat-conducting oil furnace is connected with a heat system in a penetrating way.

The heat-conducting oil furnace is connected with the quenching tower through a booster pump.

The spray washing tower comprises a spray structure which is connected with an alkali pipeline.

The dissolving unit comprises a dissolving kettle, a heat conduction oil pipe a for controlling heating is connected in the dissolving kettle, the outlet end of the dissolving kettle is connected with a vacuum pump, and the bottom of the dissolving kettle is connected with a residue recovery tank through a control valve a.

The rectifying unit comprises a rectifying still, the inlet end of the rectifying still is connected with a vacuum pump, the bottom of the rectifying still is connected with a residue recovery tank through a control valve b, the rectifying still is internally connected with a heat-conducting oil pipe b for controlling heating, the top of the rectifying still is connected with the inlet end of a rectifying tower through a pipeline, and the outlet end of the rectifying tower is sequentially connected with a condenser, a gas-liquid separator, a storage tank and a sheeting apparatus.

The liquid phase end of the gas-liquid separator is connected with the rectifying still through the collector.

The utility model has the advantages that:

the utility model provides a phthalic anhydride waste recovery system, which can recycle more than 99% of phthalic anhydride waste and has no solid waste pollution to the environment; secondly, the final residue is calcined, the generated gas is filtered in multiple stages, and the gas discharged into the air has no pollution to the environment.

Drawings

FIG. 1 is a schematic structural diagram of a dissolving unit, a rectifying unit and a phthalic anhydride condensation and recovery unit in the utility model;

FIG. 2 is a diagram of a water crushing unit in the present invention;

FIG. 3 is a schematic structural diagram of a medium oxidative cracking unit of the present invention.

In the figure, 1, a dissolving kettle, 2, a vacuum pump, 3, a rectifying kettle, 4, a rectifying tower, 5, a residue recovery tank, 6, a water crushing tank, 7, a solid-liquid centrifuge, 8, a cooling kettle, 9, a crushing system, 10, a feeding device, 11, a heat conduction oil furnace, 12, a quenching tower, 13, a dry spray tower, 14, a bag-type dust remover, 15, an induced draft fan, 16, an SCR denitration system, 17, a spray washing tower, 18, a wet electric dust remover, 19, a primary combustion chamber, 20, a secondary combustion chamber, 21, a combustion-supporting system, 22, a slag discharging system, 23, a urea spray gun joint, 24, a heat utilization system, 25, a condenser, 26, a gas-liquid separator, 27, a storage tank, 28, a flaker and 29, a collector are arranged.

Detailed Description

The present invention will be described in detail with reference to the accompanying drawings and specific embodiments.

The utility model discloses phthalic anhydride waste recovery system, as shown in figure 1, figure 2, including the unit of dissolving that connects gradually, vacuum pump 2, the rectification unit, phthalic anhydride condensation recovery unit, dissolve the unit, rectification unit bottom all connects gradually residue accumulator 5, water breaker 6, solid-liquid centrifuge 7, cooling kettle 8 connects the oxidative cracking unit, heat through dissolving the unit and dissolve the phthalic anhydride waste that is in solid-state, can melt phthalic anhydride waste and discharge into the rectification unit through vacuum pump 2, wherein the waste that fails to melt discharges to residue accumulator 5 through the deposit, the rectification unit can further purify the phthalic anhydride waste that gets into wherein and retrieve, discharge the residue into residue accumulator 5, carry out the water broke in residue accumulator 5 and draw wherein and be in solid-state waste, so as to facilitate the cracking treatment by the oxidative cracking unit.

As shown in fig. 3, the oxidative cracking unit includes a crushing system 9 connected to the cooling kettle 8, and the crushing system 9 is connected to a feeding device 10, a combustion system, a heat-conducting oil furnace 11, a quenching tower 12, a dry spraying tower 13, a bag-type dust remover 14, an induced draft fan 15, an SCR denitration system 16, a spray washing tower 17, and a wet electric dust remover 18 in sequence.

The combustion system comprises a primary combustion chamber 19 connected with the feeding device 10, the primary combustion chamber 19 is connected with a secondary combustion chamber 20, and the secondary combustion chamber 20 is connected with the heat-conducting oil furnace 11.

