CN107353935A - A kind of method of wood tar hydrogenation combined unit substep dehydration - Google Patents
A kind of method of wood tar hydrogenation combined unit substep dehydration Download PDFInfo
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- CN107353935A CN107353935A CN201710665214.4A CN201710665214A CN107353935A CN 107353935 A CN107353935 A CN 107353935A CN 201710665214 A CN201710665214 A CN 201710665214A CN 107353935 A CN107353935 A CN 107353935A
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- wood tar
- high pressure
- dehydration
- separator
- cold
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- HYBBIBNJHNGZAN-UHFFFAOYSA-N Furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 title claims abstract description 59
- 239000011276 wood tar Substances 0.000 title claims abstract description 59
- 238000006297 dehydration reaction Methods 0.000 title claims abstract description 57
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 42
- 238000000605 extraction Methods 0.000 claims abstract description 16
- 239000002994 raw material Substances 0.000 claims abstract description 15
- 239000002283 diesel fuel Substances 0.000 claims abstract description 14
- 230000001131 transforming Effects 0.000 claims abstract description 11
- 239000000835 fiber Substances 0.000 claims description 69
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 59
- 239000000047 product Substances 0.000 claims description 33
- 238000000926 separation method Methods 0.000 claims description 19
- 238000004517 catalytic hydrocracking Methods 0.000 claims description 8
- 230000004048 modification Effects 0.000 claims description 5
- 238000006011 modification reaction Methods 0.000 claims description 5
- 239000007795 chemical reaction product Substances 0.000 claims description 4
- 230000002209 hydrophobic Effects 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 22
- 238000005265 energy consumption Methods 0.000 abstract description 12
- 238000006243 chemical reaction Methods 0.000 abstract description 8
- 238000005516 engineering process Methods 0.000 abstract description 8
- 239000001257 hydrogen Substances 0.000 abstract description 4
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 4
- 238000007792 addition Methods 0.000 abstract description 2
- 238000010977 unit operation Methods 0.000 abstract 1
- 208000005156 Dehydration Diseases 0.000 description 43
- 239000003921 oil Substances 0.000 description 19
- 239000000463 material Substances 0.000 description 16
- 239000012530 fluid Substances 0.000 description 14
- 230000000694 effects Effects 0.000 description 13
- 239000002028 Biomass Substances 0.000 description 10
- 239000012075 bio-oil Substances 0.000 description 8
- 238000004581 coalescence Methods 0.000 description 7
- 239000012528 membrane Substances 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 4
- 230000001172 regenerating Effects 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 3
- 239000010779 crude oil Substances 0.000 description 3
- 230000018109 developmental process Effects 0.000 description 3
- 230000005684 electric field Effects 0.000 description 3
- 238000004945 emulsification Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000011068 load Methods 0.000 description 3
- 210000004080 Milk Anatomy 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000009954 braiding Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000007806 chemical reaction intermediate Substances 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000005238 degreasing Methods 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 230000001804 emulsifying Effects 0.000 description 2
- 239000000839 emulsion Substances 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000000543 intermediate Substances 0.000 description 2
- 239000008267 milk Substances 0.000 description 2
- 235000013336 milk Nutrition 0.000 description 2
- 239000002594 sorbent Substances 0.000 description 2
- 239000011269 tar Substances 0.000 description 2
- 229940010415 CALCIUM HYDRIDE Drugs 0.000 description 1
- UUGAXJGDKREHIO-UHFFFAOYSA-N Calcium hydride Chemical compound [H-].[H-].[Ca+2] UUGAXJGDKREHIO-UHFFFAOYSA-N 0.000 description 1
- 229940108066 Coal Tar Drugs 0.000 description 1
- 229920002488 Hemicellulose Polymers 0.000 description 1
- 229920002521 Macromolecule Polymers 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Natural products OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 230000004308 accommodation Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive Effects 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 230000000903 blocking Effects 0.000 description 1
- XFYHPLORZKFKSC-UHFFFAOYSA-N calcium;alumanuide Chemical compound [AlH4-].[AlH4-].[Ca+2] XFYHPLORZKFKSC-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic Effects 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 238000005039 chemical industry Methods 0.000 description 1
