CN106635112A - Hydrothermal liquidization system and hydrothermal liquidization method for biomass - Google Patents
Hydrothermal liquidization system and hydrothermal liquidization method for biomass Download PDFInfo
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- CN106635112A CN106635112A CN201611270675.3A CN201611270675A CN106635112A CN 106635112 A CN106635112 A CN 106635112A CN 201611270675 A CN201611270675 A CN 201611270675A CN 106635112 A CN106635112 A CN 106635112A
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- 239000002028 Biomass Substances 0.000 title claims abstract description 72
- 238000000034 method Methods 0.000 title claims abstract description 23
- 238000006243 chemical reaction Methods 0.000 claims abstract description 110
- 239000000047 product Substances 0.000 claims description 237
- 239000000463 material Substances 0.000 claims description 99
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 56
- 239000012075 bio-oil Substances 0.000 claims description 49
- 238000001514 detection method Methods 0.000 claims description 26
- 238000003860 storage Methods 0.000 claims description 26
- 238000003756 stirring Methods 0.000 claims description 25
- 239000007790 solid phase Substances 0.000 claims description 21
- 239000006227 byproduct Substances 0.000 claims description 20
- 238000000605 extraction Methods 0.000 claims description 19
- 238000000935 solvent evaporation Methods 0.000 claims description 19
- 239000003921 oil Substances 0.000 claims description 12
- 239000006228 supernatant Substances 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 8
- 239000012263 liquid product Substances 0.000 claims description 7
- 238000002207 thermal evaporation Methods 0.000 claims description 6
- 239000000872 buffer Substances 0.000 claims description 5
- 238000004062 sedimentation Methods 0.000 claims description 5
- 238000013019 agitation Methods 0.000 claims description 4
- 230000008859 change Effects 0.000 claims description 4
- 238000004090 dissolution Methods 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 230000008602 contraction Effects 0.000 claims description 2
- 239000002775 capsule Substances 0.000 claims 1
- 238000007599 discharging Methods 0.000 abstract description 12
- 239000002002 slurry Substances 0.000 description 26
- 239000007789 gas Substances 0.000 description 22
- 238000012360 testing method Methods 0.000 description 15
- 239000012530 fluid Substances 0.000 description 13
- 241000195493 Cryptophyta Species 0.000 description 12
- 239000008367 deionised water Substances 0.000 description 12
- 229910021641 deionized water Inorganic materials 0.000 description 12
- 230000005540 biological transmission Effects 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 10
- 239000007795 chemical reaction product Substances 0.000 description 8
- 239000002904 solvent Substances 0.000 description 8
- 235000017060 Arachis glabrata Nutrition 0.000 description 6
- 241001553178 Arachis glabrata Species 0.000 description 6
- 235000010777 Arachis hypogaea Nutrition 0.000 description 6
- 235000018262 Arachis monticola Nutrition 0.000 description 6
- 210000003608 fece Anatomy 0.000 description 6
- 239000010871 livestock manure Substances 0.000 description 6
- 235000020232 peanut Nutrition 0.000 description 6
- 230000000717 retained effect Effects 0.000 description 6
- 239000010802 sludge Substances 0.000 description 6
- 239000010902 straw Substances 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical group [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 230000001276 controlling effect Effects 0.000 description 5
- 238000013461 design Methods 0.000 description 5
- 239000000706 filtrate Substances 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000011031 large-scale manufacturing process Methods 0.000 description 4
- 238000011017 operating method Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 206010054949 Metaplasia Diseases 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000002242 deionisation method Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 150000002632 lipids Chemical class 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000015689 metaplastic ossification Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 239000012066 reaction slurry Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000013517 stratification Methods 0.000 description 1
- 230000007306 turnover Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/008—Controlling or regulating of liquefaction processes
-
- 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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (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 discloses a hydrothermal liquidization system and a hydrothermal liquidization method for biomass, relates to the technical field of biomass energy and aims to solve the problem that the hydrothermal liquidization system for the biomass in the prior art difficultly carries out continuous reaction of continuous feeding and continuous discharging. The hydrothermal liquidization system for the biomass provided by the invention comprises a reactor, a product collector and a flow control structure, wherein a feeding pipe and a product discharging pipe are connected to the reactor; a pressurizing device is serially connected onto the feeding pipe; the product collector is hermetically connected with the exhaust end of the product discharging pipe; the flow control structure is arranged between the product collector and the reactor and is used for controlling the flow, discharging to the product collector from the product discharging pipe, of the product, so that the discharging flow of the product discharging pipe is equal to the feeding flow of the feeding pipe. The hydrothermal liquidization system for the biomass, disclosed by the invention, is used for carrying out the continuous reaction of the continuous feeding and the continuous discharging.
Description
Technical field
The present invention relates to biomass energy technology field, more particularly to a kind of biomass by hydro-thermal liquefaction system and method.
Background technology
Biomass by hydro-thermal liquefaction technology is referred to using thermochemical method, in the presence of with or without catalyst, in high temperature
The conversion of biomass (such as silk algae, ball algae, sludge, peanut straw, pig manure etc.) raw material is made a living under the liquid phase hydrothermal condition of high pressure
The process of material oil.Biomass by hydro-thermal liquefaction technology is a kind of very biomass liquefaction technology with development prospect, with perhaps
Many advantages.First, traditional thermochemical study technology (as gasified and being pyrolyzed) is contrasted, biomass by hydro-thermal liquefaction technology can be direct
Undried wet biomass is converted into into the bio-oil of energy-intensive, is disappeared so as to avoid the additional high-energy of dry run
Consumption, therefore with lower energy expenditure rate, be particularly suitable for processing the wet biomass such as biomass.Secondly, biomass by hydro-thermal liquefaction
Grease in biomass not only can be changed into bio-oil, the protein that can also contain biomass and glucide by technology
It is also converted to the bio-oil of high heating value.Simultaneously there is biomass higher growth rate, growing environment to be not take up arable land, higher
Lipid content, huge environment and economic benefit can be produced.Therefore, the biomass liquid fuel life with biomass as raw material
Product technology possesses economic and technical feasibility, it has also become one of main development trend in the field, and it is carried for environmental pollution is alleviated
High-energy source is significant safely.
But, during biomass liquefaction reaction, because the reaction temperature and reaction pressure in reactor is generally even
(i.e. temperature requirement is 200～400 DEG C, pressure to be difficult to be maintained at the claimed range of liquefaction reaction during continuous charging and continuous discharge
Power requires to be 5～25Mpa) in, therefore biomass liquefaction reaction system is difficult to continuous feed and continuously goes out in prior art
The continuous reaction of material, is thus unfavorable for the large-scale production that biomass by hydro-thermal liquefies.
The content of the invention
The present invention provides a kind of biomass by hydro-thermal liquefaction system and method, can be during biomass liquefaction reaction by instead
Answer reaction temperature and reaction pressure in device to be held in liquefaction reaction claimed range so that liquefaction reaction can continuous feed and
Continuous discharge, is beneficial to the large-scale production of biomass by hydro-thermal liquefaction.
