CN114774161B - Multi-generation comprehensive utilization system and treatment process for treating residual oil by biomass volatilization - Google Patents
Multi-generation comprehensive utilization system and treatment process for treating residual oil by biomass volatilization Download PDFInfo
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- CN114774161B CN114774161B CN202210214656.8A CN202210214656A CN114774161B CN 114774161 B CN114774161 B CN 114774161B CN 202210214656 A CN202210214656 A CN 202210214656A CN 114774161 B CN114774161 B CN 114774161B
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- 239000002028 Biomass Substances 0.000 title claims abstract description 79
- 238000000034 method Methods 0.000 title claims abstract description 18
- 230000008569 process Effects 0.000 title claims abstract description 12
- 239000000295 fuel oil Substances 0.000 claims abstract description 72
- 239000003921 oil Substances 0.000 claims abstract description 72
- 238000004821 distillation Methods 0.000 claims abstract description 69
- 239000002994 raw material Substances 0.000 claims abstract description 66
- 238000000197 pyrolysis Methods 0.000 claims abstract description 48
- 230000008016 vaporization Effects 0.000 claims abstract description 45
- 238000009834 vaporization Methods 0.000 claims abstract description 41
- 238000002485 combustion reaction Methods 0.000 claims abstract description 29
- 239000006227 byproduct Substances 0.000 claims abstract description 17
- 239000003039 volatile agent Substances 0.000 claims abstract description 5
- 238000000605 extraction Methods 0.000 claims abstract description 4
- 239000000047 product Substances 0.000 claims description 63
- 238000007599 discharging Methods 0.000 claims description 46
- 238000010438 heat treatment Methods 0.000 claims description 45
- 238000005292 vacuum distillation Methods 0.000 claims description 16
- 238000010992 reflux Methods 0.000 claims description 15
- 238000002309 gasification Methods 0.000 claims description 12
- 230000006837 decompression Effects 0.000 claims description 8
- 238000012545 processing Methods 0.000 claims description 7
- 239000000446 fuel Substances 0.000 claims description 6
- 238000010079 rubber tapping Methods 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 5
- 238000005194 fractionation Methods 0.000 claims description 3
- 239000002956 ash Substances 0.000 description 10
- 239000000126 substance Substances 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 239000004566 building material Substances 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000003912 environmental pollution Methods 0.000 description 4
- 239000004005 microsphere Substances 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000010882 bottom ash Substances 0.000 description 2
- 239000011449 brick Substances 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 241001474374 Blennius Species 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 241000209140 Triticum Species 0.000 description 1
- 235000021307 Triticum Nutrition 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 239000002351 wastewater Substances 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
- 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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a poly-generation comprehensive utilization system and a treatment process for treating residual oil by biomass volatilization, wherein the system comprises the following components: the fuel oil main output unit is used for extracting fuel oil in the heavy raw oil; the vaporization unit is used for vaporizing light components and heavy components in the heavy raw oil; a fuel oil byproduct extraction unit for extracting fuel oil from heavy components in the heavy raw oil; a biomass pyrolysis unit for providing volatiles into the system; the biomass pyrolysis unit and the fuel oil byproduct unit are overlapped in the vacuum rectifying tower (14) and the combustion furnace (13); the biomass pyrolysis unit and the fuel oil main output unit are overlapped on the device raw material tank (3) and the primary distillation tower (8). Compared with the prior art, the invention designs the whole link into a closed loop, does not need to provide heat from the outside, is self-sufficient, completes the circulation of the whole system, organically combines biomass, heavy raw oil, residual oil and the like, and realizes the scientific, efficient and comprehensive utilization of biomass energy.
Description
Technical Field
The invention relates to the technical field of comprehensive utilization of biomass resources, in particular to a comprehensive utilization system and a treatment process for poly-generation of residual oil treated by biomass volatilization.
Background
Along with the development of the economy in China and the improvement of the living standard of people, people increasingly recognize the importance of environmental and non-renewable energy protection. In recent years, the residual oil yield of each plant is also increasing, so how to process heavy raw oil and generated residual oil is also an important subject in modern city management.
In the current society, biomass is available in a large number of sources, but is not reasonably developed and utilized, and is often directly treated in a burning or landfill mode, so that the biomass is not effectively utilized. There is currently no similar solution for treating resid with biomass volatiles.
Patent CN112843764a discloses a vacuum rectifying tower with a satellite type tower kettle and a vacuum rectifying method for atmospheric residuum, which have very great development significance in the leading edge of the era, but the satellite implementation is more complex, and biomass and other substances are not utilized for reutilization; patent CN106753553A discloses a device and a method for producing carbon microspheres by lightening residual oil/coal tar, wherein a hydrogenation method is also applied to improve the yield of the carbon microspheres and produce carbon microspheres which are urgently needed in China, but the carbon microspheres are not combined with biomass. Furthermore, the above patent does not report on the energy and heat coupling portion.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a biomass volatilization processing residual oil poly-generation comprehensive utilization system and a processing technology capable of reusing energy and heat of biomass and residual oil.
