CN211522134U - Raw coke oven gas waste heat recovery utilizes system - Google Patents
Raw coke oven gas waste heat recovery utilizes system Download PDFInfo
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- CN211522134U CN211522134U CN201921010270.5U CN201921010270U CN211522134U CN 211522134 U CN211522134 U CN 211522134U CN 201921010270 U CN201921010270 U CN 201921010270U CN 211522134 U CN211522134 U CN 211522134U
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Abstract
The utility model discloses a raw coke oven gas waste heat recycling system, which comprises a waste heat recycling system and a waste heat utilization system, wherein the waste heat recycling system comprises a saturated steam heat exchanger group, an overheated steam heat exchanger group, a steam pocket with a steam-water separator, a circulating water pump group and a water supply pump group; the waste heat utilization system comprises a condensed ammonia water heater, a condensed rich oil heater, an ammonia still and a debenzolization tower. The waste heat recycling system and the waste heat recycling method of the utility model not only are environment-friendly and energy-saving, but also have significant economic benefit; the waste heat utilization rate of enterprises can be improved, carbon emission and waste gas emission can be reduced, and the economic value of externally supplied steam can be generated.
Description
Technical Field
The invention belongs to the technical field of raw gas waste heat recovery of coke ovens, and particularly relates to a raw gas waste heat recovery and utilization system.
Background
In the coking industry, a large amount of high-temperature raw coke oven gas is discharged from a coke oven, the gas temperature is 700-800 ℃, the gas is cooled by a spraying mode, the gas temperature is reduced from 700-800 ℃ to 80-90 ℃, and heat is wasted. In addition, at present, a tubular heating furnace is generally used for heating rich oil and ammonia water in a chemical production workshop of the coking industry, coke oven gas is combusted by the heating furnace to heat media in the tube, the exhaust gas temperature of the heating furnace reaches 300 ℃, the heat efficiency is low, and the tubular heating furnace is high-energy-consumption equipment which is eliminated by the country. The process flow is shown in figure 1, raw coke oven gas with the temperature of 700-800 ℃ conveyed from the outlet of a coke oven carbonization chamber passes through an ascending pipe and a primary cooler 10, the temperature of the raw coke oven gas is reduced to 22-35 ℃ after the raw coke oven gas is sprayed and cooled by ammonia water, then a part of the raw coke oven gas is conveyed to an external gas supply end 11 through a coke oven gas pipe network, a part of the raw coke oven gas is conveyed to an oil-rich tubular furnace 12 for heat supply, and a part of the raw coke oven gas is conveyed to a waste liquid tubular furnace 13 for; the debenzolization tower 14 supplies heat through high-temperature steam; the ammonia still 15 supplies heat through low-temperature steam; heating the benzene-containing rich oil medium in the rich oil tube furnace 12 to about 185 deg.c, introducing into the debenzolization tower 14 for debenzolization, and returning the debenzolization medium at about 135 deg.c to the rich oil tube furnace 12 for cyclic debenzolization; the ammonia-containing waste liquid is heated to 110-130 ℃ in the waste liquid tube furnace 13 and then enters the ammonia still 15 for deamination treatment, and the wastewater subjected to deamination treatment and having a temperature of 102-107 ℃ returns to the waste liquid tube furnace 13 for deamination treatment in a circulating manner.
Firstly, the high-temperature raw gas is cooled by spraying ammonia water, so that heat in the raw gas is wasted, and the spraying of circulating ammonia water is additionally increased, so that the power consumption is increased; secondly, the rich oil tubular furnace 12 and the waste liquid tubular furnace 13 are heated by utilizing heat generated by burning the cooled crude gas, SO that the consumption of the crude gas is increased, and SO is additionally generated2、NOxAnd CO2The exhaust gas can cause air pollution if directly discharged, and brings serious environmental problemsOr high tail gas treatment equipment is used for treatment, so that the production cost of an enterprise is increased, and the economic benefit of the enterprise is reduced; finally, the debenzolization tower 14 and the ammonia still 15 need to be additionally supplied with high-temperature steam for heating, and the energy consumption is high.
In addition, because 2 tubular furnaces are located in first class danger article production region, although safe distance accords with relevant standard requirement, because 2 tubular furnaces have naked light, still have the potential safety hazard.
Disclosure of Invention
In order to solve the technical problem that the waste heat of the raw gas is unreasonably utilized in the prior art, the invention provides a raw gas waste heat recycling system which can efficiently recycle the waste heat of the raw gas.
