CN116751613A - Energy-saving negative pressure debenzolization process and system - Google Patents
Energy-saving negative pressure debenzolization process and system Download PDFInfo
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- CN116751613A CN116751613A CN202310603930.5A CN202310603930A CN116751613A CN 116751613 A CN116751613 A CN 116751613A CN 202310603930 A CN202310603930 A CN 202310603930A CN 116751613 A CN116751613 A CN 116751613A
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- 238000000034 method Methods 0.000 title claims abstract description 61
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 663
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 159
- 238000000926 separation method Methods 0.000 claims abstract description 66
- 239000007788 liquid Substances 0.000 claims abstract description 42
- 230000000630 rising effect Effects 0.000 claims abstract description 14
- 239000012071 phase Substances 0.000 claims description 36
- 238000005406 washing Methods 0.000 claims description 33
- 238000010992 reflux Methods 0.000 claims description 22
- 230000008929 regeneration Effects 0.000 claims description 16
- 238000011069 regeneration method Methods 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 15
- 239000010865 sewage Substances 0.000 claims description 11
- 239000007791 liquid phase Substances 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 10
- 238000005191 phase separation Methods 0.000 claims description 7
- 238000001704 evaporation Methods 0.000 claims description 5
- 230000008020 evaporation Effects 0.000 claims description 5
- 230000006837 decompression Effects 0.000 claims description 4
- 239000002351 wastewater Substances 0.000 abstract description 12
- 230000008901 benefit Effects 0.000 abstract description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 230000007547 defect Effects 0.000 abstract description 2
- 230000000694 effects Effects 0.000 abstract description 2
- 230000018044 dehydration Effects 0.000 abstract 1
- 238000006297 dehydration reaction Methods 0.000 abstract 1
- 238000004939 coking Methods 0.000 description 8
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 description 3
- 150000001555 benzenes Chemical class 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 230000006866 deterioration Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- QXJACNQZKMBMJY-UHFFFAOYSA-N phenol cyanide Chemical compound N#[C-].OC1=CC=CC=C1 QXJACNQZKMBMJY-UHFFFAOYSA-N 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
- C10K1/18—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids hydrocarbon oils
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
- B01D17/02—Separation of non-miscible liquids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1412—Controlling the absorption process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1487—Removing organic compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
- B01D2257/7027—Aromatic hydrocarbons
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention relates to an energy-saving negative pressure debenzolization process and system, wherein the system comprises a debenzolization tower, an evaporator, a steam superheater, a lean oil regenerator, an oil-rich heater, a crude benzene separation water preheater, a regenerated lean oil heater, a lean oil-rich heat exchanger, a crude benzene condenser, a gas-liquid separator, an oil-water separator and vacuum equipment; the invention improves the defects existing in the three prior art, a part of crude benzene separation water is sent into an evaporator to be heated by medium pressure steam condensate to generate steam, and the generated steam is sent into a lean oil regenerator to be circularly heated together with regenerated lean oil after being overheated by a steam superheater and the medium pressure steam condensate, thereby providing rising stripping steam for the bottom of the lean oil regenerator and the bottom of the debenzolization and dehydration; has the advantages of less fixed investment, low operation cost, good benzene removal effect, simple flow, no additional production of wastewater and the like.
Description
Technical Field
The invention relates to the technical field of coking chemical product recovery, in particular to an energy-saving negative pressure debenzolization process and system.
Background
Benzene series in coke oven gas in coking industry belongs to high-value byproducts, and benefits can be created for coking enterprises after recovery. At present, the recovery mode that coking enterprises generally adopt is: the coking wash oil is utilized to absorb benzene series in coke oven gas to form rich oil, and the rich oil is subjected to a benzene removal process to obtain high-value byproducts such as crude benzene or light benzene. The debenzolization process generally comprises an atmospheric pressure superheated steam stripping debenzolization process, a negative pressure superheated steam stripping debenzolization process and a negative pressure steam-free debenzolization process. Wherein:
the normal pressure superheated steam stripping process has mature technology and stable operation, but the process consumes a large amount of steam, about 1.5 tons of 400 ℃ superheated steam is consumed for obtaining 1 ton of crude benzene, the part of steam and crude benzene steam both come out of the top of the benzene removal tower and enter a crude benzene condenser to be condensed, and a large amount of wastewater is generated after oil-water separation is carried out, and the part of wastewater cannot be directly discharged and needs to be discharged to a tar and ammonia water separation unit, so that the amount of residual ammonia water is increased finally, and the treatment cost of the subsequent ammonia evaporation and phenol-cyanide wastewater procedures is increased.
The negative pressure superheated steam stripping process for removing benzene is gradually popularized in the coking industry in recent years, and the process utilizes vacuum equipment to extract noncondensable gas which is not condensed after a crude benzene condenser, so that a benzene removing system is in a negative pressure state. Compared with the normal pressure superheated steam stripping process, the process increases small investment of vacuum equipment and the like, but can greatly reduce the consumption of superheated steam, and about 0.75 to 0.8 ton of superheated steam is consumed for obtaining 1 ton of crude benzene. However, the part of steam and crude benzene steam still can be discharged from the top of the benzene removal tower and enter the crude benzene condenser, and wastewater is generated after oil-water separation, so that the production of wastewater is greatly reduced compared with the normal pressure superheated steam stripping process, and the treatment cost of the subsequent wastewater is increased.