- 238000005253 cladding Methods 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000005686 electrostatic field Effects 0.000 description 1
- 239000003995 emulsifying agent Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 150000002170 ethers Chemical class 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 150000002240 furans Chemical class 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000001764 infiltration Methods 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 230000004301 light adaptation Effects 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 150000003881 polyketide derivatives Chemical class 0.000 description 1
- 229930001119 polyketides Natural products 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 239000002023 wood 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
Abstract
The invention discloses a kind of method of wood tar in wood tar hydrogen addition technology field hydrogenation combined unit substep dehydration, this method comprises the following steps：(1) the wood tar raw material of wood tar hydrogenation deoxidation device first passes through deep dehydration unit；(2) BDO device reactions product enters transformation BDO cold high pressure separators and carries out preliminary hydro-extraction processing；(3) OTM device reactions product enters in transformation OTM cold high pressure separators and carries out preliminary hydro-extraction processing；(4) naphtha and light diesel fuel product most dispatch from the factory after deep dehydrator is handled afterwards.The technological process proposed using this method, combined unit raw material, intermediate product, final products are hydrogenated with to wood tar and carry out substep dewater treatment.Wood tar hydrogenation combined unit operation energy consumption after substep dewater treatment technique significantly declines, and product quality greatly improves, and device parallel-adder settle-out time increases significantly, improves the economic benefit of package unit.
Description
Technical field
The invention belongs to the field of bio-crude oil Hydrogenation petrol and diesel oil device oil dehydrating, and in particular to a kind of wood tar adds
The method of hydrogen combined unit distribution dehydration, specifically, the raw material, intermediate product, final production of combined unit are hydrogenated with to wood tar
Product carry out deep dehydration processing, realize the low energy consumption of wood tar hydrogenation combined unit, the target of stable operation.
Background technology
The energy is the important substance basis for maintaining the stable existence of the mankind and long-run development, non-renewable fossil energy with
A large amount of exploitations of the mankind use, and will inevitably welcome the day of exhaustion.The continuous reduction of fossil energy and bring increasingly tight
The problem of environmental pollution of weight, all promotes the fast development of regenerative resource.
Biomass energy can efficiently be utilized by biomass energy switch technology, produce various clean energy resource and chemical industry productions
Product, so as to reduce dependence of the mankind for fossil energy, mitigate fossil energy and consume to pollution caused by environment.At present, the world
Especially developed country of various countries, all it is being directed to developing efficient, free of contamination biomass energy utilization technologies, with the ore deposit of protection this country
Thing energy resources, to realize that the sustainable development of national economy provides basic guarantee.Biomass pyrolytic refers to that biomass is not having
Oxidant (air, oxygen, vapor etc.) exists or is provided only with conditions of limiting oxygen, is heated to exceed 500 DEG C, passes through heat chemistry
Fuel material (the solid-state compared with small molecule is resolved into biomass macromolecular substances (lignin, cellulose and hemicellulose) in reaction
Charcoal, combustible gas, bio oil) thermochemical study technical method.The fuel energy conversion ratio of biomass pyrolytic is up to 95.5%, most
Biomass energy is converted into energy products by limits, is made the best use of everything, and be pyrolyzed and burning and gasify it is essential just
Stage beginning.
Bio oil is high as a kind of get more and more people's extensive concerning but bio oil oxygen content of regenerative resource, complicated components.
Include the multiclass material such as phenols, aldehydes, ketone, ethers and furans, exist it is aqueous it is more, calorific value is low, poor chemical stability, no
It can dissolve each other and the shortcomings of corrosivity, current motive power machine equipment can not be directly applied to, it is necessary to by catalytic hydrodeoxygenation essence
Unionfining technique is made and be hydrocracked to be modified, improves the standard that clean fuel is can be only achieved after the quality of oil product.