To reach above-mentioned purpose, embodiments of the invention are adopted the following technical scheme that：
On the one hand, the invention provides a kind of biomass by hydro-thermal liquefaction system, including：Reactor, the reactor is used for
Liquefaction reaction is carried out, the reactor is connected with feed pipe and product discharge pipe, on the feed pipe pressue device is serially connected with；Produce
Thing collector, the outlet side airtight connection of the product collector and the product discharge pipe；Flow control structure, the flow
Control structure is arranged between the product collector and the reactor, and is discharged by the product for controlling the product
Pipe is expelled to the flow of the product collector, so that the feed stream of the discharge flow of the product discharge pipe and the feed pipe
Amount is equal.
On the other hand, the invention provides a kind of biomass water heat liquefaction method, methods described includes：
S1, aqueous preheating material is pressed into into reactor by feed pipe and pressue device, and causes the preheating thing
Water in material receives thermal evaporation expansion in the reactor, to increase the temperature and pressure in the reactor, while by producing
Thing discharge pipe discharges pre- hot；
S2, when the temperature in the reactor increases to the second preset range, and pressure is increased in the first preset range,
The preheating material is replaced by into reaction mass, and is pressed into the reaction mass by the feed pipe and the pressue device
In the reactor, so that the reaction mass produces liquefaction reaction in the reactor and generates hydrothermal liquefaction product；
S3, the hydrothermal liquefaction product is expelled in product collector by product discharge pipe, and by flow control
Hydrothermal liquefaction product described in structure control is expelled to the flow of the product collector by the product discharge pipe, so that the product
The discharge flow of thing discharge pipe is equal with the feed rate of the feed pipe.
A kind of biomass by hydro-thermal liquefaction system and method that the present invention is provided, are passing through feed pipe and pressue device to reaction
In device after the aqueous preheating material of press-in, the water in preheating material can receive thermal evaporation expansion in reactor, by reactor
Interior temperature and pressure is increased to respectively in the second preset range and the first preset range, from there through the pre- thermal response of preheating material
Device；Afterwards, preheating material can be replaced by reaction mass, and reaction mass is pressed into by reactor by feed pipe and pressue device
It is interior, so that reaction mass is produced in the temperature in the second preset range and under the pressure environment in the first preset range
Liquefaction reaction, the product of liquefaction reaction is expelled in product collector by product discharge pipe, and by flow control structure control
The discharge flow of product discharge pipe, so that the discharge flow of product discharge pipe is equal with the feed rate of feed pipe, so as to by instead
The temperature and pressure in device is answered to be respectively retained in the second preset range and the first preset range.Thus, can be by feed pipe
With pressue device continuously to reactor feed, and while the material in reactor is continuously discharged by product discharge pipe, will be anti-
The temperature and pressure in device is answered to be maintained at respectively in the second preset range and the first preset range, so as to be capable of achieving biomass by hydro-thermal
The continuous reaction of liquefaction system, and then be conducive to the large-scale production of biomass by hydro-thermal liquefaction.
Description of the drawings
In order to be illustrated more clearly that the embodiment of the present invention or technical scheme of the prior art, below will be to embodiment or existing
The accompanying drawing to be used needed for having technology description is briefly described, it should be apparent that, drawings in the following description are only this
Some embodiments of invention, for those of ordinary skill in the art, on the premise of not paying creative work, can be with
Other accompanying drawings are obtained according to these accompanying drawings.
Fig. 1 is the first structural representation of embodiment of the present invention biomass by hydro-thermal liquefaction system；
Fig. 2 is second structural representation of embodiment of the present invention biomass by hydro-thermal liquefaction system；
Fig. 3 is the structural representation of flow control valve in embodiment of the present invention biomass by hydro-thermal liquefaction system；
Fig. 4 is the structural representation of filter in embodiment of the present invention biomass by hydro-thermal liquefaction system；
Fig. 5 is the flow chart of embodiment of the present invention biomass water heat liquefaction method.
Reference：
1- reactors；2- feed pipes；3- product discharge pipes；4- pressue devices；5- product collectors；6- flow controls
Structure processed；61- housings；62- runners；63- inverted cone-shaped valve ports；The tapered pins of 64-；65- leading screws；66- handles；67- products
Entrance；68- product exits；7- supplies gas supercharging device；8- counterbalance valves；9- extract injecting structures；10- stirring structures；
11- knockouts；12- filters；121- shells；122- inlets；123- leakage fluid drams；124- slag-drip openings；125- is filtered
Core；13- solvent evaporation devices；14- material storage devices；15- agitating devices；16- flow pulse buffers；17- particles
Device；18- preheating devices；100- first transmits pump；200- second transmits pump.
Specific embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is carried out clear, complete
Site preparation is described, it is clear that described embodiment is only a part of embodiment of the invention, rather than the embodiment of whole.It is based on
Embodiment in the present invention, it is every other that those of ordinary skill in the art are obtained under the premise of creative work is not made
Embodiment, belongs to the scope of protection of the invention.
In describing the invention, it is to be understood that term " " center ", " on ", D score, "front", "rear", " left side ",
The orientation or position relationship of the instruction such as " right side ", " vertical ", " level ", " top ", " bottom ", " interior ", " outward " is based on shown in the drawings
Orientation or position relationship, be for only for ease of description the present invention and simplify description, rather than indicate or imply indication device or
Element with specific orientation, with specific azimuth configuration and operation, therefore must be not considered as limiting the invention.
In description of the invention, unless otherwise stated, " multiple " are meant that two or more.
With reference to Fig. 1, Fig. 1 for embodiment of the present invention biomass by hydro-thermal liquefaction system a specific embodiment, the present embodiment
Biomass by hydro-thermal liquefaction system include：Reactor 1, the reactor 1 is used to carry out liquefaction reaction, and the reactor 1 connects
There are feed pipe 2 and product discharge pipe 3, pressue device 4 is serially connected with the feed pipe 2；Product collector 5, the collection of products
The outlet side airtight connection of device 5 and the product discharge pipe 3；Flow control structure 6, the flow control structure 6 is arranged at institute
State between product collector 5 and the reactor 1, and for control the product be expelled to by the product discharge pipe 3 it is described
The flow of product collector 5, so that the discharge flow of the product discharge pipe 3 is equal with the feed rate of the feed pipe 2.
A kind of biomass by hydro-thermal liquefaction system that the present invention is provided, is passing through feed pipe 2 and pressue device 4 to reactor 1
After the aqueous preheating material of interior press-in, the water in preheating material can receive thermal evaporation expansion in reactor 1, by reactor 1
Interior temperature and pressure is increased to respectively in the second preset range and the first preset range, has been preheated instead from there through preheating material
Answer device 1；Afterwards, preheating material can be replaced by reaction mass, and is pressed into reaction mass by feed pipe 2 and pressue device 4
In reactor 1, so that reaction mass is in the temperature and the pressure rings in the first preset range in the second preset range
Liquefaction reaction is produced under border, the product of liquefaction reaction is expelled in product collector 5 by product discharge pipe 3, and by flow control
The discharge flow of the control product of structure processed 6 discharge pipe 3, so that the feed rate of the discharge flow of product discharge pipe 3 and feed pipe 2
It is equal, so as to the temperature and pressure in reactor 1 is respectively retained in the second preset range and the first preset range.Thus,
Continuous to the feed of reactor 1 by feed pipe 2 and pressue device 4, and reactor 1 can continuously be discharged by product discharge pipe 3
While interior material, the temperature and pressure in reactor 1 is maintained at respectively in the second preset range and the first preset range,
So as to be capable of achieving the continuous reaction of biomass by hydro-thermal liquefaction system, and then be conducive to the scale metaplasia of biomass by hydro-thermal liquefaction
Produce.
