CN101735843A - Biomass high-pressure continuous tower-type liquefying process with pretreatment step - Google Patents
Biomass high-pressure continuous tower-type liquefying process with pretreatment step Download PDFInfo
- Publication number
- CN101735843A CN101735843A CN201010000853A CN201010000853A CN101735843A CN 101735843 A CN101735843 A CN 101735843A CN 201010000853 A CN201010000853 A CN 201010000853A CN 201010000853 A CN201010000853 A CN 201010000853A CN 101735843 A CN101735843 A CN 101735843A
- Authority
- CN
- China
- Prior art keywords
- pressure
- phase
- tower
- water
- liquefaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 32
- 239000002028 Biomass Substances 0.000 title claims abstract description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 26
- 230000007062 hydrolysis Effects 0.000 claims abstract description 24
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 24
- 239000012071 phase Substances 0.000 claims abstract description 24
- 239000002002 slurry Substances 0.000 claims abstract description 17
- 239000000446 fuel Substances 0.000 claims abstract description 15
- 238000010438 heat treatment Methods 0.000 claims abstract description 6
- 239000007791 liquid phase Substances 0.000 claims abstract description 6
- 239000007790 solid phase Substances 0.000 claims abstract description 6
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 239000002994 raw material Substances 0.000 claims abstract description 5
- 238000006114 decarboxylation reaction Methods 0.000 claims abstract description 4
- 230000003139 buffering effect Effects 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 7
- 230000035484 reaction time Effects 0.000 claims description 6
- 238000007670 refining Methods 0.000 claims description 4
- 239000000945 filler Substances 0.000 claims description 3
- 238000002203 pretreatment Methods 0.000 claims description 3
- 230000003068 static effect Effects 0.000 claims description 3
- 239000011800 void material Substances 0.000 claims description 3
- 230000003301 hydrolyzing effect Effects 0.000 abstract 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract 1
- 229910052799 carbon Inorganic materials 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 16
- 238000000197 pyrolysis Methods 0.000 description 7
- 239000007789 gas Substances 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000010779 crude oil Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 208000012839 conversion disease Diseases 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 241000195493 Cryptophyta Species 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000012075 bio-oil Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 230000009969 flowable effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 235000021419 vinegar Nutrition 0.000 description 1
- 239000000052 vinegar Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a biomass high-pressure continuous tower-type liquefying process with a pretreatment step. The process comprises the following steps of: adding biomasses and water into a high-pressure hydrolyzing pot; after intermittent type hydrolysis slurry state pretreatment, enable hydrolysis slurry to pass through an intermediate buffer pot, and then continuously pressurizing and conveying hydrolysis slurry to a heat exchanger and a heating furnace by a high-pressure pump to quickly heat, and adding the hydrolysis slurry into a liquefying tower for decarboxylation and liquefaction under high pressure; and dividing a liquefying product into a gas phase, a liquid phase and a solid phase through a high-pressure three-phase separator, wherein after heat exchange and cooling, the liquid phase and the slurry enter an oil-water separator and are divided into an oil phase and a water phase; a part of the water phase is drained, a part of the water phase returns to the high-pressure hydrolyzing pot, and the oil phase is refined and used as a product; the gas phase is used as a fuel of the heating furnace; and the solid phase is discharged and used as an active carbon raw material or a fuel.
Description
One, technical field
The present invention relates to have the continuous tower liquefaction process of pretreated biomass high-pressure, belong to the biomass energy source domain.
Two, background technology
Convert biomass to high-grade geseous fuel and liquid fuel, can reduce dependence fossil oils such as oil, coals.Simultaneously, utilize biomass energy, can slow down CO
2Discharging becomes the focus that the countries in the world chemical circles is studied.The route that biomass are converted into liquid fuel can be divided into fast pyrolysis liquefaction and high-pressure liquefaction.Fast pyrolysis liquefaction is adapted to low water-contained biomass, as stalk, sawdust etc.; High-pressure liquefaction is adapted to high water-contained biomass, as little algae, Herba Eichhorniae, marine alga, pasture and water etc.Carry out the process of pyrolysis in the hot water of high water-contained biomass temperature in high pressure, need not to dehydrate and pulverize.The same with the high temperature fast pyrolysis process, generate gas, liquid and solid.The light constituent wood vinegar component (xanthohumic acid) that pyrolysis produces is dissolved in the water, and oil and solid mix.Bio oil is a main products, and oxygen level is less than 20%, 1.5 times of the suitable high temperature rapid pyrolysis oil of calorific value.But because biomass high-pressure liquefaction research just has been in the starting stage, research mostly is the autoclave batch operation greatly, is difficult to realize large-scale industrial production, and biomass high-pressure liquefaction process and the device of setting up continous way have more practical significance.