Biomass energy is as a kind of regenerative resource of cleaning, and unique regenerative resource, the fast speed heat of biomass
It is considered as one of most potential application technology that solution bio oil and bio oil catalytic hydrogenation, which prepare green traffic fuel, its
In be most widely used with wood tar.Wood tar be organic matter in agricultural solid waste by fast pyrolysis technology, it is produced
Liquid bio-oil, key component includes tar, solvent naphtha and oxygenatedchemicals etc., can be used directly as fuel, by adding
The substitute of fossil fuel can be turned into after hydrogen refinement treatment.Wood tar hydrogenation combined unit is that wood tar raw material is de- by hydrogenation
After oxygen PROCESS FOR TREATMENT is handled with hydrocracking process, final output hydrotreated naphtha product.Combined unit is hydrogenated with hydrogenation process
In can produce minor amount of water, existing dehydration equipment can not carry out deep dehydration processing to material, plant running be caused compared with heavy load,
Plant running high energy consumption at present, Useful Time of Hydrogenation Catalyst is short, and device parallel-adder settle-out time is short, and main cause is hydrogenation joint
Water content is high in device single unit system, and severe jamming is caused to plant running, is badly in need of one kind and hydrogenation combined unit substep is dehydrated
Technique, reduce single unit system water content.
The method of oil dehydrating at present mainly have gravitational separation process, centrifugal separation, electric field dehydration method, vacuum dehydration method,
The methods of chemical demulsification evaporation, absorption process, absorption method, membrane separation process, coalescence evaporation.
The larger fluid of aqueous concentration is typically handled using gravitational separation process, from the point of view of service condition, the master of gravitational settling
Want equipment and have except water pot, except pond etc., it is necessary to very big container and very low flow velocity, processing time is longer, degreasing fluid can not be removed
In dissolving water and emulsified water.
Centrifugal separation is typically used for the quick separating of free water, is not suitable for dissolving the separation of water and emulsified water.It is quiet
Electric dehydration method refers to that crude oil emulsion in the presence of electrostatic field, realizes electrostatic demulsifying, makes water droplet in gravity or centrifugation masterpiece
Grown up with lower rapid coalescence, to reach the purpose of water-oil separating, but electric field dehydration method has the defects of obvious：Equipment operation energy consumption
Compare high, operating safety risks be present.
Vacuum dehydration refer to due to oil it is different with the boiling point of water, the two separation can be made by the method for vacuum distillation, but
Vacuum dehydration needs that fluid is heated to the boiling point of water under the pressure under vacuo, so energy consumption is very high.The equipment of vacuum dehydration
General capacity is smaller, and treatment effeciency is relatively low.
Chemical demulsification is dehydrated, and mainly utilizes the materials such as the stronger demulsifier of surface-active so that demulsification agent molecule penetrates into
And adsorb on oil-water interface, the additive molecules such as emulsifying agent therein are displaced, change interface membrane property ruptures up to film,
So that the small water droplet of cladding constantly collides coalescence into large water droplet in film, divide under the effect of the other manners such as gravity with fluid
Leave and, although demulsifier is widely used in crude oil emulsion dehydration field, because the addition of chemical reagent may
Secondary pollution can be produced to oil product, its physical and chemical performance be influenceed, so the application in terms of fluid dehydration is ripe not enough.
Material (such as calcium hydride, aluminum hydride and the metal oxide easily to be chemically reacted with water is added in fluid
Deng), the moisture in fluid, referred to as absorption dewatering method are consumed using these materials, this method mainly removes degreasing fluid
In free water.But the material easily to be chemically reacted with moisture is added into fluid, then need to carry out sternly reaction product
Lattice processing, thus improve the complexity of dewatering process and equipment, while add cost, institute is in this way in practice also very
Few application.
Absorption method i.e. using the material such as the preferable polymeric sorbent of water absorbing properties, by Free water contained in fluid and
Emulsified water absorbs, and to realize water-oil separating, but absorbent material can quickly reach its saturation degree, and the cost of polymeric sorbent with
Regeneration cost is all higher, thus absorption method applies in general to the very low occasion of fluid water content.
