CN116875340A - System for be used for heavy aromatic separation - Google Patents
System for be used for heavy aromatic separation Download PDFInfo
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- CN116875340A CN116875340A CN202310762887.7A CN202310762887A CN116875340A CN 116875340 A CN116875340 A CN 116875340A CN 202310762887 A CN202310762887 A CN 202310762887A CN 116875340 A CN116875340 A CN 116875340A
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- tube
- shell
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- inlet
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- 238000000926 separation method Methods 0.000 title claims abstract description 101
- 125000003118 aryl group Chemical group 0.000 title claims abstract description 59
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 22
- 238000004804 winding Methods 0.000 claims abstract description 20
- 239000002994 raw material Substances 0.000 claims abstract description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 5
- 239000007788 liquid Substances 0.000 claims description 99
- 238000004781 supercooling Methods 0.000 claims description 41
- 238000009833 condensation Methods 0.000 claims description 37
- 230000005494 condensation Effects 0.000 claims description 37
- 238000010992 reflux Methods 0.000 claims description 33
- 230000002093 peripheral effect Effects 0.000 claims description 24
- 238000004891 communication Methods 0.000 claims description 13
- 238000000034 method Methods 0.000 claims description 9
- 210000002445 nipple Anatomy 0.000 claims 1
- 239000007789 gas Substances 0.000 description 26
- 238000010586 diagram Methods 0.000 description 8
- 239000012071 phase Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- GWHJZXXIDMPWGX-UHFFFAOYSA-N 1,2,4-trimethylbenzene Chemical compound CC1=CC=C(C)C(C)=C1 GWHJZXXIDMPWGX-UHFFFAOYSA-N 0.000 description 4
- SQNZJJAZBFDUTD-UHFFFAOYSA-N durene Chemical compound CC1=CC(C)=C(C)C=C1C SQNZJJAZBFDUTD-UHFFFAOYSA-N 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- AUHZEENZYGFFBQ-UHFFFAOYSA-N mesitylene Substances CC1=CC(C)=CC(C)=C1 AUHZEENZYGFFBQ-UHFFFAOYSA-N 0.000 description 2
- 125000001827 mesitylenyl group Chemical group [H]C1=C(C(*)=C(C([H])=C1C([H])([H])[H])C([H])([H])[H])C([H])([H])[H] 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1096—Aromatics or polyaromatics
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- Water Supply & Treatment (AREA)
- General Chemical & Material Sciences (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
A system for separating heavy aromatics comprises a heavy aromatics separation tower and a flash tower, wherein the bottom of the flash tower is provided with a product outlet; the device comprises a first winding tube type heat exchanger with a first shell side and at least two tube sides, wherein an inlet of the first shell side is communicated with a top outlet of a heavy aromatic hydrocarbon separation tower, an outlet of the first shell side is communicated with the downstream, the two tube sides are respectively a first tube side and a second tube side, the first tube side is positioned at the upstream of the second tube side along the direction from the inlet of the first shell side to the outlet of the shell side, the inlet of the first tube side supplies hot water to be input, the outlet of the first tube side supplies steam to be output, and the inlet of the second tube side supplies heavy aromatic hydrocarbon raw material to be input; a second wound tube heat exchanger having a second shell side, at least one fourth tube side; the first outlet at the bottom of the heavy aromatic separation tower is communicated with the inlet at the middle part of the flash tower through a second pipeline, and a second heater is arranged on the second pipeline. Compared with the prior art, the invention can improve the heat utilization rate.
Description
Technical Field
The invention belongs to the technical field of gasoline processing, and particularly relates to a system for heavy aromatic separation.
Background
The existing system for heavy aromatic separation is as in the patent application of application number 202010882077.1, namely an efficient and energy-saving heavy aromatic separation process (application publication number CN 112047800A), and uses a C9-removing tower and a durene tower to purify heavy aromatic, so that durene enriched materials can be extracted from heavy aromatic materials which are byproducts of the reaction of a reforming device, and the energy consumption of operation is reduced to a greater extent by adopting a double-effect rectification and partition wall rectification thermal coupling technology, so that compared with the conventional double-tower rectification process, the energy can be saved by more than 45%.
Another example is the invention patent application No. 201911141949.2, separation C 9 The heavy aromatic hydrocarbon method (application publication No. CN 112824366A) uses reformed heavy aromatic hydrocarbon as raw material, adopts a rectification method to separate raw material oil, and the light components can be rectified to obtain mesitylene and pseudocumene, the purity of both the mesitylene and the pseudocumene can be greater than 85%, the components with the distillation range of 170-190 ℃ in the heavy components can be rectified and separated to obtain the hemimellitic benzene with the purity of not less than 85%, and other heavy components can be used as heavy aromatic hydrocarbon solvent oil.
However, the heat utilization of the existing systems for heavy aromatics separation needs to be further improved.
Disclosure of Invention
The invention aims to solve the technical problem of providing a system for separating heavy aromatic hydrocarbon so as to improve the heat utilization rate.
The technical scheme adopted for solving the technical problems is as follows: a system for heavy aromatic separation comprises a heavy aromatic separation tower and a flash tower, wherein the bottom of the flash tower is provided with a product outlet;
it is characterized in that the method also comprises the following steps:
the device comprises a first winding tube type heat exchanger with a first shell side and at least two tube sides, wherein an inlet of the first shell side is communicated with a top outlet of the heavy aromatic separation tower, an outlet of the first shell side is communicated to the downstream, the two tube sides are respectively a first tube side and a second tube side, the first tube side is positioned at the upstream of the second tube side along the direction from the inlet to the outlet of the first shell side, the inlet of the first tube side supplies hot water for input, the outlet of the first tube side supplies steam for output, and the inlet of the second tube side supplies heavy aromatic raw material for input;
a second wound tube heat exchanger having a second shell side with an inlet in communication with the top outlet of the flash column, at least a fourth tube side with an outlet in communication with the outlet of the second tube side of the first wound tube heat exchanger, the outlet of the second shell side being in communication downstream; the outlet of the fourth tube pass is communicated with the middle inlet of the heavy aromatic separation tower through a first pipeline, and a first heater is arranged on the first pipeline;
The first outlet at the bottom of the heavy aromatic separation tower is communicated with the inlet at the middle part of the flash tower through a second pipeline, and a second heater is arranged on the second pipeline.
Preferably, the first wound tube heat exchanger further has a third tube pass located downstream of the first tube pass and upstream of the second tube pass along a direction of the shell-side medium from the inlet to the outlet of the first shell pass.
Preferably, the system also comprises a first bypass pipeline, wherein the inlet of the first bypass pipeline is used for inputting the heavy aromatic hydrocarbon raw material, and the outlet of the first bypass pipeline is communicated with the inlet of the fourth tube side of the second winding tube type heat exchanger; and a first temperature control valve is arranged on the first bypass pipeline and is arranged to adjust the flow of heavy aromatic hydrocarbon raw material in the first bypass pipeline by sensing the medium temperature output by the outlet of the first shell side.