The negative pressure steam-free benzene removal process is different from the two benzene removal processes, and the crude benzene is stripped by using wash oil which is heated and flashed to form wash oil steam. The negative pressure steam-free process has no external steam entering the benzene removing system, no waste water generation, and obvious advantages compared with other two benzene removing processes. However, compared with the other two benzene removal processes, the process system has higher vacuum degree, and increases the equipment investment of a vacuum pump, a lean oil reboiler, a lean oil circulating pump and the like; compared with the lean oil temperature at the bottom of the debenzolization tower in the steam stripping debenzolization process which is 175-180 ℃, the lean oil temperature at the bottom of the debenzolization tower in the steam-free debenzolization process is generally controlled to 220-240 ℃, the lean oil temperature at the bottom of the debenzolization tower is higher, the deterioration degree of wash oil is increased, and the consumption of wash oil is further increased.
Disclosure of Invention
The invention provides an energy-saving negative pressure debenzolization process and system, which are improved for overcoming the defects of the existing three debenzolization processes, wherein a part of crude benzene separation water is sent into an evaporator to be heated by medium-pressure steam condensate to generate steam, and the generated steam is superheated by a steam superheater and the medium-pressure steam condensate and then is sent into a lean oil regenerator to be circularly heated together with regenerated lean oil, so that rising stripping steam is provided for the bottom of the lean oil regenerator and the debenzolization bottom; has the advantages of less fixed investment, low operation cost, good benzene removal effect, simple flow, no additional production of wastewater and the like,
in order to achieve the above purpose, the invention is realized by adopting the following technical scheme:
an energy-saving negative pressure debenzolization process comprises the following steps:
(1) The rich oil sent by the final cooling benzene washing unit enters a lean rich oil heat exchanger to exchange heat with the hot lean oil extracted from the bottom of the benzene removal tower, then enters a rich oil heater to be heated by medium-pressure steam, and enters the benzene removal tower to carry out benzene removal operation; the heat-exchanged heat lean oil is cooled by a first-stage lean oil cooler and a second-stage lean oil cooler and then sent to a benzene washing tower of a final-cooling benzene washing unit for benzene washing operation;
(2) Crude benzene steam and water steam at the top of the debenzolization tower enter a crude benzene condenser to be condensed, and a condensed gas-liquid mixture enters a gas-liquid separator to be separated into gas phases and liquid phases;
(3) The liquid phase part separated by the gas-liquid separator enters an oil-water separator to carry out oil-water two-phase separation operation, one part of crude benzene oil phase separated by the two phases is pumped to the top of a benzene removal tower by a crude benzene reflux pump to be used as the top reflux of the tower, and the other part is directly sent to an oil depot to be stored; the non-condensable gas phase separated by the gas-liquid separator is pumped by vacuum equipment to generate negative pressure, so that the debenzolization system maintains a negative pressure state; the non-condensable gas phase after being pumped is discharged into a gas pipeline before benzene washing after passing through vacuum equipment;
(4) The regenerated hot lean oil at the bottom of the lean oil regenerator is sent to a regenerated lean oil heater through a lean oil regeneration circulating pump, is heated by medium-pressure steam and enters the lean oil regenerator for decompression flash evaporation after being heated, and provides a part of rising stripping steam for lean oil regeneration operation;
(5) Pressurizing crude benzene separation water separated by an oil-water separator by a crude benzene separation water pump, wherein a part of crude benzene separation water is sent to a crude benzene separation water preheater to be heated and then enters the bottom of an evaporator tube pass, and a part of crude benzene separation water in the evaporator tube pass is used as sewage to be sent to a final cold benzene washing unit; the crude benzene separation water in the evaporator tube pass exchanges heat with medium-pressure steam condensate entering the bottom of the evaporator shell pass to generate steam, and part of the steam enters a steam superheater and enters the lower part of a tray of a lean oil regenerator after exchanging heat with the medium-pressure steam condensate coming out of an oil-rich heater to provide another part of rising stripping steam for the lean oil regeneration operation;
(6) The wash oil steam and water steam at the top of the lean oil regenerator enter the bottom of the debenzolization tower to provide rising stripping steam for debenzolization operation.
Further, in the step (1), the rich oil temperature entering the debenzolization tower is 185-205 ℃, and the lean oil temperature at the bottom of the debenzolization tower is 175-200 ℃; the operating vacuum degree of the debenzolization tower is-60 kPa to-80 kPa.
Further, in the step (4), the operation vacuum degree of the lean oil regenerator is-40 kPa to-60 kPa; the lean oil temperature at the bottom of the lean oil regenerator is 210-280 ℃.
In the step (5), the temperature of the crude benzene separation water after the crude benzene separation water preheater is 80-100 ℃.
Further, in the step (5), the operation vacuum degree of the evaporator is-35 kPa to-55 kPa; the temperature of the steam after the steam superheater is 150-250 ℃.