It should be noted that due to when the discharge flow of product discharge pipe 3 is more than the feed rate of feed pipe 2, reacting
Material amount retained in device 1 is reduced, therefore the reaction pressure in reactor 1 is reduced, while during stop of the material in reactor 1
Between shorten, heat time of the material in reactor 1 shortens, and reaction temperature in reactor 1 is reduced；Conversely, when product is discharged
When the discharge flow of pipe 3 is less than the feed rate of feed pipe 2, the material amount retained in reactor 1 gradually rises, therefore reactor
Reaction pressure increase in 1, while the time of staying of the material in reactor 1 is elongated, heat time of the material in reactor 1
Elongated, the reaction temperature in reactor 1 is raised.Therefore, only when the discharge flow of product discharge pipe 3 is equal to entering for feed pipe 2
During stream amount, the reaction temperature and reaction pressure in reactor 1 just can be respectively retained in the second preset range and first presets
In the range of.
Wherein, preheating material can be water, or the mixture of biomass and water composition, here does not do concrete limit
It is fixed.Reaction mass is the mixture that biomass and water are constituted.
In addition, it is necessary to explanation, the first preset range is for needed for reaction mass in reactor 1 can carry out liquefaction reaction
Pressure limit, temperature range of second preset range for needed for reaction mass in reactor 1 can carry out liquefaction reaction.
Furthermore, product is continuously received in order to pass through product collector 5, preferred product collector 5 is multiple, when many
One in individual product collector 5, can be using other collection of products when for collecting the product discharged by product discharge pipe 3
Device 5 carries out the operation such as extraction or separation of product, and from there through product collector 5 the continuous reception of product is capable of achieving.Wherein, produce
The quantity of thing collector 5 can be two, three or four etc., and here is not specifically limited.
In the embodiment shown in fig. 1, reactor 1 can be tubular reactor, or tank reactor, here is not
It is specifically limited.
In the embodiment shown in fig. 1, pressue device 4 is used to material is pressed in reactor 1 along charging 2, it is preferable that pressurization
Device 4 is high-pressure plunger pump, and the power of high-pressure plunger pump is strong, and is easy to the intrusion for controlling to calculate reactant.
In order to control the flow that product is expelled to product collector 5 by product discharge pipe 3, flow control structure 6 specifically may be used
Including the flow control valve being serially connected with product discharge pipe 3, by adjusting the aperture of flow control valve product edge is can control
Product discharge pipe 3 is expelled to the flow of product collector 5, so that the feed stream of the discharge flow of product discharge pipe 3 and feed pipe 2
Amount is equal.
Wherein, the concrete structure of flow control valve is not limited, as long as can realize that product is arranged by flow control valve
The regulation of the discharge flow of outlet pipe 3.Example, flow control valve can be made as structure shown in Fig. 3, i.e. flow control valve
Including housing 61, housing 61 is provided with product inlet 67 and product exit 68, in housing 61, product inlet 67 and product exit 68
Between be formed with runner 62, inverted cone-shaped valve port 63 is provided with runner 62, also including tapered pin 64, the diameter small end of tapered pin 64
Fit through in inverted cone-shaped valve port 63, the end that is relatively large in diameter of tapered pin 64 is connected with leading screw 65, and leading screw 65 is stretched out outside housing 61,
And the axis of leading screw 65 is conllinear with the axis of tapered pin 64, the position of correspondence leading screw 65 offers and leading screw 65 on housing 61
The screwed hole that upper screw thread coordinates, leading screw 65 stretches out the one end outside housing 61 and is connected with handle 66, is by the rotating threaded shaft of handle 66
The aperture of adjustable valve port 63, thus have adjusted the aperture of flow control valve.
In addition, flow control valve can be manually operated being adjusted, it is also possible to be adjusted by automatically controlling,
This is not specifically limited.But, because compared to adjusting manually, the degree of regulation for automatically adjusting and accuracy are generally higher, because
This preferred flow control valve is automatically adjusted by automatically controlling, specifically, in order to realize flow control valve aperture from
It is dynamic to adjust, following two concrete implementation modes can be included：
The first implementation：Flow control structure 6 also includes pressure sensing cell (not shown) and the first control
Unit (not shown), pressure sensing cell is located in reactor 1, and for detecting the reaction pressure in reactor 1, first
Control unit is used for the pressure value detected according to pressure sensing cell, controls to adjust the aperture of flow control valve.
Specifically, the control and regulation process of the first control unit can be：When pressure sensing cell is detected in reactor 1
Reaction pressure force value less than minimum of a value in the first preset range when, opening for flow control valve is turned in the control of the first control unit down
Degree, to increase the reaction pressure in reactor 1；When pressure sensing cell detects reaction pressure force value in reactor 1 more than the
During maximum in one preset range, the control of the first control unit tunes up the aperture of flow control valve, to reduce in reactor 1
Reaction pressure.
Second implementation：Flow control structure 6 also includes first flow detector unit (not shown), second
Amount detection unit (not shown) and the second control unit (not shown), first flow detector unit is used to detect charging
The feed rate of pipe 2, second flow detector unit is used for the rate of discharge of detection flows regulating valve, when second flow detector unit
When the flow value that detection is obtained is unequal with the flow value that the detection of first flow detector unit is obtained, the control of the second control unit is adjusted
The aperture of throttling adjustable valve.
Specifically, the control and regulation process of the second control unit can be：When second flow detector unit detects what is obtained
When flow value is less than the flow value that the detection of first flow detector unit is obtained, the control of the second control unit tunes up flow control valve
Aperture；When the flow value that the detection of second flow detector unit is obtained detects the flow value for obtaining more than first flow detector unit
When, the aperture of flow control valve is turned in the control of the second control unit down.Thus the discharge flow and feed pipe 2 of product discharge pipe 3 are made
Feed rate it is equal.
Further, for the reaction pressure in the holding reactor 1 during liquefaction reaction, it is preferred that such as Fig. 2 institutes
Show, what biomass by hydro-thermal liquefaction system also included being connected with product collector 5 supply gas supercharging device 7 and be arranged at collection of products
Counterbalance valve 8 on device 5, supercharging device 7 of supplying gas was used for before product collector 5 is connected with the outlet side of product discharge pipe 3, to
Conveying gas in product collector 5, so that the pressure in product collector 5 increases to, back pressure equal with the pressure in reactor 1
The pressure adjustable section of valve 8 is extremely equal with the pressure in reactor 1.Thus, can be in product collector 5 and the row of product discharge pipe 3
Before going out end connection, the pressure of counterbalance valve 8 is adjusted, so that the pressure of counterbalance valve 8 is equal with the pressure in reactor 1, and passed through
Supercharging device 7 of supplying gas conveys gas into product collector 5, so that the pressure in product collector 5 and the pressure in reactor 1
It is equal, now, after the outlet side of product discharge pipe 3 is connected with this product collector 5, the pressure in product collector 5
All the time balance with the reaction pressure in reactor 1, the reaction pressure in reactor 1 is thus maintained during liquefaction reaction.
