CN214664484U - Waste gas and waste liquid incineration treatment device in ethylene glycol production - Google Patents
Waste gas and waste liquid incineration treatment device in ethylene glycol production Download PDFInfo
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- CN214664484U CN214664484U CN202022931667.7U CN202022931667U CN214664484U CN 214664484 U CN214664484 U CN 214664484U CN 202022931667 U CN202022931667 U CN 202022931667U CN 214664484 U CN214664484 U CN 214664484U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
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Abstract
The utility model provides a waste gas and liquid incineration treatment device in ethylene glycol production, which comprises an incinerator, a waste heat boiler, an SCR reactor, a boiler feed water preheater and an air preheater; the incinerator receives waste gas and waste liquid generated in the production of ethylene glycol; the flue gas of the incinerator is guided to the high part of a chimney by an induced draft fan after sequentially passing through a waste heat boiler, an SCR reactor, a boiler feed water preheater and an air preheater and then is discharged; a cold fluid inlet of the boiler feed water preheater receives boiler feed water from a pipe network, and a cold fluid outlet of the boiler feed water preheater is connected with a cold fluid inlet of the waste heat boiler; the cold fluid inlet of the air preheater receives air from the outside, and the cold fluid outlet of the air preheater is connected with the air inlet of the incinerator through a combustion fan. The waste gas and waste liquid generated in the production process are incinerated, so that the cost is reduced, and the production is not limited by the processing capacity of a hazardous waste recycling and collecting company.
Description
Technical Field
The utility model relates to an ethylene glycol production field specifically is a waste gas waste liquid incineration disposal device in ethylene glycol production.
Background
Dangerous wastes such as light fractions, fusel oil, DMO heavy components and EG heavy fractions generated in the ethylene glycol production process do not have matched treatment facilities, can only be treated by a dangerous waste recovery treatment company, improves the production cost, and is influenced by the treatment capacity of a dangerous waste recovery treatment factory to limit the ethylene glycol production capacity.
SUMMERY OF THE UTILITY MODEL
To the problem that exists among the prior art, the utility model provides a waste gas waste liquid incineration disposal device in ethylene glycol production carries out incineration disposal to waste gas, the waste liquid that produces in the production process, and reduce cost makes production not receive the restriction of the useless company throughput of danger.
The utility model discloses a realize through following technical scheme:
a waste gas and waste liquid incineration treatment device in ethylene glycol production comprises an incinerator, a waste heat boiler, an SCR (selective catalytic reduction) reactor, a boiler water supply preheater and an air preheater;
the incinerator receives waste gas and waste liquid generated in the production of ethylene glycol; the flue gas outlet of the incinerator is connected with the hot fluid inlet of the waste heat boiler, the hot fluid outlet of the waste heat boiler is connected with the flue gas inlet of the SCR reactor, the flue gas outlet of the SCR reactor is connected with the hot fluid inlet of the boiler feed water preheater, the hot fluid outlet of the boiler feed water preheater is connected with the hot fluid inlet of the air preheater, and hot fluid discharged by the air preheater is guided to the high position of a chimney to be discharged through an induced draft fan;
a cold fluid inlet of the boiler feed water preheater receives boiler feed water from a pipe network, and a cold fluid outlet of the boiler feed water preheater is connected with a cold fluid inlet of the waste heat boiler; the cold fluid inlet of the air preheater receives air from the outside, and the cold fluid outlet of the air preheater is connected with the air inlet of the incinerator through a combustion fan.
Preferably, the exhaust gas comprises: the hydrogen is retrieved and is decomposed gas, low pressure flash drum flash distillation gas, MN recovery tower tail gas and VOCs discharge, and the waste liquid includes: DMC light ends, DMC heavy ends, DMO heavy ends, MF waste, ethanol product column waste, and ethylene glycol flare waste.
Preferably, four burners are arranged in the incinerator, one of the four burners is a waste gas burner, three waste gases, namely hydrogen recovery and decomposition gas, MN recovery tower tail gas and low-pressure flash evaporation tank flash evaporation gas, enter the incinerator through the waste gas burner, and VOCs (volatile organic compounds) exhaust gas is directly sent into the incinerator through a pipeline; the remaining three are waste liquid burners, each waste liquid burner processing two different waste liquids.
