CN209065841U - Coking dry coke quenching and negative pressure benzene removal thermal coupling equipment - Google Patents
Coking dry coke quenching and negative pressure benzene removal thermal coupling equipment Download PDFInfo
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- CN209065841U CN209065841U CN201821532352.1U CN201821532352U CN209065841U CN 209065841 U CN209065841 U CN 209065841U CN 201821532352 U CN201821532352 U CN 201821532352U CN 209065841 U CN209065841 U CN 209065841U
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Abstract
The utility model discloses a kind of coking dry coke quenching and negative pressure benzene removal thermal coupling equipment, including debenzolizing tower and dry coke quenching residual heat boiler, Multi-layer exchanging heat device is equipped in the dry coke quenching residual heat boiler from top to bottom, the interlude of Multi-layer exchanging heat device is middle layer heat exchanger, the debenzolizing tower tower bottom outlet is connect by connecting tube with the input port of an oil circulating pump, the entrance that the delivery outlet of the oil circulating pump is connected to middle layer heat exchanger by pumping oil pipe, the outlet of middle layer heat exchanger is connected to the circulation oil-in of debenzolizing tower tower bottom by circulating pipe, the top exit of the debenzolizing tower is connected to one end of a negative pressure benzene vapour pipeline, and the lower sides of debenzolizing tower are equipped with raw material rich oil entrance.The utility model can make full use of the heat that coking dry coke quenching process generates during negative pressure benzene removal, coke dry quenching furnace is promoted to discharge of the coke temperature stability, wastewater treatment capacity and outer discharge capacity can be reduced simultaneously, reduces the energy waste and cost of investment of heating, promotes reliability of operation.
Description
Technical field
The utility model relates to a kind of coking dry coke quenching and negative pressure benzene removal thermal coupling equipment, belong to chemical production equipment.
Background technique
Currently, domestic coke-oven plant de-benzene process mainly uses the direct stripping of water vapour, crude benzol is produced with single column under normal pressure
Or two kinds of benzene (light benzene and heavy benzol), crude benzol is distilled from washing oil completely at a lower temperature, which stablizes.
But the direct stripping method of water vapour need to use superheated steam as heat source, and water vapour can generate phenol wastewater after condensing, and increase waste water
Treating capacity and outer discharge capacity, impact environment；And since the control of crude benzol tower top temperature is about 93 DEG C below dew point, have water
Steam condensation concentrates at tower top, liquid phase need to be drawn to and be carried out water-oil separating in tower top, and the oil isolated returns to tower top, such as separates
Effect will be bad to cause tower top pressure to fluctuate, and influence to produce；In addition, because of the accumulation of on-condensible gas in vapor condensation cooling procedure
Often cause tower top pressure to increase, need regular outlet on-condensible gas.In recent years, negative pressure benzene removal technology utilization vacuum holding newly developed
It sets the on-condensible gas in extraction crude benzol tower, reduce air pressure in tower, and is between reducing the boiling point of crude benzol, improving component opposite
Volatility makes water-oil separating, solves the problems, such as that normal pressure takes off some of benzene distillation technique.
The heat source used during negative pressure benzene removal is usually diamond heating method, and diamond heating method needs to utilize coke oven
Coal gas is fuel, and there are the wastes of resource, and diamond heating needs independent cloth to install there are the production safety risk of coking
It is standby, improve input cost；At the same time, in coke-oven plant's production, the circulating air that is discharged through coke-oven plant's dry coke quenching residual heat boiler
Cognition is passed directly in coke dry quenching furnace, since recyclegas temperature is higher and temperature fluctuation is larger, will lead to coke dry quenching furnace
Temperature of the discharging of the coke is unstable, reduces product quality.
Summary of the invention
In view of the above-mentioned problems of the prior art, the purpose of the utility model is to provide a kind of coking dry coke quenching and negative pressure
De- benzene thermal coupling equipment during the heat that coking dry coke quenching process generates capable of being made full use of negative pressure benzene removal, is promoted dry
Quenching furnace discharges of the coke temperature stability, while can reduce steam and use, reduce wastewater treatment capacity and outer discharge capacity, reduces the energy of heating
Source waste and cost of investment, promote reliability of operation.
