CN107189806B

CN107189806B - A kind of batch-type biomass liquefying process

Info

Publication number: CN107189806B
Application number: CN201710551051.7A
Authority: CN
Inventors: 于洪江
Original assignee: Shanghai Jincheng Environmental Technology Co Ltd
Current assignee: Shanghai Jincheng Environmental Technology Co Ltd
Priority date: 2017-07-07
Filing date: 2017-07-07
Publication date: 2019-03-15
Anticipated expiration: 2037-07-07
Also published as: CN107189806A

Abstract

The present invention relates to a kind of batch-type biomass liquefying process, the technique directly recycles the thermal energy in pyrolysis liquefying biomass using indirect heat exchange mode, and technique includes two groups or more batch-type biomass liquefying unit being arranged in parallel and high-temperature heat-conductive oil circuit piping and the thermally conductive oil circuit piping of low temperature that batch-type biomass liquefying unit matching uses.Compared with prior art, present invention process principle is simple, process system integral pressure is low, occupied area is small, small investment, it is one kind selection well for manufacturing biomass fuel, SBH reactor directly recycles the thermal energy in pyrolysis liquefying biomass using indirect heat exchange method, it is few using equipment, recovery efficiency is high, and SBH reactor is during entire biomass liquefying, remain closed state, no steam release, without adding catalyst, pressure is controlled by the saturated vapor pressure that relevant temperature is lauched, heat-energy losses are few, the loss of organic volatile part is few in biomass, it has a good application prospect.

Description

A kind of batch-type biomass liquefying process

Technical field

The invention belongs to field of renewable energy technology, are related to a kind of biomass processes technique, more particularly, to a kind of sequence Batch biomass liquefying process.

Background technique

As fossil energy is increasingly depleted, the mankind increasingly improve the interest of renewable bioenergy, countries in the world Substantial contribution and manpower, the technique of development and production renewable energy are all put into.All fossil energies also derive from earliest in fact Biomass, by geology transition in more than one hundred million years, the moisture in biomass was gradually precipitated, and the microstructure in biomass also occurs Variation, becomes petroleum, natural gas, the coal etc. that we use today, is referred to as fossil energy.We develop various now Renewable bioenergy technology seeks to shorten the time that biomass develops, and it is more than one hundred million to complete the Nature needs with the very short time The transformation that year could complete.

The key of exploitation renewable bioenergy is the original structure of biomass to be cracked, and will wherein a large amount of moisture It removes.Copy the process of the Nature manufacture fossil energy, it is necessary first to liquefy to biomass, then extract people in a liquid The energy required for class.

Continuous biomass liquefaction (Continuous Biosolid Hydrolysis, CBH) is current manufacture biomass The main method of fuel.In CBH, the biomass solid containing large quantity of moisture is returned by continuous processing, temperature-pressure, then thermal energy It receives, it is cooling, it depressurizes, dehydration and drying can be obtained with the biomass fuel compared with high heating value.In biomass CBH, for heating life Most of thermal energy of substance is recovered, and the utilization efficiency of thermal energy has reached highest.In addition, in CBH, if operating condition is not Become, once all equipment stable operation, is not necessarily to frequent operation and adjustment, this, which is greatly lowered, wants system automatic control It asks.

Although continuous biomass liquefies, CBH has lot of advantages, and there is also some defects.Firstly, the whole pressure of CBH Power is higher, gets used to often being unwilling using the user of low-voltage equipment using high-tension apparatus；Secondly as the pressure of system compared with The process procedure of height, whole system is more, and system investments are also bigger than normal, this is also that many users are unacceptable；Third, CBH's Equipment is more, system complex, and occupied area is also relatively large.

In order to simplify CBH system, system pressure is reduced, currently, there is multiple producers (especially in Europe) to research and develop hydro-thermal carbon Chemical industry skill (Hydro Thermal Carbonization, HTC).The biomass carbonization process of HTC technique is in a reactor tank It completes, material heating is close to input high-temperature steam in tank and realizes.After acidic catalyst is added in reactor, the temperature of biomass carbonization Degree can be reduced to 200 DEG C, and system pressure can be reduced to 2.0MPa.The raising of HTC system processing capacity and production it is continuous Property realized by installing multiple HTC reactor tanks.

Since material heating is close to input high-temperature steam realization in tank in HTC technique, in order to guarantee that steam can be in low pressure It is continuously inputted under environment, HTC reactor tank needs constantly to depressurize in steam injection.Frequently decompression, increases the complexity of system. In addition, steam of the decompression in release reactor tank realizes that a part of organic volatile substance also evaporates simultaneously in biomass, this makes Calorific value in final carbonated product is accordingly reduced.The energy regenerating of HTC system is realized by the sensible heat and latent heat of recovered steam, Since the vapor (steam) temperature of reactor tank release is very low, energy source temperature after the recovery is lower, and this low value energy is difficult to be utilized, therefore The energy consumption of HTC system is higher.

The original intention of HTC technique is to complete all biological matter carbonisation by a reactor tank, to simplify CBH system System reduces investment and land occupation.But it is gradually complicated due to increasing links, the techniques such as steam release, steam condensation, thermal energy recycling. The investment and occupied area and continous way CBH systematic comparison that multiple case histories of HTC show its integrated artistic be not in phase Under.

Summary of the invention

It is an object of the present invention to overcome the above-mentioned drawbacks of the prior art and provide one kind can pass through indirect matchmaker The energy of bio liquid after matter recycling carbonization, recovery efficiency is high, and occupied area is small, the good batch-type biomass of economic and practical Liquefaction process.

The present invention is a kind of batch-type biomass liquefying process (Sequence Biosolid Hydrolysis, SBH).It should The purpose of system invention seeks to overcome the defect of existing batch-type hydrothermal carbonization technology.There was only a kind of structure in SBH system Simple reactor, principle is simple, and system integral pressure is low, and occupied area is small, small investment, is the one kind for manufacturing biomass fuel Selection well.

The purpose of the present invention can be achieved through the following technical solutions:

A kind of batch-type biomass liquefying process, the technique directly recycle lysate metaplasia using indirect heat exchange mode Thermal energy in substance, the technique include batch-type biomass liquefying unit and the sequence that two groups or more is arranged in parallel The high-temperature heat-conductive oil circuit piping and the thermally conductive oil circuit piping of low temperature that batch biomass liquefying unit matching uses；

In the operating condition, when one group of batch-type biomass liquefying unit is heated using high temperature heat conductive oil, another group of sequence Batch biomass liquefying unit feed, the biomass in the batch-type biomass liquefying unit using high temperature heat conductive oil heating are complete After liquefaction, closed with the high-temperature heat-conductive oil circuit piping that the batch-type biomass liquefying unit matching uses, low temperature conduction oil Circulation line is opened, and the low temperature for opening simultaneously the batch-type biomass liquefying unit that another group has been completed biomass charging is thermally conductive The heat for the batch-type biomass liquefying unit that biomass liquefying is completed has been directly passed to another group by oil circuit piping Complete the batch-type biomass liquefying unit of biomass charging.