Three. summary of the invention
Purpose of the present invention just provides and has the continuous tower liquefaction process of pretreated biomass high-pressure.The high water-contained biomass of this art breading need not to dehydrate and pulverize, can be by the required optimal temperature conditions control reaction temperature of reaction, advantages of simple, reaction conversion ratio and rate of recovery height, water need not vaporization in whole process, energy consumption is low, is easy to large-scale industrial production.
Technical scheme of the present invention:
Have the continuous tower liquefaction process of pretreated biomass high-pressure, after biomass and water are added in the pre-treatment of highly pressured hydrolysis jar intermittent type hydrolysis slurry attitude, by the intermediate buffering jar, be pressed and delivered to interchanger and process furnace rapid heating continuously and enter the liquefaction of liquefaction tower mesohigh decarboxylation with high-pressure pump; Liquefied product is divided into gas-liquid-solid three-phase by the high pressure triphase separator; Enter water-and-oil separator after liquid phase and the slurry heat exchange cooling, be divided into oil phase and water under the low pressure, aqueous portion effluxes, and part is returned the highly pressured hydrolysis jar, and oil phase is refining as product; Gas phase is as the fuel of process furnace, and solid phase effluxes as gac raw material or fuel.
180-270 ℃ of highly pressured hydrolysis jar hydrolysis slurry attitude pretreatment operation temperature, working pressure is a water saturation vapour pressure under this temperature, reaction time 5-70 minute.
The aspect ratio of liquefaction tower is 3: 1～30: 1, and static mixer, filler or column plate can be housed, and also can be void tower.
Liquefaction service temperature 270-350 ℃ of tower, working pressure is a water saturation vapour pressure under this temperature, reaction time 5-70 minute.
Four, description of drawings
Accompanying drawing is the process flow sheet of invention.
Wherein: the outlet of 1-highly pressured hydrolysis jar 2-intermediate buffering jar 3-high-pressure pump 4-interchanger 5-process furnace 6-liquefaction tower 7-high pressure triphase separator 8-water-and-oil separator 9-pyrolysis dry gas outlet 10-solid outlet 11-oil export 12-water
Five. embodiment
The present invention will be described in detail below in conjunction with accompanying drawing: have the continuous tower liquefaction process of pretreated biomass high-pressure, processing unit mainly comprises highly pressured hydrolysis jar (1), intermediate buffering jar (2), high-pressure pump (3), interchanger (4), process furnace (5), liquefaction tower (6), high pressure triphase separator (7), water-and-oil separator (8) etc.After biomass and water are added in the pre-treatment of highly pressured hydrolysis jar (1) intermittent type hydrolysis slurry attitude, by intermediate buffering jar (2), be pressed and delivered to interchanger (4) and process furnace (5) rapid heating continuously and enter the liquefaction of liquefaction tower (6) mesohigh decarboxylation with high-pressure pump (3); Liquefied product is divided into gas-liquid-solid three-phase by high pressure triphase separator (7); Enter water-and-oil separator (8) after liquid phase and the slurry heat exchange cooling, be divided into oil phase and water under the low pressure, aqueous portion effluxes from water outlet (12), and part is returned highly pressured hydrolysis jar (1), and oil phase is refining as product; Gas phase is as the fuel of process furnace, and solid phase effluxes as gac raw material or fuel.
180-270 ℃ of hydrolysis slurry attitude pretreatment operation temperature, working pressure is a water saturation vapour pressure under this temperature, reaction time 5-70 minute.
The aspect ratio of liquefaction tower is 3: 1～30: 1, and static mixer, filler or column plate can be housed, and also can be void tower.
Liquefaction service temperature 270-350 ℃ of tower, working pressure is a water saturation vapour pressure under this temperature, reaction time 5-70 minute.