An energy-saving negative pressure debenzolization system comprises a debenzolization tower, an evaporator, a steam superheater, a lean oil regenerator, an oil-rich heater, a crude benzene separation water preheater, a regenerated lean oil heater, a lean oil-rich heat exchanger, a crude benzene condenser, a gas-liquid separator, an oil-water separator and vacuum equipment;
the bottom of the debenzolization tower is provided with a hot lean oil outlet, the lower part is provided with a mixed steam inlet, the upper part is provided with a rich oil inlet, and the top is provided with a mixed steam outlet and a crude benzene reflux port; the hot lean oil outlet is connected with a lean oil inlet of the lean rich oil heat exchanger through a hot lean oil pipeline, and a hot lean oil pump is arranged on the hot lean oil pipeline; the lean oil outlet of the lean-rich oil heat exchanger is connected with a lean oil input pipeline of the final cooling benzene washing unit through a lean oil pipeline, and a first-stage lean oil cooler and a second-stage lean oil cooler are sequentially arranged on the lean oil pipeline;
the upper part in the lean oil regenerator is provided with a tray, the bottom of the lean oil regenerator is provided with an residue outlet, a regenerated lean oil inlet and a steam inlet are arranged on a tower body below the tray, and the top of the tower body is provided with a mixed steam outlet and a hot lean oil inlet; the mixed steam outlet of the lean oil regenerator is connected with the mixed steam inlet of the debenzolization tower through a mixed steam pipeline; a hot lean inlet of the lean oil regenerator is connected with a hot lean pipe downstream of the hot lean pump through a pipe; the regenerated lean oil outlet of the lean oil regenerator is connected with the regenerated lean oil inlet through a regenerated lean oil pipeline, and a lean oil regeneration circulating pump and a regenerated lean oil heater are arranged on the regenerated lean oil pipeline; the bottom of the evaporator is provided with a sewage outlet, and the lower part of the evaporator is provided with a crude benzene separation water inlet;
the evaporator consists of a tube side and a shell side, wherein the top of the tube side is provided with a steam outlet, the bottom of the tube side is provided with a sewage outlet, and the lower part of the tube side is provided with a crude benzene separation water inlet; one side of the lower part of the shell pass is provided with a condensate inlet, and the other side of the upper part of the shell pass is provided with a condensate outlet; the steam outlet of the evaporator is connected with the steam inlet of the steam superheater through a steam pipeline, and the steam outlet of the steam superheater is connected with the steam inlet of the lean oil regenerator; the crude benzene separation water inlet of the evaporator is connected with the water phase outlet of the oil-water separator through a crude benzene separation water pipeline, a crude benzene separation water preheater is arranged on the crude benzene separation water pipeline close to the evaporator, and a crude benzene separation water pump is arranged on the crude benzene separation water pipeline close to the oil-water separator; the condensate inlet of the evaporator is connected with the condensate outlet of the steam superheater through a condensate pipeline, and the condensate inlet of the steam superheater is connected with the condensate outlet of the oil-rich heater; the condensate outlet of the evaporator is connected with the condensate inlet of the crude benzene separation water preheater;
the rich inlet of the rich heater is connected with the rich outlet of the lean-rich heat exchanger, and the rich outlet of the rich heater is connected with the rich inlet of the debenzolization tower; the rich oil inlet of the lean-rich oil heat exchanger is connected with the rich oil output pipeline of the final cooling benzene washing unit;
the mixed steam outlet of the debenzolization tower is connected with the steam inlet at the top of the crude benzene condenser, and the gas-liquid mixture outlet at the bottom of the crude benzene condenser is connected with the gas-liquid mixture inlet of the gas-liquid separator; the gas phase outlet at the top of the gas-liquid separator is connected with the gas inlet of the vacuum equipment; the non-condensable gas outlet of the vacuum equipment is connected with a gas pipeline before benzene washing; the liquid phase outlet at the bottom of the gas-liquid separator is connected with the inlet of the oil-water separator; an oil phase outlet and a water phase outlet are arranged at the bottom of the oil-water separator, the oil phase outlet is connected with a crude benzene reflux port of the benzene removal tower through a crude benzene pipeline, and a crude benzene reflux pump and a product crude benzene outlet are arranged on the crude benzene pipeline.
Further, the regenerated lean oil heater is provided with a medium-pressure steam inlet and a condensate outlet, and the rich oil heater is provided with a medium-pressure steam inlet and a condensate outlet.
Further, the benzene removal tower is a packed benzene removal tower, a plate benzene removal tower or a benzene removal tower with a packing and plate combined structure; the lean oil regenerator is a plate type lean oil regenerator.
Further, the first lean oil cooler is provided with a circulating water inlet and a circulating water outlet, and the circulating water inlet is connected with the circulating water outlet through a circulating water system; the second-stage lean oil cooler is provided with a low-temperature water inlet and a low-temperature water outlet, and the low-temperature water inlet is connected with the low-temperature water outlet through a low-temperature water circulation system.
Compared with the prior art, the invention has the beneficial effects that:
1) Sending a part of crude benzene separation water into an evaporator, heating by medium-pressure steam condensate to generate steam, and then sending the generated steam into a lean oil regenerator to be circularly heated together with regenerated lean oil after the generated steam is overheated by a steam superheater and the medium-pressure steam condensate, so as to provide rising stripping steam for the bottom of the lean oil regenerator and the bottom of the debenzolization and the bottom; compared with the existing normal-pressure and negative-pressure superheated steam stripping process for benzene removal, the energy-saving negative-pressure benzene removal process does not additionally generate coking wastewater, and effectively reduces the running cost of enterprises;
2) Compared with the prior conventional negative pressure steam-free process for benzene removal, the method adopts a mode of circulating heating by introducing water steam into the bottom of the lean oil regenerator and regenerating lean oil, thereby providing rising stripping steam for the bottom of the lean oil regenerator and the bottom of the benzene removal tower, greatly reducing the lean oil temperature of the bottom of the benzene removal tower and the bottom of the lean oil regenerator, effectively suppressing the deterioration degree of wash oil, reducing the consumption of wash oil in the process of benzene elution and further reducing the running cost of enterprises;
3) Compared with the conventional normal-pressure and negative-pressure superheated steam stripping process, the energy-saving negative-pressure debenzolization process disclosed by the invention gets rid of the dependence of debenzolization on superheated steam, and meanwhile, the reduction of the temperature of lean oil at the bottoms of a debenzolization tower and a lean oil regenerator also reduces the dependence of the debenzolization process on a high-quality heat source to a certain extent.
