CN215627704U - Combined utilization system for condensate waste heat of carbon four and aromatic hydrocarbon device - Google Patents
Combined utilization system for condensate waste heat of carbon four and aromatic hydrocarbon device Download PDFInfo
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- CN215627704U CN215627704U CN202121449772.5U CN202121449772U CN215627704U CN 215627704 U CN215627704 U CN 215627704U CN 202121449772 U CN202121449772 U CN 202121449772U CN 215627704 U CN215627704 U CN 215627704U
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Abstract
A system for jointly utilizing condensate waste heat of a carbon four and aromatic hydrocarbon device comprises steam condensate from three sets of devices including MTBE/butylene-1, butadiene extraction and aromatic hydrocarbon extraction, wherein the steam condensate is conveyed to a first pipeline in a boundary area of the MTBE/butylene-1 device through a factory boundary pipe gallery pipeline to be converged, then is conveyed to a static mixer through the first pipeline to be mixed, is discharged through a second pipeline connected with the static mixer and is conveyed into a pipe layer of a shell-and-tube reboiler of a tower bottom reboiler II of a deisobutanizer, exchanges heat with shell layer tower kettle materials which are fed through a third pipeline connected with the tower bottom reboiler II and are discharged from the bottom of the deisobutanizer, and the steam condensate after heat exchange is conveyed to a whole plant steam condensate header pipe outside the boundary area of the device through a fourth pipeline connected with the tower bottom reboiler II; and a fifth pipeline connected with the second tower top reboiler returns the shell layer tower kettle material of the deisobutanizer after heat exchange to the deisobutanizer. The utility model saves steam consumption.
Description
Technical Field
The utility model relates to the technical field of recycling of steam condensate heat of a chemical device, and particularly provides a combined utilization system for condensate waste heat of a carbon four and aromatic hydrocarbon device.
Background
In the prior art, steam condensate of M TBE/butylene-1, butadiene extraction and aromatic hydrocarbon extraction devices is directly pumped to a factory steam condensate pipe network through a condensate pump, and is not fully utilized; the reboiler of the deisobutanizer of the existing M TBE/butene-1 device adopts low-pressure steam as a heat source, which causes energy consumption. Therefore, the waste heat of the steam condensate of the three sets of the M TBE/butene-1 device, the butadiene extraction device and the aromatic hydrocarbon extraction device is fully utilized to reduce the low-pressure steam consumption of the reboiler of the deisobutanizer of the M TBE/butene-1 device, which is a problem to be solved urgently,
SUMMERY OF THE UTILITY MODEL
The utility model provides a combined utilization system for condensate waste heat of a carbon four and aromatic hydrocarbon device, and aims to solve the technical problem of reducing low-pressure steam consumption of a reboiler of a deisobutanizer of an M TBE/butene-1 device by fully utilizing the waste heat of steam condensate of the M TBE/butene-1 device, butadiene extraction device and aromatic hydrocarbon extraction device.
The technical scheme of the utility model is as follows:
a combined utilization system of condensate waste heat of a carbon four and aromatic hydrocarbon device comprises an M TBE/butene-1 device, a butadiene extraction device and an aromatic hydrocarbon extraction device, wherein steam condensate of the M TBE/butene-1 device, steam condensate of the butadiene extraction device and steam condensate of the aromatic hydrocarbon extraction device from the M TBE/butene-1, butadiene extraction and aromatic hydrocarbon extraction three sets of devices are conveyed to a pipeline I in a boundary area of the M TBE/butene-1 device through a factory boundary pipe gallery pipeline to be converged, then the steam condensate is conveyed into a static mixer through the pipeline I to be mixed, then the steam condensate is discharged through a pipeline II connected with the static mixer and is conveyed into a pipe layer of a shell-and-tube reboiler of a tower bottom reboiler II of an deisobutanizer, and the steam condensate is subjected to heat exchange with shell-layer tower kettle materials which are conveyed through a pipeline III connected with the tower bottom reboiler and are discharged from the bottom of the deisobutanizer, the steam condensate after heat exchange is sent to a whole plant steam condensate header outside a device boundary area through a pipeline four connected with the tower bottom reboiler II; and a fifth pipeline connected with the second tower bottom reboiler returns the shell layer tower kettle material of the deisobutanizer after heat exchange to the deisobutanizer.