In order to achieve the above purposes, the technical solution adopted by the utility model is: a kind of coking dry coke quenching and negative pressure benzene removal heat
Coupling device, including debenzolizing tower and dry coke quenching residual heat boiler are equipped with Multi-layer exchanging heat in the dry coke quenching residual heat boiler from top to bottom
Device, the interlude of Multi-layer exchanging heat device are middle layer heat exchanger, and the debenzolizing tower tower bottom outlet passes through connecting tube and an oil circulating pump
Input port connection, the entrance that the delivery outlet of the oil circulating pump is connected to middle layer heat exchanger by pumping oil pipe, middle layer heat exchanger
Outlet the circulation oil-in of debenzolizing tower tower bottom, the top exit of the debenzolizing tower and a negative pressure benzene are connected to by circulating pipe
One end of jet chimney is connected to, and the lower sides of debenzolizing tower are equipped with raw material rich oil entrance.
Preferably, the middle layer heat exchanger includes upper and lower part, and the delivery outlet of the oil circulating pump is connected to lower part
Entrance, the outlet of lower part are connected to the circulation oil-in of debenzolizing tower tower bottom by circulating pipe, and the circulating pipe is equipped with one
Branch line, the branch line are connected to the entrance on top, and the outlet on top is connected to a regenerating unit by delivery pipe
The delivery outlet of input port, the regenerating unit is connected to debenzolizing tower.From the tower bottom recycle oil small part warp of the outlet outflow of lower part
Branch line enters top, continues to exchange heat with dry coke quenching recyclegas, more due to the dry coke quenching recyclegas temperature by top
Height, tower bottom recycle oil temperature after exchanging heat again can rise to 255 DEG C, after being exported from the outlet on top by delivery pipe directly into
Enter and be regenerated as rich oil in regenerating unit, the rich oil of generation can enter in debenzolizing tower to carry out directly as feedstock transportation de- benzene, while again
The micro regeneration dregs of fat that generating apparatus generates can be sent directly into tar system.
Further, the tower bottom for convenience in adjustment branch line recycles oil mass, and the branch line is equipped with self-regulated
Valve.
It further, further include a poor oil-rich heat exchanger and an oil gas heat exchanger, the pumping oil pipe is equipped with a branch
Pipe, bypass duct are connected to the top side entrance of poor oil-rich heat exchanger, the bottom side outlet of the poor oil-rich heat exchanger
To the raw material rich oil entrance of debenzolizing tower, the bottom other side outlet of poor oil-rich heat exchanger washes benzene series to one and unites；The negative pressure
The other end of benzene vapour pipeline is connected to the top side entrance of oil gas heat exchanger, the bottom side outlet of oil gas heat exchanger with it is poor
Another side entrance connection in the top of rich oil heat exchanger.Negative pressure benzene vapour pipeline enters benzene vapour from the top side of oil gas heat exchanger
In mouth input oil gas heat exchanger, cooling obtains crude benzol after the rich oil heat exchange with another side entrance input in top from oil gas heat exchanger
Product is exported from the bottom other side of oil gas heat exchanger to flow out；Rich oil temperature after exchanging heat is raised through the top of poor oil-rich heat exchanger
Another side entrance in portion enters in poor oil-rich heat exchanger, exchange heat with the tower bottom recycle oil come by bypass duct conveying after be delivered to de- benzene
Raw material of the raw material rich oil entrance of tower as negative pressure benzene removal, the tower bottom recycle oil that bypass duct conveying comes cool after exchanging heat,
From the bottom of poor oil-rich heat exchanger, another side outlet, which is delivered to, washes benzene series system.
In use, the tower bottom recycle oil of debenzolizing tower bottom passes through pumping oil pipe after extracting out via oil circulating pump be sent into dry coke quenching
Dry coke quenching recyclegas in the middle layer heat exchanger of waste heat boiler with 450-520 DEG C exchanges heat, the tower bottom recycle oil after heat exchange
Temperature is at 245 DEG C or so；Enter in debenzolizing tower after the heat exchange of tower bottom recycle oil and flash, the washing oil and benzene vapour of generation are as debenzolizing tower
The heat source of distillation procedure makes the benzene from the raw material rich oil that raw material rich oil entrance enters in debenzolizing tower become benzene vapour evolution, and
It is extracted out by negative pressure benzene vapour pipeline, realizes the negative-pressure operation of debenzolizing tower；Tower bottom in dry coke quenching circulating air and middle layer heat exchanger
Temperature reduces after recycle oil heat exchange, into secondary filter, and is sent into coke dry quenching furnace and is recycled.