In order to realize the purpose of the invention, the invention adopts the technical scheme that:
the utility model provides a raw coke oven gas waste heat recovery utilizes system, includes waste heat recovery system and waste heat utilization system, wherein:
the waste heat recovery system comprises: the system comprises a saturated steam heat exchanger group, a superheated steam heat exchanger group, a steam drum with a steam-water separator, a circulating water pump group and a water feed pump group;
the waste heat utilization system comprises: ammonia water heater, rich oil heater, ammonia still and debenzolization tower;
the water inlet of the saturated steam heat exchanger group is communicated with the water outlet of the steam drum through a circulating water pump group, the first water inlet of the steam drum at the water outlet of the saturated steam heat exchanger group is communicated, and the steam outlet of the steam drum is communicated with the waste heat utilization system through a steam pipe network;
and the air inlet of the superheated steam heat exchanger group is communicated with the steam outlet of the steam drum through a steam pipe network, and the air outlet of the superheated steam heat exchanger group is communicated with the debenzolization tower through a steam pipe network.
Furthermore, the circulating water pump set and the water supply pump set comprise a plurality of circulating water pumps and a plurality of water supply pumps, the plurality of circulating water pumps are connected in parallel, and the plurality of water supply pumps are connected in parallel. Water in the steam pocket enters the saturated steam heat exchanger group for heat exchange in a forced circulation mode, and the plurality of parallel circulating water pumps or water feeding pumps do not influence each other, so that the system is convenient to stop and overhaul. The arrangement of a plurality of circulating water pumps or water feeding pumps connected in parallel can ensure that the whole waste heat utilization system can continuously and stably operate.
Furthermore, the raw coke oven gas waste heat recycling system also comprises a water supplementing system, and a water outlet of the water supplementing system is communicated with a second water inlet of the steam drum through a water supply pump set. Be equipped with the desalination deaerating plant in the water charging system, when the water source in the steam pocket is insufficient, can pass through water charging system, carry the waste heat recovery system with the water through the desalination deoxidization to guarantee that whole waste heat utilization system is continuous, operate steadily.
Preferably, the ammonia water heater and the rich oil heater are both condensing heaters. The heat exchange medium is arranged in the condensing ammonia water heater and the condensing rich oil heater in a countercurrent mode, so that a high heat transfer coefficient can be achieved, and the heat exchange efficiency is improved.
Preferably, the saturated steam heat exchanger bank and the superheated steam heat exchanger bank comprise a plurality of riser pipe heat exchangers connected in parallel. The riser heat exchanger can adopt a jacket type heat exchanger, a jacket consists of an inner cylinder and an outer cylinder, high-temperature raw coke oven gas flows through the inner cylinder, and water flows through the jacket; the plurality of riser heat exchangers are connected in parallel, so that the heat exchange efficiency can be improved, and each riser heat exchanger is independent, so that a single riser heat exchanger can be conveniently replaced, and the continuous, efficient and stable operation of the whole system can be ensured.
The temperature of the raw gas which is conveyed from the outlet of the coke oven carbonization chamber and has the temperature of 700-800 ℃ can be reduced by 250-350 ℃ after the raw gas passes through the waste heat recycling system. Preferably, the temperature of 800 ℃ raw gas can be reduced to 450-500 ℃ after passing through the waste heat recycling system, then the temperature of the raw gas is reduced to 80-90 ℃ by adopting ammonia water spraying, and finally the temperature of the raw gas is reduced to 22-35 ℃ after passing through a primary cooler and is sent out for gas supply.
The raw gas waste heat recycling system can produce saturated steam and/or superheated steam, each ton of coke can produce at least 0.1t of saturated steam or 0.08t of superheated steam per hour, the temperature of the saturated steam can reach 204 ℃, the temperature of the superheated steam can reach 400 ℃, and the economic benefit is remarkable.
The invention also provides a raw coke oven gas waste heat recycling method, which comprises the following steps:
step one, conveying water in a steam drum to a saturated steam heat exchanger group through a circulating water pump group, and returning a mixture of saturated steam and water generated after heat exchange of the saturated steam heat exchanger group to the steam drum through a first water inlet of the steam drum;
step two, conveying a part of saturated steam generated in the steam drum to a waste heat utilization system through a steam pipe network through a gas-liquid separator to provide heat energy for an ammonia water heater, a rich oil heater and an ammonia still; condensed water separated after heat exchange of the saturated steam with the ammonia water heater and the rich oil heater returns to the steam drum through the water feed pump unit for next circulation;
step three, conveying a part of saturated steam generated in the steam drum to a superheated steam heat exchanger group through a steam pipe network through a gas-liquid separator, and conveying superheated steam generated after heat exchange of the superheated steam heat exchanger group to a debenzolization tower to provide heat energy;
and step four, taking part of saturated steam generated in the steam drum as surplus steam through a gas-liquid separator, and supplying heat through a steam pipe network.