Membrane separation process is the lipophile or hydrophily using porous membrane, is oozed by screening, film split-phase, counter-infiltration or surpass
Saturating principle separates oil and the water in liquid liquid dispersion, but membrane separation process processing speed is slow, the low service life of film is film point
From the technical barrier of method.In addition, when removing the high lubricating oil of viscosity, also without good membrane separation assemblies.
5-20um emulsification state water droplet can be kept completely separate by coalescence evaporation, and without adding chemical reagent, equipment is taken up an area
Area is small, and cost of investment is low.
Patent ZL01823742.8 oil dehydrators disclose a kind of method that oily dehydration is carried out using film, but exist use into
This height, easily pollute the problem of damage；The patent of Application No. 200810042145.2 disclose a kind of method of diesel oil dewatering with
Device, the patent are separated using eddy flow method, due to the technical characteristic of cyclonic separation, only can be suitably used for more than 15 μm of trip
From the separation of water droplet, and it is larger to operate pressure drop, it is impossible to realizes oil product efficiently and the deep dehydration of low consumption；Patent
ZL201010145423.4 discloses a kind of heavy oil and coal tar dehydrator, using roller evaporated form be dehydrated, relative energy consumption compared with
Height, operation is complex, is only applicable to the oil dehydrating process of particular medium, ZL200910065725.8 discloses a kind of use
The method and device of electric field dehydration, patent 201010261697.X disclose a kind of method and dress using ultrasonic technology dehydration
Put, the patent of Application No. 201310352748.3 discloses a kind of method using filtering-eddy flow-coalescence-eddy flow and carries out weight
The method of dirty oil dewatering, above patented technology are only applicable in specific occasion, all there is that energy consumption is higher, accommodation is narrower asks
Topic, the requirement of oil product deep dehydration is not reached yet.
Wood tar hydrogenation combined unit is badly in need of a kind of strong applicability, dehydrating effect stabilization, the dehydration technique of efficiency high at present,
Substep dehydration is carried out to water caused by hydrogenation each process of combined unit, reduces plant energy consumption, lifting device economic benefit.
The content of the invention
In order to solve the deficiencies in the prior art, the present invention based on nona modified fiber modular polyketide junction depth dehydration technique with
Its special form of presentation, X-type form of presentation and Ω type form of presentations, unique demulsification advantage, are different from general filer element type
Coalescence dehydration, fibre module porosity is larger, can pass through minute solid particles, it is not easy to the advantages that blocking, has invented a kind of wood
The method of hydrogenation of tar combined unit distribution dehydration, concrete technical scheme are as follows：
A kind of method of wood tar hydrogenation combined unit substep dehydration, comprises the following steps：
(1) the wood tar raw material of wood tar hydrogenation deoxidation device (BDO devices) first passes through deep dehydration unit；Taken off through depth
Wood tar after water is mixed into BDO device hydrogenation deoxidation reactors with the light diesel fuel raw material of BDO devices again；
(2) BDO device reactions product enters transformation BDO cold high pressure separators and carries out preliminary hydro-extraction processing；Engineered BDO
Distillate after cold high pressure separator preliminary hydro-extraction is entered in transformation BDO cold low separators, after carrying out deep dehydration processing
Wood tar is entered to be hydrocracked in (OTM) device；
(3) OTM device reactions product, which is entered in transformation OTM cold high pressure separators, carries out preliminary hydro-extraction processing, engineered
Distillate after OTM cold high pressure separator preliminary hydro-extractions is entered in transformation OTM cold low separators, carries out deep dehydration processing
Enter afterwards in fractionating column and be fractionated, output naphtha and light diesel fuel product；
(4) naphtha and light diesel fuel product most dispatch from the factory after deep dehydrator is handled afterwards.