The batch-type biomass liquefying unit includes SBH reactor, the biomass object that SBH reactor bottom is arranged in Material imported valve, the magnetic coupling blender being plugged in SBH reactor, the first steam escape valve that SBH reactor head is set Door, the heat exchanger being arranged in SBH reactor side wall, is matched with heat exchanger at the steam collector being connected with the first steam bleeding valve Close the heat exchange control unit used, the discharge gate that SBH reactor bottom is set, the flash tank being connected with discharge gate；

In the operating condition, the batch-type biomass liquefying unit of biomass liquefying is completed after heat transfer, the sequence batch SBH inside reactor temperature in formula biomass liquefying unit reduces, and when temperature is reduced to limiting value, closes and the batch-type The thermally conductive oil circuit piping of the low temperature that biomass liquefying unit matching uses, open discharge gate, by liquefied biomass with Steam explosion mode enters in flash tank；

And it completes the SBH reactor in another group of batch-type biomass liquefying unit of biomass charging and is led by low temperature After the heat transfer of hot oil circulating pipeline, SBH inside reactor temperature is increased, when the batch-type biomass for completing biomass liquefying When the thermally conductive oil circuit piping of the low temperature of liquefaction unit is closed, then the low temperature of another group of batch-type biomass liquefying unit is simultaneously closed off Thermally conductive oil circuit piping, and open the high-temperature heat-conductive oil circulating pipe used with another group of batch-type biomass liquefying unit matching The biomass of SBH reactor in another group of batch-type biomass liquefying unit is heated on road, until biomass liquefies completely.

The liquefied set temperature of SBH reactor endogenous substance is 200-300 DEG C, and the liquefaction duration is 10-30 Minute.

It is equipped in the SBH reactor for detecting the thermometer of oil temperature in heat exchanger, for detecting biomass temperature Thermometer, the liquidometer for detecting biomass liquid level, the explosive valve for preventing SBH reactor superpressure, for detecting heat exchanger With the pressure gauge of SBH reactor internal pressure.

The heat exchanger includes but is not limited to one in coil exchanger, tubular heat exchanger or jacketed type exchanger Kind；

The heat exchange control unit includes the first valve for connecting with coil exchanger and passing through for high temperature heat conductive oil Door and the second valve, the third valve and the 4th valve that connect with coil exchanger and pass through for low temperature conduction oil；

The top of the flash tank is equipped with the second steam bleeding valve, which passes through pipeline and steam collector It is connected.

The high-temperature heat-conductive oil circuit piping include in each batch-type biomass liquefying unit the first valve and High-temperature heat-conductive oil circulation pipe that second valve is connected, the high-temperature heat-conductive oil pump being arranged in high-temperature heat-conductive oil circulation pipe, High temperature heat conductive oil high position expansion slot, circuit control valve, high-temperature heat-conductive oil heat exchanger, high temperature heat conductive oil gate gurgle valve, urgent cooler And be used cooperatively with urgent cooler urgent cooler control valve, let out with high temperature heat conductive oil gate gurgle valve is used cooperatively first Oil groove, to the heat source of high-temperature heat-conductive oil circulation pipe heat supply；

The heat source includes but is not limited to one of biomass heat-conduction thermo oil boiler, steam oven or electric furnace.

The heat source mechanism includes being exchanged heat by heat-source Cycles pipeline and high temperature heat conductive oil as a preferred technical solution, Biomass heat-conduction thermo oil boiler that device is connected, conduction oil high position expansion slot, is led the Heat-transfer Oil Pump being arranged on heat-source Cycles pipeline The second drain pan that hot oil control valve and conduction oil gate gurgle valve and conduction oil gate gurgle valve are used cooperatively.

The thermally conductive oil circuit piping of the low temperature include in each batch-type biomass liquefying unit third valve and The thermally conductive oil circulation pipe of low temperature that 4th valve is connected, the low temperature Heat-transfer Oil Pump being arranged in the thermally conductive oil circulation pipe of low temperature, The third draining that low temperature conduction oil high position expansion slot and low temperature conduction oil gate gurgle valve and low temperature conduction oil gate gurgle valve are used cooperatively Slot.

The flash tank is successively connected with liquefying biomass liquid storage tank, subsequent bio matter lysate dehydration unit It connects.

The liquefying biomass liquid storage tank is hermetically sealed liquid storage tank, and the top of liquefying biomass liquid storage tank is put equipped with third Steam valve door, the third steam bleeding valve are connected by pipeline with steam collector；

The subsequent bio matter lysate dehydration unit includes successively being connected with liquefying biomass liquid storage tank Lysate heat exchanger, dehydrator and drier, the anaerobic digestor being connected with dehydrator, setting anaerobic digestor with split Solve the cooling water pump and cooling tower between liquid heat exchanger；

Liquid pump, the dehydrator and anaerobism are equipped between the liquefying biomass liquid storage tank and lysate heat exchanger Dehydration liquid delivery pump is equipped between digester；

The drier is equipped with the 4th steam bleeding valve, and the 4th steam bleeding valve is connected by pipeline with steam collector It is logical.

In the operating condition, it has cracked and the biomass cracking liquid to cool down through flash process is stored in liquefying biomass storage Liquid pool, lysate is delivered to the tube side of lysate heat exchanger, cracking after cooling by liquid pump in liquefying biomass liquid storage tank Liquid temperature drop to 50 DEG C hereinafter, and be delivered to dehydrator again from the lysate that lysate heat exchanger exports and be dehydrated, be dehydrated Biomass solid afterwards is delivered to drier again, obtains biomass dry particle of the moisture content less than 10%, and steam is by putting 4th steam bleeding valve is delivered to steam collector, discharges after processing；

The liquid deviate from when dehydration is high concentrated organic wastewater, and high concentrated organic wastewater generates biogas, natural pond through anaerobic digestion Gas uses after filtering, desulfurization as fuel, alternatively, high concentrated organic wastewater is through aerobic sigestion, direct processing up to standard.

The liquid deviate from when being dehydrated as a preferred technical solution, is high concentrated organic wastewater, by being dehydrated liquid delivery pump It is delivered to anaerobic digestor, and the hot water that the cooling biomass of lysate heat exchanger shell pass generates is conveyed to anaerobism by cooling water pump Thermal energy of the digester as hot digestion liquid, the biogas that anaerobic digestor generates filter, after desulfurization, the combustion as methane boiler Material, the thermal energy of methane boiler production then supply drier use.The biogas of generation can use in own system, can also be used as The energy is supplied to other users use.The biogas slurry that anaerobic digestion generates can be arranged directly if having had reached discharge standard It puts；If its certain index is still higher than discharge standard, need further to handle.The solid natural pond generated after anaerobic digestion Slag is still a kind of biomass, can be used as biomass material and reenters biomass liquefaction system processing.

The core apparatus of batch-type biomass liquefying (SBH) technique of the present invention is SBH reactor.Reactor is a circle Columnar tank is equipped with magnetic coupling blender.Helix tube type heat exchanger tube is installed in the side wall of reactor.Biomass enters anti- After answering device, the material inlet valve and steam bleeding valve of reactor are closed, and high temperature heat conductive oil heats biomass by heat exchanger, blender Work.With the raising of biomass temperature, a small amount of moisture in biomass can evaporate, but since reactor is that closed pressure is held Device (pressure resistance > 3MPa), the moisture when the steam pressure that evaporation generates is equal to the saturated vapor pressure of corresponding coolant-temperature gage, in biomass Evaporation will stop.After the biomass temperature in reactor is increased to cracking temperature, the biomass in reactor cracks substantially, Biomass is liquefied.