Furthermore, a water-sealed tank is respectively arranged corresponding to the hydrogen recovery decomposition gas and the low-pressure flash evaporation tank flash evaporation gas, the hydrogen recovery decomposition gas and the low-pressure flash evaporation tank flash evaporation gas respectively enter the incinerator after passing through the corresponding water-sealed tanks, a pressure stabilizing tank is arranged corresponding to the tail gas of the MN recovery tower, and the tail gas of the MN recovery tower enters the incinerator after passing through the pressure stabilizing tank.
Further, corresponding buffer tanks are respectively arranged corresponding to the six waste liquids, and the six waste liquids are sent into the incinerator after passing through the respective buffer tanks; and the waste gas discharged by each buffer tank is sent to an ethylene glycol flare pipe network.
Preferably, the waste liquid is sprayed into the incinerator through an atomizing spray gun.
Preferably, the system also comprises an ammonia water storage tank, wherein an ammonia water outlet of the ammonia water storage tank is respectively connected with an ammonia water inlet of the SCR reactor and an ammonia water inlet of the waste heat boiler.
Preferably, the ammonia gas absorption device further comprises an ammonia gas absorption tank, and a gas outlet of the ammonia water storage tank is connected with the ammonia gas absorption tank.
Compared with the prior art, the utility model discloses following profitable technological effect has:
the utility model is provided with an incinerator to incinerate waste gas and waste liquid generated in the production process of dimethyl oxalate and ethylene glycol, high-pressure flue gas generated by incineration is subjected to heat recovery through a waste heat boiler, is subjected to denitration treatment through an SCR reactor, is subjected to heat recovery through a boiler feed water preheater and an air preheater in sequence, and is discharged; feeding preheated boiler feed water into a preheating boiler for heat exchange to recover the heat of the flue gas; the air preheated by the air preheater is used as combustion-supporting air to enter the incinerator. The utility model discloses waste gas waste liquid burns device can regard as the supporting facility of dimethyl oxalate, ethylene glycol production, solves the waste gas waste liquid in the production process, and production no longer receives the restriction of the useless recovery processing company of danger, and gas discharge reaches national exhaust emission standard. Meanwhile, heat energy is recovered through steam production, and enterprise consumption is reduced.
Drawings
FIG. 1 is a schematic view of the structure of the present invention
In the figure: the system comprises an incinerator 1, a waste heat boiler 2, an SCR reactor 3, a boiler feed water preheater 4, an air preheater 5, an ammonia water storage tank 6 and an ammonia gas absorption tank 7.
Detailed Description
The present invention will now be described in further detail with reference to the accompanying drawings, which are provided for purposes of illustration and not limitation.
As shown in figure 1, the waste gas and waste liquid incineration treatment device in the ethylene glycol production comprises an incinerator 1, a waste heat boiler 2, an SCR reactor 3, a boiler feed water preheater 4, an air preheater 5, an ammonia water storage tank 6 and an ammonia absorption tank 7.
The incinerator 1 receives four kinds of waste gas and six kinds of waste liquid generated in the production of ethylene glycol, four kinds of waste gas: hydrogen recovery and decomposition gas, low-pressure flash evaporation tank flash evaporation gas, MN recovery tower tail gas and VOCs discharge gas, six waste liquids: DMC light ends, DMC heavy ends, DMO heavy ends, MF waste, ethanol product column waste, and ethylene glycol flare waste. Four burners are arranged in the incinerator 1, one of the burners is a waste gas burner, three waste gases including hydrogen recovery analysis gas, MN recovery tower tail gas and low-pressure flash evaporation tank flash evaporation gas are treated, the other three burners are waste liquid burners, two different waste liquids are respectively treated, and VOCs (volatile organic compounds) discharge gas is directly sent into the incinerator 1 through a pipeline.
The hydrogen recovery decomposition gas and the low-pressure flash evaporation tank flash evaporation gas respectively pass through the corresponding water seal tanks and then enter the incinerator 1 through the waste gas burner inlet, the MN recovery tower tail gas passes through the pressure stabilizing tank and then enters the incinerator 1 through the waste gas burner inlet. And flow meters and regulating valves are respectively arranged on pipelines of the hydrogen recovery analysis gas, the low-pressure flash evaporation tank flash evaporation gas, the MN recovery tower tail gas and the VOCs discharge gas.