Wherein, the product of the gas for conveying into product collector 5 for the supercharging device 7 that prevents from supplying gas and liquefaction reaction it
Between produce chemical reaction, the gas that supercharging device 7 of preferably supplying gas is conveyed into product collector 5 is the relatively low gas or lazy of activity
Property gas.Further, it is preferable that this gas is nitrogen, nitrogen is the low activity gas being widely present in nature, therefore easily
Realize, and cost is relatively low.
In addition, being additionally provided with relief valve (not shown) in product collector 5, relief valve is used in product collector 5
Pressure is reduced to normal pressure.
Specifically, supercharging device 7 of supplying gas can be made as structure as shown in Figure 2, i.e. supercharging device of supplying gas includes gas
Source, snorkel and the air delivery pump being serially connected with snorkel, snorkel is connected between source of the gas and product collector 5, air delivery pump
For the gas in source of the gas to be pressed into along product collector 5 along snorkel.
In the embodiment shown in fig. 1, product collector 5 can only as the collection vessel of product, then again by product
The bio oil that product in collection vessel is wrapped up in being passed through in other extraction equipment to extract solid phase material residue, product collector
5 can also as the container of extraction equipment for bio oil extraction, here is not specifically limited.But, in order to reduce life
The quantity of the parts included by material hydrothermal liquefaction system, with cost-effective, it is preferred to use above-mentioned second scheme, i.e. produce
Thing collector 5 as extraction equipment container for bio oil extraction, specifically, as shown in Fig. 2 product collector 5 is wrapped
Extract injecting structure 9 and stirring structure 10 are included, extract injecting structure 9 is used to inject extract into product collector 5, stirs
Product and extract that structure 10 is used to stir in product collector 5 are mixed, so that the bio oil in extract dissolution product, thus
The extraction of bio oil can be realized by being connected with the product collector 5 of extract injecting structure 9 and stirring structure 10, is being extracted
Cheng Hou, can stand the product and extract in product collector 5 so that in product solid phase material residue sedimentation, and with by water, dissolving
The liquid product being made up of the extract of bio oil is layered, with obtain solid phase material residue and by water, be dissolved with the extract of bio oil
The liquid product of composition, wherein, the solid phase material residue positioned at lower floor can be discharged by f passages.
Further, in order to separate liquid product in water and be dissolved with the extract of bio oil, to realize the conjunction of resource
Reason is utilized, as shown in Fig. 2 biomass by hydro-thermal liquefaction system also includes knockout 11, knockout 11 is for multi_layer extraction product receipts
Water in storage 5 and the extract of bio oil is dissolved with, with the extract for obtaining water respectively He be dissolved with bio oil, wherein,
After water is by the discharge of h passages, can be recycled as water for industrial use, and the extract for being dissolved with bio oil is biological oil product
Produce raw material, it is achieved thereby that the reasonable utilization of resource, while concentrating bio oil mixed liquor.
Before the liquid product in product collector 5 is passed through into knockout, in order to remove liquid product in remain consolidate
Phase material residue, to avoid the solid phase material residue pollution for remaining or block knockout, it is preferred that as shown in Fig. 2 biomass by hydro-thermal liquefaction system
System also includes filter 12, and filter 12 is used for water in by product collector 5 and is dissolved with the extraction of bio oil
Liquid is passed through before knockout 11, is filtered water and is dissolved with the solid phase material residue of residual in the extract of bio oil, to prevent solid phase
Material residue is polluted or blocked in knockout.Wherein, in product collector 5 water and it is dissolved with the extraction of bio oil
Liquid can be pumped in filter 12 by the first transmission pump 100, in addition, the solid phase material residue that filter 12 is filtered can be led to by g
Discharge in road.
Wherein, the concrete structure of filter 12 can be made as structure as shown in Figure 4, i.e. filter 12 includes outer
Shell 121, the top of shell 121 is provided with inlet 122, and inlet 122 is connected with product collector 5, and the bottom of shell 121 is provided with
Filter core 125 is provided with leakage fluid dram 123 and slag-drip opening 124, shell 121, the outlet of filter core 125 is connected with leakage fluid dram 123.
In order to prevent solid phase material residue from blocking the entrance of filter core 125, it is preferred that the entrance of filter core 125 is located at the upper of slag-drip opening 124
Side, thus prevent the entrance that solid phase material residue blocks filter core 125.
Further, for the water for removing the solvent being dissolved with the extract of bio oil and remain, to obtain bio oil
Product, it is preferred that as shown in Fig. 2 biomass by hydro-thermal liquefaction system also includes solvent evaporation device 13, solvent evaporation device 13 is used
In the isolated extract being dissolved with the extract of bio oil of evaporative removal knockout 11 and the water of residual, to obtain life
Thing oil.Wherein, the extract for being dissolved with bio oil that knockout 11 is isolated can pump into solvent steaming by the second transmission pump 200
In transmitting apparatus 13, and the thermal medium that solvent evaporation device 13 is adopted is passed through in solvent evaporation device 13 by j passages, and is led to by k
Solvent evaporation device 13 is discharged in road, and the water for evaporating and extract are discharged by i passages, and biological oil product is discharged by l passages.
In the embodiment shown in fig. 1, for the ease of providing reaction mass into reactor 1, it is preferred that as shown in Fig. 2
Also include storing reaction mass in material storage device 14, material storage device 14, material storage device 14 is connected to charging
The arrival end of pipe 2, for providing reaction mass to feed pipe 2.
Wherein, in order to prevent reaction mass from producing layering because long-time stands in material storage device 14, so as to lead
Cause the reacting material concentration in reactor 1 uneven, it is preferred that as shown in Fig. 2 being provided with stirring dress in material storage device 14
15 are put, agitating device 15 is used to during feed flow stir the reaction mass in material storage device 14, to prevent reaction mass
Produce stratification.
In the embodiment shown in fig. 1, in order to reduce the output flow pulse of pressue device 2, it is preferred that as shown in Fig. 2
Biomass by hydro-thermal liquefaction system also includes flow pulse buffer 16, and flow pulse buffer 16 includes cystic container (in figure not
Illustrate) and housing (not shown) outside cystic container is covered at, cystic container is serially connected with pressue device 4 and reactor 1
Between feed pipe 2 on, cystic container by resilientiy stretchable material make, housing by rigid material make, cystic container expansion
Maximum volume afterwards more than housing volume, and cystic container in contraction state when and inner walls between have gap.
Thus the reaction mass that pressue device 4 is discharged can be cached to cystic container, and in the presence of cystic container elastic contractile force
Gradually it is expelled in reactor 1, thus reduces the output flow pulse of pressue device 4.
Further, in order to improve the liquefaction reaction efficiency of reaction mass, it is preferred that as shown in Fig. 2 material storage device
14 porch is connected with crushed aggregates device 17, crushed aggregates device 17 be used for by reaction mass store to material storage device 14 it
Before, reaction mass is crushed to below 100 mesh, to improve the efficiency of liquefaction reaction.
Wherein, crushed aggregates device 17 can be pulverizer or colloid mill etc., and here is not specifically limited.