Preferably, the heavy aromatic separation tower further comprises a first tower top reflux tank, wherein the inlet of the first tower top reflux tank is communicated with the outlet of the first shell side of the first winding pipe type heat exchanger, and the bottom outlet of the first tower top reflux tank is communicated with the upper inlet of the heavy aromatic separation tower;
the flash column further comprises a second tower top reflux tank, wherein the inlet of the second tower top reflux tank is communicated with the outlet of the second shell side of the second winding tube type heat exchanger, and the bottom outlet of the second tower top reflux tank is communicated with the upper inlet of the flash column.
Further, the system also comprises a first circulating pipeline, two ends of the first circulating pipeline are respectively communicated with two interfaces at the top of the first tower top reflux tank, and a first tower top aftercooler is arranged on the first circulating pipeline;
the system also comprises a second circulating pipeline, two ends of the second circulating pipeline are respectively communicated with two interfaces at the top of the second tower top reflux tank, and a second tower top aftercooler is arranged on the second circulating pipeline.
In the above scheme, preferably, the bottom second outlet of the heavy aromatic separation column is communicated with the lower inlet of the heavy aromatic separation column through a third circulation line, and a column bottom reboiler is arranged on the third circulation line;
the bottom second outlet of the flash tower is communicated with the lower inlet of the flash tower through a fourth circulating pipeline, and a tower bottom circulating heater is arranged on the fourth circulating pipeline.
The arrangement of the reboiler outside the tower can additionally occupy the space outside the heavy aromatic separation tower, and the circulation volume of the tower bottom is limited by the installation height of the external reboiler and the pressure drop of the connecting pipeline, so that the cost is increased. And the energy consumption of the heavy aromatics separation column and reboiler investment are required to be further reduced.
Therefore, in order to further reduce the energy consumption and the investment, a tower kettle reboiler is further arranged at the lower part in the heavy aromatic separation tower.
Preferably, the tower kettle reboiler is provided with a first heat exchange tube which is spirally wound, and two ends of the second heat exchange tube are respectively used for leading heat conducting medium outside the heavy aromatic separation tower to enter and exit.
Preferably, the heavy aromatic separation tower comprises:
the tower body is internally provided with a liquid storage cavity positioned at the lower part and a gas-liquid separation cavity positioned above the liquid storage cavity, and the side wall of the gas-liquid separation cavity is provided with a feeding connecting pipe;
the first heat exchange tube is arranged in the liquid storage cavity at the lower part of the tower body along the up-down direction and is spirally wound into a plurality of layers of spiral tubes from inside to outside, and a first gap which is penetrated up and down is formed between the adjacent layers of spiral tubes;
the heavy aromatic separation tower also comprises:
the tube side inlet connecting tube for inputting the heat conducting medium is arranged on the side wall of the tower body and is communicated with the upper end tube orifice of the first heat exchange tube;
the tube side outlet connecting tube for outputting the heat conducting medium is arranged on the side wall of the tower body and is communicated with the lower end tube orifice of the first heat exchange tube.
So, locate the liquid storage intracavity of tower body lower part with first heat exchange tube, can the direct heating liquid in the liquid storage intracavity, and the liquid after the heating flows along first clearance upwards because of the density reduces, until the vapour after the boiling overflows and gets into the gas-liquid separation intracavity and carries out gas-liquid separation, and whole process can reduce the energy consumption of separator tower, and makes overall structure comparatively compact, reduce investment.
Preferably, the heavy aromatic separation tower further comprises a guide cylinder vertically arranged, the guide cylinder is sleeved on the periphery of the outermost spiral pipe, and a second gap is formed by the interval opposition between the peripheral wall of the guide cylinder and the inner peripheral wall of the tower body. Therefore, after the liquid in the guide cylinder is heated, the liquid can flow upwards along the first gap due to the density reduction, the liquid outside the guide cylinder has higher density and automatically flows downwards, and a self-circulation flow is formed.
Preferably, the upper port of the guide cylinder gradually increases from bottom to top. Thereby being beneficial to the gas-liquid two-phase diffusion to the periphery.
Preferably, the inner peripheral wall of the guide cylinder is opposite to the interval between the spiral pipes on the outermost layer, and the interval distance is consistent with the interval distance between the spiral pipes on the adjacent layer.
Further, the spiral directions of adjacent spiral pipes are opposite.
In each of the above embodiments, preferably, the multi-layer spiral pipe wound with the first heat exchange pipe is a group of heat exchange units, at least two groups of heat exchange units are circumferentially spaced apart;
the pipe orifices at the upper ends of the first heat exchange pipes of each group of heat exchange units are communicated with the pipe side inlet connecting pipes;
the lower pipe orifices of the first heat exchange pipes of each group of heat exchange units are communicated with the pipe side outlet connecting pipe.
Of course, there may be only one group of heat exchange units.
Preferably, an upper collecting pipe is arranged at a position above each group of heat exchange units in the tower body, an input port of the upper collecting pipe is communicated with the tube side inlet connecting tubes, the number of output ports of the upper collecting pipe is consistent with that of the heat exchange units, and each output port of the upper collecting pipe is communicated with an upper end pipe orifice of a first heat exchange pipe of the corresponding heat exchange unit;
the tower body is internally provided with lower collecting pipes at positions below the heat exchange units, the output ports of the lower collecting pipes are communicated with the tube side outlet connecting tubes, the number of the input ports of the lower collecting pipes is consistent with that of the heat exchange units, and each input port of the lower collecting pipes is communicated with the lower end tube orifice of the first heat exchange tube of the corresponding heat exchange unit.
More preferably, the heat exchange units have four groups and are equally spaced in the circumferential direction.
In each of the above embodiments, preferably, a bottom wall of the liquid storage chamber is provided with a condensate outlet connection pipe.
Preferably, the tube side inlet connection tube is arranged perpendicular to the side wall of the tower body.