In practical application, the biomass of second group of SBH reactor, which is fed, to be completed when first group of SBH reactor heats up. After biomass liquefying in first group of SBH reactor, high temperature heat conductive oil will stop the heating of biomass.Low temperature conduction oil passes through Low temperature Heat-transfer Oil Pump, heat exchanger give thermal energy conduction to second group of SBH reactor, and the biomass in second group of SBH reactor will be by Preheating, and the lysate temperature in first group of SBH reactor will decline, pressure also decreases.When in second group of SBH reactor When the temperature of biomass is preheated to maximum value, the lysate temperature in first group of SBH reactor is also reduced to minimum.This When, the temperature in first group of SBH reactor will slightly above 100 DEG C, and pressure is slightly larger than atmospheric pressure.After preheating, first group of SBH Reactor starts to discharge, and second group of SBH reactor starts to be heated by high temperature heat conductive oil.

By opening the valve of first group of SBH reactor lower part, the lysate of decrease temperature and pressure enters flash tank (Flash Tank), the temperature of lysate also have decline by a small margin, pressure reduction to normal pressure (atmospheric pressure).Splitting after flash distillation Solution liquid enters liquid storage tank.Lysate in liquefying biomass liquid storage tank is through supercooling, dehydration, drying (if necessary), i.e., It can get carbonized particles.Since the evaporation of biomass during the reaction is very small, it will in carbonized particles obtained Retain very high combustion value, is good solid fuel.If the ingredient of biomass is municipal sludge, the calorific value of carbonized particles is general It can be more than 3000 kilocalories/kg, it is suitable with the combustion value of lignite, it can be used as the fuel of SBH system biological matter heat-conducting oil furnace.

Process system the present invention is based on batch-type biomass liquefier is batch-type work, each SBH reactor Duty cycle be 2-8 hour (according to the type of biomass, the volume determination of reactor).When biological quality to be treated compared with When big, need to install multiple groups SBH reactor.

In present invention process, biomass liquefying is completed by 2 or 2 or more SBH reactors, every group of SBH reactor In magnetic coupling blender, heat exchanger and other necessary monitorings and safety equipment are installed.Biomass is complete in SBH reactor It is that temperature of the biomass in SBH reactor reaches set temperature, and continue for the time of setting at liquefied judgment criteria.

When SBH reactor feed, SBH reactor should be kept interior, and there are certain vaporization spaces, i.e. biomass after charging Volume is less than the volume of SBH inside reactor.When SBH reactor feed, to guarantee that charging smoothly, is mounted on SBH reactor The steam bleeding valve on top should be opened, and after the completion of charging, to keep the pressure in SBH reactor, be mounted on SBH reactor top Steam bleeding valve should close.Be mounted on SBH reactor top steam bleeding valve release gas should collect after do deodorization, condensation process After can discharge.After the discharge valve for opening SBH reactor, in order to ensure whole crack biomass give off SBH reactor, also Open the steam bleeding valve for being mounted on SBH reactor top.Discharging flash tank top is equipped with large aperture steam bleeding valve, and SBH is anti- It should be opened before answering device to discharge.The gas that flash tank steam bleeding valve issues can discharge after doing deodorization, condensation process after should collecting.

In actual moving process, as long as there is material in SBH reactor, the magnetic stirring apparatus installed in SBH reactor is answered Remain operating status.

The heat exchanger of SBH reactor side wall installation can be jacket type, can also be coiled, the pressure resistance of collet or coil pipe Grade should be equal to the stress levels of reactor.

High temperature heat conductive oil required for SBH reactor heats is conveyed by a high-temperature and high-presure resistent Heat-transfer Oil Pump, and thermal energy is logical A heat-condutive oil heat exchanger is crossed to obtain.High temperature heat conductive oil flows in the tube side of heat exchanger, shell fluid flow of the heat source in heat exchanger. Thermal expansion tank, oil unloading trough and urgent cooler are installed in high-temperature heat-conductive oil return line.

The urgent cooler of high-temperature heat-conductive oil return line is a water-cooled cooler, by the 2 valve controls in outlet and entrance. Generally always there is a reactor to need to heat in high-temperature heat-conductive oil return line, therefore urgent cooler is often used without.When high temperature is led When not having reactor to need to heat in hot oil circuit, the heat source provided to high-temperature heat-conductive oil return line should be reduced, until closing.But work as The reduction of heat source is not prompt enough, and the constant temperature of high temperature heat conductive oil increases, and starts when up to or over permissible value urgent Cooler.

Low temperature conduction oil required for SBH reactor heats is conveyed by a high-temperature and high-presure resistent Heat-transfer Oil Pump, conduction oil Pump is recycled by conduction oil, and the heat of cracking reactor is sent to and completes biomass charging SBH reactor.One group of low temperature Heat-transfer Oil Pump circuit can only pass through low temperature Heat-conduction oil circulation system exchange heat within the same time between 2 groups of SBH reactors Energy.If necessary to have multipair SBH reactor in the same time while passing through low temperature Heat-conduction oil circulation system exchange thermal energy, then need A set of low temperature Heat-conduction oil circulation system is installed to each pair of SBH reactor.Every group of thermally conductive oil return line of low temperature is mounted on thermal expansion tank And oil unloading trough.

It can be high temperature heat conductive oil in heat-condutive oil heat exchanger shell side, led by biomass heat-conduction oil-furnace heating, and by one Hot oil pump is conveyed and is recycled, and forms heat-conducting oil furnace heat transfer oil circulation loop.Thermal expansion tank, oil unloading trough are installed in circuit.It is thermally conductive It is also possible to high-temperature steam in oil heat exchanger shell side, is provided by external high temperature vapour source.

The biomass fuel or other biological matter fuel that biomass heat-conduction oil oven can be produced directly using system itself.Such as Fruit does not have condition using biomass heat-conduction oil oven, can also use the heat-conducting oil furnace of other any patterns.

For biomass after cracking after flashing, temperature is still higher, needs to be squeezed into SBH cooler with pump first, cold But the biomass after enters holding pond.Subsequent dewatering process is waited to use.

Dewatered biomass can be used directly as fuel, can also be re-used as fuel use after drying.

The present invention replaces common steam directly to exchange heat using indirect heat exchange method, only has a kind of structure simple in technique Reactor, principle is simple, and process system integral pressure is low, and occupied area is small, small investment, be manufacture biomass fuel it is a kind of very Good selection.Present invention process directly recycles the thermal energy in pyrolysis liquefying biomass using indirect heat exchange method, using setting Standby few, recovery efficiency is high, during entire biomass liquefying, remains closed state, no steam release is urged without addition Agent, pressure are controlled by the saturated vapor pressure that relevant temperature is lauched.Since the thermal energy in present invention process is effectively recycled, Temperature of the biomass of pyrolysis liquefying in finally release (flash distillation) be close to 100 DEG C, and pressure is close to normal pressure, the thermal energy of loss Few, the loss of organic volatile part is few in biomass, and not only the utility value of final products is high, and greatly reduces operating cost.