Corresponding buffer tanks are respectively arranged corresponding to the six waste liquids, the retention time is not less than 2 hours, and the six waste liquids are sprayed into the incinerator 1 through respective buffer tanks and then sequentially through a delivery pump and a high-efficiency atomization spray gun. And the waste gas discharged by each buffer tank is sent to an ethylene glycol flare pipe network.
An air inlet of the incinerator 1 is connected with a combustion fan, and combustion air is introduced into the incinerator 1 through the combustion fan. Organic matters in the materials are combusted and decomposed in the furnace, the combustion temperature is ensured to be higher than 1100 ℃, the retention time is longer than 2 seconds, and the complete combustion is ensured.
Burn the exhanst gas outlet of burning furnace 1 and exhaust-heat boiler 2's hot-fluid inlet connection, exhaust-heat boiler 2's hot-fluid outlet and SCR reactor 3's flue gas inlet connection, SCR reactor 3's exhanst gas outlet and boiler feedwater heater 4's hot-fluid inlet connection, boiler feedwater heater 4's hot-fluid outlet and air heater 5's hot-fluid inlet connection, the hot-fluid of air heater 5 exhaust leads the chimney eminence to discharge through the draught fan. Waste gas and waste liquid are combusted in the incinerator 1, high-temperature flue gas at the temperature of-1226 ℃ generated by the incinerator 1 enters the waste heat boiler 2, is firstly cooled to the temperature of-1100 ℃ through a water protection section, 20% concentration ammonia water is sprayed through an SNCR spray gun to preliminarily remove NOx in the flue gas, the flue gas after SNCR denitration continuously exchanges heat with a membrane type wall + tube bundle of the waste heat boiler 2, the temperature of the flue gas is reduced to the temperature of-380 ℃, and 3.5MPa saturated steam is a byproduct. And (4) enabling the flue gas at the outlet of the waste heat boiler 2 to enter the SCR reactor 3 for denitration. The SCR reactor 3 is provided with a 1-stage reactor, and the catalyst arrangement adopts a 3+1 mode, namely three layers are installed and one layer is reserved. When the NOx in the flue gas passes through the catalyst layer, the NOx in the flue gas and a reducing agent (20% ammonia water) are subjected to selective reaction on the surface of the catalyst layer, so that the aim of further removing the NOx in the flue gas is fulfilled. The SCR denitration efficiency is designed to be more than 90%, and after the system is adopted, NOx in the flue gas can completely meet the requirement of environmental protection emission.
And (3) conveying the flue gas at the temperature of between 5 and 150 ℃ from the outlet of the air preheater to a chimney through a draught fan to be discharged at a high point, and arranging an online monitoring system on the chimney to perform online monitoring on the escape of particulate matters, NOx, non-methane total hydrocarbons and ammonia in the flue gas.
An ammonia water outlet of the ammonia water storage tank 6 is respectively connected with an ammonia water inlet of the SCR reactor 3 and an ammonia water inlet of the waste heat boiler 2, and a gas outlet of the ammonia water storage tank 6 is connected with an ammonia gas absorption tank 7.
And a cold fluid inlet of the boiler feed water preheater 4 receives boiler feed water from a pipe network, a cold fluid outlet of the boiler feed water preheater 4 is connected with a cold fluid inlet of the waste heat boiler 2, and a cold fluid outlet of the waste heat boiler 2 discharges saturated steam. The cold fluid inlet of the air preheater 5 receives air from the outside, and the cold fluid outlet of the air preheater 5 is connected with the air inlet of the incinerator 1 through a combustion fan. A flow meter is arranged on a connecting pipeline between the combustion fan and the air inlet of the incinerator 1.
The utility model discloses the control of device is as follows:
liquid level and pressure control of waste liquid buffer tank
1.1 liquid level control of waste liquid buffer tank
The buffer tanks of the six kinds of waste liquid are all provided with pneumatic liquid supplementing valves which are interlocked with respective liquid levels, the liquid levels reach a low limit alarm value, the liquid supplementing valves are opened to supplement the liquid, the liquid levels reach a high limit alarm value, and the liquid supplementing valves are closed to stop supplementing the liquid.
1.2 waste liquor buffer tank pressure control
The buffer tanks of the six waste liquids are all provided with nitrogen seal protection, the pressure of the buffer tanks, the respective nitrogen protection valves and the main pipe regulating valve of the flame-off torch form a regulating loop, and the normal set value of the pressure in the buffer tanks is 0.15 MPaG.