The medium output from the outlet of the first shell side of the first wound tube heat exchanger is usually required to be supercooled, and the supercooling is usually required to be condensed and cooled in a condenser, and then is input into a liquid storage tank to carry out gas-liquid separation, the liquid after gas-liquid separation can return to the heavy aromatic separation tower again, and the noncondensable gas after gas-liquid separation is discharged. Whereas the supercooling of the medium usually requires a two-stage cooling, i.e. at least two condensers are required in series or the volume of the condensers is very large. And the existing liquid storage tank and the condenser are separately designed, so that the liquid storage tank usually needs to consider a larger gas-liquid separation space, a space for storing liquid and various connecting pipes, and the size of the liquid storage tank is huge. Therefore, the whole occupied area of the condensing equipment formed by combining the existing condensers and the liquid storage tank is large, the investment is large, and the pressure loss of the system is increased by the connecting pipeline between the two condensers and the connecting pipeline between the condensers and the liquid storage tank. Therefore, in order to achieve condensation, supercooling, gas-liquid separation, and liquid storage functions in a small space for a compact structure, it is preferable that the first wound tube heat exchanger includes:
A first shell-side cylinder extending up and down, the upper part of which is provided with a shell-side inlet as an inlet of the first shell-side and the lower end of which is opened as a first shell-side outlet;
the second heat exchange tube is axially arranged in the first shell side cylinder;
the second shell side cylinder body extends up and down, and at least the upper part of the second shell side cylinder body is sleeved on the periphery of the bottom of the first shell side cylinder body;
the condensing and supercooling piece is arranged in the second shell-side cylinder and below the first shell-side cylinder, and is provided with a condensing and supercooling channel which extends up and down, and the upper port of the condensing and supercooling channel is communicated with the first shell-side outlet of the first shell-side cylinder; the outer peripheral wall of the condensation supercooling channel is opposite to the inner peripheral wall of the second shell-side cylinder at intervals to form a third gap;
a non-condensable gas outlet is arranged on the second shell side cylinder body at a position above the condensing supercooling member;
the space, below the condensation supercooling piece, of the second shell-side cylinder body is used as a liquid storage chamber communicated with the lower port of the condensation supercooling channel, and the liquid storage chamber is communicated with a noncondensable gas outlet through the third gap;
the bottom of the second shell pass cylinder body is provided with a second shell pass outlet serving as an outlet of the first shell pass and communicated with an upper inlet of the heavy aromatic separation tower.
Therefore, the design of the second heat exchange tube can perform primary condensation on the shell side medium to be condensed, the shell side medium after primary condensation performs secondary condensation and gas-liquid separation in the condensation supercooling channel, liquid after gas-liquid separation flows into the liquid storage chamber under the action of self gravity, non-condensable gas is output from the non-condensable gas outlet through the spiral channel, and therefore the condensation, gas-liquid separation and liquid storage functions can be realized in a smaller space. In addition, the invention integrates condensation, gas-liquid separation and liquid storage into one device, and no connecting pipeline is needed to be additionally arranged. Meanwhile, the equipment of the invention is vertically installed, and brings great economic benefits to investment, occupied land, system operation cost and the like.
In order to improve the condensation and gas-liquid separation effects, preferably, the condensation supercooling channel is spirally arranged from inside to outside. Therefore, the contact area between the condensation supercooling channel and the shell side medium can be increased, and the condensation and gas-liquid separation effects are improved.
The condensation supercooling channel can be electrified for refrigeration, preferably, the condensation supercooling member is provided with a central pipe and a spiral plate, the central pipe extends up and down, the upper port of the central pipe is communicated with the lower pipe orifice of the second heat exchange pipe, and the lower port of the central pipe is closed; the spiral plate is arranged on the periphery of the central tube, two spiral plates are wound into two adjacent spiral channels clockwise or anticlockwise along the circumferential direction, wherein the first spiral channel is used as the condensation supercooling channel, the upper port and the lower port of the second spiral channel are closed, the inner port, close to the central tube, of the second spiral channel are communicated with the central tube, a first tube side inlet connecting pipe communicated with the outer port, far away from the central tube, of the second spiral channel is arranged on the side wall of the second shell side cylinder, and the first tube side inlet connecting pipe is used as the inlet of one tube side of the first winding tube type heat exchanger. Therefore, the tube side medium for condensation firstly enters the second spiral channel to condense the shell side medium in the first spiral channel, and then enters the heat exchange tube to condense the shell side medium in the first shell side cylinder, so that the shell side medium is condensed and supercooled.
To enhance the effect of the gas-liquid separation, further, the first spiral channel has a central portion relatively close to the central tube and a peripheral portion relatively far from the central tube;
the lower port of the first shell-side cylinder is opposite to and communicated with the upper port of the central part of the first spiral channel, and the periphery of the lower port of the first shell-side cylinder horizontally extends outwards to form a baffle plate covering the upper port of the peripheral part of the first spiral channel.
Thus, the liquid phase in the shell-side medium leaves the central portion of the first spiral channel, and the gas phase can flow spirally outward to the peripheral portion, then enters the gap and is discharged from the noncondensable gas outlet.
Preferably, a portion of the baffle relatively remote from the non-condensable gas outlet extends outwardly to the inner peripheral wall of the second shell-side barrel. Thus, the noncondensable gas can flow to the noncondensable gas outlet in a concentrated way.
Further, the lower end part of the first shell side cylinder body is in a reverse cone shape.
Further, a sidewall of the reverse taper is opposite the non-condensable gas outlet. Thus, the non-condensable gas can be accelerated to flow out.
In each of the above schemes, preferably, a first liquid level gauge and a second liquid level gauge are arranged on the side wall of the second shell side cylinder, the first liquid level gauge is arranged corresponding to the central part of the condensation supercooling channel in the up-down direction, and the second liquid level gauge is positioned below the condensation supercooling channel and above the second shell side outlet.
Preferably, the side wall of the second shell-side cylinder is provided with a pressure gauge port for detecting the system pressure, and the pressure gauge port is positioned above the non-condensable gas outlet.
Compared with the prior art, the invention has the advantages that: the heat of the gas phase at the top of the heavy aromatic separation tower and the flash evaporation tower is recovered by arranging the first winding pipe type heat exchanger and the second winding pipe type heat exchanger without arranging an air cooler; the first winding tube type heat exchanger is low in pressure drop and low in vacuum, and the heat exchange is carried out in a grading temperature-dividing mode, and meanwhile, the integration of heat exchangers with different diameters is realized;
in the invention, the heavy aromatic separation tower adopts negative pressure operation, reduces the vaporization temperature of the feed, adopts high feed vaporization rate, provides 70% of heat during the feed, and only provides 30% of heat by the reboiler at the bottom of the tower;
the flash tower adopts full vacuum operation, the tower feed adopts high gasification rate, 100% of heat of the tower operation is provided at the feed position, the tower bottom circulating heater is only used as standby, and the flash tower is used when the second heater is not heated enough;
the two towers, namely the heavy aromatic separation tower and the flash distillation tower, are respectively from materials of the device or nearby devices, heat transfer does not exist, the device belongs to primary heat utilization, and the device is different from conventional low-temperature heat recovery, utilizes hot water to take heat and then supplies the heat of the hot water to other devices, so that energy loss exists;
The heat utilization rate of the system of the invention reaches more than 95 percent.