Deep dehydration unit described in step (1) is nona modified fiber modularization dehydrator, in modularization dehydrator
Portion's structure uses the dehydrated structure that Chinese patent ZL201410210965.3 is proposed, is rectification mould respectively according to flow direction
Block, X-type establishment fibre module, ripple plate module, Ω types establishment fibre module, the wood tar feed moisture content is 0.5%-
0.6%, wood tar water content is in below 100ppm after processing.
Study and find through inventor's long-term experiment, in X-type cohesive fiber module, when lipophilic-hydrophobic property fiber is dredged with hydrophilic
When oiliness fiber angle is 25~45 °, there is efficient separative efficiency to emulsification water droplet, because when angle is smaller, emulsify water droplet
When moving at two kinds of fiber nodes, water droplet receives the drag of hydrophilic and oleophobic property fiber, and angle is smaller, horizontal displacement distance phase
Deng when water droplet loading process it is longer, it is easier to separate.When lipophilic-hydrophobic property fiber and hydrophilic category oiliness fiber angle are 45~60 °
When, the quick separating of the water droplet poor to emulsifying effectiveness has preferable effect.In Ω moldeed depth degree separates fibre module, fiber
Number of braided strand is more, and voidage is smaller, and fibre module separating effect is better；It is hydrophilic to dredge under the conditions of the braiding of identical fibre number of share of stock
Oiliness fiber proportion is more, then depth water removal effect is better.X-type cohesive fiber module and Ω moldeed depth degree separation fibre module
In two kinds of fibers pass through modification, fiber string diameter is smaller, by the cross sectional flow rate of fiber it is smaller i.e. fluid in fiber mould
The residence time is longer in block, has preferably for the break milk separation for disperseing the capture of water droplet, coalescence is grown up and emulsifies water droplet
Effect.
Cold high pressure separator described in step (2) and step (3) is to separate with cold low reform of separator method
Install separation internals inside device additional, cold high pressure separator internals are that X-type works out fibre module, ripple plate module, cold low separator
Internals are that Ω types work out fibre module；Water content is in below 1000ppm after cold high pressure separator is handled, through cold low separator
Water content after processing is in below 100ppm.
Deep dehydrator described in step (4) uses nona modified fiber candle filter, nona modified fiber filter
Core is wrapped in core pipe and is made by hydrophilic, hydrophobic two kinds of fibers shuffling in varing proportions.Fiber string diameter is 50-200 μm,
The a diameter of DN50-DN500 of core pipe.Through deep dehydration device processing after product water content below 50ppm (temperature control 50 DEG C with
Under), reach technical indicator of dispatching from the factory.
The beneficial effects of the present invention are：
(1) present invention is dehydrated for the charging of wood tar hydrogenation combined unit, intermediate product, final products substep, for
Different material, different treatment technology indexs, design respective dehydrator inner member, are ensureing the technical requirements of technique dehydration,
Reduce the design cost of device.
(2) dehydrating effect of the present invention is good, and operating flexibility is big, the dewater treatment requirement suitable for hydrogenation process integration, drop
The operation energy consumption of low each technological process, improve product quality, the economic benefit of lifting device.
(3) present invention, which can use, transforms existing apparatus or newly goes up equipment, and improvement cost is low, dehydration equipment operation energy consumption
It is low, extra processing cost is not produced.
Brief description of the drawings
Fig. 1 is the device flow chart of embodiment 1；
Fig. 2 is nona modified fiber modularization evaporator structure schematic diagram；
Fig. 3 is nona modified fiber candle filter structural representation.