Compared with prior art, the invention has the characteristics that:

1) biomass material completes whole liquefaction process in a reactor, and simple process adds life into reactor When material charge, to adding, pump required pressure is low, not harsh to the requirement of material size in system, as long as delivery pump can connect By particle size bigger (such as 5cm) is also without influence；

2) pressure in reactor is only related with the temperature of material, and is never more than the saturated vapor of corresponding temperature water Pressure, therefore being not necessarily to acid or basic catalyst during entire biomass liquefying reduces reaction pressure；

3) due in system operation, not adding acid or basic catalyst, therefore when general neutrophilous organism matter liquefaction, to system The requirement of middle equipment and pipe material reduces, without high anti-corrosion material (such as Stainless steel 316 L)；

4) it when material is heated in reactor tank by indirect medium, without depressurizing and discharging steam, is released without steam Put device, vapour condensation device etc.；

5) due to not having steam release in heating process, organic volatile part in biomass is sufficiently reserved, final carbon The calorific value for changing product is high；

6) by the energy of bio liquid after the recycling carbonization of indirect medium, simple process, recovery efficiency is high, total system Simple process, occupied area is small, invests small.

Detailed description of the invention

Fig. 1 is batch-type biomass liquefying cellular construction schematic diagram of the present invention；

In figure, 1-biomass material, 2-SBH reactor, 3-flash tank, 4-liquefying biomass liquid storage tank, 5-steam Collector, 6-subsequent bio matter lysate dehydration unit, 010-magnetic coupling blender, 01-the first valve, 02- Second valve, 03-third valve, 04-the 4th valve, 05-biomass material imported valve, 06-discharge gate, 07-the One steam bleeding valve, 08-the second steam bleeding valve, 09-third steam bleeding valve；

Fig. 2 is that present invention process stream illustrates journey figure；

In figure, 101,102,103,104-SBH reactor, 201-low temperature Heat-transfer Oil Pump, 202-low temperature conduction oil is high-order Expansion slot, 203-low temperature conduction oil gate gurgle valve, 204-third drain pan, 301-high-temperature heat-conductive oil pump, 302-high-temperature heat-conductive Oily high position expansion slot, 303,307-circuit control valve, 304-high-temperature heat-conductive oil heat exchanger, 305-high temperature heat conductive oil gate gurgle valve, 306-the first drain pan, 308,309-urgent cooler control valve, 310-urgent cooler, 401-biomass heat-conduction oil cauldron Furnace, 402-Heat-transfer Oil Pump, 403-conduction oil high position expansion slot, 404,405-thermally conductive oil control valve, 406-conduction oil draining Valve, 407-the second drain pan；

Fig. 3 is the flow diagram of subsequent bio matter lysate dehydration unit of the present invention；

In figure, 4-liquefying biomass liquid storage tank, 501-liquid pump, 502-lysate heat exchanger, 503-dehydrator, 504-drier, 505-the 4th steam bleeding valve, 5-steam collector, 601-anaerobic digestor, 602-cooling water pump, 603 - dehydration liquid delivery pump, 604-cooling tower, 7-subsequent technique, 8-the biogas of anaerobic digestor production, 9-biogas slurry, 10- Biogas residue.

Specific embodiment

The present invention is described in detail with specific embodiment below in conjunction with the accompanying drawings.

Embodiment:

A kind of batch-type biomass liquefying process, the technique directly recycle lysate metaplasia using indirect heat exchange mode Thermal energy in substance, technique include that two groups or more batch-type biomass liquefying unit being arranged in parallel and batch-type are raw The high-temperature heat-conductive oil circuit piping and the thermally conductive oil circuit piping of low temperature that substance liquefaction unit is used cooperatively, in the operating condition, When one group of batch-type biomass liquefying unit using high temperature heat conductive oil heat when, another group of batch-type biomass liquefying unit into Material, after the biomass in the batch-type biomass liquefying unit using high temperature heat conductive oil heating completes liquefaction, with the batch-type The high-temperature heat-conductive oil circuit piping that biomass liquefying unit matching uses is closed, and the thermally conductive oil circuit piping of low temperature is opened, and is beaten simultaneously Another group of thermally conductive oil circuit piping of low temperature for having completed the batch-type biomass liquefying unit of biomass charging is opened, will be completed The heat of the batch-type biomass liquefying unit of biomass liquefying is directly passed to another group of sequence for having completed biomass charging Batch biomass liquefying unit.

As shown in Figure 1, batch-type biomass liquefying unit includes SBH reactor 2, the life that 2 bottom of SBH reactor is arranged in Material charge imported valve 05, the magnetic coupling blender 010 being plugged in SBH reactor 2, setting are at 2 top of SBH reactor The first steam bleeding valve 07, be connected with the first steam bleeding valve 07 steam collector 5, be arranged in 2 side wall of SBH reactor Heat exchanger, the heat exchange control unit being used cooperatively with heat exchanger, the discharge gate 06 that 2 bottom of SBH reactor is set and discharging The flash tank 3 that valve 06 is connected.

In the operating condition, the batch-type biomass liquefying unit of biomass liquefying is completed after heat transfer, the sequence batch 2 internal temperature of SBH reactor in formula biomass liquefying unit reduces, and when temperature is reduced to limiting value, closes and the sequence batch The thermally conductive oil circuit piping of low temperature that formula biomass liquefying unit matching uses opens discharge gate 06, by liquefied biology Matter is entered in a manner of steam explosion in flash tank 3；

And the SBH reactor 2 in another group of batch-type biomass liquefying unit of biomass charging is completed by low temperature After the heat transfer of thermally conductive oil circuit piping, 2 internal temperature of SBH reactor is increased, when the batch-type for completing biomass liquefying is raw When the thermally conductive oil circuit piping of the low temperature of substance liquefaction unit is closed, then another group of batch-type biomass liquefying unit is simultaneously closed off The thermally conductive oil circuit piping of low temperature, and open the high temperature heat conductive oil used with another group of batch-type biomass liquefying unit matching and recycle Pipeline heats the biomass of SBH reactor 2 in another group of batch-type biomass liquefying unit, until biomass liquefies completely.

The liquefied set temperature of 2 endogenous substance of SBH reactor is 200-300 DEG C, and the liquefaction duration is 10-30 minutes.

It is equipped in SBH reactor 2 for detecting the thermometer of oil temperature in heat exchanger, the temperature for detecting biomass temperature Meter, the liquidometer for detecting biomass liquid level, the explosive valve for preventing 2 superpressure of SBH reactor, for detecting heat exchanger and SBH The pressure gauge of 2 internal pressure of reactor.

Heat exchanger includes but is not limited to one of coil exchanger, tubular heat exchanger or jacketed type exchanger.? In the present embodiment, heat exchanger is coil exchanger, and heat exchange control unit includes connecting with coil exchanger and for high temperature The first valve 01 and the second valve 02 that conduction oil passes through, for connecting with coil exchanger and passing through for low temperature conduction oil Three valves 03 and the 4th valve 04；

The top of flash tank 3 is equipped with the second steam bleeding valve 08, which passes through pipeline and steam collector 5 It is connected.