Drawings
Fig. 1 is a flow chart (schematic structural diagram of a system) of an energy-saving negative pressure debenzolization process according to the invention.
In the figure: 1. the system comprises a debenzolization tower 2, a lean oil regenerator 3, a steam superheater 4, a regenerated lean oil heater 5, a hot lean oil pump 6, a lean oil regeneration circulating pump 7, a crude benzene reflux pump 8, a crude benzene condenser 9, a gas-liquid separator 10, a vacuum device 11, an oil-water separator 12, a lean rich oil heat exchanger 13, a rich oil heater 14, a first-stage lean oil cooler 15, a second-stage lean oil cooler 16, an evaporator 17, a crude benzene separation water preheater 18, a crude benzene separation water pump
Detailed Description
The following is a further description of embodiments of the invention, taken in conjunction with the accompanying drawings:
as shown in fig. 1, the energy-saving negative pressure debenzolization process provided by the invention comprises the following steps:
(1) The rich oil sent by the final cooling benzene washing unit enters a lean rich oil heat exchanger 12 to exchange heat with the hot lean oil extracted from the bottom of the benzene removal tower 1, then enters an rich oil heater 13 to be heated by medium-pressure steam, and enters the benzene removal tower 1 to carry out benzene removal operation; the heat-exchanged heat lean oil is cooled by a first-stage lean oil cooler 14 and a second-stage lean oil cooler 15 and then sent to a benzene washing tower of a final cooling benzene washing unit for benzene washing operation;
(2) Crude benzene steam and water vapor at the top of the debenzolization tower 1 enter a crude benzene condenser 8 for condensation, and a condensed gas-liquid mixture enters a gas-liquid separator 9 for gas-liquid two-phase separation;
(3) The liquid phase part separated by the gas-liquid separator 9 enters the oil-water separator 11 to carry out oil-water two-phase separation operation, one part of crude benzene oil phase after two-phase separation is sent to the top of the benzene removal tower 1 by the crude benzene reflux pump 7 to be used as the top reflux, and the other part is directly sent to an oil depot to be stored; the noncondensable gas phase separated by the gas-liquid separator 9 is pumped by the vacuum equipment 10 to generate negative pressure, so that the debenzolization system maintains a negative pressure state; the non-condensable gas phase after being sucked is discharged into a gas pipeline before benzene washing after passing through the vacuum equipment 10;
(4) The regenerated hot lean oil at the bottom of the lean oil regenerator 2 is sent to a regenerated lean oil heater 4 through a lean oil regeneration circulating pump 6, is heated by medium-pressure steam and enters the lean oil regenerator 2 for decompression flash evaporation after being heated, and provides a part of rising stripping steam for lean oil regeneration operation;
(5) The crude benzene separating water separated by the oil-water separator 11 is pressurized by a crude benzene separating water pump 18, a part of the crude benzene separating water is sent to a crude benzene separating water preheater 17 to be heated and then enters the bottom of the tube side of the evaporator 16, and a part of the crude benzene separating water on the tube side of the evaporator 16 is used as sewage to be sent to a final cold benzene washing unit; the crude benzene separated water in the tube side of the evaporator 16 exchanges heat with the medium-pressure steam condensate entering the bottom of the shell side of the evaporator 16 to generate steam, and part of the steam enters the steam superheater 3 to exchange heat with the medium-pressure steam condensate exiting from the oil-rich heater 13 and then enters the lower part of a tray of the lean oil regenerator 2, so that another part of rising stripping steam is provided for the lean oil regeneration operation;
(6) The wash oil steam and water steam at the top of the lean oil regenerator 2 enter the bottom of the debenzolization tower 1 to provide rising stripping steam for debenzolization operation.
Further, in the step (1), the rich oil temperature entering the debenzolization tower 1 is 185-205 ℃, and the lean oil temperature at the bottom of the debenzolization tower 1 is 175-200 ℃; the operating vacuum degree of the debenzolization tower 1 is-60 kPa to-80 kPa.
Further, in the step (4), the operation vacuum degree of the lean oil regenerator 2 is-40 kPa to-60 kPa; the lean oil temperature at the bottom of the lean oil regenerator 2 is 210-280 ℃.
Further, in the step (5), the temperature of the raw benzene separation water after the raw benzene separation water preheater 17 is 80 ℃ to 100 ℃.
Further, in the step (5), the operation vacuum degree of the evaporator 16 is-35 kPa to-55 kPa; the steam temperature after the steam superheater 3 is 150-250 ℃.