The concrete technological line matter utilization shovel loader a plurality of highly pressured hydrolysis jars (1) in parallel of packing into of making a living are warmed up to 180-250 ℃ by certain heating curve, and the pressure about 15Kg/cm is incubated 5-70 minute, makes its solid biologic be changed into flowable slurry; Put into intermediate buffering jar (2) removal of impurities by jar, high-pressure pump (3) send interchanger (4) and process furnace (5) to be rapidly heated 270-350 ℃ by certain temperature rise rate then, enters the liquefaction of liquefaction tower (6) hydro-thermal and produces liquid fuel; The hydro-thermal liquefied product separates admittedly through high pressure triphase separator (7) gas-liquid; Enter water-and-oil separator (8) after liquid phase and the slurry heat exchange cooling, be divided into oil phase and water under the low pressure, aqueous portion effluxes to concentrate from water outlet (12) produces foliage fertilizer, biogasoline or Snow Agent etc., part is returned highly pressured hydrolysis jar (1), and oil phase is refining to obtain bio-crude oil (gasoline and diesel oil) as product; Gas phase is as the fuel of process furnace, and solid phase effluxes as gac raw material or fuel.The whole hydro-thermal liquefaction process of biomass needs time 10-140 minute to producing liquid fuel again from being warmed up to 200-220 ℃.The bio-crude oil calorific value that generates contains oxygen 10-20% about 30MJ/Kg, want high relatively about the bio-crude oil calorific value 20MJ/Kg of biomass gas phase fast pyrogenation, and it is low to contain oxygen.
Of the present invention have following outstanding advantage with pretreated biomass high-pressure continuous tower-type liquefying process: (1) can be by the required optimal temperature conditions control reaction temperature of reaction, advantages of simple, reaction conversion ratio and rate of recovery height are easy to heavy industrialization; (2) water need not vaporization in overall process, energy consumption is low; (3) a plurality of highly pressured hydrolysis tank batch (-type)s hydrolysis slurry attitude preliminary treatment can make living beings need not to dehydrate and the high energy consumption step such as pulverizing; (4) good product quality, oxygen content is lower, the calorific value height.
Claims (4)
1. have the continuous tower liquefaction process of pretreated biomass high-pressure, main technique equipment comprises highly pressured hydrolysis jar, intermediate buffering jar, high-pressure pump, interchanger, process furnace, liquefaction tower, high pressure triphase separator, water-and-oil separator etc., its technical characterictic is after biomass and water add the pre-treatment of highly pressured hydrolysis jar intermittent type hydrolysis slurry attitude, by the intermediate buffering jar, be pressed and delivered to interchanger and process furnace rapid heating continuously and enter the liquefaction of liquefaction tower mesohigh decarboxylation with high-pressure pump; Liquefied product is divided into gas-liquid-solid three-phase by the high pressure triphase separator; Enter water-and-oil separator after liquid phase and the slurry heat exchange cooling, be divided into oil phase and water under the low pressure, aqueous portion effluxes, and part is returned the highly pressured hydrolysis jar, and oil phase is refining as product; Gas phase is as the fuel of process furnace, and solid phase effluxes as gac raw material or fuel.
2. have the continuous tower liquefaction process of pretreated biomass high-pressure according to claim 1 provided, it is characterized in that 180-270 ℃ of hydrolysis slurry attitude pretreatment operation temperature, working pressure is a water saturation vapour pressure under this temperature, reaction time 5-70 minute.
3. had the continuous tower liquefaction process of pretreated biomass high-pressure according to claim 1 provides, the aspect ratio of the tower that it is characterized in that liquefying is 3: 1 ~ 30: 1, and static mixer, filler or column plate can be housed, and also can be void tower.