High-temperature heat-conductive oil circuit piping includes and the first valve 01 and second in each batch-type biomass liquefying unit High-temperature heat-conductive oil circulation pipe that valve 02 is connected, the high-temperature heat-conductive oil pump 301 being arranged in high-temperature heat-conductive oil circulation pipe, High temperature heat conductive oil high position expansion slot 302, circuit control valve 303,307, high-temperature heat-conductive oil heat exchanger 304, high temperature heat conductive oil draining Valve 305, urgent cooler 310 and the urgent cooler control valve 308,309 being used cooperatively with urgent cooler 310 and height The first drain pan 306 that warm conduction oil gate gurgle valve 305 is used cooperatively, to the heat source of high-temperature heat-conductive oil circulation pipe heat supply；Heat source Including but not limited to one of biomass heat-conduction thermo oil boiler, steam oven or electric furnace.

In the present embodiment, heat source uses biomass heat-conduction thermo oil boiler, including passes through heat-source Cycles pipeline and high-temperature heat-conductive It is biomass heat-conduction thermo oil boiler 401 that oil heat exchanger 304 is connected, the Heat-transfer Oil Pump 402 being arranged on heat-source Cycles pipeline, thermally conductive Oily high position expansion slot 403, thermally conductive oil control valve 404,405 and conduction oil gate gurgle valve 406 make with the cooperation of conduction oil gate gurgle valve 406 Second drain pan 407.

The thermally conductive oil circuit piping of low temperature includes and the third valve 03 and the 4th in each batch-type biomass liquefying unit The thermally conductive oil circulation pipe of the low temperature that valve 04 is connected, the low temperature Heat-transfer Oil Pump 201 being arranged in the thermally conductive oil circulation pipe of low temperature, Low temperature conduction oil high position expansion slot 202 and low temperature conduction oil gate gurgle valve 203 are used cooperatively with low temperature conduction oil gate gurgle valve 203 Third drain pan 204.

Flash tank 3 is successively connected with liquefying biomass liquid storage tank 4, subsequent bio matter lysate dehydration unit 6.

Liquefying biomass liquid storage tank 4 is hermetically sealed liquid storage tank, and the top of liquefying biomass liquid storage tank 4 is equipped with third steam escape valve Door 09, the third steam bleeding valve 09 are connected by pipeline with steam collector 5；

Subsequent bio matter lysate dehydration unit includes the lysate being successively connected with liquefying biomass liquid storage tank 4 Heat exchanger 502, dehydrator 503 and drier 504, are arranged in anaerobism the anaerobic digestor 601 being connected with dehydrator 503 Cooling water pump 602 and cooling tower 604 between digester 601 and lysate heat exchanger 502；

Liquid pump 501 is equipped between liquefying biomass liquid storage tank 4 and lysate heat exchanger 502, dehydrator 503 disappears with anaerobism Change and is equipped with dehydration liquid delivery pump 603 between tank 601；

Drier 504 is equipped with the 4th steam bleeding valve 505, and the 4th steam bleeding valve 505 passes through pipeline and steam collector 5 It is connected.

In practical application, biomass material imported valve 05 and the first steam bleeding valve 07 will be simultaneously when biomass is fed It opens, room temperature biomass material 1 enters SBH reactor 2 by biomass material imported valve 05, by raw material in SBH reactor 2 The gas of extrusion enters steam collector 5 by the first steam bleeding valve 07.After the completion of biomass charging, biomass material inlet valve Door 05 and the first steam bleeding valve 07 will simultaneously close off, and SBH reactor 2 is begun to warm up, at this point, the first valve 01, the second valve 02 It opens, remaining valve is closed.High temperature heat conductive oil enters coil exchanger, companion by valve the first valve 01, the second valve 02 With the starting of heat-conducting oil furnace, high temperature heat conductive oil is gradually warmed up, and the temperature of biomass also will be increased constantly in SBH reactor 2. Magnetic coupling blender 010 in SBH reactor 2 works, and keeps the biomass temperature in entire reactor uniform as much as possible.Add In thermal process, a small amount of moisture in biomass can evaporate, and generate steam, and the pressure in SBH reactor 2 also gradually rises.But by In SBH reactor 2 be closed pressure vessel (pressure resistance > 3MPa, or higher), when the pressure in reactor be equal to corresponding coolant-temperature gage Saturated vapor pressure (saturated vapor pressure) when, evaporation will stop.When the temperature of biomass in SBH reactor 2 When degree is increased to the biomass cracking temperature of setting, biomass is by pyrolysis liquefying.

After biomass liquefying, the first valve 01, the second valve 02 are closed.When first group of SBH reactor 2 heats, second group The biomass charging of SBH reactor 2 has been completed.First group and second group of third valve 03, the 4th valve 04 are opened, Remaining valve remains off.At this point, under the driving of external Heat-transfer Oil Pump, the coil heat exchanger of first group of SBH reactor 2 and Conduction oil in the coil heat exchanger of second group of SBH reactor 2, which will be formed, to be recycled, the lysate temperature in first group of SBH reactor 2 Degree and pressure decline, and the biomass temperature and pressure in second group of SBH reactor 2 will rise, in pyrolysis liquefying biomass Thermal energy is recycled.

When the temperature of first group of SBH reactor 2 drops to slightly above 100 DEG C, pressure is slightly above atmospheric pressure, and second group When the temperature of SBH reactor 2 is close to 100 DEG C, the preheating of biomass material terminates in second group.At this point, first group of SBH reactor 2 and third valve 03, the 4th valve 04 of second group of SBH reactor 2 be turned off.First valve of second group of SBH reactor 2 01, the second valve 02 is opened, and starts to heat second group of SBH reactor 2 with high temperature heat conductive oil.

The preheating of second group of SBH reactor 2 terminates also to indicate that first group of 2 decrease temperature and pressure of SBH reactor terminates, at this point, beating The dispensing valve 06 of first group of 2 bottom of SBH reactor is opened, lysate enters flash tank (Flash Tank) 3,3 top of flash tank The second steam bleeding valve 08 open, the steam that when flash distillation generates enters steam collector 5 by pipeline.After lysate flash distillation, temperature Degree will decrease to 100 DEG C hereinafter, and pressure will be reduced to normal pressure.After flash distillation, by connecting the pipeline of liquefying biomass liquid storage tank 4, Lysate will enter liquefying biomass liquid storage tank 4, and lysate passes through pipeline to subsequent bio matter lysate dehydration again Unit 6.There is blender in liquefying biomass liquid storage tank 4, prevents cracking liquid precipitate.

In Fig. 2, reactor 101,102,103,104 is 4 groups of SBH reactors in system, and the reactor in figure only gives The signal of each reactor heating heat conduction oil circuit, the principle of rest part refer to Fig. 1.

Low temperature Heat-transfer Oil Pump 201 is low temperature Heat-transfer Oil Pump, further includes that low temperature conduction oil is high in the thermally conductive oil circuit piping of low temperature Position expansion slot 202, low temperature conduction oil gate gurgle valve 203 and third drain pan 204.

High-temperature heat-conductive oil pump 301 is high-temperature heat-conductive oil circulating pump, further includes high-temperature heat-conductive in high-temperature heat-conductive oil circuit piping Oily high position expansion slot 302, circuit control valve 303 and 307, high-temperature heat-conductive oil heat exchanger 304,305 He of high temperature heat conductive oil gate gurgle valve First drain pan 306, urgent cooler 310, urgent cooler control valve 308 and 309.The heat source of high temperature heat conductive oil is from biology Matter heat conducting oil boiler 401, heat source mechanism further include Heat-transfer Oil Pump 402, conduction oil high position expansion slot 403, thermally conductive oil control valve 404 With 405, conduction oil gate gurgle valve 406 and the second drain pan 407.