The aim of the invention can be achieved by the following technical scheme:
a multi-cogeneration integrated utilization system for processing residuum by volatilizing biomass, the system comprising:
the fuel oil main output unit is used for extracting fuel oil in the heavy raw oil;
the vaporization unit is used for vaporizing light components and heavy components in the heavy raw oil;
a fuel oil byproduct extraction unit for extracting fuel oil from heavy components in the heavy raw oil;
a biomass pyrolysis unit for providing volatiles into the system;
the vaporization unit and the fuel oil main output unit are overlapped in the primary distillation tower; the vaporization unit and the fuel oil byproduct unit are overlapped in the vacuum rectifying tower;
the biomass pyrolysis unit and the vaporization unit are overlapped in the vacuum rectifying tower and the primary distillation tower; the biomass pyrolysis unit and the fuel oil byproduct unit are overlapped in the vacuum rectifying tower and the combustion furnace; the biomass pyrolysis unit and the fuel oil main output unit are overlapped on the device raw material tank and the primary distillation tower.
Further, the main fuel oil output unit comprises the following components:
the device material tank is used for preheating heavy raw oil; the device raw material tank is provided with an outlet, and water and a small amount of impurities are discharged from the bottom of the tank;
the primary distillation tower is used for fractionating heavy raw oil;
the main finished product collecting tank is used for collecting first-line fuel oil extracted by fractionation;
the primary distillation tower is connected with the vaporization unit through a tower top discharging pipe a and a tower bottom discharging pipe c respectively, and is connected with the main finished product collecting tank through a side discharging pipe b;
and the side discharge pipe is also provided with a reflux pipeline connected with the primary tower.
Further, the fuel oil main output unit further comprises a tank area raw material tank for storing heavy raw material oil, a conveying pump is arranged between the tank area raw material tank and a device raw material tank, and a heat exchanger group is arranged between the device raw material tank and the primary distillation tower;
the heat exchanger group comprises a two-wire heat exchanger, a three-wire heat exchanger and a tower bottom heat exchanger which are connected in parallel, and the tower bottom heat exchanger comprises a tower bottom primary heat exchanger and a tower bottom secondary heat exchanger which are connected in series.
Further, the vaporization unit comprises a heating vaporization furnace, a primary distillation tower and a reduced pressure distillation tower;
the primary distillation tower is connected with a heating vaporization furnace through a tower top discharging pipe a and a tower bottom discharging pipe c respectively, the heating vaporization furnace is connected with a reduced pressure rectifying tower, and the reduced pressure rectifying tower is connected with the tower top discharging pipe a through a tower top discharging pipe A;
the tower top discharging pipe a is also provided with a first main condenser, and the tower top discharging pipe a is also provided with a second condenser.
Further, the fuel oil byproduct outlet unit comprises a decompression rectifying tower, a finished product collecting tank area and a combustion furnace;
the finished product collecting tank area comprises a first auxiliary finished product collecting tank, a second auxiliary finished product collecting tank and a third auxiliary finished product collecting tank; the pressure reducing rectifying tower is connected with the pressure reducing rectifying tower through a first side line discharging pipe B 1 Connected with a first auxiliary finished product collecting tank, and the vacuum rectifying tower is connected with a second side discharging pipe B 2 Connected with a second byproduct collecting tank, the vacuum rectifying tower is connected with a third side discharge pipe B 3 Is connected with a third auxiliary finished product collecting tank;
the vacuum rectifying tower is connected with the combustion furnace through a tower bottom discharging pipe C;
the first side line discharging pipe B 1 The upper part is also provided with a first auxiliary condenser, and the second side discharge pipe B 2 A second auxiliary condenser is also arranged on the upper part, and the third side line discharging pipe B 3 A third auxiliary condenser is also arranged on the upper part.
Further, the first side line discharging pipe B 1 And/or a second side tapping pipe B 2 The device is in heat exchange connection with a raw material tank of the device; the first side line discharging pipe B 1 And/or a second side tapping pipe B 2 And a reflux pipeline connected with the decompression rectifying tower is arranged on the upper part.
Further, the biomass pyrolysis unit comprises a device raw material tank, a primary distillation tower, a biomass pyrolysis reactor, a combustion furnace and a reduced pressure rectifying tower;
the combustion furnace is respectively connected with the biomass pyrolysis reactor and a raw material tank of the device in a heat exchange manner; the discharge port of the biomass pyrolysis reactor is respectively connected with the vacuum rectifying tower, the primary distillation tower and the combustion furnace, and the biomass pyrolysis reactor is connected with the device raw material tank in a heat exchange way.