Symbol description：
1 wood tar raw material dehydration device；2 BDO hydrogenation deoxidation reactors；3 BDO cold high pressure separators；
4 BDO cold low separators；5 OTM hydrocracking reactors；6 OTM cold high pressure separators；
7 OTM cold low separators；8 COU bio oil fractionating columns；9 product oil deep dehydration devices；
10 fluid rectification distributors；11 X-type cohesive fiber modules；12 strengthen settling module；
13 Ω moldeed depth degree separate fibre module；14 nona modified fiber filter cores；
F1 wood tar raw materials；Wood tar raw material after F2 dehydrations；F3 hydrogenation deoxidation reaction intermediates；
Material after the cold high score preliminary hydro-extractions of F4；Material after the cold low point of deep dehydration of F5；
F6 hydrocracking reaction intermediate products；Material after the cold high score preliminary hydro-extractions of F7；
Material after the cold low point of preliminary hydro-extraction of F8；F9 fractionator products；F10 product oils；
Embodiment
The present invention is specifically described below by embodiment 1.It is necessarily pointed out that following examples are only used
In the invention will be further described, it is impossible to be interpreted as limiting the scope of the invention, professional and technical personnel in the field
Some the nonessential modifications and adaptations made according to present disclosure, still fall within protection scope of the present invention.
30,000 tons/year of wood tar hydrogenation joint pilot-plants of certain energy company, by wood tar hydrogenation deoxidation device, (BDO is filled
Put), wood tar hydrocracking unit (OTM devices) constituted jointly with biological oil separating device (COU devices), combined unit is main
Effect is final output light diesel fuel, heavy diesel fuel by wood tar raw material after hydrogenation deoxidation technique and hydrocracking process processing
With the conventional fossil fuel product such as naphtha.But device is found in the process of running, material moisture index is tight in combined unit
Weight is exceeded, and micro-moisture is produced in hydrogenation process, subsequent reactions device is interfered, existing dehydration equipment can not be to thing
Material carries out deep dehydration processing, at present plant running high energy consumption, and Useful Time of Hydrogenation Catalyst is short, device parallel-adder settle-out time
Short, main cause is that water content is high in hydrogenation combined unit single unit system, and severe jamming is caused to plant running, and it is a kind of right to be badly in need of
Combined unit substep dehydrating process is hydrogenated with, reduces single unit system water content.The invention provides a kind of wood tar hydrogenation to combine
The method of device substep dehydration.Process chart is as shown in Figure 1：
Wood tar raw material first passes through deep dehydration unit 1；Wood tar after the deep dehydration light diesel fuel with BDO devices again
Raw material is mixed into BDO device hydrogenation deoxidations reactor 2；BDO device reaction products enter transformation BDO cold anticyclone separation
Device 3 carries out preliminary hydro-extraction processing；It is cold low that distillate after the engineered preliminary hydro-extraction of BDO cold high pressure separators 3 enters transformation BDO
Press in separator 4, entering wood tar after progress deep dehydration processing is hydrocracked in (OTM) reactor 5；OTM device reactions
Product, which is entered in transformation OTM cold high pressure separators 6, carries out preliminary hydro-extraction processing, and engineered OTM cold high pressure separators 6 are tentatively de-
Distillate after water is entered in transformation OTM cold lows separator 7, enters bio oil separator after carrying out deep dehydration processing
In fractionating column 8 in be fractionated, output naphtha and light diesel fuel product；Naphtha and light diesel fuel product are most afterwards through deep dehydration
Dispatched from the factory after the processing of device 9.
The deep dehydration unit that the present invention uses is nona modified fiber modularization dehydrator, as shown in Figure 2.Modularization takes off
Hydrophone internal structure uses the dehydrated structure that Chinese patent ZL201410210965.3 is proposed, according to flow direction, is respectively
Rectification module, X-type establishment fibre module, ripple plate module, Ω types establishment fibre module, the wood tar feed moisture content are
0.5%-0.6%, wood tar water content is in below 100ppm after processing.