Compared with the existing technology, the utility model has the advantage that
(1) the utility model set-up mode is ingenious, and coking dry coke quenching process is combined with negative pressure benzene removal, is passed through
The heat that coking dry coke quenching process generates is fully absorbed utilization by the energy exchange processes using tower bottom recycle oil as heat transferring medium
To during negative pressure benzene removal, the washing oil and benzene vapour that the tower bottom recycle oil to absorb heat generates after flashing are not required to as heat source
It is introduced separately into water vapour, reduces subsequent wastewater treatment amount and outer discharge capacity, alleviates the influence to environment.
(2) negative low-voltage operating conditions are relied on, reduce rich oil boiling point, and improve the relative volatility of benezene material,
Far below normal pressure rich oil boiling point, it is de- lower than that can steam benezene material from rich oil under the conditions of the temperature of atmospheric operation temperature, make
Rich oil is regenerated.
(3) due to not needing to consume extra energy heat supply, and without increasing the equipment newly put into, throwing is reduced costs
Enter, the risk of production safety will not be brought；Temperature reduces after into the dry coke quenching circulating air heat exchange of dry coke quenching residual heat boiler, warp
From coke dry quenching furnace, rear temperature is substantially reduced out and temperature value is stablized after final dusting, improves the discharging of the coke for subsequent coke dry quenching furnace
Temperature stability directly improves product quality, and due to temperature reduction after the heat exchange of dry coke quenching circulating air, avoids and set to subsequent
Standby high-temperature damage, extends service life.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the utility model；
In figure, 1, debenzolizing tower, 1-1, circulation oil-in, 1-2, raw material rich oil entrance, 2, dry coke quenching residual heat boiler, 3, rich or poor
Oil heat exchanger, 4, oil gas heat exchanger, 5, oil circulating pump, 5-1, bypass duct, 6, circulating pipe, 6-1, branch line, 6-2, self-regulated
Valve, 7, negative pressure benzene vapour pipeline, 8, regenerating unit, 10, Multi-layer exchanging heat device, 12, middle layer heat exchanger, 12a, top, 12b, under
Portion.
Specific embodiment
The utility model is described in further detail with reference to the accompanying drawing.
As shown in Figure 1, a kind of coking dry coke quenching and negative pressure benzene removal thermal coupling equipment, including debenzolizing tower 1 and dry coke quenching waste heat
Boiler 2, is equipped with Multi-layer exchanging heat device 10 in the dry coke quenching residual heat boiler 2 from top to bottom, during the interlude of Multi-layer exchanging heat device 10 is
Layer heat exchanger 12,1 tower bottom of the debenzolizing tower outlet are connect by connecting tube with the input port of an oil circulating pump 5, the recycle oil
The entrance that the delivery outlet of pump 5 is connected to middle layer heat exchanger 12 by pumping oil pipe, the outlet of middle layer heat exchanger 12 passes through recycle oil
Pipe 6 is connected to the circulation oil-in 1-1 of 1 tower bottom of debenzolizing tower, the top exit of the debenzolizing tower 1 and a negative pressure benzene vapour pipeline 7
One end connection, and the lower sides of debenzolizing tower 1 be equipped with raw material rich oil entrance 1-2.
In use, dry coke quenching circulating air can enter dry coke quenching residual heat boiler 2 from top and from top to bottom from Multi-layer exchanging heat device
10 pass through.The tower bottom recycle oil of 1 bottom of debenzolizing tower passes through pumping oil pipe and is sent into dry coke quenching waste heat pot after extracting out via oil circulating pump 5
Dry coke quenching recyclegas in the middle layer heat exchanger 12 of furnace 2 with 450-520 DEG C exchanges heat, and the flow of control loop oil pump 5 makes
Tower bottom recycle oil after heat exchange obtains enough heats, temperature at 245 DEG C or so；Pass through circulating pipe after the heat exchange of tower bottom recycle oil
6 enter in debenzolizing tower 1 and flash through recycling oil-in 1-1, heat of the washing oil and benzene vapour of generation as 1 distillation procedure of debenzolizing tower
Source makes the benzene from the raw material rich oil that raw material rich oil entrance 1-2 enters in debenzolizing tower 1 become benzene vapour evolution, and passes through negative pressure
Benzene vapour pipeline 7 is extracted out, realizes the negative-pressure operation of debenzolizing tower 1.