A treatment process of a poly-generation comprehensive utilization system based on processing residual oil by volatilizing biomass, which comprises the following steps:
(a) Heavy raw oil in a raw material tank of a tank area is sent into a raw material tank of a device by a conveying pump, and is heated in the raw material tank of the device;
(b) The heavy raw oil enters a primary distillation tower for reduced pressure distillation after heat is recovered by a heat exchanger group;
(c) The fraction distilled under reduced pressure in the primary distillation tower enters a main finished product collecting tank and a heating gasification furnace respectively, and enters a reduced pressure rectifying tower after being heated by the heating gasification furnace
(d) The fraction distilled under reduced pressure in the reduced pressure rectifying tower enters a finished product collecting tank area, a combustion furnace and a heating vaporization furnace respectively;
(e) Volatile matters generated in the biomass pyrolysis reactor enter a vacuum rectifying tower and a primary distillation tower, and micromolecular substances in the volatile matters generated after biomass pyrolysis can improve the C/H atomic ratio of oil production of each line and improve the quality of the produced oil; and meanwhile, the generated heat exchanges heat with the raw material tank of the device, so that the heavy raw material oil is heated, and the heat is reused.
Further, the step (c) specifically comprises:
the distillate on the top of the primary distillation tower is condensed by a first main condenser and then is collected and timely sent into a heating vaporization furnace to be burnt as fuel;
the side line distillate of the primary distillation tower is first-line fuel oil, one part of the side line distillate is returned to the primary distillation tower by a reflux pump and used for controlling the temperature of the primary distillation tower, and the other part of the side line distillate enters a main finished product collecting tank and is sold as a product;
the residual materials in the primary distillation tower enter a heating vaporization furnace for heating, and enter a vacuum rectifying tower after being heated by the heating vaporization furnace;
the step (d) is specifically as follows:
the tower top fraction of the vacuum rectifying tower is cooled by a second condenser and then is sent to a heating vaporization furnace to be used as fuel;
the first side-line fraction of the vacuum rectifying tower is first-line fuel oil, and is cooled by a first auxiliary condenser and then sent to a first auxiliary finished product collecting tank to be sold as a product.
The second side line distillate of the vacuum rectifying tower is two-line fuel oil, after heat exchange with a raw material tank of the device, the second side line distillate is cooled by a second auxiliary condenser, and a part of the second side line distillate is pumped back to the vacuum rectifying tower by a reflux pump and is used for controlling the side line temperature of the rectifying tower; pumping one part of the waste water to a finished product second subsidiary product collecting tank to be sold as a product;
the third side line distillate of the vacuum rectifying tower is three-line fuel oil, after heat exchange with a raw material tank of the device, the third side line distillate is cooled by a third auxiliary condenser, and a part of the third side line distillate is pumped back to the vacuum rectifying tower by a reflux pump and is used for controlling the side line temperature of the rectifying tower, and the other part of the third side line distillate enters a third auxiliary product collecting tank and is sold as a product;
the bottom fraction of the vacuum rectifying tower is vacuum residue, namely heavy oil, enters a combustion furnace to be combusted together with semicoke generated in a biomass pyrolysis reactor, heat is provided for the biomass pyrolysis reactor, and heat circulation is realized.
Further, the heating temperature in the raw material tank of the device is 65-75 ℃, and the device is kept stand for 1.5-2.5 hours;
the top fraction of the primary distillation tower is mixed oil gas at 45-55 ℃, and the side fraction of the primary distillation tower is first-line fuel oil at 145-155 ℃; the heating temperature of the heating vaporization furnace is 375-385 ℃;
the top fraction of the vacuum distillation tower is mixed oil gas at 45-55 ℃, the first side-line fraction of the vacuum distillation tower is first-line fuel oil at 145-155 ℃, the second side-line fraction of the vacuum distillation tower is second-line fuel oil at 235-255 ℃, the third side-line fraction of the vacuum distillation tower is third-line fuel oil at 315-325 ℃, and the bottom fraction of the vacuum distillation tower is vacuum residue at 355-365 ℃;
the operating temperature of the combustion furnace is 850-900 ℃. The method has the advantages that the generation and emission of NOx are effectively controlled, the activity of ash is favorably kept, the content of bottom ash and fly ash in the burned ash is less than 2%, the burned ash can be directly used as building materials, and further high-added-value products such as bricks, cement and the like are manufactured by using the burned ash as the building materials so as to be fully utilized, so that the recycling utilization of semicoke and ash is realized, and the environmental pollution is effectively reduced.