The invention relates to an energy-saving negative pressure debenzolization system which comprises a debenzolization tower 1, an evaporator 16, a steam superheater 3, a lean oil regenerator 2, an oil-rich heater 13, a crude benzene separation water preheater 17, a regenerated lean oil heater 4, a lean oil-rich heat exchanger 12, a crude benzene condenser 8, a gas-liquid separator 9, an oil-water separator 11 and vacuum equipment 10;
the bottom of the debenzolization tower 1 is provided with a hot lean oil outlet, the lower part is provided with a mixed steam inlet, the upper part is provided with a rich oil inlet, and the top is provided with a mixed steam outlet and a crude benzene reflux port; the hot lean oil outlet is connected with a lean oil inlet of the lean rich oil heat exchanger 12 through a hot lean oil pipeline, and the hot lean oil pipeline is provided with a hot lean oil pump 5; the lean oil outlet of the lean-rich oil heat exchanger 12 is connected with a lean oil input pipeline of the final cooling benzene washing unit through a lean oil pipeline, and a first-stage lean oil cooler 14 and a second-stage lean oil cooler 15 are sequentially arranged on the lean oil pipeline;
the upper part in the lean oil regenerator 2 is provided with a tray, the bottom of the lean oil regenerator 2 is provided with an residue oil outlet, a regenerated lean oil inlet and a steam inlet are arranged on a tower body below the tray, and the top is provided with a mixed steam outlet and a hot lean oil inlet; the mixed steam outlet of the lean oil regenerator 2 is connected with the mixed steam inlet of the debenzolization tower 1 through a mixed steam pipeline; the hot lean inlet of the lean regenerator 2 is connected by a pipe to the hot lean pipe downstream of the hot lean pump 5; the regenerated lean oil outlet of the lean oil regenerator 2 is connected with a regenerated lean oil inlet through a regenerated lean oil pipeline, and a lean oil regeneration circulating pump 6 and a regenerated lean oil heater 4 are arranged on the regenerated lean oil pipeline; the bottom of the evaporator 16 is provided with a sewage outlet, and the lower part is provided with a crude benzene separation water inlet;
the evaporator 16 consists of a tube side and a shell side, wherein the top of the tube side is provided with a steam outlet, the bottom of the tube side is provided with a sewage outlet, and the lower part of the tube side is provided with a crude benzene separation water inlet; one side of the lower part of the shell pass is provided with a condensate inlet, and the other side of the upper part of the shell pass is provided with a condensate outlet; the steam outlet of the evaporator 16 is connected with the steam inlet of the steam superheater 3 through a steam pipeline, and the steam outlet of the steam superheater 3 is connected with the steam inlet of the lean oil regenerator 2; the crude benzene separation water inlet of the evaporator 16 is connected with the water phase outlet of the oil-water separator 11 through a crude benzene separation water pipeline, a crude benzene separation water preheater 17 is arranged on the crude benzene separation water pipeline close to the evaporator 16, and a crude benzene separation water pump 18 is arranged on the crude benzene separation water pipeline close to the oil-water separator 11; the condensate inlet of the evaporator 16 is connected with the condensate outlet of the steam superheater 3 through a condensate pipeline, and the condensate inlet of the steam superheater 3 is connected with the condensate outlet of the oil-rich heater 13; the condensate outlet of the evaporator 16 is connected with the condensate inlet of the crude benzene separation water preheater 17;
the rich inlet of the rich heater 13 is connected with the rich outlet of the lean-rich heat exchanger 12, and the rich outlet of the rich heater 13 is connected with the rich inlet of the debenzolization tower 1; the rich inlet of the lean-rich heat exchanger 12 is connected with a rich output pipeline of the final cooling benzene washing unit;
the mixed steam outlet of the debenzolization tower 1 is connected with the steam inlet at the top of the crude benzene condenser 8, and the gas-liquid mixture outlet at the bottom of the crude benzene condenser 8 is connected with the gas-liquid mixture inlet of the gas-liquid separator 11; the gas phase outlet at the top of the gas-liquid separator 11 is connected with the gas inlet of the vacuum equipment 10; the non-condensable gas outlet of the vacuum equipment 10 is connected with a gas pipeline before benzene washing; the liquid phase outlet at the bottom of the gas-liquid separator 11 is connected with the inlet of the oil-water separator 11; an oil phase outlet and a water phase outlet are arranged at the bottom of the oil-water separator 11, the oil phase outlet is connected with a crude benzene reflux port of the debenzolization tower 1 through a crude benzene pipeline, and a crude benzene reflux pump 7 and a product crude benzene outlet are arranged on the crude benzene pipeline.
Further, the regenerated lean oil heater 4 is provided with a medium pressure steam inlet and a condensate outlet, and the rich oil heater 13 is provided with a medium pressure steam inlet and a condensate outlet.
Further, the benzene removal tower 1 is a packed benzene removal tower, a plate benzene removal tower or a benzene removal tower with a packing and plate combined structure; the lean oil regenerator 2 is a plate type lean oil regenerator.
Further, the first lean oil cooler 14 is provided with a circulating water inlet and a circulating water outlet, and the circulating water inlet is connected with the circulating water outlet through a circulating water system; the second-stage lean oil cooler 15 is provided with a low-temperature water inlet and a low-temperature water outlet, and the low-temperature water inlet is connected with the low-temperature water outlet through a low-temperature water circulation system.
The following examples are given by way of illustration of detailed embodiments and specific procedures based on the technical scheme of the present invention, but the scope of the present invention is not limited to the following examples.
[ example ]
In this embodiment, an energy-saving negative pressure debenzolization system comprises a debenzolization tower 1, a lean oil regenerator 2, a steam superheater 3, a regenerated lean oil heater 4, a hot lean oil pump 5, a regenerated lean oil circulating pump 6, a crude benzene reflux pump 7, a crude benzene condenser 8, a gas-liquid separator 9, a vacuum device 10, an oil-water separator 11, a lean-rich oil heat exchanger 12, an oil-rich heater 13, a first-stage lean oil cooler 14, a second-stage lean oil cooler 15, an evaporator 16, a crude benzene separation water preheater 17 and a crude benzene separation water pump 18, wherein all the devices are connected through pipelines.