The primary combustion chamber 19 and the secondary combustion chamber 20 are respectively connected with a combustion-supporting system 21 and a slag-out system 22, the combustion-supporting system 21 can respectively provide combustion-supporting fuel oxygen for the primary combustion chamber 19 and the secondary combustion chamber 20, and the slag-out system 22 can timely clean slag in the primary combustion chamber 19 and the secondary combustion chamber 20.

The urea spray gun connector 23 is connected to the heat conduction oil furnace 11, and the heat conduction oil in the heat conduction oil furnace 11 penetrates through the heat utilization system 24.

The heat conduction oil furnace 11 is connected with the quenching tower 12 through a booster pump, and the booster pump can discharge flue gas in the heat conduction oil furnace 11 into the quenching tower 12.

The spray washing tower 17 internally comprises a spray structure, the spray structure is connected with an alkaline path pipeline, sodium carbonate is added into an alkaline solution pool, and the alkaline solution pool is sprayed into the spray washing tower 17 through the alkaline path pipeline to carry out alkaline washing treatment on the flue gas.

The dissolving unit comprises a dissolving kettle 1, a heat conduction oil pipe a for controlling heating is connected in the dissolving kettle 1, the outlet end of the dissolving kettle 1 is connected with a vacuum pump 2, and the bottom of the dissolving kettle 1 is connected with a residue recovery tank 5 through a control valve a.

The rectifying unit comprises a rectifying still 3, the inlet end of the rectifying still 3 is connected with a vacuum pump 2, the bottom of the rectifying still 3 is connected with a residue recovery tank 5 through a control valve b, the rectifying still 3 is internally connected with a heat-conducting oil pipe b for controlling heating, the top of the rectifying still 3 is connected with the inlet end of a rectifying tower 4 through a pipeline, and the outlet end of the rectifying tower 4 is sequentially connected with a condenser 25, a gas-liquid separator 26, a storage tank 27 and a sheeting apparatus 28.

The liquid phase end of the gas-liquid separator 26 is connected with the rectifying still 3 through the collector 29, and the gas phase from the gas-liquid separator 26 returns to the rectifying still 3 after being collected by the collector 29.

The utility model discloses phthalic anhydride waste recycling system includes the three, and the first part is phthalic anhydride's recovery, and the second part is the garrulous unit of water for waste material water in to residue accumulator 5 is garrulous, and the third part is the burning to the waste material.

The first part of the specific recovery process comprises the following steps: blocky crude phthalic anhydride (phthalic anhydride waste) is loaded into a melting kettle 1 by a forklift, the melting kettle 1 is heated by heat conduction oil, when the temperature reaches about 135 ℃, the crude phthalic anhydride is melted, the melted crude phthalic anhydride is pumped into a rectifying kettle 3 by a vacuum pump 2 for rectification, reduced pressure rectification is carried out, a heat conduction oil interlayer is heated, the temperature is controlled to be 200-240 ℃ for 10 hours, phthalic anhydride steam enters a rectifying tower 4 from the kettle top, the reduced pressure rectification is continued, the temperature is controlled to be 180-200 ℃, the phthalic anhydride steam enters a condenser (micro negative pressure) from the tower top through rectification, the phthalic anhydride steam enters a gas-liquid separator 26 (micro negative pressure) after condensation, the liquid material is the phthalic anhydride product, the phthalic anhydride enters a storage tank 27, the phthalic anhydride is sliced by a flaker 28, and the phthalic anhydride is packaged into 50 kg/bag and then is sent into a warehouse. The gas phase from the gas-liquid separator 26 is collected by the collector 29 and returned to the still pot 3. The distillation residual liquid tar enters a residue recovery tank 5 from the bottom 3 of the distillation kettle.

The second partial water grinding specific process comprises the following steps: heating and dissolving the waste in the residue recovery tank 5, uniformly putting the dissolved material into the water breaking tank 6, uniformly stirring, controlling the temperature to be 80 ℃, fully and uniformly separating the material to 2-4mm particles, centrifuging, performing solid-liquid separation, conveying the solid to an oxidative cracking system, and circulating the liquid to a water breaking kettle.