If recycled in reactor 101, the thermal energy of crack biomass is preheated to the biomass in reactor 102, low Warm Heat-transfer Oil Pump 201 should start, 03 and of third valve of the third valve 03 and the 4th valve 04 of reactor 101, reactor 102 4th valve 04 is opened, remaining valve is closed, then the temperature and pressure of 101 endogenous substance lysate of reactor reduces, and reacts The temperature of 102 endogenous substance of device increases.In system shown in Fig. 2, in the same time, can only have between 2 groups of reactors by low Warm Heat-conduction oil circulation system exchanges thermal energy.It is recycled if necessary to have multipair reactor in the same time while passing through low temperature conduction oil Systems exchange thermal energy then needs to install a set of low temperature Heat-conduction oil circulation system to each pair of reactor.The heating expansion of low temperature conduction oil When, extra conduction oil will enter low temperature conduction oil high position expansion slot 202.It, can be by the circulatory system when heat-conducting oil system is safeguarded Low temperature conduction oil gate gurgle valve 203 is opened, and conduction oil flows into third drain pan 204.

High temperature heat conductive oil is reheated by high-temperature heat-conductive oil pump 301 to the biomass having been warmed up in reactor.At this point, returning Road control valve 303 and 307 should be at opening state.It heats specifically to which reactor, is determined according to the valve opened.Such as First valve 01 of reactor 101 and the second valve 02 are opened, remaining valve is closed, then high temperature heat conductive oil adds reactor 101 Heat.The heat source of high temperature heat conductive oil is obtained by high-temperature heat-conductive oil heat exchanger 304.High temperature heat conductive oil is in high-temperature heat-conductive oil heat exchanger It is flowed in 304 tube side, and the conduction oil that biomass heat-conduction boiler 401 heats is in the shell side stream of high-temperature heat-conductive oil heat exchanger 304 It is dynamic.When high temperature heat conductive oil heating expansion, extra conduction oil will enter high temperature heat conductive oil high position expansion slot 302.Heat-conducting oil system When maintenance, the high temperature heat conductive oil gate gurgle valve 305 of cycling element can be opened, conduction oil flows into the first drain pan 306.High-temperature heat-conductive A urgent cooler 310 is parallel in oil return line.Under normal circumstances, in high-temperature heat-conductive oil return line, always there is more than one reaction Device is heated using high temperature heat conductive oil.When not having reactor to heat in system using high temperature heat conductive oil, biomass heat-conduction oil oven is answered This subtracts fiery cooling.If since thermal inertia acts on, high temperature heat conductive oil persistently overheating has been approached or opens when more than setting value Urgent cooler 310 is moved, and opens simultaneously urgent cooler control valve 308 and 309.Urgent cooler 310 is a cooling dress It sets, by thermal energy consumption, the temperature of high temperature heat conductive oil can be reduced.

The heat source of high temperature heat conductive oil is provided by biomass heat-conduction thermo oil boiler 401, and Heat-transfer Oil Pump 402 is biomass heat-conduction oil oven When the circulating pump of conduction oil, biomass heat-conduction thermo oil boiler 401 and Heat-transfer Oil Pump 402 are run, thermally conductive oil control valve 404 and 405 is answered It is in the open state.Biomass heat-conduction thermo oil boiler 401 heat conduction oil high-temperature heat-conductive oil heat exchanger 304 shell fluid flow, To the high temperature heat conductive oil heating of tube side flow.When the conduction oil heating expansion that biomass heat-conduction thermo oil boiler 401 heats, extra is led Hot oil will enter conduction oil high position expansion slot 403.It, can be by the conduction oil of cycling element when biomass heat-conduction oil boiler system is safeguarded Gate gurgle valve 406 is opened, and conduction oil flows into the second drain pan 407.

As shown in figure 3, subsequent bio matter lysate dehydration unit includes successively being connected with liquefying biomass liquid storage tank 4 The lysate heat exchanger 502, dehydrator 503 and the drier 504 that connect, the anaerobic digestor 601 being connected with dehydrator 503, Cooling water pump 602 and cooling tower 604 between anaerobic digestor 601 and lysate heat exchanger 502 are set.

Liquid pump 501 is equipped between liquefying biomass liquid storage tank 4 and lysate heat exchanger 502, dehydrator 503 disappears with anaerobism Change and is equipped with dehydration liquid delivery pump 603 between tank 601.

In practical application, cracked and through flash process cool down biomass cracking liquid be stored in liquefying biomass storage Liquid pool 4, lysate is delivered to the tube side of lysate heat exchanger 502 by liquid pump 501 in liquefying biomass liquid storage tank 4, cooling Lysate temperature afterwards will settle to 50 DEG C hereinafter, various conventional equipments can be handled it.It is exported from lysate heat exchanger 502 Lysate be delivered to dehydrator 503 again, dewatered biomass solid is delivered to drier 504 (if necessary) again, Biomass dry particle of the moisture content less than 10% can finally be obtained.Biological particles are delivered in subsequent technique 7, can be made For energy use.Since biomass has cracked, dewatered biomass solid moisture content very little can be down to 30% hereinafter, such as Fruit continues to dry it.The steam that drying process generates is also seldom.Steam is delivered to steam receipts by putting the 4th steam bleeding valve 505 Storage 5 discharges after processing.

In the present embodiment, high concentrated organic wastewater is delivered to anaerobic digestor 601 by being dehydrated liquid delivery pump 603.Cracking The hot water that the cooling biomass of 502 shell side of liquid heat exchanger generates is conveyed to anaerobic digestor 601 as heating by cooling water pump 602 The thermal energy of digestive juice.The biogas 8 that anaerobic digestor 601 generates filters, after desulfurization, can be used as the fuel of methane boiler, biogas pot The thermal energy of furnace production then can be supplied to drier 504, as the heat source (not shown) that biomass is further dried.If dehydration Biomass afterwards is more than thermal energy required for drier 504 without the thermal energy that drying or methane boiler produce, and extra biogas is also Other usings energy source can be done.

The postdigestive biogas slurry 9 of anaerobic digestor 601, if having had reached discharge standard, it can direct emission；If Its certain index is still higher than discharge standard, then needs further to handle.The biogas residue 10 that anaerobic digestor 601 generates after digesting (few) then can be delivered to original biomass intensively, re-liquefied into SBH system together with other biological matter.

In the present embodiment process system, biomass liquefying is completed by 2 or 2 or more SBH reactors 2, and every group Magnetic coupling blender 010, heat exchanger and other necessary monitorings and safety equipment are installed in SBH reactor 2.