Temperature reduces after tower bottom recycle oil heat exchange in dry coke quenching circulating air and middle layer heat exchanger 12, into final dusting
Device, and enter the boosting heating of circulating air blower, cool down subsequently into secondary economizer, is sent into coke dry quenching furnace and is recycled.
Preferably, the middle layer heat exchanger 12 includes top 12a and lower part 12b, and the delivery outlet of the oil circulating pump 5 connects
To the entrance of lower part 12b, the outlet of lower part 12b is connected to the circulation oil-in 1-1 of 1 tower bottom of debenzolizing tower, institute by circulating pipe 6
It states circulating pipe 6 and is connected to the entrance of top 12a equipped with branch line a 6-1, the branch line 6-1, top 12a's goes out
Mouth is connected to the input port of a regenerating unit 8 by delivery pipe, and the delivery outlet of the regenerating unit 8 is connected to debenzolizing tower 1.
By above-mentioned setting, the tower bottom recycle oil small part flowed out from the outlet of lower part 12b enters upper through branch line 6-1
Portion 12a continues to exchange heat with dry coke quenching recyclegas, and due to higher by the dry coke quenching recyclegas temperature of top 12a, tower bottom is followed
Ring oil temperature after exchanging heat again can rise to 255 DEG C, be directly entered regeneration after exporting from the outlet of top 12a by delivery pipe
Rich oil is regenerated as in device, the rich oil of generation can enter in debenzolizing tower 1 to carry out directly as feedstock transportation de- benzene, while regenerating unit
The micro regeneration dregs of fat generated can be sent directly into tar system.
Further, the tower bottom for convenience in adjustment branch line 6-1 recycles oil mass, sets on the branch line 6-1
There is self-regulated valve 6-2.
It further, further include a poor oil-rich heat exchanger 3 and an oil gas heat exchanger 4, the pumping oil pipe is equipped with one
Road pipe 5-1, bypass duct 5-1 are connected to the top side entrance of poor oil-rich heat exchanger 3, the bottom one of the poor oil-rich heat exchanger 3
Side outlet is connected to the raw material rich oil entrance 1-2 of debenzolizing tower 1, and the bottom other side outlet of poor oil-rich heat exchanger 3 to one is washed
Benzene series system；The other end of the negative pressure benzene vapour pipeline 7 is connected to the top side entrance of oil gas heat exchanger 4, oil gas heat exchanger 4
Bottom side outlet be connected to another side entrance in the top of poor oil-rich heat exchanger 3.
By above-mentioned setting, benzene vapour is inputted oil from the top side entrance of oil gas heat exchanger 4 by negative pressure benzene vapour pipeline 7
In gas heat exchanger 4, with from cooling after the rich oil heat exchange that another side entrance in the top of oil gas heat exchanger 4 inputs obtain crude benzol product from
The bottom other side of oil gas heat exchanger 4 exports outflow；The top that rich oil temperature after exchanging heat is raised through poor oil-rich heat exchanger 3 is another
One side entrance enters in poor oil-rich heat exchanger 3, exchange heat with the tower bottom recycle oil come by bypass duct 5-1 conveying after be delivered to de- benzene
Raw material of the raw material rich oil entrance 1-2 of tower 1 as negative pressure benzene removal, the tower bottom recycle oil that bypass duct 5-1 conveying comes are cold after exchanging heat
But cool down, from the bottom of poor oil-rich heat exchanger 3, another side outlet, which is delivered to, washes benzene series system.
Preferably, the Multi-layer exchanging heat device 10 is dividing wall type heat exchanger.In dividing wall type heat exchanger, cold and hot two media quilt
Partition separates, and directly carries out heat exchange by partition.
Claims (4)
1. a kind of coking dry coke quenching and negative pressure benzene removal thermal coupling equipment, including debenzolizing tower (1) and dry coke quenching residual heat boiler (2),
It is characterized in that, is equipped with Multi-layer exchanging heat device (10) from top to bottom in the dry coke quenching residual heat boiler (2), in Multi-layer exchanging heat device (10)
Between section be middle layer heat exchanger (12), debenzolizing tower (1) tower bottom outlet is connected by the input port of connecting tube and an oil circulating pump (5)
It connects, the entrance that the delivery outlet of the oil circulating pump (5) is connected to middle layer heat exchanger (12) by pumping oil pipe, middle layer heat exchanger
(12) outlet is connected to the circulation oil-in (1-1) of debenzolizing tower (1) tower bottom by circulating pipe (6), the debenzolizing tower (1)
Top exit is connected to one end of a negative pressure benzene vapour pipeline (7), and the lower sides of debenzolizing tower (1) are equipped with raw material rich oil and enter
Mouth (1-2).