The third part is that the specific process of burning the waste materials is as follows:

1) firstly, the draught fan is opened, the primary combustion chamber 19 and the secondary combustion chamber 20 are swept for five minutes, combustion-supporting fuel is conveyed into the primary combustion chamber 19 and the secondary combustion chamber 20 through the combustion-supporting system 19, the ignition burner ignites the combustion-supporting fuel, and the heat of the burner is released to enable the temperature in the primary combustion chamber 19 and the temperature in the secondary combustion chamber 20 to be gradually raised.

2) And the solid waste is firstly coarsely crushed and finely crushed and then sprayed into the rotary kiln of the primary combustion chamber 19 by an air supply system, and the combustion temperature is controlled at 850 ℃ by controlling the oxygen supplement amount.

3) The flue gas generated by the primary combustion chamber 19 enters the secondary combustion chamber 20 through a pipeline, and the ash generated by incineration is automatically discharged through a slag discharging system 22 (namely a wet scraper).

4) The smoke generated by burning is further burned at high temperature in the secondary combustion chamber 20, the burning temperature is increased to 1100 ℃, the burning is more complete, the effects of no smoke, no odor and no secondary pollution are achieved, the staying time of the smoke in the secondary chamber is more than 2.0 seconds, trace organic matters and dioxin in the smoke can be fully decomposed, the decomposition efficiency exceeds 99.99 percent, and the organic components and carbon particles which are not decomposed in the smoke are ensured to be completely decomposed at the temperature of about 1100 ℃. The secondary combustion chamber adopts multi-stage combustion, so that the generation of oxynitride is effectively inhibited.

5) The flue gas that the postcombustion chamber 20 came out gets into waste heat conduction oil furnace 11, respectively reserves two urea spray gun joints 23 on postcombustion chamber 20 exit position and boiler, and 10% urea aqueous solution is spouted into the stove through urea spray gun joint 23 and is carried out high temperature SNCR reduction denitration, gets rid of NOx in the flue gas, then high temperature flue gas and heat system 24 carry out the heat transfer, and the heating conduction oil is sent into and is circulated and use with heat system 24. Meanwhile, ash in the flue gas is further settled in the heat-conducting oil furnace 11, so that the cleanliness of the flue gas is improved.

6) And at the moment, heat energy is recovered, the steam generator can be connected to generate steam, the generated steam is used for production, and the rest part is sold to peripheral enterprises with energy requirements.

7) And the flue gas from the heat-conducting oil furnace 11 enters a semi-dry quenching tower 12. The atomized droplets are atomized into fine droplets by the two-fluid nozzle, the atomized droplets are acted by upward hot flue gas to form a high-density area in which the droplets are suspended near the nozzle, and the temperature is controlled to be rapidly reduced to about 200 ℃ within 1s by adjusting the spraying amount, so that the regeneration of dioxin is effectively inhibited. Meanwhile, some sparks in the smoke are extinguished by the sprayed water mist, so that a subsequent cloth bag is protected from being burnt out.

8) And then the flue gas enters a dry spray tower 13 (a dry type deacidification and dioxin absorption device) which is provided with a storage tank for containing carbon lime and active carbon, the carbon lime and the active carbon are conveyed by a star-shaped ash discharge valve, blown by high-pressure air and enter a connecting flue to react with the burning tail gas, and the tail gas is further purified. The sprayed charcoal lime has the function of removing HCl, NOx and other acidic components in the absorbed flue gas, and the activated carbon has the function of adsorbing and removing a small amount of dioxin furan and the like remained in the flue gas.

9) And the tail gas enters a gas exhaust type bag-type dust collector 14 to remove fine dust remained in the smoke. The mixture of the carbon lime and the active carbon sprayed in the dry spraying tower enters a bag-type dust collector and is adsorbed on a bag, and the carbon lime and the active carbon which are not fully reacted and adsorbed continue to absorb and react. The dust remover is provided with a bypass flue, when the inlet temperature of the bag-type dust remover is not within the limit range, the bag-type bypass electromagnetic valve is opened, smoke enters the chimney through the bypass, and therefore fatal damage to the bag is avoided when the smoke temperature is abnormal.

10) And the flue gas that comes out from sack cleaner 14 introduces SCR deNOx systems 16 (add urea to the SCR dissolving tank, carry out the denitration treatment to the flue gas) through the draught fan for further get rid of oxynitride.