Study and find through inventor's long-term experiment, in X-type cohesive fiber module, when lipophilic-hydrophobic property fiber is dredged with hydrophilic
When oiliness fiber angle is 25~45 °, there is efficient separative efficiency to emulsification water droplet, because when angle is smaller, emulsify water droplet
When moving at two kinds of fiber nodes, water droplet receives the drag of hydrophilic and oleophobic property fiber, and angle is smaller, horizontal displacement distance phase
Deng when water droplet loading process it is longer, it is easier to separate.When lipophilic-hydrophobic property fiber and hydrophilic category oiliness fiber angle are 45~60 °
When, the quick separating of the water droplet poor to emulsifying effectiveness has preferable effect.In Ω moldeed depth degree separates fibre module, fiber
Number of braided strand is more, and voidage is smaller, and fibre module separating effect is better；It is hydrophilic to dredge under the conditions of the braiding of identical fibre number of share of stock
Oiliness fiber proportion is more, then depth water removal effect is better.X-type cohesive fiber module and Ω moldeed depth degree separation fibre module
In two kinds of fibers pass through modification, fiber string diameter is smaller, by the cross sectional flow rate of fiber it is smaller i.e. fluid in fiber mould
The residence time is longer in block, has preferably for the break milk separation for disperseing the capture of water droplet, coalescence is grown up and emulsifies water droplet
Effect.
The cold high pressure separator that the present invention uses is to install additional to divide in separator interior with cold low reform of separator method
From internals, cold high pressure separator internals are that X-type works out fibre module, ripple plate module, and cold low separator internals are compiled for Ω types
Fibre module processed；Water content is aqueous after the processing of cold low separator in below 1000ppm after cold high pressure separator is handled
Amount is in below 100ppm.
The deep dehydrator that the present invention uses uses nona modified fiber candle filter, as shown in Figure 3.Nano modification
Fabric filter element is wrapped in core pipe and is made by hydrophilic, hydrophobic two kinds of fibers shuffling in varing proportions.Fiber string diameter is 50-
200 μm, a diameter of DN50-DN500 of core pipe.In below 50ppm, (temperature control exists product water content after the processing of deep dehydration device
Less than 50 DEG C), reach technical indicator of dispatching from the factory.
After 30,000 tons/year of wood tar hydrogenation combined units of certain energy company are transformed using method provided by the invention, warp
Wood tar raw material is demarcated after deep dehydration cell processing, feed moisture content drops to below 100ppm by 0.5%, and wood tar adds
Hydrogen device for deoxidizing (BDO devices) takes off with wood tar hydrocracking unit (OTM devices) product water content through preliminary hydro-extraction and depth
Stability contorting is in below 100ppm after water process, and control is in below 50ppm when running preferable；(COU is filled biological oil separating device
Put) the product oil that fractionates out after deep dehydrator is handled, product oil water content control 50ppm (temperature 50 DEG C with
Under).Calibration result proves that the substep dewatering through the present invention, the energy consumption of wood tar hydrogenation combined unit significantly declines, and urges
The agent life-span greatly prolongs, and product quality significantly improves, and device economic benefit significantly improves.
Claims (4)
1. a kind of method of wood tar hydrogenation combined unit substep dehydration, this method comprise the following steps：
(1) the wood tar raw material of wood tar hydrogenation deoxidation device first passes through deep dehydration unit；Wood tar after deep dehydration
Wood tar hydrogenation deoxidation device hydrogenation deoxidation reactor is mixed into the light diesel fuel raw material of wood tar hydrogenation deoxidation device again
In；
(2) wood tar hydrogenation deoxidation device reaction product enters wood tar hydrogenation deoxidation cold high pressure separator and carries out preliminary hydro-extraction
Processing；Distillate after wood tar hydrogenation deoxidation cold high pressure separator preliminary hydro-extraction enters wood tar hydrogenation deoxidation cold low
In separator, entered after carrying out deep dehydration processing in wood tar hydrocracking unit；
(3) wood tar hydrocracking unit reaction product enters transformation wood tar and is hydrocracked in cold high pressure separator at the beginning of progress
Dewater treatment is walked, the distillate after wood tar is hydrocracked cold high pressure separator preliminary hydro-extraction enters wood tar and is hydrocracked
In cold low separator, enter after progress deep dehydration processing in fractionating column and be fractionated, output naphtha and light diesel fuel product；
(4) naphtha and light diesel fuel product most handle post processing through deep dehydrator afterwards and completed.