In order to reduce the operating cost of biomass by hydro-thermal liquefaction system, capacity usage ratio is improved, it is preferred that as shown in Fig. 2
Biomass by hydro-thermal liquefaction system also includes preheating device 18, and preheating device 18 includes outer tube (not shown) and positioned at outer tube
Interior inner tube (not shown), has clearance channel between outer tube and inner tube, inner tube is serially connected with feed pipe 2, clearance channel
In being serially connected with product discharge pipe 3, or, inner tube is serially connected with product discharge pipe 3, and clearance channel is serially connected with feed pipe 2.Thus
Make use of the waste heat after liquefaction reaction to carry out the material before pre- thermal response, so as to reduce the operation of biomass by hydro-thermal liquefaction system into
This, improves capacity usage ratio.
In the embodiment shown in Fig. 1 or Fig. 2, preferred reactor 1 be magnetic agitation reactor, magnetic agitation reactor energy
Enough stirring reaction materials during the course of the reaction, thus can improve reactivity, while avoiding the solid phase material residue in product from blocking reaction
Device 1, and the sealing property of magnetic agitation reactor is more excellent, more conducively keeps the reaction pressure in reactor 1.
Referring to Fig. 5, the embodiment of the present invention additionally provides a kind of biomass water heat liquefaction method, and the method includes：
S1, aqueous preheating material is pressed into into reactor by feed pipe and pressue device, and causes the preheating thing
Water in material receives thermal evaporation expansion in the reactor, to increase the temperature and pressure in the reactor, while by producing
Thing discharge pipe discharges pre- hot；
S2, when the temperature in the reactor increases to the second preset range, and pressure is increased in the first preset range,
The preheating material is replaced by into reaction mass, and is pressed into the reaction mass by the feed pipe and the pressue device
In the reactor, so that the reaction mass produces liquefaction reaction in the reactor and generates hydrothermal liquefaction product；
S3, the hydrothermal liquefaction product is expelled in product collector by product discharge pipe, and by flow control
Hydrothermal liquefaction product described in structure control is expelled to the flow of the product collector by the product discharge pipe, so that the product
The discharge flow of thing discharge pipe is equal with the feed rate of the feed pipe.
A kind of biomass water heat liquefaction method that the present invention is provided, is passing through feed pipe and pressue device to reactor internal pressure
After entering aqueous preheating material, the water in preheating material can receive thermal evaporation expansion in reactor, by the temperature in reactor
Degree and pressure are increased to respectively in the second preset range and the first preset range, and from there through preheating material reactor has been preheated；
Afterwards, preheating material can be replaced by reaction mass, and reaction mass is pressed in reactor by feed pipe and pressue device,
So that reaction mass produces liquid in the temperature in the second preset range and under the pressure environment in the first preset range
Change reaction, the product of liquefaction reaction is expelled in product collector by product discharge pipe, and produced by flow control structure control
The discharge flow of thing discharge pipe, so that the discharge flow of product discharge pipe is equal with the feed rate of feed pipe, so as to react
Temperature and pressure in device is respectively retained in the second preset range and the first preset range.Thus, can by feed pipe and
Pressue device will react continuously to reactor feed, and while the material in reactor is continuously discharged by product discharge pipe
Temperature and pressure in device is maintained at respectively in the second preset range and the first preset range, so as to be capable of achieving biomass water hydrothermal solution
The continuous reaction of change system, and then be conducive to the large-scale production of biomass by hydro-thermal liquefaction.
In the above-described embodiments, hydrothermal liquefaction product is controlled by flow control structure and product receipts is expelled to by thing discharge pipe
The flow of storage is specifically included：The aperture of flow control valve is adjusted, is expelled to by product discharge pipe with controlling hydrothermal liquefaction product
The flow of product collector.
Wherein, the aperture of flow control valve is adjusted, can specifically includes following two different operating procedures：
The first operating procedure：The reaction pressure in reactor is detected using pressure sensing cell；Work as pressure sensing cell
When the pressure value that detection is obtained is less than the minimum of a value in the first preset range, flow control valve is turned in the control of the first control unit down
Aperture；When the pressure value that pressure sensing cell detection is obtained is more than the maximum in the first preset range, the first control unit
Control tunes up the aperture of flow control valve.
Second operating procedure：The feed rate of feed pipe is detected using first flow detector unit, and utilizes second
The rate of discharge of amount detection unit detection flows regulating valve；When the flow value that the detection of second flow detector unit is obtained is less than first
During the flow value that flow detection unit detection is obtained, the control of the second control unit tunes up the aperture of flow control valve；Work as second
When the flow value that amount detection unit detection is obtained is more than the flow value that the detection of first flow detector unit is obtained, the second control unit
The aperture of flow control valve is turned in control down.
Further, preset model in first to remain the reaction pressure in reactor during liquefaction reaction
In enclosing, it is preferred that method also includes：Before the outlet side of product discharge pipe is connected with product collector, counterbalance valve is adjusted
Pressure so that the pressure of counterbalance valve is located in the first preset range, and is conveyed into product collector by supercharging device of supplying gas
Gas so that the pressure in product collector is located in the first preset range, so that the reaction temperature and reaction pressure in reactor
Power after the outlet side of product discharge pipe is connected with product collector, the pressure in product collector all the time with reactor in
Reaction pressure is balanced, and thus all the time the reaction pressure in reactor is held in into the first preset range during liquefaction reaction
It is interior.
It is after step s 3, further comprising the steps of for the hydrothermal liquefaction product in extract and separate product collector：
S4, extract is injected into product collector by extract injecting structure, and hydro-thermal is stirred by stirring structure
5～120min of liquefaction products and extract, so that the bio oil in extract dissolution hydrothermal liquefaction product；
S5, by product collector stand 1～3h so that in product collector solid phase material residue sedimentation, and with by water, extraction
The liquid product layering of liquid and bio oil composition；
S6, the supernatant in product collector is passed through in filter, to filter supernatant in the solid phase material residue that remains,
And obtain by water and be dissolved with the mixed liquor that the extract of bio oil is constituted；
S7, mixed liquor is passed through in knockout, and stands 10～60min so that the water sedimentation in mixed liquor, and with mix
The extract layering of bio oil is dissolved with liquid；
S8, the extract for being dissolved with bio oil is passed through in solvent evaporation device, bio oil is dissolved with evaporative removal
The water of extract and residual in extract, and obtain bio oil.
In order to avoid the internal high pressure of product collector produces impact to the injection smoothness of extract, while avoiding product
The internal high temperature of collector makes extract volatilize, it is preferred that after step s 3, before S4, also includes：Open product collector
Relief valve, the pressure in product collector is reduced to into normal pressure, while the temperature in product collector is cooled to into 30 DEG C of left sides
The right side, produces impact, while avoiding product collector with the internal high pressure for avoiding product collector on the injection smoothness of extract
Internal high temperature make extract volatilize and affect extraction process.
In the embodiment shown in fig. 5, the reaction mass in step S2 is the mixture being made up of biomass and water, mixing
The mass ratio of biomass and water is 0.01～0.3 in thing.
Wherein, biomass can be silk algae, ball algae, sludge, peanut straw, pig manure etc., and here is not specifically limited, only
Liquefaction reaction can be carried out and bio oil is generated.
With reference to the various embodiments described above, carry out liquefying instead individually below by taking silk algae, ball algae, sludge, peanut straw, pig manure as an example
Should, and generate bio oil.