11) And the flue gas enters a spray washing tower device 17 (sodium carbonate is added into an alkali liquor pool, the pH value of circulating water in the alkali liquor pool is controlled to be 10-12, and the flue gas is subjected to alkali washing treatment), and the main function is to wash off acidic gas, oxynitride and dust in the flue gas.

12) The flue gas is treated by a wet electrostatic precipitator to remove small-particle dust again, so as to ensure that the dust content reaches 10mg/m³And (4) standard, and discharging the flue gas reaching the standard in a chimney.

The alkali liquor discharged after passing through the spray washing tower device 17 and the wet electrostatic dust collector 18 is recycled to the alkali liquor pool for recycling.

The utility model discloses phthalic anhydride waste recovery system can make more than 99% phthalic anhydride waste obtain the recovery and recycle, does not have the pollution of solid useless to the environment; secondly, the final residue is calcined, the generated gas is filtered in multiple stages, and the gas discharged into the air has no pollution to the environment.

Claims

1. The phthalic anhydride waste recovery system is characterized by comprising a dissolving unit, a vacuum pump (2), a rectifying unit and a phthalic anhydride condensation recovery unit which are sequentially connected, wherein the bottoms of the dissolving unit and the rectifying unit are sequentially connected with a residue recovery tank (5), a water crushing tank (6), a solid-liquid centrifuge (7) and a cooling kettle (8), and the cooling kettle (8) is connected with an oxidative cracking unit.

2. The phthalic anhydride waste recovery system of claim 1, wherein the oxidative cracking unit comprises a crushing system (9) connected with a cooling kettle (8), and the crushing system (9) is sequentially connected with a feeding device (10), a combustion system, a heat-conducting oil furnace (11), a quench tower (12), a dry spraying tower (13), a bag-type dust remover (14), an induced draft fan (15), an SCR denitration system (16), a spray washing tower (17) and a wet electric dust remover (18).

3. The phthalic anhydride waste recycling system of claim 2, wherein the combustion system comprises a primary combustion chamber (19) connected to the feeding device (10), the primary combustion chamber (19) is connected to a secondary combustion chamber (20), and the secondary combustion chamber (20) is connected to the heat-conducting oil furnace (11).

4. The phthalic anhydride waste recovery system of claim 3, wherein the primary combustion chamber (19) and the secondary combustion chamber (20) are connected to a combustion system (21) and a slag tapping system (22), respectively.

5. The phthalic anhydride waste recycling system of claim 3, wherein the heat transfer oil furnace (11) is connected to a urea spray gun connector (23), and the heat transfer oil in the heat transfer oil furnace (11) is connected to a heat system (24).

6. The phthalic anhydride waste recovery system of claim 3, wherein the heat-conducting oil furnace (11) is connected to the quenching tower (12) by a booster pump.

7. The phthalic anhydride waste recovery system of claim 3, wherein the spray scrubber (17) comprises spray structures therein, the spray structures being connected to caustic piping.

8. The phthalic anhydride waste recycling system of claim 1, wherein the dissolving unit comprises a dissolving kettle (1), a heat conducting oil pipe a for controlling heating is connected in the dissolving kettle (1), the outlet end of the dissolving kettle (1) is connected with a vacuum pump (2), and the bottom of the dissolving kettle (1) is connected with a residue recycling tank (5) through a control valve a.

9. The phthalic anhydride waste recovery system of claim 1, wherein the rectification unit comprises a rectification kettle (3), the inlet end of the rectification kettle (3) is connected with a vacuum pump (2), the bottom of the rectification kettle (3) is connected with a residue recovery tank (5) through a control valve b, the rectification kettle (3) is internally connected with a heat conduction oil pipe b for controlling heating, the top of the rectification kettle (3) is connected with the inlet end of a rectification tower (4) through a pipeline, and the outlet end of the rectification tower (4) is sequentially connected with a condenser (25), a gas-liquid separator (26), a storage tank (27) and a sheeting apparatus (28).

10. The phthalic anhydride waste recovery system of claim 9, wherein the liquid phase end of the gas-liquid separator (26) is connected to the rectifying still (3) via an accumulator (29).