Drawings
FIG. 1 is a schematic diagram of a first embodiment of the present invention;
fig. 2 is an enlarged view of a portion a in fig. 1;
FIG. 3 is an enlarged view of portion B of FIG. 1;
FIG. 4 is a schematic diagram of a heavy aromatic separation column according to a second embodiment of the present invention;
FIG. 5 is a schematic diagram showing a partial structure of a heavy aromatic separation column according to a third embodiment of the present invention;
FIG. 6 is a top view of FIG. 5;
FIG. 7 is a use state diagram of FIG. 5;
FIG. 8 is a schematic diagram of a single heat exchange unit according to a third embodiment of the present invention;
FIG. 9 is a schematic view showing a partial structure of each layer of spiral pipe in the third embodiment of the present invention;
FIG. 10 is a schematic diagram showing a partial structure of a medium-heavy aromatics separation column according to a fourth embodiment of the present invention;
FIG. 11 is a use state diagram of FIG. 10;
FIG. 12 is a schematic diagram of a fifth embodiment of the present invention;
fig. 13 is an enlarged view of a portion C in fig. 12;
fig. 14 is an enlarged view of the portion D in fig. 12;
fig. 15 is a schematic view showing a partial structure of a first wound tube heat exchanger in a fifth embodiment of the present invention;
fig. 16 is an enlarged view of a partial structure of fig. 15.
Detailed Description
The invention is described in further detail below with reference to the embodiments of the drawings.
Embodiment one:
as shown in fig. 1 to 3, which are a preferred embodiment of a system for heavy aromatics separation according to the present invention, the system includes a first coiled tube heat exchanger 100, a heavy aromatics separation column 200, a flash column 300, and a second coiled tube heat exchanger 400.
The first wound tube heat exchanger 100 is arranged vertically, and has a first shell side 101 and three tube sides. The inlet at the top of the first shell side 101 is in communication with the top outlet of the heavy aromatics separation column 200, the outlet at the bottom of the first shell side 101 is in communication with the inlet of the downstream first overhead reflux drum 500, and the bottom outlet of the first overhead reflux drum 500 is in communication with the upper inlet of the heavy aromatics separation column 200. The system also comprises a first circulation pipeline 501, two ends of the first circulation pipeline 501 are respectively communicated with two interfaces at the top of the first tower top reflux tank 500, and a first tower top aftercooler 502 is arranged on the first circulation pipeline 501. The first overhead aftercooler 502 is a heat exchanger and the cooling medium is circulating water to heat the circulating water.
The three tube passes of the first wound tube heat exchanger 100 are respectively a first tube pass 102, a second tube pass 103 and a third tube pass 104, and the first tube pass 102, the third tube pass 104 and the second tube pass 103 are sequentially arranged along the direction from the inlet to the outlet (i.e. the direction from top to bottom) of the shell pass medium from the first shell pass 101. And the inlet of the first tube side 102 supplies hot water input, and the outlet of the first tube side 102 supplies steam output. The inlet of the second tube side 103 is used for inputting heavy aromatic hydrocarbon raw materials, and the outlet of the second tube side 103 is used for outputting heated heavy aromatic hydrocarbon raw materials. The inlet of the third tube side 104 is for the input of a medium (which may be from an adjacent device) having a temperature of 40 ℃. The outlet of the third tube side 104 is used for being communicated with downstream equipment, and the temperature of the medium output by the outlet of the third tube side 104 is 130 ℃.
The second wound tube heat exchanger 400 is laid flat and has a second shell side 401, eight tube sides, the inlet of the second shell side 401 is communicated with the top outlet of the flash column 300, the outlet of the second shell side 401 is communicated with the inlet of the downstream second overhead reflux drum 510, and the bottom outlet of the second overhead reflux drum 510 is communicated with the upper inlet of the flash column 300. And a second circulation pipeline 511, two ends of which are respectively communicated with two interfaces at the top of the second tower top reflux tank 510, wherein a second tower top aftercooler 512 is arranged on the second circulation pipeline 511. The second overhead aftercooler 512 is a heat exchanger and the cooling medium is circulating water to heat the circulating water.
One of the eight tube passes of the second coiled tube heat exchanger 400 is a fourth tube pass 402, the fourth tube pass 402 is closest to the inlet of the second shell pass 401 relative to the other seven tube passes, and the inlet of the fourth tube pass 402 is communicated with the outlet of the second tube pass 103 of the first coiled tube heat exchanger 100; the outlet of the fourth pipeline 402 is communicated with the middle inlet of the heavy aromatic separation tower 200 through a first pipeline 403, and a first heater 404 is arranged on the first pipeline 403; along the direction from the inlet to the outlet of the second shell pass 401, the other seven tube passes are distributed in sequence and are respectively supplied with heavy C9 with the temperature of 40 ℃, medium I with the temperature of 40 ℃, medium II with the temperature of 40 ℃, medium III with the temperature of 40 ℃, medium IV with the temperature of 40 ℃, medium five with the temperature of 40 ℃ and medium six with the temperature of 40 ℃ for input. The temperature of the heavy C9 after heat exchange is 115 ℃, the temperature of the medium I after heat exchange is 115 ℃, the temperature of the medium II after heat exchange is 100 ℃, the temperature of the medium III after heat exchange is 100 ℃, the temperature of the medium IV after heat exchange is 100 ℃, the temperature of the medium V after heat exchange is 85 ℃, and the temperature of the medium VI after heat exchange is 65 ℃. The heavy C9 and the medium one to medium six may be from adjacent devices.
Also included is a first bypass line 105 having an inlet for the input of heavy aromatic feedstock and an outlet in communication with the inlet of the fourth tube pass 402 of the second coiled tube heat exchanger 400; and a first thermo valve 106 is provided on the first bypass line 105, the first thermo valve 106 being arranged to be able to adjust the flow of heavy aromatic feedstock in the first bypass line 105 by sensing the temperature of the medium output from the outlet of the first shell side 101. Under normal working conditions, all heavy aromatic hydrocarbon raw materials go through the first bypass pipeline 105 and do not participate in heat exchange, when the top condensation temperature of the first top reflux tank 500 does not reach the standard, the bypass opening is reduced, so that part of heavy aromatic hydrocarbon raw materials participate in heat exchange, and the condensate temperature is maintained to be not higher than 80 ℃.
The first outlet at the bottom of the heavy aromatic separation column 200 is communicated with the inlet at the middle part of the flash column 300 through a second pipeline 301, and a second heater 302 is arranged on the second pipeline 301.
The second outlet at the bottom of the heavy aromatic separation column 200 is communicated with the inlet at the lower part of the heavy aromatic separation column 200 through a third circulation pipeline 201, and a column bottom reboiler 202 is arranged on the third circulation pipeline; the bottom second outlet of the flash column 300 is connected to the lower inlet of the flash column 300 through a fourth circulation line 303, and a bottom circulation heater 304 is provided on the fourth circulation line. And the bottom of the flash column 300 has a product outlet.
In this embodiment, the first heater 404, the second heater 302, the tower reboiler 202, and the bottom circulation heater 304 are all wound tube heat exchangers, and heat medium of the wound tube heat exchangers adopts heat transfer oil. And the second heater 302 adopts a winding pipe type heat exchanger, so that the feed gasification rate of the flash tower 300 can be improved to the greatest extent.