The system for jointly utilizing the condensate waste heat of the carbon four and arene device is characterized in that a shell layer tower kettle material at the bottom of the deisobutanizer is output through a pipeline six connected with the bottom of the deisobutanizer, the pipeline six is connected with a pipeline three and one end of a pipeline seven in parallel, and the pipeline six conveys the shell layer tower kettle material to the interior of the pipeline three and the pipeline seven; the seventh pipeline feeds the shell layer tower kettle material into a first tower bottom reboiler connected with the seventh pipeline, and exchanges heat with low-pressure steam in a pipe layer of a shell-and-tube reboiler fed into the first tower bottom reboiler through an eighth pipeline, and the shell layer tower kettle material is returned into the deisobutanizer through a ninth pipeline connected with the first tower bottom reboiler after exchanging heat; condensing the low-pressure steam after heat exchange into steam condensate, and sending the steam condensate to a steam condensate header pipe of the whole plant through a pipeline ten connected with a tower bottom reboiler I; and the tower bottom reboiler I and the tower bottom reboiler II work and operate simultaneously.
Effect of the utility model
The utility model realizes that the condensate waste heat of the M TBE/butylene-1, butadiene extraction and aromatic hydrocarbon extraction devices can be recycled, and can save steam consumption, energy and reasonably and fully utilize energy for the M TBE/butylene-1 device.
Drawings
FIG. 1 is a schematic diagram of the system connection of the present invention.
Description of the figures
1. The deisobutanizer comprises a deisobutanizer (IC-501), 2, a tower bottom reboiler I (E-503), 3, a tower bottom reboiler II (E-503N), 4, a static mixer (M-841), 5, M TBE/butene-1 device steam condensate, 6, butadiene extraction device steam condensate, 7, aromatic extraction device steam condensate, 8, (steam condensate to) whole plant condensate header pipe, 9, low-pressure steam, 10, steam condensate I, a pipeline I101, a pipeline II 102, a pipeline III 103, a pipeline IV 104, a pipeline V105, a pipeline VI 106, a pipeline VII 107, a pipeline VIII, a pipeline VII 109 and a pipeline VII 100.
Detailed Description
Referring to fig. 1, the combined utilization system of condensate waste heat of a carbon four and aromatic hydrocarbon device comprises an M TBE/butene-1 device, a butadiene extraction device and an aromatic hydrocarbon extraction device, wherein M TBE/butene-1 device steam condensate 5, butadiene extraction device steam condensate 6 and aromatic hydrocarbon extraction device steam condensate 7 from the M TBE/butene-1, butadiene extraction and aromatic hydrocarbon extraction three sets of devices are conveyed to a pipeline I101 in a boundary area of the M TBE/butene-1 device through a factory boundary pipeline gallery and are converged, then the merged pipeline I101 is conveyed into a static mixer 4 for mixing, then the mixed liquid is discharged through a pipeline II 102 connected with the static mixer 4 and is conveyed into a pipe layer of a shell-and-tube reboiler of a tower bottom reboiler II 3 of a deisobutanizer 1, and the mixed liquid is conveyed through a pipeline III 103 connected with the tower bottom reboiler II 3, Exchanging heat of a shell layer tower kettle material discharged from the bottom of the deisobutanizer (IC-501) 1, and sending steam condensate after heat exchange to a whole plant steam condensate header pipe 8 outside a device boundary area through a pipeline IV 104 connected with the tower bottom reboiler II (E-503N) 3; and a fifth pipeline 105 connected with the second tower bottom reboiler (E-503N) 3 returns the shell layer tower kettle material of the deisobutanizer (IC-501) 1 after heat exchange to the deisobutanizer 1.
The system for jointly utilizing the condensate waste heat of the carbon four and aromatic hydrocarbon device is characterized in that the steam condensate 5 of the M TBE/butene-1 device, the steam condensate 6 of the butadiene extraction device and the steam condensate 7 of the aromatic hydrocarbon extraction device are respectively at 90 ℃, 90 ℃ and 130 ℃.