Embodiment one：
Liquefaction reaction test is carried out by taking silk algae (the long 80cm of algal filament) as an example, tests below step is specifically included：First, by silk
Algae presses 3 with deionized water:17 ratio is well mixed, and adds crushed aggregates device so that crushing material to be less than or equal to as particle diameter
The slurry of 1mm enters standby after material storage device；Then, it is passed through into tubular reactor by feed pipe and high-pressure plunger pump
Deionized water, to preheat tubular reactor, while pre- hot is discharged by product discharge pipe, when the temperature in tubular reactor
330 DEG C are reached, pressure reaches 20MPa, start for deionized water to be replaced by standby slurry, and opened in material storage device
Agitating device and material storage device bottom discharge mouth valve, slurry is passed through in high-pressure plunger pump, opens high-pressure plunger pump
Outlet valve, to be passed through slurry into reactor, at the same adjust flow control valve aperture, make system can continuous-stable turnover
Material, wherein, high-pressure plunger pump presets time of staying 3min design discharge, uninterrupted formula L according to slurry in reactor
=60V* ρ/t is calculated, and wherein L represents flow, and V represents the volume of reactor, and ρ represents slurry density at reaction conditions, and t is represented
The time of staying of the slurry in reactor.The liquefaction reaction product that reactor is discharged is entered in product collector, product collector
For two, after the half of the liquefaction reaction collection of products in one of product collector to product collector volume, switching
It is collected for another product collector；Liquefaction reaction product in product collector is cooled to after 30 DEG C or so, is pressed
Ratio adds extract, while opening stirring structure, stirring 30min carries out standing 1h after fully extraction, makes solid phase material residue abundant
Deposit to the bottom of product collector；Then, the slag-drip opening valve and leakage fluid dram valve of filter are closed, inlet valve is opened
Door, and will have the supernatant in product collector to pump in filter with the first transmission pump, then, leakage fluid dram valve is opened,
Filtrate is set to flow in knockout, and standing 1h is fully layered in knockout, and by second pump is transmitted by the dissolving isolated
The extract for having bio oil is pumped in solvent evaporation device；Finally, by solvent evaporation device to being dissolved with the extraction of bio oil
Liquid carries out solvent abjection, and remaining product is obtained coarse biometric oil.
Test knot shows：Silk algae continuously liquefies the biological oily yield of generation 28%, calorific value in 35MJ/kg or so, it is oxygen-containing
15% or so, and intermittently liquefaction optimum condition liquefaction products yield and property are suitable.
Embodiment two：
Liquefaction reaction test is carried out by taking ball algae (a diameter of 3-8um) as an example, tests below step is specifically included：By ball algae with
Deionized water presses 2:8 ratios are well mixed to form slurry, and add material storage device with standby；Then, by feed pipe and
High-pressure plunger pump is passed through deionized water into reactor, with pre- thermal reactor, while pre- hot is discharged by product discharge pipe,
When the temperature in reactor reaches 330 DEG C, pressure reaches 20MPa, starts for deionized water to be replaced by standby slurry, and opens
Agitating device and material storage device bottom discharge mouth valve in material storage device, by slurry high-pressure plunger pump is passed through
In, the outlet valve of high-pressure plunger pump is opened, to be passed through slurry into reactor, while adjusting the aperture of flow control valve, make
System can continuous-stable input and output material, wherein, high-pressure plunger pump according to slurry in reactor preset the time of staying 1min design stream
Amount, in addition, reactor is the tank reactor without stirring structure.The liquefaction reaction product that reactor is discharged enters product collector
In, product collector is two, when the liquefaction reaction collection of products in one of product collector is to product collector volume
Half after, switch to another product collector to be collected；Liquefaction reaction product in product collector is cooled to 30
DEG C or so after, be proportionally added into extract, at the same open stirring structure, stirring 30min carry out fully extraction after stand 1h, make
Solid phase material residue is fully deposited to the bottom of product collector；Then, the slag-drip opening valve and leakage fluid dram valve of filter are closed,
Inlet valve is opened, and there will be the supernatant in product collector to pump in filter with the first transmission pump, then, opened
Leakage fluid dram valve, makes filtrate flow in knockout, and standing 1h is fully layered in knockout, and will be divided by the second transmission pump
The extract for being dissolved with bio oil for separating out is pumped in solvent evaporation device；Finally, by solvent evaporation device to being dissolved with life
The extract of thing oil carries out solvent abjection, and remaining product is obtained coarse biometric oil.
Test knot shows：Ball algae continuously liquefies the biological oily yield of generation 46%, calorific value in 37MJ/kg or so, it is oxygen-containing
9% or so, and intermittently liquefaction optimum condition liquefaction products yield and property are suitable.
Embodiment three：
Liquefaction reaction test is carried out by taking sludge as an example, tests below step is specifically included：It is to water content by sludge condensation
85% or so, and crushed aggregates device is added to be to fill into material storing after slurry of the particle diameter less than or equal to 1mm by crushing material
Purchase use；Then, deionized water is passed through into reactor by feed pipe and high-pressure plunger pump, with pre- thermal reactor, while logical
Cross product discharge pipe and discharge pre- hot, when the temperature in reactor reaches 330 DEG C, pressure reaches 20MPa, starts deionization
Water is replaced by standby slurry, and opens the agitating device in material storage device and material storage device bottom discharge mouth valve
Door, slurry is passed through in high-pressure plunger pump, opens the outlet valve of high-pressure plunger pump, to be passed through slurry into reactor, together
When adjust flow control valve aperture, make system can continuous-stable input and output material, wherein, high-pressure plunger pump is according to slurry in reactor
Interior default time of staying 5min design discharges, in addition, reactor is continuous stir reactor formula reactor.The liquefaction reaction that reactor is discharged is produced
Thing is entered in product collector, and product collector is two, when the liquefaction reaction collection of products in one of product collector
To the half of product collector volume, another product collector is switched to be collected；Liquefaction in product collector
Product is cooled to after 30 DEG C or so, is proportionally added into extract, while opening stirring structure, stirring 30min is filled
Divide after extraction and stand 1h, solid phase material residue is fully deposited to the bottom of product collector；Then, the slag-drip opening of filter is closed
Valve and leakage fluid dram valve, open inlet valve, and will have the supernatant in product collector to pump into the first transmission pump
In filter device, then, leakage fluid dram valve is opened, filtrate is flow in knockout, and 1h is stood in knockout and be fully layered, and
The extract for being dissolved with bio oil isolated is pumped in solvent evaporation device by the second transmission pump；Finally, by solvent
Vaporising device carries out solvent abjection to the extract for being dissolved with bio oil, and remaining product is obtained coarse biometric oil.
Test knot shows：Sludge continuously liquefies the biological oily yield of generation 30%, calorific value in 36MJ/kg or so, it is oxygen-containing
13% or so, and intermittently liquefaction optimum condition liquefaction products yield and property are suitable.