4. had the continuous tower liquefaction process of pretreated biomass high-pressure according to claim 1 provides, service temperature 270-350 ℃ of the tower that it is characterized in that liquefying, working pressure is a water saturation vapour pressure under this temperature, reaction time 5-70 minute.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010000853A CN101735843A (en) | 2010-01-19 | 2010-01-19 | Biomass high-pressure continuous tower-type liquefying process with pretreatment step |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010000853A CN101735843A (en) | 2010-01-19 | 2010-01-19 | Biomass high-pressure continuous tower-type liquefying process with pretreatment step |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101735843A true CN101735843A (en) | 2010-06-16 |
Family
ID=42459880
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010000853A Pending CN101735843A (en) | 2010-01-19 | 2010-01-19 | Biomass high-pressure continuous tower-type liquefying process with pretreatment step |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101735843A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105731452A (en) * | 2016-01-22 | 2016-07-06 | 青岛大学 | Active carbon electrode material as well as preparation method and application thereof |
| CN109099435A (en) * | 2018-02-13 | 2018-12-28 | 郭祖诚 | A kind of method of waste incineration and generating electricity and hydrothermal liquefaction cooperative disposal rubbish |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1473188A (en) * | 2000-09-04 | 2004-02-04 | �����ɷ� | Process for production of liquid fuels from biomass |
| CN101113348A (en) * | 2007-09-06 | 2008-01-30 | 昆明理工大学 | Process for preparing biofuel by high-pressure fluid conversion technology |
-
2010
- 2010-01-19 CN CN201010000853A patent/CN101735843A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1473188A (en) * | 2000-09-04 | 2004-02-04 | �����ɷ� | Process for production of liquid fuels from biomass |
| CN101113348A (en) * | 2007-09-06 | 2008-01-30 | 昆明理工大学 | Process for preparing biofuel by high-pressure fluid conversion technology |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105731452A (en) * | 2016-01-22 | 2016-07-06 | 青岛大学 | Active carbon electrode material as well as preparation method and application thereof |
| CN109099435A (en) * | 2018-02-13 | 2018-12-28 | 郭祖诚 | A kind of method of waste incineration and generating electricity and hydrothermal liquefaction cooperative disposal rubbish |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102071038A (en) | Microalgae high-pressure continuous tower-type liquefying process | |
| CN101113348B (en) | Process for preparing bio-fuel by high-pressure fluid transformation technique | |
| CN104910946A (en) | Process for hydrothermal carbonization of biomass and cogeneration of bio-oil | |
| CN101648847B (en) | Composite process of fuel alcohol and edible alcohol | |
| CN102002381B (en) | Method for preparing biological oil from algae biomass through direct catalytic liquefaction method | |
| CN102260506A (en) | Novel method for comprehensively utilizing waste materials of rubber tree processing sheets | |
| EP3352928B1 (en) | System and process for production of biofuel | |
| CN101407727A (en) | Method for preparing biomass liquefied oil by biomass catalytic liquefaction | |
| CN103113187A (en) | Method for producing ethanol and coproducing ethyl acetate with acetic acid | |
| Islam et al. | A short review on hydrothermal liquefaction of livestock manure and a chance for Korea to advance swine manure to bio-oil technology | |
| CN101624530A (en) | Biomass liquefied oil and preparation method thereof | |
| CN101648848B (en) | Combined production method for fuel alcohol and edible alcohol | |
| CN101260309A (en) | Method for producing fuel oil by continuous catalytic cracking of mixed waste plastics | |
| CN113337310A (en) | Method for preparing biodiesel by deep processing of biomass residual oil | |
| CN105038853B (en) | A kind of method utilizing FCC slurry and coal to refine oil altogether | |
| CN101735843A (en) | Biomass high-pressure continuous tower-type liquefying process with pretreatment step | |
| CN103242882B (en) | Method for producing oil by using co-liquefaction of cotton stalks and coal without adding catalyst | |
| CN106118706A (en) | A kind of method utilizing abandoned biomass to prepare composite biodiesel | |
| CN103305252A (en) | Method for preparing liquid fuel through coliquefaction of coal and alage | |
| CN111234888B (en) | A system and method for synergistic wet biomass resource utilization of supercritical water reaction products | |
| CN103254923B (en) | Biomass hydrogen-donating pyrolysis technique of naphthenic base oil in presence of hydrogen-donating distillate oil | |
| CN101691494B (en) | A method for circulating liquefaction of plant biomass and waste polyester mixed with supercritical fluid | |
| CN201574142U (en) | Biomass high-pressure continuous tower liquefaction unit with pretreatment | |
| CN104845668A (en) | Method for prolonging operation cycle of deoxidized biomass oil hydrogenation device | |
| CN103194255B (en) | Catalytic cracking animal-plant oil produces the method for clean fuel |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20100616 |