The system for jointly utilizing the waste heat of the condensate of the carbon four and aromatic hydrocarbon device is characterized in that the temperature of the uniformly mixed condensate of the static mixer 4 is 110 ℃.
The system for jointly utilizing the condensate waste heat of the carbon four and aromatic hydrocarbon device is characterized in that the material temperature of the shell layer tower kettle before heat exchange is 65 ℃.
The system for jointly utilizing the condensate waste heat of the carbon four and aromatic hydrocarbon device is characterized in that a shell layer tower kettle material at the bottom of the deisobutanizer 1 is output through a pipeline six 106 connected with the bottom of the deisobutanizer, the pipeline six 106 is connected with one end of a pipeline three 103 and one end of a pipeline seven 107 in parallel, and the pipeline six 106 conveys the shell layer tower kettle material to the pipeline three 103 and the pipeline seven 107; the seventh pipeline 107 feeds the shell layer tower kettle material into a first tower reboiler 2 of the deisobutanizer 1 connected with the seventh pipeline, the shell layer tower kettle material exchanges heat with low-pressure steam 9 fed into a pipe layer of a shell-and-tube reboiler of the first tower reboiler 2 through an eighth pipeline 108, and the shell layer tower kettle material after heat exchange returns to the deisobutanizer (IC-501) 1 through a ninth pipeline 109 connected with the first tower reboiler (E-503) 2; condensing the low-pressure steam 9 after heat exchange into steam condensate I10, and sending the steam condensate I10 to a steam condensate header pipe of the whole plant through a pipeline ten 100 connected with a tower bottom reboiler I (E-503) 2; and the tower bottom reboiler I (E-503) 2 and the tower bottom reboiler II (E-503N) are operated simultaneously.
The working principle of the utility model is as follows:
referring to the figure 1, the steam condensate 5 of an M TBE/butene-1 device, the steam condensate 6 of a butadiene extraction device and the steam condensate 7 of an aromatic hydrocarbon extraction device from the M TBE/butene-1 device, the butadiene extraction device and the aromatic hydrocarbon extraction device of 3 sets of devices are respectively at the temperature of 90 ℃, 90 ℃ and 130 ℃, the steam condensate is conveyed to a boundary area of the M TBE/butene-1 device through a factory boundary pipe gallery, the three steam condensates are uniformly mixed through a static mixer M-8414 after being converged, the mixed temperature is 110 ℃, the mixed steam condensate is conveyed to a shell-and-tube reboiler layer of a reboiler II E-503N 3 at the bottom of an isobutane removing tower and exchanges heat with a shell layer tower kettle material of an isobutane removing tower IC-5011, the tower kettle material temperature is 65 ℃, and the steam condensate after heat exchange is conveyed to a whole plant steam condensate main pipe outside the boundary area of the devices.
The waste heat of the steam condensate 5 of the M TBE/butene-1 device, the steam condensate 6 of the butadiene extraction device and the steam condensate 7 of the aromatic hydrocarbon extraction device is fully utilized to the low-pressure steam consumption of the reboiler I C-5011 of the deisobutanizer, and the steam consumption of the reboiler I E-5032 at the bottom of the deisobutanizer is reduced.
The material in the deisobutanizer IC-501 is led out of the pipeline 105 from the upper part of the second E-503N shell layer of the tower bottom reboiler after being heated by steam condensate in the second E-503N shell layer of the tower bottom reboiler, and is led out of the lower opening of the deisobutanizer IC-501, and the pipeline 105 is connected with the lower opening of the tower through a flange.
A second tower bottom reboiler E-503N adopts a shell-and-tube heat exchanger, and is a common general structure;
static mixer M-841, is a common general structure. The principle is that fluid flows in a pipeline to impact various plate elements, the velocity gradient of laminar flow motion of the fluid is increased or turbulent flow is formed, the laminar flow is divided, moved and recombined, and in the turbulent flow, the fluid can generate violent vortex in the section direction besides the three conditions, and strong shearing force acts on the fluid to further divide and mix the fluid.
Examples
The utility model carries out systematic trial, and compares with the prior art, the systematic connection diagram of the trial is shown in figure 1, statistics shows that the consumption of the E-503 steam of the reboiler at the bottom of the deisobutanizer is reduced by 3.88t/h, and the low-pressure steam is saved by 3.34 ten thousand tons/year.