Compared with the prior art, the invention has the following advantages:
(1) According to the invention, heavy raw oil is sent into the rectifying tower, and required first-line, second-line and third-line oil can be obtained through twice rectification, and meanwhile, the oil from the rectifying tower can exchange heat again to exchange heat with the raw material area, so that the heat input from the raw material area of the device is reduced, the heat is recovered in a large range, and the heat is in accordance with the hot tide of the current energy utilization;
(2) According to the invention, the biomass pyrolysis reactor is added before the rectifying tower, the volatile matters generated by biomass pyrolysis have a large amount of heat and micromolecular substances, and the volatile matters of biomass are utilized to be similar to hydrogenation reaction and are divided into two paths to the rectifying tower and the raw material pipe of the device, so that the quality of commodity oil in the primary distillation tower and the vacuum rectifying tower is greatly improved, and meanwhile, residual oil is positioned at an important position in the whole energy and heat circulation, and the heat closed loop is completed.
(3) In the reaction process, the biomass selection can be diversified, and the reaction and the system have wide adaptability to raw materials and high comprehensive utilization degree. The reuse of biomass in the current society is also a hot point discussed by researchers, and the raw materials in the biomass pyrolysis reactor in the system can be selected variously, so that the biomass pyrolysis reactor is suitable for the comprehensive utilization of other biomasses such as seaweed, wheat straw, wet garbage and the like;
(4) The micromolecular substances contained in the biomass volatile matters can improve the rectification oil yield in the whole system, simultaneously avoid the problem of environmental pollution caused by solid wastes (semicoke and residual oil), and finally realize the clean and efficient utilization of biomass and residual oil.
Drawings
FIG. 1 is a schematic diagram of a comprehensive utilization system of the present invention;
the reference numerals in the figures indicate: the device comprises a tank farm raw material tank 1, a delivery pump 2, a device raw material tank 3, a two-wire heat exchanger 4, a three-wire heat exchanger 5, a tower bottom primary heat exchanger 6, a tower bottom secondary heat exchanger 7, a primary distillation tower 8, a first main condenser 9, a main finished product collecting tank 10, a heating gasification furnace 11, a biomass pyrolysis reactor 12, a combustion furnace 13, a reduced pressure rectifying tower 14, a second condenser 15, a first auxiliary condenser 16, a second auxiliary condenser 17, a third auxiliary condenser 18, a first auxiliary finished product collecting tank 19, a second auxiliary finished product collecting tank 20 and a third auxiliary finished product collecting tank 21.
Detailed Description
The invention will now be described in detail with reference to the drawings and specific examples. The present embodiment is implemented on the premise of the technical scheme of the present invention, and a detailed implementation manner and a specific operation process are provided, but the protection scope of the present invention is not limited to the following embodiments.
Examples
A multi-generation comprehensive utilization system for processing residual oil by volatilizing biomass, referring to fig. 1, the system comprises:
the fuel oil main output unit is used for extracting fuel oil in the heavy raw oil;
the vaporization unit is used for vaporizing light components and heavy components in the heavy raw oil;
a fuel oil byproduct extraction unit for extracting fuel oil from heavy components in the heavy raw oil;
a biomass pyrolysis unit for providing volatiles into the system;
the vaporization unit and the fuel oil main output unit are overlapped in the primary distillation tower 8; the vaporization unit and the fuel oil byproduct unit are overlapped in the vacuum rectification tower 14;
the biomass pyrolysis unit and the vaporization unit are overlapped with each other in the vacuum rectifying tower 14 and the primary distillation tower 8; the biomass pyrolysis unit and the fuel oil byproduct unit are overlapped in the vacuum rectifying tower 14 and the combustion furnace 13; the biomass pyrolysis unit and the fuel oil main output unit are overlapped on the device raw material tank 3 and the primary distillation tower 8.
The main fuel oil output unit comprises the following components: the device raw material tank 3 is used for preheating heavy raw material oil; the device raw material tank 3 is provided with an outlet, and water and a small amount of impurities are discharged from the bottom of the tank; the primary distillation tower 8 is used for fractionating heavy raw oil; a main finished product collection tank 10 for collecting the first-line fuel oil extracted by fractionation; the primary distillation tower 8 is connected with the vaporization unit through a tower top discharging pipe a and a tower bottom discharging pipe c respectively, and the primary distillation tower 8 is connected with the main finished product collecting tank 10 through a side discharging pipe b; and a reflux pipeline connected with the primary tower 8 is also arranged on the side discharge pipe.
The fuel oil main output unit further comprises a tank farm raw material tank 1 for storing heavy raw material oil, a conveying pump 2 is arranged between the tank farm raw material tank 1 and a device raw material tank 3, and a heat exchanger group is arranged between the device raw material tank 3 and a primary distillation tower 8; the heat exchanger group comprises a two-wire heat exchanger 4, a three-wire heat exchanger 5 and a tower bottom heat exchanger which are mutually connected in parallel, and the tower bottom heat exchanger comprises a tower bottom primary heat exchanger 6 and a tower bottom secondary heat exchanger 7 which are mutually connected in series.