The heat exchange process of this embodiment is as follows:
the process of the C9 raw material separation optimizing project mainly comprises a feeding and normal pressure separation part and a decompression separation part.
The heavy aromatic hydrocarbon raw material in the tank area is conveyed to the second tube side 103 of the first winding tube type heat exchanger 100, exchanges heat with the tower top gas output from the top of the heavy aromatic hydrocarbon separation tower 200, and then enters the fourth tube side 402 of the second winding tube type heat exchanger 400 to exchange heat, and is heated by the first heater 404 and then enters the heavy aromatic hydrocarbon separation tower 200.
The heavy aromatic separation tower 200 is operated by micro negative pressure, and the top gas output from the top of the heavy aromatic separation tower passes through the first tube pass 102 of the first winding tube type heat exchanger 100, heats water in the first tube pass 102 into steam, and then is cooled by the third tube pass 104 and the second tube pass 103 of the first winding tube type heat exchanger 100 and then goes to the first top reflux tank 500. The medium output from the bottom outlet of the first tower top reflux tank 500 is pressurized by the tower top extraction pump and then is divided into two paths, one path is used as the tower top reflux and returns to the heavy aromatic separation tower 200, and the other path is used as the product JQ-1 for delivery after being cooled by the air cooler. The gas phase medium output from the top outlet of the first tower top reflux drum 500 is connected to the first tower top aftercooler 502 and cooled by circulating water. The first overhead aftercooler 502 employs split control, nitrogen is introduced and vented to the flare, leaving the vacuum pump-out process.
The tower bottom circulating liquid output from the second outlet at the bottom of the heavy aromatic separation tower 200 enters the tower bottom reboiler 202 through the tower bottom circulating pump and then returns to the tower, and heat source is provided by heat conduction oil.
The bottom liquid output from the first outlet at the bottom of the heavy aromatic separation column 200 is conveyed to the second heater 302 by the column bottom extraction pump and then enters the flash column 300 after being heated. The flash column 300 is operated with a negative pressure. The top gas output from the top outlet of the flash tower 300 is cooled by heat exchange through a second winding tube type heat exchanger 400 and then goes to a second top reflux tank 510, the medium output from the bottom outlet of the second top reflux tank 510 is pressurized through a top extraction pump and then is divided into two paths, one path is used as top reflux and returns to the flash tower 300, the other path is used for cooling heavy aromatic hydrocarbon output from the first outlet at the bottom of the flash tower 300 through a heavy aromatic hydrocarbon/JQ-5 heat exchanger (the heavy aromatic hydrocarbon output from the first outlet at the bottom of the flash tower 300 is output after heat exchange), and the heavy aromatic hydrocarbon is cooled through an air cooler and then is used as a product JQ-5 to be sent out. The gas phase medium output from the top outlet of the second tower top reflux drum 510 is connected to a second tower top aftercooler 512, and cooled by circulating water. The top gas phase of the second overhead aftercooler 512 is connected to a vacuum pump.
The bottom circulation liquid output from the second outlet at the bottom of the flash tower 300 enters the bottom circulation heater 304 through the bottom circulation pump and returns to the tower, and heat conduction oil provides a heat source.
In this embodiment, the heavy aromatic separation column 200 adopts a slight negative pressure operation, so as to reduce the temperature of the feed, reduce the use temperature of the heat transfer oil, reduce the operation load of the column, the recovery rate at the top of the column is 45/72=62.5%, the recovery rate at the bottom of the column is 39/72= 54.17%, and the reflux ratio is controlled to be r=12/33= 0.3636.
The flash column 300 is operated in high vacuum, reducing the column operating temperature and the column feed temperature, reducing the use temperature of the heat transfer oil, and reducing the column operating load. The tower top extraction rate is 39/39=100%, the tower bottom is 3/39=7.7%, and the reflux ratio is controlled to be R=3/36=0.083.
In addition, the embodiment utilizes the winding tube type heat exchanger to realize low-temperature difference heat exchange, so that the temperature of a heating medium can be reduced, and the conventional 300 ℃ heat conduction oil system of engineering can meet the heating requirement, and the heat conduction medium is safe and reliable.
Embodiment two:
as shown in fig. 4, a second preferred embodiment of a system for heavy aromatic separation according to the present invention is basically the same as the first preferred embodiment, except that in this preferred embodiment, the bottom reboiler 202 is disposed at a lower position in the heavy aromatic separation column 200, and the bottom reboiler 202 has a first heat exchange tube 220 spirally wound, and two ends of the first heat exchange tube 220 are respectively supplied with a heat transfer medium outside the heavy aromatic separation column 200.
Embodiment III:
as shown in fig. 5 to 9, a third preferred embodiment of a system for heavy aromatics separation according to the present invention is basically the same as the second embodiment, except that the heavy aromatics separation column 200 in this embodiment includes a column body 210, a first heat exchange tube 220, a tube side inlet connection tube 230, a tube side outlet connection tube 240, and a guide tube 250.
The tower body 210 is internally provided with a liquid storage cavity 211 positioned at the lower part and a gas-liquid separation cavity 212 positioned above the liquid storage cavity 211, the gas-liquid separation cavity 212 is directly communicated with the liquid storage cavity 211, and a gas-liquid separation tower plate is arranged in the gas-liquid separation cavity 212 and is of the prior art and is not described herein. And a feeding connecting pipe 213 is arranged on the side wall of the gas-liquid separation cavity 212 at a position close to the liquid storage cavity 211. The bottom wall of the liquid storage cavity 211 is provided with a condensate outlet connection pipe 214.
The tube side inlet connection pipe 230 is used for inputting heat-conducting medium, and is disposed on the sidewall of the gas-liquid separation chamber 212 of the tower 210 near the liquid storage chamber 211, and the tube side inlet connection pipe 230 is disposed perpendicular to the sidewall of the tower 210.
The tube side outlet connection tube 240 is used for outputting heat conducting medium and is arranged on the side wall of the bottom of the liquid storage cavity 211 of the tower body 210.
The first heat exchange tube 220 is disposed in the liquid storage cavity 211 at the lower portion of the tower 210 along the up-down direction, and spirally winds into a plurality of spiral pipes 221 from inside to outside, the spiral directions of the adjacent spiral pipes 221 are opposite, and a first gap 222 penetrating up and down is formed between the adjacent spiral pipes 221, as shown in fig. 9. The guide cylinder 250 is vertically disposed and sleeved on the outer periphery of the outermost spiral pipe 221, and the inner peripheral wall of the guide cylinder 250 is spaced from the outermost spiral pipe 221 by a distance consistent with the distance between adjacent spiral pipes 221. Meanwhile, the upper port of the guide cylinder 250 gradually increases from bottom to top.