Preferably, the method further comprises a fifth step of supplementing water into the steam drum through a water supplementing system, wherein a water outlet of the water supplementing system is communicated with a second water inlet of the steam drum through a water supply pump set.
Compared with the utilization mode of crude gas in the industrial production workshop of the coking industry, the invention has the following advantages:
(1) the waste heat recovery and waste heat utilization system is used for exchanging heat between water and high-temperature raw gas to produce saturated steam and superheated steam, so that part of heat in the high-temperature raw gas is effectively recovered, and the waste of heat is avoided;
(2) the waste heat recycling system can produce saturated steam and/or superheated steam, each ton of coke can produce at least 0.1t of saturated steam or 0.08t of superheated steam per hour, the temperature of the saturated steam can reach 204 ℃, the temperature of the superheated steam can reach 400 ℃, and the economic benefit is remarkable;
(3) the invention adopts two condensing ammonia water heaters and an oil-rich heater to replace the traditional tubular furnace for heating, thereby not only saving a large amount of coke oven gas, but also reducing SO2、NOxAnd a large amount of CO2The emission of gas and waste gas is beneficial to environmental protection;
(4) the invention adopts two condensing ammonia water heaters and a rich oil heater to replace the traditional tubular furnace for heating, thereby eliminating the potential safety production hazard of a chemical plant and achieving the intrinsic safety;
(5) the temperature of the crude gas in the riser can be reduced to 250-350 ℃ by using the waste heat recycling system, so that the spraying amount of the circulating ammonia water can be reduced by 20-30%, the treatment cost of the crude gas is reduced, and the electricity consumption of the circulating ammonia water pump is saved by 20-30% every year.
The waste heat recycling system is environment-friendly, energy-saving and remarkable in economic benefit, can improve the waste heat utilization rate of enterprises, can reduce carbon emission and waste gas emission, and can generate economic value for externally supplying steam.
Drawings
FIG. 1 is a flow chart of waste heat utilization of raw coke oven gas in a chemical production workshop of the coking industry at present;
fig. 2 is a flow chart of a raw gas waste heat recycling system provided in embodiment 1 of the present invention.
The system comprises a 1-saturated steam heat exchanger group, a 2-superheated steam heat exchanger group, a 3-steam drum, a 4-ammonia water heater, a 5-rich oil heater, 6 and 15-ammonia stills, 7 and 14-debenzolization towers, 8, a water feed pump group, 9, a circulating water pump group, 10, an ascending pipe and a primary cooler, 11, an external air supply end, 12, an oil-rich pipe furnace, 13 and a waste liquid pipe furnace.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
The present invention will be further described with reference to specific examples.
Example 1
The embodiment 1 of the invention provides a high-temperature raw gas waste heat recycling system, which is shown in fig. 2.
The raw gas waste heat recycling system comprises a waste heat recycling system and a waste heat utilization system, wherein the waste heat recycling system comprises a saturated steam heat exchanger group 1, an overheated steam heat exchanger group 2, a steam drum 3 with a steam-water separator, a water feed pump group 8 and a circulating water pump group 9; the waste heat utilization system comprises a condensed ammonia water heater 4, a condensed rich oil heater 5, an ammonia still 6 and a debenzolization tower 7; the water inlet of the saturated steam heat exchanger group 1 is communicated with the water outlet of the steam drum 3 through a circulating water pump group 9, the water outlet of the saturated steam heat exchanger group 1 is communicated with the first water inlet of the steam drum 3, and the steam outlet of the steam drum 3 is communicated with a waste heat utilization system through a steam pipe network; the air inlet of the superheated steam heat exchanger group 2 is communicated with the steam outlet of the steam drum 3 through a steam pipe network, and the air outlet of the superheated steam heat exchanger group 2 is communicated with the debenzolization tower 7 through a steam pipe network. The water supplementing system supplements water through a water supplementing pipe network, and a water outlet of the water supplementing system is communicated with a second water inlet of the steam pocket 3 through a water supply pump set 8. The saturated steam heat exchanger group 1 and the superheated steam heat exchanger group 2 comprise a plurality of parallel-connected ascending pipe heat exchangers.