The vaporization unit comprises a heating vaporization furnace 11, a primary distillation tower 8 and a reduced pressure rectifying tower 14; the primary distillation tower 8 is connected with the heating gasification furnace 11 through a tower top discharging pipe a and a tower bottom discharging pipe c respectively, the heating gasification furnace 11 is connected with the reduced pressure rectifying tower 14, and the reduced pressure rectifying tower 14 is connected with the tower top discharging pipe a through a tower top discharging pipe A; the tower top discharging pipe a is also provided with a first main condenser 9, and the tower top discharging pipe a is also provided with a second condenser 15.
The fuel oil byproduct outlet unit comprises a decompression rectifying tower 14, a finished product collecting tank area and a combustion furnace 13; the finished product collection tank farm comprises a first secondary product collection tank 19, a second secondary product collection tank 20 and a third secondary product collection tank 21; the pressure reducing rectifying tower 14 is connected with the discharge pipe B through a first side line 1 Connected with a first auxiliary finished product collecting tank 19, the pressure reducing rectifying tower 14 is connected with a second side line discharging pipe B 2 Connected with a second secondary product collecting tank 20, the pressure reducing rectifying tower 14 is connected with a third side line discharging pipe B 3 Is connected with a third subsidiary product collection tank 21; the vacuum rectifying tower 14 is connected with the combustion furnace 13 through a tower bottom discharging pipe C; first side line discharging pipe B 1 The upper part is also provided with a first auxiliary condenser 16 and a second side discharge pipe B 2 The upper part is also provided with a second auxiliary condenser 17 and a third side discharge pipe B 3 A third sub-condenser 18 is also provided. First side line discharging pipe B 1 And/or a second side tapping pipe B 2 The device is in heat exchange connection with a device raw material tank 3; first side line discharging pipe B 1 And/or a second side tapping pipe B 2 And is provided with a reflux pipeline connected with the decompression rectifying tower 14.
The biomass pyrolysis unit comprises a device raw material tank 3, a primary distillation tower 8, a biomass pyrolysis reactor 12, a combustion furnace 13 and a reduced pressure rectifying tower 14; the combustion furnace 13 is respectively connected with the biomass pyrolysis reactor 12 and the device raw material tank 3 in a heat exchange manner; the discharge port of the biomass pyrolysis reactor 12 is respectively connected with a vacuum rectifying tower 14, a primary distillation tower 8 and a combustion furnace 13, and the biomass pyrolysis reactor 12 is connected with a device material tank 3 in a heat exchange manner.
A treatment process of a poly-generation comprehensive utilization system for processing residual oil based on the above biomass volatilization, which comprises the following steps:
(a) Feeding heavy raw oil in a raw material tank 1 of a tank farm into a raw material tank 3 of the device by a delivery pump 2, and heating the raw material tank 3 of the device; heating the raw material tank 3 at 70 ℃ and standing for 2 hours;
(b) The heavy raw oil enters a primary distillation tower 8 for reduced pressure distillation after heat is recovered by a heat exchanger group;
(c) The fraction distilled under reduced pressure in the primary distillation tower 8 enters a main finished product collecting tank 10 and a heating gasification furnace 11 respectively, and enters a reduced pressure rectifying tower 14 after being heated by the heating gasification furnace 11;
the method comprises the following steps: the distillate at the top of the primary distillation tower 8 is condensed by a first main condenser 9 and then is collected and timely sent into a heating vaporization furnace 11 to be burnt as fuel;
the side line distillate of the primary distillation tower 8 is first-line fuel oil, one part of the side line distillate is returned to the primary distillation tower 8 by a reflux pump and used for controlling the temperature of the primary distillation tower, and the other part of the side line distillate enters a main finished product collecting tank 10 and is sold as a product;
the residual materials in the primary distillation tower 8 enter a heating vaporization furnace 11 for heating, and enter a reduced pressure rectifying tower 14 after being heated by the heating vaporization furnace 11;
the top fraction of the primary distillation tower 8 is mixed oil gas at 50 ℃, and the side fraction of the primary distillation tower 8 is first-line fuel oil at 150 ℃; the heating temperature of the heating vaporization furnace 11 is 380 ℃;
(d) The fractions distilled under reduced pressure in the reduced pressure rectifying tower 14 enter a finished product collecting tank area, a combustion furnace 13 and a heating vaporization furnace 11 respectively;
the step (d) is specifically as follows: the top fraction of the vacuum rectifying tower 14 is cooled by a second condenser 15 and then is sent to a heating vaporization furnace 11 to be used as fuel;
the first side-draw fraction from the vacuum distillation column 14 is first line fuel oil, cooled by a first secondary condenser 16 and sent to a first secondary product collection tank 19 for sale as a product.