Prior art before transformation: the M TBE/butene-1 device is provided with a device for delivering 16 tons of 90 ℃ steam condensate every hour; the butadiene extraction device has 16 tons of steam condensate with the temperature of 90 ℃ per hour and is sent out of the device; the aromatic extraction device has 35 tons of high-temperature condensate at 130 ℃ per hour, and the condensate is sent out of the device after being cooled to 90 ℃ by air cooling, so that the heat of the condensate is not effectively utilized. An M TBE/butene-1 device is connected with a deisobutanizer C-501/C-502 (in series), the design temperature of a deisobutanizer IC-501 substrate material is 65.1 ℃, a tower bottom reboiler E-503 uses 0.4MPa steam as a heat source, and the low-pressure steam quantity is consumed by 7.5 t/h.
Claims (2)
1. The combined utilization system of the condensation waste heat of the carbon four and aromatic hydrocarbon device comprises an MTBE/butene-1 device, a butadiene extraction device and an aromatic hydrocarbon extraction device, and is characterized in that the MTBE/butene-1 device steam condensate (5), the butadiene extraction device steam condensate (6) and the aromatic hydrocarbon extraction device steam condensate (7) from the MTBE/butene-1, butadiene extraction and aromatic hydrocarbon extraction three sets of devices are conveyed to a first pipeline (101) in a boundary area of the MTBE/butene-1 device through a factory boundary pipe gallery pipeline to be converged, then are conveyed to a static mixer (4) through a first pipeline (101) to be mixed, are discharged through a second pipeline (102) connected with the static mixer (4), are conveyed into a pipe layer of a shell-and-tube shell type of a second reboiler (E-503N) (3) at the bottom of the deisobutanizer (1), and are conveyed to a reboiler through a third pipeline (103) connected with the second pipeline (E-503N) (3) at the bottom of the deisobutanizer (1), Exchanging heat of the shell layer tower kettle material discharged from the bottom of the deisobutanizer (1), and sending the steam condensate after heat exchange to a whole plant steam condensate header pipe (8) outside a device boundary area through a pipeline IV (104) connected with the tower bottom reboiler II (E-503N) (3); and a fifth pipeline (105) connected with the second tower bottom reboiler (E-503N) (3) returns the shell layer tower kettle material of the deisobutanizer (1) after heat exchange to the deisobutanizer (1).
2. The system for jointly utilizing the condensate waste heat of the carbon four aromatic hydrocarbon device according to claim 1, wherein the shell layer tower kettle material at the bottom of the deisobutanizer (1) is output through a pipeline six (106) connected with the bottom of the deisobutanizer, the pipeline six (106) is connected with one end of a pipeline three (103) and one end of a pipeline seven (107) in parallel, and the pipeline six (106) conveys the shell layer tower kettle material to the pipeline three (103) and the pipeline seven (107); the seventh pipeline (107) feeds the shell layer tower kettle material into a first tower reboiler (E-503) (2) of the deisobutanizer (1) connected with the seventh pipeline (107), and exchanges heat with low-pressure steam (9) in a pipe layer of a shell-and-tube reboiler fed into the first tower reboiler (E-503) (2) through an eighth pipeline (108), and the shell layer tower kettle material returns to the deisobutanizer (1) through a ninth pipeline (109) connected with the first tower reboiler (E-503) (2) after exchanging heat; condensing the low-pressure steam (9) after heat exchange into steam condensate I (10), and sending the steam condensate I (10) to a steam condensate header pipe of the whole plant through a pipeline ten (100) connected with a tower bottom reboiler I E-503 (2); and the first tower bottom reboiler E-503 (2) and the second tower bottom reboiler E-503N are operated simultaneously.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115120997A (en) * | 2022-06-30 | 2022-09-30 | 浙江卫星能源有限公司 | Separation system and method for n-butyraldehyde and isobutyraldehyde |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115120997A (en) * | 2022-06-30 | 2022-09-30 | 浙江卫星能源有限公司 | Separation system and method for n-butyraldehyde and isobutyraldehyde |
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