The bottom of the debenzolization tower 1 is connected with the inlet of a hot lean oil pump 5, and the outlet of the hot lean oil pump 5 is connected with a lean oil-rich oil heat exchanger 12; the lean-rich oil heat exchanger 12 is connected with a lean oil cooler 14; the first-stage lean oil cooler 14 is connected with the second-stage lean oil cooler 15; the top of the debenzolization tower 1 is sequentially connected with a crude benzene condenser 8 and a gas-liquid separator 9; the gas phase outlet of the gas-liquid separator 9 is connected with a vacuum device 10, and the vacuum device 10 is connected with a gas pipeline before final cooling benzene washing; the liquid phase outlet of the gas-liquid separator 9 is connected with the oil-water separator 11; the oil phase outlet of the oil-water separator 11 is connected with the inlet of the crude benzene reflux pump 7, and the outlet of the crude benzene reflux pump 7 is connected with the top of the debenzolization tower 1; the water phase outlet of the oil-water separator 11 is connected with the inlet of a crude benzene separation water pump 18, the outlet of the crude benzene separation water pump 18 is connected with the separation water inlet of a crude benzene separation water preheater 17, and the separation water outlet of the crude benzene separation water preheater 17 is connected with the bottom tube side inlet of the evaporator 16; the tower body below the tray of the lean oil regenerator 2 is also connected with the inlet of a regenerated lean oil circulating pump 6, the outlet of the regenerated lean oil circulating pump 6 is connected with the inlet of a regenerated lean oil heater 4, and the outlet of the regenerated lean oil heater 4 is connected with the tower bottom of the lean oil regenerator 2 (the space inside the tower body below the tray is the tower bottom); the top of the lean oil regenerator 2 is connected with the bottom of the debenzolization tower 1; the top of the evaporator 16 is connected with the steam superheater 3, and the steam superheater 3 is connected with the bottom of the lean oil regenerator 2; the medium-pressure steam pipeline is connected with a steam inlet of the oil-rich heater 13, a condensate outlet of the oil-rich heater 13 is connected with a condensate inlet of the steam superheater 3, a condensate outlet of the steam superheater 3 is connected with a tube side inlet of the evaporator 16, and a tube side outlet of the evaporator 16 is connected with a condensate inlet of the crude benzene separation water preheater 17.
In this example, the wash oil circulation amount was 300m 3 And/h, the yield of crude benzene is 5.5t/h, and the flow rate of the recycled crude benzene separation water is 2m 3 /h。
In the embodiment, the rich oil sent by the final cooling benzene washing unit is subjected to heat exchange with the hot lean oil extracted from the bottom of the benzene removal tower 1 through the lean oil-rich oil heat exchanger 12 to 160 ℃, then enters the rich oil heater 13, is heated to 190 ℃ through medium-pressure steam, and then enters the benzene removal tower 1 for benzene removal operation; crude benzene steam and water steam at the top of the debenzolization tower 1 enter a crude benzene condenser 8 to be condensed to 25 ℃ under the working conditions of the operating pressure of 70kPaG and the operating temperature of 61 ℃, and the condensed gas-liquid mixture enters a gas-liquid separator 9 to be subjected to gas-liquid two-phase separation. The liquid phase part separated by the gas-liquid separator 9 enters the oil-water separator 11 to carry out oil-water two-phase separation operation, and part of the crude benzene oil phase separated by the two phases is sent to the top of the benzene removal tower 1 by the crude benzene reflux pump 7 to be used as the top reflux, and the mass reflux ratio is controlled to be 3; and the other part of crude benzene oil phase is directly sent to an oil depot for storage as crude benzene product. The non-condensable gas phase separated by the gas-liquid separator is pumped by the vacuum equipment 10 to generate negative pressure, so that the debenzolization system maintains a negative pressure state; the non-condensable gas phase after being sucked is discharged into a gas pipeline before benzene washing after passing through the vacuum equipment 10.
The temperature of the bottom of the lean oil regenerator 2 is 250 ℃, the regenerated hot lean oil is sent to the regenerated lean oil heater 4 through the lean oil regeneration circulating pump 6, and enters the top of the lean oil regenerator 2 for decompression flash evaporation after being heated by medium pressure steam, so as to provide a part of rising stripping steam for the lean oil regeneration operation. The lean oil regenerator top was operated at-48 kPaG and 177 ℃.
The crude benzene separated water from the oil-water separator 11 is sent to a crude benzene separated water preheater 17 by a crude benzene separated water pump 18, and enters the bottom of the tube pass of the evaporator 16 after being heated to 90 ℃, and the flow is controlled at 2.9m 3 And/h, wherein a part of separated water is continuously pumped out from the bottom of the tube pass of the evaporator 16 as sewage to be sent to a final cold benzene washing unit, and the sewage flow is controlled to be 0.9m 3 /h。
The crude benzene separated water sent to the bottom of the tube side of the evaporator 16 exchanges heat with the medium-pressure steam condensate water entering the bottom of the shell side of the evaporator 16 to generate steam, the operating pressure at the top of the evaporator is-40 kPaG, the operating temperature is 86 ℃, and part of the steam enters the steam superheater 3 to exchange heat with the medium-pressure condensate water with the temperature of 204 ℃ coming out of the oil-rich heater 13 to 180 ℃ and then enters the bottom of the lean oil regenerator 2.