The second side stream of the vacuum rectifying tower 14 is two-line fuel oil, after heat exchange with the device raw material tank 3, the second side stream is cooled by the second auxiliary condenser 17, and a part of the second side stream is pumped back to the vacuum rectifying tower 14 by a reflux pump for controlling the side stream temperature of the rectifying tower; a portion is pumped to a finished second by-product collection tank 20 for sale as a product;
the third side stream of the vacuum rectifying tower 14 is three-wire fuel oil, after heat exchange with the device raw material tank 3, the third side stream is cooled by the third auxiliary condenser 18, a part of the fuel oil is pumped back to the vacuum rectifying tower 14 by a reflux pump for controlling the side stream temperature of the rectifying tower, and the other part of fuel oil enters the third auxiliary finished product collecting tank 21 to be sold as a product;
the bottom fraction of the vacuum rectifying tower 14 is vacuum residue, namely heavy oil, enters the combustion furnace 13 to be combusted together with semicoke generated in the biomass pyrolysis reactor 12, heat is provided for the biomass pyrolysis reactor 12 to realize heat circulation, and in addition, the bottom fraction of the vacuum rectifying tower 14 can be reused through the combustion furnace 13 and can be sold as commodity oil after being cooled through a condenser, so that both methods are feasible;
the operating temperature of the burner 13 is 850-900 c. The method has the advantages that the generation and emission of NOx are effectively controlled, the activity of ash is favorably kept, the content of bottom ash and fly ash in the burned ash is less than 2%, the burned ash can be directly used as building materials, and further high-added-value products such as bricks, cement and the like are manufactured by using the burned ash as the building materials so as to be fully utilized, so that the recycling utilization of semicoke and ash is realized, and the environmental pollution is effectively reduced.
The overhead fraction of the vacuum distillation column 14 is a mixed oil gas at 50 ℃, the first side-cut fraction of the vacuum distillation column 14 is a first-line fuel oil at 150 ℃, the second side-cut fraction of the vacuum distillation column 14 is a second-line fuel oil at a liquid phase temperature of 240 ℃, the third side-cut fraction of the vacuum distillation column 14 is a third-line fuel oil at a liquid phase temperature of 320 ℃, and the bottom fraction of the vacuum distillation column 14 is a vacuum residue at 360 ℃.
(e) Volatile matters generated in the biomass pyrolysis reactor 12 enter a vacuum rectifying tower 14 and a primary distillation tower 8, and micromolecular substances in the volatile matters generated after biomass pyrolysis can improve the C/H atomic ratio of oil production of each line and improve the quality of the produced oil; and meanwhile, the generated heat exchanges heat with the raw material tank 3 of the device, so that the heavy raw material oil is heated, and the heat is reused.
In summary, the main technical point of the invention is that the biomass pyrolysis reactor 12 is added before the rectifying tower, the volatile matters generated by biomass pyrolysis have a large amount of heat and small molecular substances, and the quality of the commodity oil in the primary distillation tower 8 and the vacuum rectifying tower 14 is greatly improved by utilizing the volatile matters of biomass similar to hydrogenation reaction, and meanwhile, residual oil is also positioned at an important position in the whole energy and heat circulation, so that the heat closed loop is completed. In the reaction process, the selection of biomass can be diversified, and the reaction and the system have wide adaptability to raw materials and high comprehensive utilization degree. The small molecular substances contained in the biomass volatile matters can improve the rectification oil yield in the whole system, simultaneously avoid the problem of environmental pollution caused by solid wastes (semicoke and residual oil), comprehensively consider the resource, environment and social and economic benefits, and realize the scientific utilization of biomass and residual oil.
The invention designs the whole link into a closed loop, does not need to provide heat from the outside, is self-sufficient, and completes the circulation of the whole system. The invention organically combines biomass, heavy raw oil, residual oil and the like, and realizes scientific, efficient and comprehensive utilization of biomass energy. Semicoke generated by biomass pyrolysis can be continuously combusted to provide heat, so that heat coupling is realized.
The above description is only a preferred embodiment of the present invention, and is not intended to limit the invention in any way, and any person skilled in the art may make modifications or alterations to the disclosed technical content to the equivalent embodiments. However, any simple modification, equivalent variation and variation of the above embodiments according to the technical substance of the present invention still fall within the protection scope of the technical solution of the present invention.