2. coking dry coke quenching according to claim 1 and negative pressure benzene removal thermal coupling equipment, which is characterized in that the middle layer is changed
Hot device (12) includes top (12a) and lower part (12b), and the delivery outlet of the oil circulating pump (5) is connected to entering for lower part (12b)
Mouthful, the outlet of lower part (12b) is connected to the circulation oil-in (1-1) of debenzolizing tower (1) tower bottom by circulating pipe (6), described to follow
Ring oil pipe (6) is equipped with a branch line (6-1), and the branch line (6-1) is connected to the entrance of top (12a), top
The outlet of (12a) is connected to the input port of a regenerating unit (8) by delivery pipe, the delivery outlet of the regenerating unit (8) and de-
Benzene column (1) connection.
3. coking dry coke quenching according to claim 2 and negative pressure benzene removal thermal coupling equipment, which is characterized in that the branched pipe
Road (6-1) is equipped with self-regulated valve (6-2).
4. coking dry coke quenching according to claim 1 and negative pressure benzene removal thermal coupling equipment, which is characterized in that further include one poor
Rich oil heat exchanger (3) and an oil gas heat exchanger (4), the pumping oil pipe are equipped with a bypass duct (5-1), and bypass duct (5-1) is even
It is connected to the top side entrance of poor oil-rich heat exchanger (3), the bottom side outlet of the poor oil-rich heat exchanger (3) to de- benzene
The raw material rich oil entrance (1-2) of tower (1), the bottom other side outlet of poor oil-rich heat exchanger (3) wash benzene series to one and unite；It is described
The other end of negative pressure benzene vapour pipeline (7) is connected to the top side entrance of oil gas heat exchanger (4), the bottom of oil gas heat exchanger (4)
One side outlet of portion is connected to another side entrance in top of poor oil-rich heat exchanger (3).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821532352.1U CN209065841U (en) | 2018-09-19 | 2018-09-19 | Coking dry coke quenching and negative pressure benzene removal thermal coupling equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821532352.1U CN209065841U (en) | 2018-09-19 | 2018-09-19 | Coking dry coke quenching and negative pressure benzene removal thermal coupling equipment |
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| Publication Number | Publication Date |
|---|---|
| CN209065841U true CN209065841U (en) | 2019-07-05 |
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ID=67092841
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201821532352.1U Expired - Fee Related CN209065841U (en) | 2018-09-19 | 2018-09-19 | Coking dry coke quenching and negative pressure benzene removal thermal coupling equipment |
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| CN (1) | CN209065841U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111518582A (en) * | 2020-03-16 | 2020-08-11 | 临涣焦化股份有限公司 | Device and method for debenzolizing coal tar steam |
| CN112610941A (en) * | 2020-12-30 | 2021-04-06 | 中冶焦耐(大连)工程技术有限公司 | Low-grade waste heat recovery system and process of coking production system |
-
2018
- 2018-09-19 CN CN201821532352.1U patent/CN209065841U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111518582A (en) * | 2020-03-16 | 2020-08-11 | 临涣焦化股份有限公司 | Device and method for debenzolizing coal tar steam |
| CN112610941A (en) * | 2020-12-30 | 2021-04-06 | 中冶焦耐(大连)工程技术有限公司 | Low-grade waste heat recovery system and process of coking production system |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20220104 Address after: 221700 chemical industry park, Fengxian Economic Development Zone, Xuzhou City, Jiangsu Province Patentee after: Xuzhou Jiantao Energy Co.,Ltd. Address before: 221000 Li Guo Zhen Ma Yuan Cun, Tongshan District, Xuzhou City, Jiangsu Province Patentee before: XUZHOU WEITIAN CHEMICAL CO.,LTD. |
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| TR01 | Transfer of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20190705 |
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| CF01 | Termination of patent right due to non-payment of annual fee |