In this embodiment, the plurality of spiral pipes 221 and the corresponding guide cylinders 250 wound by the first heat exchange pipe 220 are four groups of heat exchange units, which are circumferentially arranged in the liquid storage chamber 211 at equal intervals, and a second gap 251 is formed between a part of the outer peripheral wall of the guide cylinder 250 of each group of heat exchange units and the inner peripheral wall of the tower 210. The upper pipe orifices of the first heat exchange pipes 220 of each group of heat exchange units are communicated with the pipe inlet connecting pipe 230; the lower pipe orifices of the first heat exchange pipes 220 of each group of heat exchange units are communicated with the pipe side outlet connection pipe 240. Specifically, an upper collecting pipe 260 is disposed in the tower body 210 above each group of heat exchange units, an input port of the upper collecting pipe 260 is communicated with the tube side inlet connection tube 230, four output ports of the upper collecting pipe 260 are provided, and each output port is communicated with an upper end tube orifice of the first heat exchange tube 220 of the corresponding heat exchange unit. The tower body 210 is provided with a lower collecting pipe 270 at a position below each group of heat exchange units, the output port of the lower collecting pipe 270 is communicated with the tube side outlet connecting pipe 240, four input ports of the lower collecting pipe 270 are provided, and each input port is communicated with the lower end pipe orifice of the first heat exchange tube 220 of the corresponding heat exchange unit.
In this way, under the action of the heat-conducting medium in the first heat exchange tube 220, the liquid in the guide cylinder 250 can flow upwards along the first gap 222 due to the density reduction after being heated until the boiled gas overflows and enters the gas-liquid separation cavity 212 to perform gas-liquid separation, and the liquid outside the guide cylinder 250 has higher density and automatically flows downwards to form a self-circulation flow. See in particular fig. 7.
Embodiment four:
as shown in fig. 10 and 11, which are a preferred embodiment of a system for heavy aromatics separation according to the present invention, this embodiment is basically the same as the third embodiment, except that there is only one group of heat exchange units in this embodiment, and the upper pipe orifice of the first heat exchange pipe 220 in this group of heat exchange units is directly connected to the pipe side inlet connection pipe 230, and the lower pipe orifice is directly connected to the pipe side outlet connection pipe 240.
Fifth embodiment:
as shown in fig. 12 to 16, a fifth preferred embodiment of a system for heavy aromatic separation according to the present invention is basically the same as the first embodiment, except that the first overhead reflux drum 500, the first overhead aftercooler 502, the second overhead reflux drum 510, and the second overhead aftercooler 512 are not required to be additionally provided in the present embodiment. Specifically, the first wound tube heat exchanger 100 of the present embodiment includes a first shell-side cylinder 110, a second heat exchange tube 120, a second shell-side cylinder 130, and a condensing subcooler 140.
The first shell-side cylinder 110 extends up and down, and has a shell-side inlet 111 at its upper end as an inlet of the first shell-side 101 and an open lower end as a first shell-side outlet 112. And the lower end of the first shell-side cylinder 110 has a reverse taper.
The second heat exchange tube 120 is axially disposed in the first shell side cylinder 110;
the second shell-side cylinder 130 extends up and down, and at least an upper portion thereof is sleeved on the outer periphery of the bottom of the first shell-side cylinder 110. A noncondensable gas outlet 132 is provided in the sidewall of the second shell-side cylinder 130 at a position corresponding to the reverse taper of the lower end of the first shell-side cylinder 110. The space at the lower portion of the second shell-side cylinder 130 serves as a liquid reservoir 133. The bottom of the second shell-side cylinder 130 is provided with a second shell-side outlet 135 as an outlet of the first shell-side 101 and communicates with the upper inlet of the heavy aromatics separation column 200.
The condensing and supercooling member 140 is disposed in the second shell-side cylinder 130, below the first shell-side cylinder 110, and above the liquid storage chamber 133, the condensing and supercooling member 140 has a condensing and supercooling channel 141 extending up and down, and an upper port of the condensing and supercooling channel 141 is communicated with the first shell-side outlet 112 of the first shell-side cylinder 110; the lower port of the condensing supercooling channel 141 communicates with the liquid storage chamber 133; the outer circumferential wall of the condensing and supercooling channel 141 is formed with a third gap 131 spaced opposite to the inner circumferential wall of the second shell-side cylinder 130, so that the liquid storage chamber 133 communicates with the non-condensable gas outlet 132 through the third gap 131.
In this embodiment, the condensing supercooling member 140 has a central tube 142 and a spiral plate 143, the central tube 142 extends up and down, and an upper port of the central tube 142 is communicated with a lower end nozzle of the second heat exchange tube 120, and a lower port of the central tube 142 is closed; the spiral plate 143 is disposed at the outer periphery of the central tube 142, and the spiral plate 143 has two adjacent spiral passages spirally disposed from inside to outside and is wound clockwise or counterclockwise in the circumferential direction, wherein a first spiral passage 1431 serves as the above-mentioned condensation supercooling passage 141, and the first spiral passage 1431 has a central portion relatively close to the central tube 142 and a peripheral portion relatively far from the central tube 142; the upper port of the central portion of the first spiral channel 1431 is opposite to and communicates with the lower port of the first shell-side cylinder 110, and the peripheral edge of the lower port of the first shell-side cylinder 110 extends horizontally outwardly to form a baffle 114 covering the upper port of the peripheral portion of the first spiral channel 1431. A portion of the baffle 114 relatively remote from the non-condensable gas outlet 132 extends outwardly to the inner peripheral wall of the second shell-side cylinder 130.
The upper and lower ports of the second spiral channel 1432 are closed, and the inner port of the second spiral channel 1432 close to the central tube 142 is communicated with the central tube 142, and a first tube side inlet connection tube 134 communicated with the outer port of the second spiral channel 1432 far from the central tube 142 is arranged on the side wall of the second shell side cylinder 130, and the first tube side inlet connection tube 134 is used as an inlet of one tube side of the first wound tube heat exchanger 100.
That is, the tube side medium enters the second spiral channel 1432 through the first tube side inlet connecting tube 134, flows to the central tube 142 from outside to inside in a spiral manner, flows into the second heat exchange tube 120, exchanges heat with the shell side medium in the first shell side cylinder 110, and is output.
The shell side medium is fed into the first shell side cylinder 110 through the shell side inlet 111, then flows downward and enters the first spiral channel 1431, exchanges heat with the tube side medium in the second spiral channel 1432, stores the liquid phase in the liquid storage chamber 133, and flows upward and is discharged from the non-condensable gas outlet 132.