Claims (4)
1. A poly-generation comprehensive utilization system for processing residual oil by volatilizing biomass, which is characterized by comprising:
the fuel oil main output unit is used for extracting fuel oil in the heavy raw oil;
the vaporization unit is used for vaporizing light components and heavy components in the heavy raw oil;
a fuel oil byproduct extraction unit for extracting fuel oil from heavy components in the heavy raw oil;
a biomass pyrolysis unit for providing volatiles into the system;
the vaporization unit and the fuel oil main output unit are overlapped in the primary distillation tower (8); the vaporization unit and the fuel oil byproduct unit are overlapped in the vacuum rectifying tower (14);
the biomass pyrolysis unit and the vaporization unit are overlapped in the vacuum rectifying tower (14) and the primary distillation tower (8); the biomass pyrolysis unit and the fuel oil byproduct unit are overlapped in the vacuum rectifying tower (14) and the combustion furnace (13); the biomass pyrolysis unit and the fuel oil main output unit are overlapped on the device raw material tank (3) and the primary distillation tower (8);
the main fuel oil output unit comprises the following components:
the device raw material tank (3) is used for preheating heavy raw oil;
a primary distillation tower (8) for fractionating heavy raw oil;
a main finished product collection tank (10) for collecting the first-line fuel oil extracted by fractionation;
the primary distillation tower (8) is connected with the vaporization unit through a tower top discharging pipe a and a tower bottom discharging pipe c respectively, and the primary distillation tower (8) is connected with the main finished product collecting tank (10) through a side discharging pipe b;
a reflux pipeline connected with the primary tower (8) is further arranged on the side discharge pipe;
the main fuel oil output unit also comprises a tank area raw material tank (1) for storing heavy raw material oil, a conveying pump (2) is arranged between the tank area raw material tank (1) and a device raw material tank (3), and a heat exchanger group is arranged between the device raw material tank (3) and a primary distillation tower (8);
the heat exchanger group comprises a two-wire heat exchanger (4), a three-wire heat exchanger (5) and a tower bottom heat exchanger which are connected in parallel, and the tower bottom heat exchanger comprises a tower bottom primary heat exchanger (6) and a tower bottom secondary heat exchanger (7) which are connected in series;
the vaporization unit comprises a heating vaporization furnace (11), a primary distillation tower (8) and a decompression rectifying tower (14);
the primary distillation tower (8) is connected with the heating gasification furnace (11) through a tower top discharging pipe a and a tower bottom discharging pipe c respectively, the heating gasification furnace (11) is connected with the reduced pressure rectifying tower (14), and the reduced pressure rectifying tower (14) is connected with the tower top discharging pipe a through a tower top discharging pipe A;
the tower top discharging pipe a is also provided with a first main condenser (9), and the tower top discharging pipe A is also provided with a second condenser (15);
the fuel oil byproduct outlet unit comprises a decompression rectifying tower (14), a finished product collecting tank area and a combustion furnace (13);
the finished product collecting tank area comprises a first auxiliary finished product collecting tank (19), a second auxiliary finished product collecting tank (20) and a third auxiliary finished product collecting tank (21); the pressure-reducing rectifying tower (14) is connected with the first side line discharging pipe B 1 Is connected with a first auxiliary finished product collecting tank (19), and the vacuum rectifying tower (14) is connected with a second side discharge pipe B 2 Is connected with a second byproduct collecting tank (20), and the vacuum rectifying tower (14) is connected with a third side discharge pipe B 3 Is connected with a third auxiliary finished product collecting tank (21);
the vacuum rectifying tower (14) is connected with the combustion furnace (13) through a tower bottom discharging pipe C;
the first side line discharging pipe B 1 The upper part is also provided with a first auxiliary condenser (16), and the second side discharge pipe B 2 A second auxiliary condenser (17) is also arranged on the upper part, and the third side line discharging pipe B 3 A third auxiliary condenser (18) is also arranged on the upper part;
the first side line discharging pipe B 1 And/or a second side tapping pipe B 2 The device is in heat exchange connection with a raw material tank (3); the first side line discharging pipe B 1 And/or a second side tapping pipe B 2 A reflux pipeline connected with the decompression rectifying tower (14) is arranged on the upper part;
the biomass pyrolysis unit comprises a device raw material tank (3), a primary distillation tower (8), a biomass pyrolysis reactor (12), a combustion furnace (13) and a reduced pressure rectifying tower (14);
the combustion furnace (13) is respectively connected with the biomass pyrolysis reactor (12) and the device raw material tank (3) in a heat exchange manner; the discharge port of the biomass pyrolysis reactor (12) is respectively connected with a decompression rectifying tower (14), a primary distillation tower (8) and a combustion furnace (13), and the biomass pyrolysis reactor (12) is connected with a device raw material tank (3) in a heat exchange manner.
2. A process for treating a multi-cogeneration integrated utilization system based on the biomass volatilizing treatment residual oil of claim 1, characterized in that the process comprises the following steps:
(a) Feeding heavy raw oil in a raw material tank (1) of a tank farm into a raw material tank (3) of the device by a delivery pump (2), and heating the raw material tank (3) of the device;
(b) The heavy raw oil enters a primary distillation tower (8) for reduced pressure distillation after heat is recovered by a heat exchanger group;
(c) The fraction distilled under reduced pressure in the primary distillation tower (8) enters a main finished product collecting tank (10) and a heating gasification furnace (11) respectively, and enters a reduced pressure rectifying tower (14) after being heated by the heating gasification furnace (11)
(d) The fractions distilled under reduced pressure in the reduced pressure rectifying tower (14) respectively enter a finished product collecting tank area, a combustion furnace (13) and a heating vaporization furnace (11);
(e) Volatile matters generated in the biomass pyrolysis reactor (12) enter a vacuum rectifying tower (14) and a primary distillation tower (8); and the generated heat exchanges heat with the raw material tank (3) of the device to heat the heavy raw material oil.