Example IV：
Liquefaction reaction test is carried out by taking peanut straw as an example, tests below step is specifically included：By peanut straw with go from
Sub- water presses 1:9 ratios are well mixed, and add crushed aggregates device laggard with the slurry by crushing material as particle diameter less than or equal to 1mm
Enter material storage device with standby；Then, deionized water is passed through into reactor by feed pipe and high-pressure plunger pump, to preheat
Reactor, while discharging pre- hot by product discharge pipe, when the temperature in reactor reaches 330 DEG C, pressure reaches
20MPa, starts for deionized water to be replaced by standby slurry, and opens the agitating device in material storage device and material storing
Bottom of device discharging opening valve, slurry is passed through in high-pressure plunger pump, the outlet valve of high-pressure plunger pump is opened, with to reaction
Slurry is passed through in device, at the same adjust flow control valve aperture, make system can continuous-stable input and output material, wherein, high-pressure plunger pump
Time of staying 7min design discharge is preset in reactor according to slurry, in addition, reactor is tubular reactor.Reactor is discharged
Liquefaction reaction product enter product collector in, product collector be two, the liquefaction in one of product collector
Product is collected to the half of product collector volume, switches to another product collector to be collected；Receive in product
Liquefaction reaction product in storage is cooled to after 30 DEG C or so, is proportionally added into extract, while stirring structure is opened, stirring
30min carries out standing 1h after fully extraction, solid phase material residue is fully deposited to the bottom of product collector；Then, close and filter
The slag-drip opening valve and leakage fluid dram valve of device, opens inlet valve, and will have in product collector with the first transmission pump
Supernatant is pumped in filter, then, opens leakage fluid dram valve, filtrate is flow in knockout, and is stood in knockout
1h is fully layered, and the extract for being dissolved with bio oil isolated is pumped in solvent evaporation device by the second transmission pump；
Finally, solvent abjection is carried out to the extract for being dissolved with bio oil by solvent evaporation device, remaining product is obtained
Coarse biometric oil.
Test knot shows：Peanut straw continuously liquefies the biological oily yield of generation 22%, and calorific value contains in 35MJ/kg or so
, 15% or so, oily yield is more slightly higher than interval liquefaction oily yield (20%), and quality is suitable for oxygen.
Embodiment five：
Liquefaction reaction test is carried out by taking pig manure as an example, tests below step is specifically included：Pig manure and deionized water are reconciled
For 1:9 ratio is well mixed, and add crushed aggregates device with by crushing material be particle diameter less than or equal to 1mm slurry after enter
Material storage device is with standby；Then, deionized water is passed through into reactor by feed pipe and high-pressure plunger pump, it is anti-to preheat
Device is answered, while discharging pre- hot by product discharge pipe, when the temperature in reactor reaches 330 DEG C, pressure reaches 20MPa,
Start for deionized water to be replaced by standby slurry, and open the agitating device in material storage device and material storage device bottom
Portion's discharging opening valve, slurry is passed through in high-pressure plunger pump, opens the outlet valve of high-pressure plunger pump, to lead to into reactor
Enter slurry, at the same adjust flow control valve aperture, make system can continuous-stable input and output material, wherein, high-pressure plunger pump is according to slurry
Material presets time of staying 5min design discharge in reactor, in addition, reactor is continuous stir reactor formula reactor.What reactor was discharged
Liquefaction reaction product enter product collector in, product collector be two, when the liquefaction in one of product collector it is anti-
After answering the half of collection of products to product collector volume, another product collector is switched to be collected；In collection of products
Liquefaction reaction product in device is cooled to after 30 DEG C or so, is proportionally added into extract, while stirring structure is opened, stirring
30min carries out standing 1h after fully extraction, solid phase material residue is fully deposited to the bottom of product collector；Then, close and filter
The slag-drip opening valve and leakage fluid dram valve of device, opens inlet valve, and will have in product collector with the first transmission pump
Supernatant is pumped in filter, then, opens leakage fluid dram valve, filtrate is flow in knockout, and is stood in knockout
1h is fully layered, and the extract for being dissolved with bio oil isolated is pumped in solvent evaporation device by the second transmission pump；
Finally, solvent abjection is carried out to the extract for being dissolved with bio oil by solvent evaporation device, remaining product is obtained
Coarse biometric oil.
Test knot shows：Pig manure continuously liquefies the biological oily yield of generation 30%, calorific value in 33MJ/kg or so, it is oxygen-containing
17% or so, oily yield is more slightly lower than interval liquefaction oily yield (32%).
In the description of this specification, specific features, structure, material or feature can be in one or more any realities
Apply and combined in an appropriate manner in example or example.
The above, the only specific embodiment of the present invention, but protection scope of the present invention is not limited thereto, any
Those familiar with the art the invention discloses technical scope in, change or replacement can be readily occurred in, all should contain
Cover within protection scope of the present invention.Therefore, protection scope of the present invention should be defined by the scope of the claims.
Claims (15)
1. a kind of biomass by hydro-thermal liquefaction system, it is characterised in that include：
Reactor, the reactor is used to carry out liquefaction reaction, and the reactor is connected with feed pipe and product discharge pipe, described
Pressue device is serially connected with feed pipe；
Product collector, the outlet side airtight connection of the product collector and the product discharge pipe；
Flow control structure, the flow control structure is arranged between the product collector and the reactor, and is used for
The flow that the product is expelled to the product collector by the product discharge pipe is controlled, so that the row of the product discharge pipe
Stream amount is equal with the feed rate of the feed pipe.
2. biomass by hydro-thermal liquefaction system according to claim 1, it is characterised in that the flow control structure includes string
The flow control valve being connected in the product discharge pipe, discharges can the product by adjusting the aperture of the flow control valve
The discharge flow of pipe is equal with the feed rate of the feed pipe.
3. biomass by hydro-thermal liquefaction system according to claim 2, it is characterised in that the flow control structure also includes
Pressure sensing cell and the first control unit, the pressure sensing cell is located in the reactor, and described anti-for detecting
The reaction pressure in device, first control unit is answered to be used for the pressure value obtained according to pressure sensing cell detection, control
System adjusts the aperture of the flow control valve.
4. biomass by hydro-thermal liquefaction system according to claim 2, it is characterised in that the flow control structure also includes
First flow detector unit, second flow detector unit and the second control unit, the first flow detector unit is used to detect
The feed rate of the feed pipe, the second flow detector unit is used to detect the rate of discharge of the flow control valve, when
The flow value that the flow value that the second flow detector unit detection is obtained is obtained with first flow detector unit detection is not
When equal, second control unit controls to adjust the aperture of the flow control valve.
5. the biomass by hydro-thermal liquefaction system according to any one of Claims 1 to 4, it is characterised in that also include and institute
State supply gas supercharging device and the counterbalance valve that is arranged in the product collector of product collector connection, the supercharging of supplying gas
Device was used for before the product collector is connected with the outlet side of the product discharge pipe, defeated into the product collector
Enter gas so that the pressure in the product collector increase to it is equal with the pressure in the reactor.
6. the biomass by hydro-thermal liquefaction system according to any one of Claims 1 to 4, it is characterised in that the product is received
Storage includes extract injecting structure and stirring structure.
7. biomass by hydro-thermal liquefaction system according to claim 6, it is characterised in that also including product separation system, institute
Filter, knockout and solvent evaporation device that product separation system includes being sequentially connected are stated,
The filter is used to filter the solid phase material residue in the quiet interior supernatant of the product collector, to obtain by water and dissolving
The mixed liquor being made up of the extract of bio oil；
The water that the knockout is used in mixed liquor described in multi_layer extraction and the extract for being dissolved with bio oil；
The solvent evaporation device is dissolved with the extract of bio oil for knockout described in evaporative removal to be isolated
The water of extract and residual, to obtain bio oil.