Meanwhile, the side wall of the second shell-side cylinder 130 is provided with a first liquid level meter 136 and a second liquid level meter 137, the first liquid level meter 136 is arranged corresponding to the central part of the condensation supercooling channel 141 in the up-down direction, the second liquid level meter 137 is positioned below the condensation supercooling channel 141 and above the second shell-side outlet 135 so as to monitor the liquid level in the liquid storage chamber 133, the highest liquid level in the liquid storage chamber 133 is not more than 10% of the width of the spiral plate 143 in the up-down direction, and the lowest liquid level is positioned between the first liquid level meter 136 and the second liquid level meter 137, specifically, as shown by a two-dot chain line in fig. 15, the two-dot chain line positioned at the upper side refers to the highest liquid level point, and the two-dot chain line positioned at the lower side refers to the lowest liquid level point.
The side wall of the second shell-side cylinder 130 is provided with a pressure gauge port 138 for sensing the system pressure, which is located above the non-condensable gas outlet 132.
The structure of the second coiled tube heat exchanger 400 in this embodiment refers to the structural design of the first coiled tube heat exchanger 100, and will not be described herein.
In the description and claims of the present invention, terms indicating directions, such as "front", "rear", "upper", "lower", "left", "right", "side", "top", "bottom", etc., are used to describe various example structural parts and elements of the present invention, but these terms are used herein for convenience of description only and are determined based on the example orientations shown in the drawings. Because the disclosed embodiments of the invention may be arranged in a variety of orientations, the directional terminology is used for purposes of illustration and is in no way limiting, such as "upper" and "lower" are not necessarily limited to being in a direction opposite or coincident with the direction of gravity.
Claims (26)
1. A system for heavy aromatics separation comprising a heavy aromatics separation column (200) and a flash column (300), the flash column (300) having a product outlet at the bottom thereof;
it is characterized in that the method also comprises the following steps:
The device comprises a first winding tube type heat exchanger (100) with a first shell side (101) and at least two tube sides, wherein an inlet of the first shell side (101) is communicated with a top outlet of a heavy aromatic hydrocarbon separation tower (200), an outlet of the first shell side (101) is communicated to the downstream, the two tube sides are respectively a first tube side (102) and a second tube side (103), the first tube side (102) is positioned at the upstream of the second tube side (103) along the direction from the inlet to the outlet of a shell side medium of the first shell side (101), the inlet of the first tube side (102) is used for supplying hot water, the outlet of the first tube side (102) is used for outputting steam, and the inlet of the second tube side (103) is used for supplying heavy aromatic hydrocarbon raw materials;
a second wound tube heat exchanger (400) having a second shell side (401), at least a fourth tube side (402), the inlet of the second shell side (401) being in communication with the top outlet of the flash column (300), the outlet of the second shell side (401) being in communication downstream, the inlet of the fourth tube side (402) being in communication with the outlet of the second tube side (103) of the first wound tube heat exchanger (100); the outlet of the fourth tube pass (402) is communicated with the middle inlet of the heavy aromatic separation tower (200) through a first pipeline (403), and a first heater (404) is arranged on the first pipeline (403);
The first outlet at the bottom of the heavy aromatic separation tower (200) is communicated with the middle inlet of the flash tower (300) through a second pipeline (301), and a second heater (302) is arranged on the second pipeline (301).
2. The system according to claim 1, wherein: the first wound tube heat exchanger (100) also has a third tube pass (104), along the direction of the shell-side medium from the inlet to the outlet of the first shell pass (101), the third tube pass (104) being located downstream of the first tube pass (102) and upstream of the second tube pass (103).
3. The system according to claim 1, wherein: also included is a first bypass line (105) having an inlet for the heavy aromatic feedstock and an outlet in communication with the inlet of the fourth tube pass (402) of the second coiled tube heat exchanger (400); and a first temperature control valve (106) is arranged on the first bypass pipeline (105), and the first temperature control valve (106) is arranged to be capable of adjusting the flow of heavy aromatic hydrocarbon raw material in the first bypass pipeline (105) by sensing the medium temperature output by the outlet of the first shell side (101).
4. The system according to claim 1, wherein: the system also comprises a first tower top reflux tank (500), wherein the inlet of the first tower top reflux tank is communicated with the outlet of the first shell side (101) of the first winding pipe type heat exchanger (100), and the bottom outlet of the first tower top reflux tank is communicated with the upper inlet of the heavy aromatic separation tower (200);
Also included is a second overhead reflux drum (510) having an inlet in communication with the outlet of the second shell side (401) of the second wound tube heat exchanger (400) and a bottom outlet in communication with the upper inlet of the flash column (300).
5. The system according to claim 4, wherein: the system also comprises a first circulating pipeline (501), wherein two ends of the first circulating pipeline are respectively communicated with two interfaces at the top of the first tower top reflux tank (500), and a first tower top aftercooler (502) is arranged on the first circulating pipeline (501);
the system also comprises a second circulation pipeline (511), two ends of the second circulation pipeline are respectively communicated with two interfaces at the top of the second tower top reflux tank (510), and a second tower top aftercooler (512) is arranged on the second circulation pipeline (511).
6. The system according to claim 1, wherein: the second outlet at the bottom of the heavy aromatic separation tower (200) is communicated with the inlet at the lower part of the heavy aromatic separation tower (200) through a third circulating pipeline (201), and a tower kettle reboiler (202) is arranged on the third circulating pipeline;
the bottom second outlet of the flash column (300) is communicated with the lower inlet of the flash column (300) through a fourth circulating pipeline (303), and a tower bottom circulating heater (304) is arranged on the fourth circulating pipeline.
7. The system according to claim 1, wherein: and a tower kettle reboiler (202) is arranged at the lower part in the heavy aromatic separation tower (200).
8. The system according to claim 7, wherein: the tower kettle reboiler (202) is provided with a first heat exchange tube (220) which is spirally wound, and two ends of the first heat exchange tube (220) are respectively used for leading heat conducting media outside the heavy aromatic separation tower (200) to enter and exit.
9. The system according to claim 8, wherein: the heavy aromatic separation tower (200) comprises:
the tower body (210) is internally provided with a liquid storage cavity (211) positioned at the lower part and a gas-liquid separation cavity (212) positioned above the liquid storage cavity (211), and the side wall of the gas-liquid separation cavity (212) is provided with a feeding connecting pipe (213);
the first heat exchange tube (220) is arranged in a liquid storage cavity (211) at the lower part of the tower body (210) along the up-down direction, and is spirally wound into a plurality of layers of spiral tubes (221) from inside to outside, and a first gap (222) which is vertically penetrated is formed between the adjacent layers of spiral tubes (221);
the heavy aromatic separation tower also comprises:
the tube side inlet connecting tube (230) for inputting the heat conducting medium is arranged on the side wall of the tower body (210) and is communicated with the upper end tube orifice of the first heat exchange tube (220);
The tube side outlet connecting tube (240) for outputting the heat conducting medium is arranged on the side wall of the tower body (210) and is communicated with the lower end tube orifice of the first heat exchange tube (220).