3. A treatment process according to claim 2, wherein step (c) is specifically:
the distillate at the top of the primary distillation tower (8) is condensed by a first main condenser (9) and then is collected and timely sent into a heating vaporization furnace (11) to be burnt as fuel;
the side line distillate of the primary distillation tower (8) is first-line fuel oil, one part of the side line distillate is pumped back to the primary distillation tower (8) by a reflux pump, and the other part of the side line distillate enters a main finished product collecting tank (10) and is sold as a product;
the residual materials in the primary distillation tower (8) enter a heating vaporization furnace (11) for heating, and enter a vacuum rectification tower (14) after being heated by the heating vaporization furnace (11);
the step (d) is specifically as follows:
the top fraction of the vacuum rectifying tower (14) is cooled by a second condenser (15) and then is sent to a heating gasification furnace (11) to be used as fuel;
the first side-line fraction of the vacuum rectifying tower (14) is first-line fuel oil, and is cooled by a first auxiliary condenser (16) and then sent to a first auxiliary finished product collecting tank (19) to be sold as a product;
the second side stream of the vacuum rectifying tower (14) is two-line fuel oil, and after heat exchange with a raw material tank (3) of the device, the second side stream is cooled by a second auxiliary condenser (17), and part of the second side stream is pumped back to the vacuum rectifying tower (14) by a reflux pump; a portion is pumped to a finished second sub-finished collection tank (20) for sale as a product;
the third side stream of the vacuum rectifying tower (14) is three-wire fuel oil, after heat exchange with a raw material tank (3) of the device, the third side stream is cooled by a third auxiliary condenser (18), part of the fuel oil is pumped back to the vacuum rectifying tower (14) by a reflux pump, and the other part of fuel oil enters a third auxiliary finished product collecting tank (21) to be sold as a product;
the bottom fraction of the vacuum rectifying tower (14) is vacuum residue, and enters a combustion furnace (13) to be combusted together with semicoke generated in the biomass pyrolysis reactor (12).
4. A treatment process according to claim 2, characterized in that the temperature of heating in the plant feed tank (3) is 65-75 ℃, standing 1.5-2.5h;
the top fraction of the primary distillation tower (8) is mixed oil gas at 45-55 ℃, and the side fraction of the primary distillation tower (8) is first-line fuel oil at 145-155 ℃; the heating temperature of the heating vaporization furnace (11) is 375-385 ℃;
the top fraction of the vacuum distillation tower (14) is mixed oil gas with the temperature of 45-55 ℃, the first side-line fraction of the vacuum distillation tower (14) is first-line fuel oil with the temperature of 145-155 ℃, the second side-line fraction of the vacuum distillation tower (14) is second-line fuel oil with the temperature of 235-255 ℃, the third side-line fraction of the vacuum distillation tower (14) is third-line fuel oil with the temperature of 315-325 ℃, and the bottom fraction of the vacuum distillation tower (14) is vacuum residue with the temperature of 355-365 ℃;
the operating temperature of the combustion furnace (13) is 850-900 ℃.
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| CN102041023A (en) * | 2009-10-16 | 2011-05-04 | 中国石油化工股份有限公司 | Method for improving residual oil hydrogenation by blending biological grease |
| CN106833736A (en) * | 2017-03-29 | 2017-06-13 | 山东铂铠环保科技有限公司 | A kind of method of waste oil regeneration base oil |
| CN109337703A (en) * | 2018-11-07 | 2019-02-15 | 山东理工大学 | A kind of biomass continous way is catalyzed preparation high-quality oil-gas integrating device online |
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| WO2012092468A1 (en) * | 2010-12-30 | 2012-07-05 | Kior Inc. | Production of renewable biofuels |
| US20150073188A1 (en) * | 2012-03-01 | 2015-03-12 | The Trustees Of Princeton University | Processes for producing synthetic hydrocarbons from coal, biomass, and natural gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102041023A (en) * | 2009-10-16 | 2011-05-04 | 中国石油化工股份有限公司 | Method for improving residual oil hydrogenation by blending biological grease |
| CN106833736A (en) * | 2017-03-29 | 2017-06-13 | 山东铂铠环保科技有限公司 | A kind of method of waste oil regeneration base oil |
| CN109337703A (en) * | 2018-11-07 | 2019-02-15 | 山东理工大学 | A kind of biomass continous way is catalyzed preparation high-quality oil-gas integrating device online |
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| 我国催化裂化能量回收机组的发展;吴文伟, 张涌, 凌之光;炼油设计(01);全文 * |
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