2. method as claimed in claim 1, it is characterised in that the deep dehydration unit described in step (1) is nano modification fibre
Modularization dehydrator is tieed up, modularization dehydrator internal structure, is rectification module, X-type establishment fiber mould respectively according to flow direction
Block, ripple plate module, Ω types establishment fibre module, the wood tar feed moisture content is 0.5%-0.6%, wood tar after processing
Water content is in below 100ppm.
3. method as claimed in claim 1, it is characterised in that cold high pressure separator described in step (2) and step (3) with it is cold
Low pressure separator is to install separation internals additional in separator interior, and cold high pressure separator internals are that X-type works out fibre module, ripple
Plate module；Cold low separator internals are that Ω types work out fibre module；Water content is in 1000ppm after cold high pressure separator is handled
Hereinafter, the water content after the processing of cold low separator is in below 100ppm.
It is 4. as claimed in claim 1, it is characterised in that the deep dehydrator described in step (4) uses nona modified fiber
Candle filter, nona modified fiber filter core are wrapped in core pipe and made by hydrophilic, hydrophobic two kinds of fibers shuffling in varing proportions
Form；Fiber string diameter is 50-200 μm, a diameter of DN50-DN500 of core pipe；The product water content after the processing of deep dehydration device
Below 50ppm.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201710665214.4A CN107353935A (en) | 2017-08-04 | 2017-08-04 | A kind of method of wood tar hydrogenation combined unit substep dehydration |
| CN201810144643.1A CN108373931A (en) | 2017-08-04 | 2018-02-11 | A kind of biomass pyrolysis liquid adds the method for hydrogen combined unit substep dehydration |
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| CN201710665214.4A CN107353935A (en) | 2017-08-04 | 2017-08-04 | A kind of method of wood tar hydrogenation combined unit substep dehydration |
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| CN201810144643.1A Pending CN108373931A (en) | 2017-08-04 | 2018-02-11 | A kind of biomass pyrolysis liquid adds the method for hydrogen combined unit substep dehydration |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108002635A (en) * | 2017-12-28 | 2018-05-08 | 上海米素环保科技有限公司 | A kind of method and device of condensation water coalescence absorption oil removing recycling |
| CN108373931A (en) * | 2017-08-04 | 2018-08-07 | 河南百优福生物能源有限公司 | A kind of biomass pyrolysis liquid adds the method for hydrogen combined unit substep dehydration |
| CN109694727A (en) * | 2019-02-21 | 2019-04-30 | 上海米素环保科技有限公司 | A kind of hydrogenation plant fractionating system online process preserving method |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103980934B (en) * | 2014-05-19 | 2015-07-01 | 华东理工大学 | Deep dehydrating method and device for oil product |
| CN104845667A (en) * | 2015-05-15 | 2015-08-19 | 河南百优福生物能源有限公司 | Deoxidization bio-oil hydrogenation device with long operation cycle |
| CN105419867A (en) * | 2015-12-30 | 2016-03-23 | 胡平 | Combined hydrogenation method and apparatus utilizing biomass oil to produce green and environment-friendly transportation fuel |
| CN107353935A (en) * | 2017-08-04 | 2017-11-17 | 上海米素环保科技有限公司 | A kind of method of wood tar hydrogenation combined unit substep dehydration |
-
2017
- 2017-08-04 CN CN201710665214.4A patent/CN107353935A/en active Pending
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108373931A (en) * | 2017-08-04 | 2018-08-07 | 河南百优福生物能源有限公司 | A kind of biomass pyrolysis liquid adds the method for hydrogen combined unit substep dehydration |
| CN108002635A (en) * | 2017-12-28 | 2018-05-08 | 上海米素环保科技有限公司 | A kind of method and device of condensation water coalescence absorption oil removing recycling |
| CN109694727A (en) * | 2019-02-21 | 2019-04-30 | 上海米素环保科技有限公司 | A kind of hydrogenation plant fractionating system online process preserving method |
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