10. The system according to claim 9, wherein: the heavy aromatic separation tower further comprises a guide cylinder (250) which is vertically arranged and sleeved on the periphery of the outermost spiral pipe (221), and a second gap (251) is formed by the opposite interval between the peripheral wall of the guide cylinder (250) and the inner peripheral wall of the tower body (210).
11. The system according to claim 10, wherein: the upper port of the guide cylinder (250) is gradually increased from bottom to top.
12. The system according to claim 10, wherein: the inner peripheral wall of the guide cylinder (250) is opposite to the interval between the spiral pipes (221) at the outermost layer, and the interval distance is consistent with the interval distance between the spiral pipes (221) at the adjacent layer.
13. The system according to claim 9, wherein: the spiral directions of adjacent spiral pipes (221) are opposite.
14. The system according to any one of claims 9 to 13, wherein: the multi-layer spiral tube (221) wound by the first heat exchange tube (220) is a group of heat exchange units, at least two groups of heat exchange units are arranged at intervals along the circumferential direction;
The upper pipe orifices of the first heat exchange pipes (220) of each group of heat exchange units are communicated with the pipe side inlet connecting pipe (230);
the lower pipe orifices of the first heat exchange pipes (220) of each group of heat exchange units are communicated with the pipe side outlet connecting pipe (240).
15. The system according to claim 14, wherein: an upper collecting pipe (260) is arranged at a position above each group of heat exchange units in the tower body (210), an input port of the upper collecting pipe (260) is communicated with the tube side inlet connecting tube (230), the number of output ports of the upper collecting pipe (260) is consistent with that of the heat exchange units, and each output port of the upper collecting pipe (260) is communicated with an upper end tube orifice of a first heat exchange tube (220) of the corresponding heat exchange unit;
the tower body (210) is internally provided with lower collecting pipes (270) at positions below the heat exchange units, the output ports of the lower collecting pipes (270) are communicated with the tube side outlet connecting tubes (240), the number of input ports of the lower collecting pipes (270) is consistent with that of the heat exchange units, and each input port of the lower collecting pipes (270) is communicated with the lower end tube ports of the first heat exchange tubes (220) of the corresponding heat exchange units.
16. The system according to claim 14, wherein: the heat exchange units are four groups and are arranged at equal intervals along the circumferential direction.
17. The system according to any one of claims 9 to 13, wherein: the bottom wall of the liquid storage cavity (211) is provided with a condensate outlet connecting pipe (214).
18. The system according to any one of claims 9 to 13, wherein: the tube side inlet nipple (230) is arranged perpendicular to the side wall of the tower body (210).
19. The system according to claim 1, wherein: the first winding tube type heat exchanger comprises:
a first shell-side cylinder (110) extending up and down, the upper part of which has a shell-side inlet (111) as the inlet of the first shell-side and the lower end of which is opened as a first shell-side outlet (112);
the second heat exchange tube (120) is axially arranged in the first shell side cylinder (110);
a second shell-side cylinder (130) extending up and down, at least the upper part of which is sleeved on the periphery of the bottom of the first shell-side cylinder (110);
the condensation supercooling piece (140) is arranged in the second shell-side barrel (130) and below the first shell-side barrel (110), the condensation supercooling piece (140) is provided with a condensation supercooling channel (141) extending up and down, and the upper port of the condensation supercooling channel (141) is communicated with the first shell-side outlet (112) of the first shell-side barrel (110); a third gap (131) is formed between the outer peripheral wall of the condensation supercooling channel (141) and the inner peripheral wall of the second shell-side cylinder (130);
A noncondensable gas outlet (132) is arranged on the second shell-side cylinder (130) and above the condensation supercooling piece (140);
the space of the second shell-side cylinder (130) below the condensation supercooling member (140) is used as a liquid storage chamber (133) communicated with the lower port of the condensation supercooling channel (141), and the liquid storage chamber (133) is communicated with the noncondensable gas outlet (132) through the third gap (131);
the bottom of the second shell-side cylinder (130) is provided with a second shell-side outlet (135) serving as an outlet of the first shell-side and communicated with an upper inlet of the heavy aromatic separation tower.
20. The system according to claim 19, wherein: the condensation supercooling channel (141) is spirally arranged from inside to outside.
21. The system according to claim 19, wherein: the condensation supercooling piece (140) is provided with a central pipe (142) and a spiral plate (143), the central pipe (142) extends up and down, the upper port of the central pipe (142) is communicated with the lower pipe orifice of the second heat exchange pipe (120), and the lower port of the central pipe (142) is closed; the spiral plate (143) is arranged on the periphery of the central tube (142), the spiral plate (143) is provided with two adjacent spiral channels which are rolled clockwise or anticlockwise along the circumferential direction, a first spiral channel (1431) is used as the condensation supercooling channel (141), the upper port and the lower port of a second spiral channel (1432) are closed, the inner port of the second spiral channel (1432) close to the central tube (142) is communicated with the central tube (142), a first tube side inlet connecting pipe (134) communicated with the outer port of the second spiral channel (1432) far away from the central tube (142) is arranged on the side wall of the second shell side barrel (130), and the first tube side inlet connecting pipe (134) is used as the inlet of one tube side of the first winding tube type heat exchanger.
22. The system according to claim 21, wherein: the first helical channel (1431) having a central portion relatively close to the central tube (142) and a peripheral portion relatively far from the central tube (142);
the lower port of the first shell-side cylinder (110) is opposite to and communicates with the upper port of the central portion of the first spiral channel (1431), and the periphery of the lower port of the first shell-side cylinder (110) extends horizontally outward to form a baffle (114) covering the upper port of the peripheral portion of the first spiral channel (1431).
23. The system according to claim 22, wherein: a portion of the baffle (114) relatively remote from the non-condensable gas outlet (132) extends outwardly to an inner peripheral wall of the second shell-side barrel (130).
24. The system according to claim 22, wherein: the lower end of the first shell side cylinder (110) is in a reverse cone shape.
25. The system according to claim 24, wherein: the side wall of the inverted cone is opposite the non-condensable gas outlet (132).
26. The system according to any one of claims 19 to 25, wherein: the side wall of the second shell side cylinder body (130) is provided with a first liquid level meter (136) and a second liquid level meter (137), the first liquid level meter (136) is arranged corresponding to the central part of the condensation supercooling channel (141) in the up-down direction, and the second liquid level meter (137) is positioned below the condensation supercooling channel (141) and above the second shell side outlet (135).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310762887.7A CN116875340A (en) | 2023-06-26 | 2023-06-26 | System for be used for heavy aromatic separation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310762887.7A CN116875340A (en) | 2023-06-26 | 2023-06-26 | System for be used for heavy aromatic separation |
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| CN116875340A true CN116875340A (en) | 2023-10-13 |
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| CN202310762887.7A Pending CN116875340A (en) | 2023-06-26 | 2023-06-26 | System for be used for heavy aromatic separation |
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| CN (1) | CN116875340A (en) |
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