In the actual operation process, when one group of SBH reactor 2 is heated with high temperature heat conductive oil, another group of SBH reactor 2 Charging.After the biomass in one group of SBH reactor 2 completes liquefaction, the high-temperature heat-conductive oil return line of this group of SBH reactor 2 is closed, The thermally conductive oil return line of low temperature is opened, and the low temperature conduction oil for opening simultaneously the SBH reactor 2 that another group has been completed biomass charging returns The heat transfer that liquefying reactor is completed has been completed the SBH reactor 2 that biomass is fed to another group by road.Complete liquid Change SBH reactor 2 after heat transfer, the temperature inside SBH reactor 2 will reduce, and when temperature is reduced to limiting value, close The thermally conductive oil return line of low temperature opens the discharge gate 06 of reactor, and liquefied biomass will enter flash tank in a manner of steam explosion 3.After all liquefied biomass dischargings, it can restart new biomass charging.

Biomass charging SBH reactor 2 is completed after the heat transfer of the thermally conductive oil return line of low temperature, in SBH reactor 2 The temperature in portion will increase, and when the thermally conductive oil return line of low temperature for completing liquefaction SBH reactor 2 is closed, simultaneously close off and complete biomass Feed the thermally conductive oil return line of low temperature of SBH reactor 2.The high-temperature heat-conductive oil return line for completing biomass charging SBH reactor 2 is opened, To the material heating in SBH reactor 2, until the biomass in SBH reactor 2 completes liquefaction.

It is that temperature of the biomass in SBH reactor 2 reaches that biomass, which completes liquefied judgment criteria, in SBH reactor 2 Set temperature, and continue for the time of setting.

The set temperature range of biomass liquefying is 200-300 DEG C, and the duration set is 10-30 minute.Specifically Temperature and duration are different according to the type of biomass, need to determine by autoclave tests.

When SBH reactor 2 is fed, SBH reactor 2 should be kept interior, and there are certain vaporization spaces, i.e. biology after charging Plastid product is less than the volume inside SBH reactor 2.When SBH reactor 2 is fed, to guarantee that charging smoothly, it is anti-to be mounted on SBH Answering the first steam bleeding valve 07 on 2 top of device should open, and after the completion of charging, to keep the pressure in SBH reactor 2, be mounted on SBH The first steam bleeding valve 07 on 2 top of reactor should close.It is mounted on the first steam bleeding valve 07 releasing on 2 top of SBH reactor Gas can discharge after doing deodorization, condensation process after should collecting.

After the discharge gate 06 for opening SBH reactor 2, in order to ensure whole crack biomass give off SBH reactor 2, Also to open the first steam bleeding valve 07 for being mounted on 2 top of SBH reactor.Discharging 3 top of flash tank is equipped with large aperture second Steam bleeding valve 08, SBH reactor 2 should be opened before discharging.The gas that the second steam bleeding valve 08 on flash tank 3 issues should be collected After do deodorization, condensation process after can discharge.

In actual moving process, as long as there is material in SBH reactor 2, the magnetic stirring apparatus installed in SBH reactor 2 It should remain operating status.

SBH reactor 2 at least also to install detection heat exchanger in oil temperature thermometer, detect temperature of charge thermometer, The liquidometer (or level meter) for detecting material liquid level, the explosive valve for preventing 2 superpressure of SBH reactor, detection heat exchanger and SBH reaction The pressure gauge etc. of 2 internal pressure of device.

The heat exchanger of 2 side wall of SBH reactor installation can be jacket type, can also be coiled, collet or coil pipe it is resistance to Pressure grade should be equal to the stress levels of reactor.

High temperature heat conductive oil required for SBH reactor 2 heats is conveyed by a high-temperature and high-presure resistent Heat-transfer Oil Pump, and thermal energy is logical A heat-condutive oil heat exchanger is crossed to obtain.High temperature heat conductive oil flows in the tube side of heat exchanger, shell fluid flow of the heat source in heat exchanger. Thermal expansion tank, oil unloading trough and urgent cooler 310 are installed in high-temperature heat-conductive oil return line.

The urgent cooler 310 of high-temperature heat-conductive oil return line is a water-cooled cooler, by outlet and 2 valve controls of entrance System.Generally always there is a reactor to need to heat in high-temperature heat-conductive oil return line, therefore urgent cooler 310 is often used without.When When not having reactor to need to heat in high-temperature heat-conductive oil return line, the heat source provided to high-temperature heat-conductive oil return line should be reduced, until closing It closes.But when the reduction of heat source is not prompt enough, the constant temperature of high temperature heat conductive oil is increased, when up to or over permissible value it is necessary to Start urgent cooler.

Low temperature conduction oil required for SBH reactor 2 heats is conveyed by a high-temperature and high-presure resistent Heat-transfer Oil Pump, conduction oil Pump is recycled by conduction oil, and the heat of cracking reactor is sent to and completes biomass charging SBH reactor 2.One group low Warm Heat-transfer Oil Pump circuit can only be exchanged between 2 groups of SBH reactors 2 by low temperature Heat-conduction oil circulation system within the same time Thermal energy.If necessary to have multipair SBH reactor 2 in the same time while exchanging thermal energy by low temperature Heat-conduction oil circulation system, then It needs that a set of low temperature Heat-conduction oil circulation system is installed to each pair of SBH reactor 2.It is swollen that every group of thermally conductive oil return line of low temperature is mounted on heat Swell and oil unloading trough.

For biomass after cracking after flashing, temperature is still higher, needs to be squeezed into SBH cooler 2 with pump first, cold But the biomass after enters liquefying biomass liquid storage tank 4.Subsequent dewatering process is waited to use.

Dewatered dehydration liquid is high concentrated organic wastewater, can utilize, can also pass through directly as liquid organic matter Anaerobic digestion makes it produce biogas.The biogas that anaerobic digestion is produced can use in own system, can also be used as the energy and mention Other users are supplied to use.The biogas slurry that anaerobic digestion generates can be with direct emission if having had reached discharge standard；If Its certain index is still higher than discharge standard, then needs further to handle.The solid biogas residue generated after anaerobic digestion is still A kind of biomass can be used as biomass material and reenter biomass liquefaction system processing.

The present embodiment replaces common steam directly to exchange heat using indirect heat exchange method, only has a kind of structure simple in system Reactor, principle is simple, and system integral pressure is low, and occupied area is small, small investment, be manufacture biomass fuel one kind very well Selection.

The present embodiment system directly recycles the thermal energy in pyrolysis liquefying biomass using indirect heat exchange method, using setting Standby few, recovery efficiency is high, during entire biomass liquefying, remains closed state, no steam release is urged without addition Agent, pressure are controlled by the saturated vapor pressure that relevant temperature is lauched.Since the thermal energy in present system is effectively recycled, Temperature of the biomass of pyrolysis liquefying in finally release (flash distillation) be close to 100 DEG C, and pressure is close to normal pressure, the thermal energy of loss Few, the loss of organic volatile part is few in biomass, and not only the utility value of final products is high, and greatly reduces operating cost.