The whole waste heat utilization system supplies water from the steam pocket 3, the water enters the saturated steam heat exchanger group 1 and the superheated steam heat exchanger group 2 through the circulating water pump group 9, the water and the high-temperature raw coke oven gas exchange heat in the saturated steam heat exchanger group 1 and the superheated steam heat exchanger group 2, the temperature of the raw coke oven gas is reduced, the water is heated into saturated steam and superheated steam, a mixture of the saturated steam and the water enters the steam pocket 3 through a first water inlet of the steam pocket 3 to be subjected to steam-water separation, the water is left in the steam pocket to continue to participate in circulation, and the steam is divided into five paths through a steam pipe network. The first path of saturated steam enters the superheated steam heat exchanger group 2, the saturated steam and high-temperature raw gas are subjected to heat exchange in the superheated steam heat exchanger group 2, the temperature of the raw gas is reduced, the saturated steam is heated into superheated steam, the superheated steam enters the debenzolization tower 7 through a steam pipe network, and the superheated steam exchanges heat with rich oil to evaporate benzene from the rich oil; the second path of saturated steam enters a condensed ammonia water heater 4, the saturated steam and the circulating ammonia water exchange heat continuously, the saturated steam releases heat to become condensed water, the condensed water returns to the steam drum 3 through a water supply pump unit 8, and the heat absorption temperature of the circulating ammonia water is raised to 110-130 ℃ and enters an ammonia still 6; the third path of saturated steam enters a condensed rich oil heater 5, the saturated steam and the circulating rich oil exchange heat continuously, the saturated steam releases heat to become condensed water, the condensed water returns to the steam drum 3 through a water feed pump unit 8, and the heat absorption temperature of the circulating rich oil is raised to about 185 ℃ and enters a debenzolization tower 7; the fourth path of saturated steam enters an ammonia still 6, and the saturated steam exchanges heat with circulating ammonia water to evaporate ammonia gas from the ammonia water; and the fifth path of saturated steam is used as surplus steam and is sent out for heat supply. The temperature of 800 ℃ raw gas can be reduced to 450-500 ℃ after passing through the waste heat recycling system, the temperature of 450-500 ℃ raw gas is reduced to 22-35 ℃ after passing through an ammonia water spraying and primary cooler, and gas is supplied outside.
Further, the raw coke oven gas waste heat recycling system also comprises a water supplementing system, and a water outlet of the water supplementing system is communicated with a second water inlet of the steam drum 3 through a water supply pump unit 8. Be equipped with the desalination deaerating plant in the water charging system, when the water yield in the steam pocket 3 is insufficient, can pass through water charging system, carry the waste heat recovery system with the water through the desalination deoxidization to guarantee that whole waste heat recovery utilizes the continuous, the operation steadily of system.
Through waste heat recovery and waste heat utilization system, utilize water and high temperature raw coke oven gas to carry out heat exchange and produce saturated steam and superheated steam, effectively retrieved partial heat in the high temperature raw coke oven gas, avoided the heat to lose uselessly. The raw gas waste heat recycling system can produce saturated steam and/or superheated steam according to user requirements, and if a large saturated steam supply amount is required, the production amount of the superheated steam is correspondingly reduced; if a larger supply of superheated steam is required, the production of saturated steam is correspondingly reduced.
The waste heat recycling system can simultaneously produce saturated steam and superheated steam, and can also independently produce saturated steam or superheated steamThe superheated steam can be used for producing at least 0.1t of saturated steam or 0.08t of superheated steam per ton of coke per hour, the temperature of the saturated steam can reach 204 ℃, the temperature of the superheated steam can reach 400 ℃, and the economic benefit is remarkable; the invention adopts two condensing ammonia water heaters and an oil-rich heater to replace the traditional tubular furnace for heating, thereby not only saving a large amount of coke oven gas, but also saving about 2365 ten thousand Nm each year3The coke oven gas of (1); can also reduce SO2、NOxAnd a large amount of CO2The emission of gas waste gas can reduce CO every year2About 18732t of discharge; can reduce SO2About 13t of discharge; can reduce NOxThe emission is about 104t, which is beneficial to environmental protection; the invention adopts two condensing ammonia water heaters and a rich oil heater to replace the traditional tubular furnace for heating, thereby eliminating the potential safety production hazard of a chemical plant and achieving the intrinsic safety; the temperature of the crude gas in the riser can be reduced by 250-350 ℃ by using the waste heat recycling system, so that the spraying amount of the circulating ammonia water can be reduced by 20-30%, the treatment cost of the crude gas is reduced, and the power consumption of a circulating ammonia water pump is saved by 20-30% every year.
The waste heat recycling system is environment-friendly, energy-saving and remarkable in economic benefit, can improve the waste heat utilization rate of enterprises, can reduce carbon emission and waste gas emission, and can generate economic value for externally supplying steam.