The hot lean oil with 177 ℃ bottom temperature of the debenzolization tower 1 is sent to a lean-rich oil heat exchanger 12 by a hot lean oil pump 5, exchanges heat with the rich oil sent by the final cooling benzene washing unit, and enters a first-stage lean oil cooler 14 and a second-stage lean oil cooler 15 to be cooled to 27 ℃.
In this example, benzene series content in wastewater at the bottom of the debenzolization tower 1 is less than 0.15%.
In this example, the saturated steam consumption of 1.6MPa is 10t/h; the circulating water consumption is 315m 3 Ammonia water/h, low temperature water consumption 300m 3 Compared with the existing conventional negative pressure superheated steam stripping process for benzene removal, the benzene removal process reduces the operation cost by 31.6%;
economic benefit analysis of the energy-saving negative pressure debenzolization process in the embodiment: with a wash oil circulation of 300m 3 The energy consumption of four benzene removal processes is compared with each other by taking 5.5t/h crude benzene yield as an exampleTable 1.
Table 1 comparison of energy consumption benefits of four debenzolization processes
From the table, the operation cost of the four benzene removal processes is as follows: the normal pressure superheated steam stripping process > negative pressure no-steam process benzene removal process > the energy-saving negative pressure benzene removal process.
Compared with the existing benzene removal process, the energy-saving negative pressure benzene removal process has the following maximum advantages: compared with the negative pressure superheated steam stripping process, the process eliminates the generation of extra coking wastewater, and compared with the negative pressure steam-free process, the process greatly reduces the temperature of lean oil at the bottom of the debenzolization tower and the regeneration tower, so that the lean oil is not easy to deteriorate, and the consumption of washing oil is reduced.
The invention is applicable to the prior art where it is not described.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (9)
1. An energy-saving negative pressure debenzolization process is characterized by comprising the following steps:
(1) The rich oil sent by the final cooling benzene washing unit enters a lean rich oil heat exchanger to exchange heat with the hot lean oil extracted from the bottom of the benzene removal tower, then enters a rich oil heater to be heated by medium-pressure steam, and enters the benzene removal tower to carry out benzene removal operation; the heat-exchanged heat lean oil is cooled by a first-stage lean oil cooler and a second-stage lean oil cooler and then sent to a benzene washing tower of a final-cooling benzene washing unit for benzene washing operation;
(2) Crude benzene steam and water steam at the top of the debenzolization tower enter a crude benzene condenser to be condensed, and a condensed gas-liquid mixture enters a gas-liquid separator to be separated into gas phases and liquid phases;
(3) The liquid phase part separated by the gas-liquid separator enters an oil-water separator to carry out oil-water two-phase separation operation, one part of crude benzene oil phase separated by the two phases is pumped to the top of a benzene removal tower by a crude benzene reflux pump to be used as the top reflux of the tower, and the other part is directly sent to an oil depot to be stored; the non-condensable gas phase separated by the gas-liquid separator is pumped by vacuum equipment to generate negative pressure, so that the debenzolization system maintains a negative pressure state; the non-condensable gas phase after being pumped is discharged into a gas pipeline before benzene washing after passing through vacuum equipment;
(4) The regenerated hot lean oil at the bottom of the lean oil regenerator is sent to a regenerated lean oil heater through a lean oil regeneration circulating pump, is heated by medium-pressure steam and enters the lean oil regenerator for decompression flash evaporation after being heated, and provides a part of rising stripping steam for lean oil regeneration operation;
(5) Pressurizing crude benzene separation water separated by an oil-water separator by a crude benzene separation water pump, wherein a part of crude benzene separation water is sent to a crude benzene separation water preheater to be heated and then enters the bottom of an evaporator tube pass, and a part of crude benzene separation water in the evaporator tube pass is used as sewage to be sent to a final cold benzene washing unit; the crude benzene separation water in the evaporator tube pass exchanges heat with medium-pressure steam condensate entering the bottom of the evaporator shell pass to generate steam, and part of the steam enters a steam superheater and enters the lower part of a tray of a lean oil regenerator after exchanging heat with the medium-pressure steam condensate coming out of an oil-rich heater to provide another part of rising stripping steam for the lean oil regeneration operation;
(6) The wash oil steam and water steam at the top of the lean oil regenerator enter the bottom of the debenzolization tower to provide rising stripping steam for debenzolization operation.
2. The energy-saving negative pressure debenzolization process of claim 1 wherein in step (1), the rich oil temperature entering the debenzolization tower is 185 ℃ to 205 ℃ and the lean oil temperature at the debenzolization tower bottom is 175 ℃ to 200 ℃; the operating vacuum degree of the debenzolization tower is-60 kPa to-80 kPa.
3. The energy-saving negative pressure debenzolization process of claim 1 wherein in step (4) the operating vacuum of the lean oil regenerator is from-40 kPa to-60 kPa; the lean oil temperature at the bottom of the lean oil regenerator is 210-280 ℃.
4. The energy-saving negative pressure debenzolization process of claim 1 wherein in step (5) the temperature of the crude benzene separation water after the crude benzene separation water preheater is 80 ℃ to 100 ℃.