Claims

1. a kind of batch-type biomass liquefying process, which directly recycles pyrolysis liquefying biology using indirect heat exchange mode Thermal energy in matter, which is characterized in that the technique includes the batch-type biomass liquefying that two groups or more is arranged in parallel Unit, the high-temperature heat-conductive oil circuit piping and the thermally conductive oil circulating pipe of low temperature used with batch-type biomass liquefying unit matching Road；

In the operating condition, when one group of batch-type biomass liquefying unit is heated using high temperature heat conductive oil, another group of batch-type Biomass liquefying unit feed, the biomass in the batch-type biomass liquefying unit using high temperature heat conductive oil heating complete liquid It after change, is closed with the high-temperature heat-conductive oil circuit piping that the batch-type biomass liquefying unit matching uses, low temperature conduction oil circulation Pipeline is opened, and the low temperature conduction oil for opening simultaneously the batch-type biomass liquefying unit that another group has been completed biomass charging follows The heat for the batch-type biomass liquefying unit that biomass liquefying is completed is directly passed to another group and completed by endless tube road The batch-type biomass liquefying unit of biomass charging；

The batch-type biomass liquefying unit include SBH reactor (2), setting SBH reactor (2) bottom biomass Material inlet valve (05), is arranged in SBH reactor (2) the magnetic coupling blender (010) being plugged in SBH reactor (2) The first steam bleeding valve (07) at top, the steam collector (5) being connected with the first steam bleeding valve (07) are arranged and react in SBH Heat exchanger in device (2) side wall, the heat exchange control unit being used cooperatively with heat exchanger, setting unloading in SBH reactor (2) bottom Material valve (06), the flash tank (3) being connected with discharge gate (06)；

In the operating condition, the batch-type biomass liquefying unit of biomass liquefying is completed after heat transfer, and the batch-type is raw SBH reactor (2) internal temperature in substance liquefaction unit reduces, and when temperature is reduced to limiting value, closes and the batch-type The thermally conductive oil circuit piping of the low temperature that biomass liquefying unit matching uses is opened discharge gate (06), by liquefied biology Matter is entered in a manner of steam explosion in flash tank (3)；

And it completes the SBH reactor (2) in another group of batch-type biomass liquefying unit of biomass charging and is led by low temperature After the heat transfer of hot oil circulating pipeline, SBH reactor (2) internal temperature is increased, when the batch-type for completing biomass liquefying is raw When the thermally conductive oil circuit piping of the low temperature of substance liquefaction unit is closed, then another group of batch-type biomass liquefying unit is simultaneously closed off The thermally conductive oil circuit piping of low temperature, and open the high temperature heat conductive oil used with another group of batch-type biomass liquefying unit matching and recycle Pipeline heats the biomass of SBH reactor (2) in another group of batch-type biomass liquefying unit, until the complete liquid of biomass Change.

2. a kind of batch-type biomass liquefying process according to claim 1, which is characterized in that the SBH reactor (2) the liquefied set temperature of endogenous substance is 200-300 DEG C, and the liquefaction duration is 10-30 minutes.

3. a kind of batch-type biomass liquefying process according to claim 1, which is characterized in that the SBH reactor (2) it is equipped in for detecting the thermometer of oil temperature in heat exchanger, the thermometer for detecting biomass temperature, for detecting biology It is the liquidometer of matter liquid level, the explosive valve for preventing SBH reactor (2) superpressure, internal for detecting heat exchanger and SBH reactor (2) The pressure gauge of pressure.

4. a kind of batch-type biomass liquefying process according to claim 1, which is characterized in that the heat exchanger includes One of but be not limited to coil exchanger, tubular heat exchanger or jacketed type exchanger；

The heat exchange control unit includes the first valve (01) and for connecting with heat exchanger and passing through for high temperature heat conductive oil Two valves (02), the third valve (03) and the 4th valve (04) for connecting with heat exchanger and passing through for low temperature conduction oil；

The top of the flash tank (3) is equipped with the second steam bleeding valve (08), which passes through pipeline and vapour Body collector (5) is connected.

5. a kind of batch-type biomass liquefying process according to claim 4, which is characterized in that the high temperature heat conductive oil Circulation line include in each batch-type biomass liquefying unit the first valve (01) and the second valve (02) be connected High-temperature heat-conductive oil circulation pipe, the high-temperature heat-conductive oil pump (301) being arranged in high-temperature heat-conductive oil circulation pipe, high temperature heat conductive oil are high Position expansion slot (302), circuit control valve (303,307), high-temperature heat-conductive oil heat exchanger (304), high temperature heat conductive oil gate gurgle valve (305), urgent cooler (310) and the urgent cooler control valve being used cooperatively with urgent cooler (310) (308, 309) the first drain pan (306) for, being used cooperatively with high temperature heat conductive oil gate gurgle valve (305) is supplied to high-temperature heat-conductive oil circulation pipe The heat source of heat；

6. a kind of batch-type biomass liquefying process according to claim 4, which is characterized in that the low temperature conduction oil Circulation line include in each batch-type biomass liquefying unit third valve (03) and the 4th valve (04) be connected The thermally conductive oil circulation pipe of low temperature, the low temperature Heat-transfer Oil Pump (201) being arranged in the thermally conductive oil circulation pipe of low temperature, low temperature conduction oil are high The third that position expansion slot (202) and low temperature conduction oil gate gurgle valve (203) and low temperature conduction oil gate gurgle valve (203) are used cooperatively Drain pan (204).

7. a kind of batch-type biomass liquefying process according to any one of claims 1 to 6, which is characterized in that described Flash tank (3) is successively connected with liquefying biomass liquid storage tank (4), subsequent bio matter lysate dehydration unit (6).

8. a kind of batch-type biomass liquefying process according to claim 7, which is characterized in that the liquefying biomass Liquid storage tank (4) is hermetically sealed liquid storage tank, and the top of liquefying biomass liquid storage tank (4) is equipped with third steam bleeding valve (09), the third Steam bleeding valve (09) is connected by pipeline with steam collector (5)；

The subsequent bio matter lysate dehydration unit includes successively splitting with what liquefying biomass liquid storage tank (4) was connected Solution liquid heat exchanger (502), dehydrator (503) and drier (504), the anaerobic digestor being connected with dehydrator (503) (601), the cooling water pump (602) and cooling tower being arranged between anaerobic digestor (601) and lysate heat exchanger (502) (604)；

Liquid pump (501) are equipped between the liquefying biomass liquid storage tank (4) and lysate heat exchanger (502), described is de- Dehydration liquid delivery pump (603) is equipped between hydrophone (503) and anaerobic digestor (601)；

The drier (504) is equipped with the 4th steam bleeding valve (505), and the 4th steam bleeding valve (505) passes through pipeline and vapour Body collector (5) is connected.

9. a kind of batch-type biomass liquefying process according to claim 8, which is characterized in that in the operating condition, Biomass cracking liquid through cracking and through flash process cooling is stored in liquefying biomass liquid storage tank (4), liquefying biomass liquid storage Lysate is delivered to the tube side of lysate heat exchanger (502), lysate temperature after cooling by liquid pump (501) in pond (4) Drop to 50 DEG C hereinafter, and be delivered to dehydrator (503) again from the lysate that lysate heat exchanger (502) export and be dehydrated, Dewatered biomass solid is delivered to drier (504) again, obtains biomass dry particle of the moisture content less than 10%, and steams Vapour is delivered to steam collector (5) by putting the 4th steam bleeding valve (505), is discharged after processing；

The liquid deviate from when dehydration is high concentrated organic wastewater, and high concentrated organic wastewater generates biogas, biogas warp through anaerobic digestion It is used after filtering, desulfurization as fuel, alternatively, high concentrated organic wastewater is through aerobic sigestion, direct processing up to standard.