Example 2
The embodiment 2 of the invention provides a raw coke oven gas waste heat recycling method, which comprises the following steps:
step one, conveying water in a steam drum 3 to a saturated steam heat exchanger group 1 through a circulating water pump group 9, and returning a mixture of saturated steam and water generated after heat exchange of the saturated steam heat exchanger group 1 to the steam drum 3 through a first water inlet on the steam drum 3;
step two, conveying a part of saturated steam generated in the steam drum 3 to a waste heat utilization system through a steam pipe network through a gas-liquid separator to provide heat energy for a condensed ammonia water heater 4, a condensed rich oil heater 5 and an ammonia still 6; the condensed water separated after the heat exchange of the saturated steam with the condensed ammonia water heater 4 and the condensed rich oil heater 5 returns to the steam drum 3 through the water feed pump unit 8 for the next circulation;
step three, conveying a part of saturated steam generated in the steam drum 3 to the superheated steam heat exchanger group 2 through a steam pipe network through a gas-liquid separator, and conveying superheated steam generated after heat exchange of the superheated steam heat exchanger group 2 to the debenzolization tower 7 to provide heat energy;
and step four, taking part of saturated steam generated in the steam drum 3 as surplus steam through a gas-liquid separator, and supplying heat through a steam pipe network. The surplus steam is sent out for heat supply, so that the economic benefit of enterprises can be further improved.
Preferably, the raw coke oven gas waste heat recycling method further comprises a water supplementing step, when the water amount in the steam drum 3 is insufficient, water is supplemented into the steam drum 3 through a water supplementing system, and a water outlet of the water supplementing system is communicated with a second water inlet of the steam drum 3 through a water supply pump unit 8. Be equipped with the desalination deaerating plant in the water charging system, when the water source in the steam pocket 3 is insufficient, can pass through water charging system, carry the waste heat recovery system with the water through the desalination deoxidization in to guarantee that whole waste heat recovery system is continuous, operate steadily.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (5)
1. The utility model provides a raw coke oven gas waste heat recovery utilizes system which characterized in that: including waste heat recovery system and waste heat utilization system, wherein:
the waste heat recovery system comprises: the system comprises a saturated steam heat exchanger group, a superheated steam heat exchanger group, a steam drum with a steam-water separator, a circulating water pump group and a water feed pump group;
the waste heat utilization system comprises: ammonia water heater, rich oil heater, ammonia still and debenzolization tower;
the water inlet of the saturated steam heat exchanger group is communicated with the water outlet of the steam drum through the circulating water pump group, the water outlet of the saturated steam heat exchanger group is communicated with the first water inlet of the steam drum, and the steam outlet of the steam drum is communicated with the waste heat utilization system through a steam pipe network;
and the air inlet of the superheated steam heat exchanger group is communicated with the steam outlet of the steam drum through a steam pipe network, and the air outlet of the superheated steam heat exchanger group is communicated with the debenzolization tower through a steam pipe network.
2. The raw coke oven gas waste heat recycling system of claim 1, characterized in that: the circulating water pump set and the water supply pump set comprise a plurality of circulating water pumps and a plurality of water supply pumps, the plurality of circulating water pumps are connected in parallel, and the plurality of water supply pumps are connected in parallel.
3. The raw coke oven gas waste heat recycling system of claim 1, characterized in that: the steam drum is characterized by further comprising a water supplementing system, and a water outlet of the water supplementing system is communicated with the second water inlet of the steam drum through the water feed pump set.
4. The raw coke oven gas waste heat recycling system of claim 1, characterized in that: the ammonia water heater and the rich oil heater are both condensing heaters.
5. The raw coke oven gas waste heat recycling system of claim 1, characterized in that: the saturated steam heat exchanger group and the superheated steam heat exchanger group comprise a plurality of parallel-connected ascending pipe heat exchangers.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110240949A (en) * | 2019-07-02 | 2019-09-17 | 武汉方特工业设备技术有限公司 | A kind of raw coke oven gas waste heat recycling system and method |
| CN110240949B (en) * | 2019-07-02 | 2024-06-28 | 武汉方特工业设备技术有限公司 | Raw gas waste heat recycling system and method |
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2019
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110240949A (en) * | 2019-07-02 | 2019-09-17 | 武汉方特工业设备技术有限公司 | A kind of raw coke oven gas waste heat recycling system and method |
| CN110240949B (en) * | 2019-07-02 | 2024-06-28 | 武汉方特工业设备技术有限公司 | Raw gas waste heat recycling system and method |
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