5. The energy-saving negative pressure debenzolization process of claim 1 wherein in step (5) the evaporator operating vacuum is from-35 kPa to-55 kPa; the temperature of the steam after the steam superheater is 150-250 ℃.
6. An energy-saving negative pressure debenzolization system for realizing the process of claim 1 and comprising a debenzolization tower, an evaporator, a steam superheater, a lean oil regenerator, an oil-rich heater, a crude benzene separated water preheater, a regenerated lean oil heater, a lean oil-rich heat exchanger, a crude benzene condenser, a gas-liquid separator, an oil-water separator and vacuum equipment;
the bottom of the debenzolization tower is provided with a hot lean oil outlet, the lower part is provided with a mixed steam inlet, the upper part is provided with a rich oil inlet, and the top is provided with a mixed steam outlet and a crude benzene reflux port; the hot lean oil outlet is connected with a lean oil inlet of the lean rich oil heat exchanger through a hot lean oil pipeline, and a hot lean oil pump is arranged on the hot lean oil pipeline; the lean oil outlet of the lean-rich oil heat exchanger is connected with a lean oil input pipeline of the final cooling benzene washing unit through a lean oil pipeline, and a first-stage lean oil cooler and a second-stage lean oil cooler are sequentially arranged on the lean oil pipeline;
the upper part in the lean oil regenerator is provided with a tray, the bottom of the lean oil regenerator is provided with an residue outlet, a regenerated lean oil inlet and a steam inlet are arranged on a tower body below the tray, and the top of the tower body is provided with a mixed steam outlet and a hot lean oil inlet; the mixed steam outlet of the lean oil regenerator is connected with the mixed steam inlet of the debenzolization tower through a mixed steam pipeline; a hot lean inlet of the lean oil regenerator is connected with a hot lean pipe downstream of the hot lean pump through a pipe; the regenerated lean oil outlet of the lean oil regenerator is connected with the regenerated lean oil inlet through a regenerated lean oil pipeline, and a lean oil regeneration circulating pump and a regenerated lean oil heater are arranged on the regenerated lean oil pipeline; the bottom of the evaporator is provided with a sewage outlet, and the lower part of the evaporator is provided with a crude benzene separation water inlet;
the evaporator consists of a tube side and a shell side, wherein the top of the tube side is provided with a steam outlet, the bottom of the tube side is provided with a sewage outlet, and the lower part of the tube side is provided with a crude benzene separation water inlet; one side of the lower part of the shell pass is provided with a condensate inlet, and the other side of the upper part of the shell pass is provided with a condensate outlet; the steam outlet of the evaporator is connected with the steam inlet of the steam superheater through a steam pipeline, and the steam outlet of the steam superheater is connected with the steam inlet of the lean oil regenerator; the crude benzene separation water inlet of the evaporator is connected with the water phase outlet of the oil-water separator through a crude benzene separation water pipeline, a crude benzene separation water preheater is arranged on the crude benzene separation water pipeline close to the evaporator, and a crude benzene separation water pump is arranged on the crude benzene separation water pipeline close to the oil-water separator; the condensate inlet of the evaporator is connected with the condensate outlet of the steam superheater through a condensate pipeline, and the condensate inlet of the steam superheater is connected with the condensate outlet of the oil-rich heater; the condensate outlet of the evaporator is connected with the condensate inlet of the crude benzene separation water preheater;
the rich inlet of the rich heater is connected with the rich outlet of the lean-rich heat exchanger, and the rich outlet of the rich heater is connected with the rich inlet of the debenzolization tower; the rich oil inlet of the lean-rich oil heat exchanger is connected with the rich oil output pipeline of the final cooling benzene washing unit;
the mixed steam outlet of the debenzolization tower is connected with the steam inlet at the top of the crude benzene condenser, and the gas-liquid mixture outlet at the bottom of the crude benzene condenser is connected with the gas-liquid mixture inlet of the gas-liquid separator; the gas phase outlet at the top of the gas-liquid separator is connected with the gas inlet of the vacuum equipment; the non-condensable gas outlet of the vacuum equipment is connected with a gas pipeline before benzene washing; the liquid phase outlet at the bottom of the gas-liquid separator is connected with the inlet of the oil-water separator; an oil phase outlet and a water phase outlet are arranged at the bottom of the oil-water separator, the oil phase outlet is connected with a crude benzene reflux port of the benzene removal tower through a crude benzene pipeline, and a crude benzene reflux pump and a product crude benzene outlet are arranged on the crude benzene pipeline.
7. The energy efficient negative pressure debenzolization system of claim 6 wherein the regenerated lean oil heater has medium pressure steam inlet and condensate outlet and the rich oil heater has medium pressure steam inlet and condensate outlet.
8. The energy-saving negative pressure debenzolization system of claim 6 wherein the debenzolization tower is a packed debenzolization tower, a plate debenzolization tower or a packed and plate combination of debenzolization towers; the lean oil regenerator is a plate type lean oil regenerator.
9. The energy-saving negative pressure debenzolization system of claim 6 wherein the one-stage lean oil cooler has a circulating water inlet and a circulating water outlet, the circulating water inlet and the circulating water outlet being connected by the circulating water system; the second-stage lean oil cooler is provided with a low-temperature water inlet and a low-temperature water outlet, and the low-temperature water inlet is connected with the low-temperature water outlet through a low-temperature water circulation system.
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| CN117069346B (en) * | 2023-10-16 | 2024-02-02 | 天津市创举科技股份有限公司 | Residual ammonia water distillation benzene removal device and application method thereof |
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