2 waste gas water seal/pressure stabilizing tank liquid level and pressure control
2.1 waste gas water seal tank level control
2.2 the respective water-sealed tanks of the hydrogen recovery decomposition gas and the flash gas of the low-pressure flash tank are respectively provided with a pneumatic liquid replenishing valve to be interlocked with respective liquid levels, the liquid levels reach a low limit alarm value, the liquid replenishing valve is opened to replenish liquid, the liquid levels reach a high limit alarm value, and the liquid replenishing valve is closed to stop replenishing liquid.
2.3 waste gas Water seal/surge tank pressure control
The water-sealed tank of the hydrogen recovery analysis gas, the surge tank of the tail gas of the MN recovery tower and the water-sealed tank of the flash gas of the low-pressure flash evaporation tank are all provided with low-pressure low-limit alarms, a boundary valve and a feed stop valve before the incinerator 1 are closed in an interlocking manner, the low-pressure low-limit alarm value of the water-sealed tank of the hydrogen recovery analysis gas is 5kPaG, and the low-pressure low-limit alarm value of the surge tank of the tail gas of the MN recovery tower and the low-pressure low-limit alarm value of the flash gas water-sealed tank of the low-pressure flash evaporation tank is 30 kPaG.
3 flow control of waste gas and waste liquid in incinerator 1
The pipelines of various waste gases and waste liquids entering the incinerator 1 are all provided with a flowmeter and an adjusting valve, and the feeding amount is adjusted according to the system load.
4 controlling the temperature and pressure of the incinerator 1
4.1 incinerator 1 temperature control
The combustion-supporting fans of the incinerator 1 are all variable frequency fans, the combustion-supporting air pipelines are all provided with flow meters, and the temperature of the flue gas outlet of the incinerator 1 is controlled to be 1226 ℃ by adjusting the feeding quantity of waste gas and waste liquid and the combustion-supporting air quantity to keep a certain proportion (the specific proportion is determined according to the field debugging condition).
Each combustor is independently provided with 1 combustion fan, so that system adjustment is facilitated.
4.2 incinerator 1 pressure control
The pressure in the incinerator 1 is controlled to be-100 PaG by adjusting the frequency of the induced draft fan.
5 waste heat boiler 2 steam drum liquid level and pressure control
5.1 exhaust-heat boiler 2 drum liquid level control
Three impulse regulating loops are formed by 3 liquid levels (three times of middle), boiler feed water flow, drum outlet steam flow and respective liquid level regulating valves of the waste heat boiler 2 drum, and the normal set value of the drum liquid level is 340 mm.
5.2 exhaust-heat boiler 2 drum pressure control
The drum pressure of the waste heat boiler 2 and respective pressure regulating valves form a regulating loop, and the normal set value of the drum pressure is 3.3 MPaG.
6 liquid level and pressure control of 6 ammonia water storage tank
6.1 Ammonia tank 6 level control
And the ammonia water storage tank 6 is provided with a pneumatic liquid supplementing valve which is interlocked with the liquid level, the liquid level reaches a low limit alarm value, the liquid supplementing valve is opened to supplement liquid, the liquid level reaches a high limit alarm value, and the liquid supplementing valve is closed to stop liquid supplementing.
6.2 Ammonia storage 6 pressure control
And (3) when the pressure of the ammonia water storage tank 6 reaches the high-limit alarm value of 300PaG, opening a liquid supplementing valve of the ammonia gas absorption tank 7 to perform in-tank spraying, and when the pressure reaches the normal value of 0PaG, closing the liquid supplementing valve of the ammonia gas absorption tank 7.
6.3 Ammonia tank 6 external spray control
And the toxic gas probe GD-006 gives an alarm, and 48XV-053 is interlocked and opened for spraying outside the tank.
7 ammonia absorption tank 7 liquid level control
The ammonia absorption tank 7 is provided with a pneumatic liquid supplementing valve which is interlocked with the liquid level, the liquid level reaches a low limit alarm value, the liquid supplementing valve is opened to supplement liquid, the liquid level reaches a high limit alarm value, and the liquid supplementing valve is closed to stop liquid supplementing.