8. biomass by hydro-thermal liquefaction system according to claim 1, it is characterised in that also including flow pulse buffer,
The flow pulse buffer includes cystic container and covers at housing outside cystic container, and the cystic container is serially connected with institute
State on the feed pipe between pressue device and the reactor, the cystic container is made by resilientiy stretchable material, institute
State housing to be made by rigid material, the maximum volume after the cystic container expansion is more than the volume of the housing, and the capsule
Shape container is when in contraction state with gap and the inner walls between.
9. biomass by hydro-thermal liquefaction system according to claim 1, it is characterised in that described pre- also including preheating device
Thermal includes outer tube and the inner tube in the outer tube, has clearance channel, institute between the outer tube and said inner tube
State inner tube to be serially connected with the feed pipe, the clearance channel is serially connected with the product discharge pipe, or, said inner tube concatenation
In the product discharge pipe, the clearance channel is serially connected with the feed pipe.
10. biomass by hydro-thermal liquefaction system according to claim 1, it is characterised in that the reactor is magnetic agitation
Reactor.
11. a kind of biomass water heat liquefaction methods, it is characterised in that methods described includes：
S1, aqueous preheating material is pressed into into reactor by feed pipe and pressue device, and is caused in the preheating material
Water in the reactor receive thermal evaporation expansion, to increase the temperature and pressure in the reactor, at the same by product arrange
Outlet pipe discharges pre- hot；
S2, when the temperature in the reactor increases to the second preset range, and pressure is increased in the first preset range, by institute
State preheating material and be replaced by reaction mass, and it is by the feed pipe and the pressue device that reaction mass press-in is described
In reactor, so that the reaction mass produces liquefaction reaction in the reactor and generates hydrothermal liquefaction product；
S3, the hydrothermal liquefaction product is expelled in product collector by product discharge pipe, and by flow control structure
The flow that the hydrothermal liquefaction product is expelled to the product collector by the product discharge pipe is controlled, so that product row
The discharge flow of outlet pipe is equal with the feed rate of the feed pipe.
12. methods according to claim 11, it is characterised in that described that the hydro-thermal liquid is controlled by flow control structure
Change product to be specifically included by the flow that the product discharge pipe is expelled to the product collector：
The aperture of flow control valve is adjusted, the product is expelled to by the product discharge pipe to control the hydrothermal liquefaction product
The flow of collector.
13. methods according to claim 12, it is characterised in that the aperture of the regulation flow control valve is specifically wrapped
Include：
The reaction pressure in the reactor is detected using pressure sensing cell；
When the pressure value that pressure sensing cell detection is obtained is less than the minimum of a value in first preset range, the first control
The aperture of the flow control valve is turned in unit control processed down；
When the pressure sensing cell pressure value that obtains of detection is more than maximum in first preset range, described the
The control of one control unit tunes up the aperture of the flow control valve.
14. methods according to claim 12, it is characterised in that the aperture of the regulation flow control valve is specifically wrapped
Include：
The feed rate of feed pipe is detected using first flow detector unit, and is adjusted using second flow detector unit detection flows
The rate of discharge of section valve；
When the flow value that the detection of second flow detector unit is obtained is less than the flow value that the detection of first flow detector unit is obtained,
The control of second control unit tunes up the aperture of the flow control valve；
When the flow value that the detection of second flow detector unit is obtained is more than the flow value that the detection of first flow detector unit is obtained,
The aperture of the flow control valve is turned in the second control unit control down.
15. methods according to claim 11, it is characterised in that after step S3, also include：
S4, extract is injected into the product collector by extract injecting structure, and it is described by stirring structure stirring
Hydrothermal liquefaction product and the 5～120min of extract, so that the biology in hydrothermal liquefaction product described in the extract dissolution
Oil；
S5, by the product collector stand 1～3h so that in the product collector solid phase material residue sedimentation, and with by water,
The liquid product layering of extract and bio oil composition；
S6, the supernatant in the product collector is passed through in filter, to filter supernatant in the solid phase material residue that remains,
And obtain by water and be dissolved with the mixed liquor that the extract of bio oil is constituted；
S7, the mixed liquor is passed through in knockout, and stands 10～60min so that the water sedimentation in the mixed liquor, and with
The extract layering of bio oil is dissolved with the mixed liquor；
S8, the extract for being dissolved with bio oil is passed through in solvent evaporation device, to be dissolved with biology described in evaporative removal
The water of extract and residual in the extract of oil, and obtain bio oil.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108203319A (en) * | 2018-02-07 | 2018-06-26 | 北京环清环境科技有限公司 | A kind of continous way hydrolysis device |
| CN108249717A (en) * | 2018-02-27 | 2018-07-06 | 广东梦之禽农业科技股份有限公司 | A kind of solar energy chicken manure harmless treatment device |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101805629A (en) * | 2010-03-22 | 2010-08-18 | 华东理工大学 | Method for producing fuel oil by biomass hydrothermal liquefaction |
| US20130331623A1 (en) * | 2012-06-08 | 2013-12-12 | Battelle Memorial Institute | Combined hydrothermal liquefaction and catalytic hydrothermal gasification system and process for conversion of biomass feedstocks |
| CN103614168A (en) * | 2013-12-09 | 2014-03-05 | 华东理工大学 | Processing method for preparing liquid fuel by performing sludge liquefaction |
| US20150126758A1 (en) * | 2013-11-06 | 2015-05-07 | Genifuel Corporation | System and process for efficient separation of biocrudes and water in a hydrothermal liquefaction system |
| CN106118705A (en) * | 2016-06-22 | 2016-11-16 | 西安交通大学 | A kind of continuous reaction system and method for microalgae hydrothermal liquefaction preparing bio-oil |
-
2016
- 2016-12-30 CN CN201611270675.3A patent/CN106635112B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101805629A (en) * | 2010-03-22 | 2010-08-18 | 华东理工大学 | Method for producing fuel oil by biomass hydrothermal liquefaction |
| US20130331623A1 (en) * | 2012-06-08 | 2013-12-12 | Battelle Memorial Institute | Combined hydrothermal liquefaction and catalytic hydrothermal gasification system and process for conversion of biomass feedstocks |
| US20150126758A1 (en) * | 2013-11-06 | 2015-05-07 | Genifuel Corporation | System and process for efficient separation of biocrudes and water in a hydrothermal liquefaction system |
| CN103614168A (en) * | 2013-12-09 | 2014-03-05 | 华东理工大学 | Processing method for preparing liquid fuel by performing sludge liquefaction |
| CN106118705A (en) * | 2016-06-22 | 2016-11-16 | 西安交通大学 | A kind of continuous reaction system and method for microalgae hydrothermal liquefaction preparing bio-oil |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108203319A (en) * | 2018-02-07 | 2018-06-26 | 北京环清环境科技有限公司 | A kind of continous way hydrolysis device |
| CN108249717A (en) * | 2018-02-27 | 2018-07-06 | 广东梦之禽农业科技股份有限公司 | A kind of solar energy chicken manure harmless treatment device |
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