Claims (8)
1. A waste gas and waste liquid incineration treatment device in ethylene glycol production is characterized by comprising an incinerator (1), a waste heat boiler (2), an SCR reactor (3), a boiler feed water preheater (4) and an air preheater (5);
the incinerator (1) receives waste gas and waste liquid generated in the production of ethylene glycol; a flue gas outlet of the incinerator (1) is connected with a hot fluid inlet of the waste heat boiler (2), a hot fluid outlet of the waste heat boiler (2) is connected with a flue gas inlet of the SCR reactor (3), a flue gas outlet of the SCR reactor (3) is connected with a hot fluid inlet of the boiler feed water preheater (4), a hot fluid outlet of the boiler feed water preheater (4) is connected with a hot fluid inlet of the air preheater (5), and hot fluid discharged by the air preheater (5) is guided to a high position of a chimney through an induced draft fan to be discharged;
a cold fluid inlet of the boiler feed water preheater (4) receives boiler feed water from a pipe network, and a cold fluid outlet of the boiler feed water preheater (4) is connected with a cold fluid inlet of the waste heat boiler (2); the cold fluid inlet of the air preheater (5) receives air from the outside, and the cold fluid outlet of the air preheater (5) is connected with the air inlet of the incinerator (1) through a combustion fan.
2. The waste gas and liquid incineration treatment device in the ethylene glycol production according to claim 1, wherein the waste gas comprises: the hydrogen is retrieved and is decomposed gas, low pressure flash drum flash distillation gas, MN recovery tower tail gas and VOCs discharge, and the waste liquid includes: DMC light ends, DMC heavy ends, DMO heavy ends, MF waste, ethanol product column waste, and ethylene glycol flare waste.
3. The waste gas and liquid incineration treatment device in the ethylene glycol production according to claim 1, wherein four burners are arranged in the incinerator (1), one of the burners is a waste gas burner, three kinds of waste gases, namely hydrogen recovery and decomposition gas, MN recovery tower tail gas and low-pressure flash drum flash gas, enter the incinerator (1) through the waste gas burner, and VOCs exhaust gas is directly sent into the incinerator (1) through a pipeline; the remaining three are waste liquid burners, each waste liquid burner processing two different waste liquids.
4. The waste gas and liquid incineration treatment device in the ethylene glycol production according to claim 2, wherein a water-sealed tank is respectively arranged corresponding to the hydrogen recovery decomposition gas and the low-pressure flash tank flash gas, the hydrogen recovery decomposition gas and the low-pressure flash tank flash gas respectively enter the incinerator (1) after passing through the corresponding water-sealed tanks, a pressure-stabilized tank is arranged corresponding to the MN recovery tower tail gas, and the MN recovery tower tail gas enters the incinerator (1) after passing through the pressure-stabilized tank.
5. The waste gas and liquid incineration treatment device in the ethylene glycol production according to claim 2, wherein corresponding buffer tanks are respectively provided for six types of waste liquid, and the six types of waste liquid are sent into the incinerator (1) after passing through the respective buffer tanks; and the waste gas discharged by each buffer tank is sent to an ethylene glycol flare pipe network.
6. The incineration disposal device for waste gas and liquid in ethylene glycol production according to claim 1, wherein the waste liquid is sprayed into the incinerator (1) through an atomization spray gun.
7. The waste gas and liquid incineration treatment device in the ethylene glycol production according to claim 1, further comprising an ammonia water storage tank (6), wherein an ammonia water outlet of the ammonia water storage tank (6) is connected with an ammonia water inlet of the SCR reactor (3) and an ammonia water inlet of the exhaust-heat boiler (2) respectively.
8. The waste gas and liquid incineration treatment device in the ethylene glycol production according to claim 1, further comprising an ammonia gas absorption tank (7), wherein a gas outlet of the ammonia water storage tank (6) is connected with the ammonia gas absorption tank (7).
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| CN202022931667.7U CN214664484U (en) | 2020-12-08 | 2020-12-08 | Waste gas and waste liquid incineration treatment device in ethylene glycol production |
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| CN202022931667.7U CN214664484U (en) | 2020-12-08 | 2020-12-08 | Waste gas and waste liquid incineration treatment device in ethylene glycol production |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113998866A (en) * | 2021-10-29 | 2022-02-01 | 广东尚鼎环境科技有限公司 | Organic solid waste treatment system and treatment process thereof |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113998866A (en) * | 2021-10-29 | 2022-02-01 | 广东尚鼎环境科技有限公司 | Organic solid waste treatment system and treatment process thereof |
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