DE102011116020A1 - Preparing synthetic algae benzine, algae kerosene and algae diesel components comprises pretreating and conditioning an algae biomass, extracting and purifying the biomass, hydrogenating the extracted biomass and isomerizing - Google Patents

Abstract

Preparing synthetic algae benzine, algae kerosene and algae diesel components comprises (a) pretreating and conditioning an algae biomass, (b) extracting the algae biomass, (c) carrying out solvent extraction with biomass purification, oil separation and filtration process, (d) carrying out catalytic hydrogenation process, (e) distillating the obtained reaction products, and (f) isomerization and/or isomer enrichment of the distillation sections of the reaction products.

Description

The present invention relates to an improved process for the preparation of synthetic hydrocarbon components, such as synthetic gasoline, kerosene, and diesel components from algae. By an appropriate combination of processes and the associated plants, the extraction and refinement of fuel components is provided using microorganisms, in particular oil, fat and lipid-containing algae as starting materials.

The process for producing synthetic fuels and fuel components from biological starting materials, in particular algae, is becoming increasingly important due to the time-consuming search and promotion of fossil fuels. While the energy production from land plants has long been operated on an industrial scale and blocks important resources in terms of land use, the production of energy sources from algae is the current hope for CO ₂ -neutral energy production.

In the patent publication WO 2010138620 discloses a multi-stage process in which the production and extraction of microalgae biomass from a wide variety of biological and inorganic starting materials to an aqueous, oily starting mixture is described in order to achieve the production of biodiesel with conventional process stages such as fluid catalytic cracking, hydrodeoxygenation and isomerization. The process is extremely complicated by the application of a procedurally complex production, pretreatment and extraction of the microorganisms.

According to the US Patent 2011095225 Algal non-polar lipids are recovered by the action of an electric field and controlled CO ₂ and alkali hydroxide treatment. The process is costly in terms of the elaborate treatment of algae cells in the aqueous medium and associated with a considerable procedural effort.

After the published WO 2010104922 Algae biomass production is achieved by elaborate conditioning such as treatment with inorganic acids, the use of elevated temperatures up to 200 ° C, electric fields, mechanical processes and the use of a non-polar solvent. The technical implementation of such numerous process stages appears very costly for the production of algae roe.

The object of the present invention is to develop a process for the production of synthetic gasoline, kerosene, and diesel components from algae. In particular, the complex methods mentioned in the prior art are more cost-effective to design by improved pre-treatment and extraction of algae. Furthermore, the refinement of algal crude oil and a related saving of reaction stages as well as the economical use of hydrogen in the refining of the algae roe to synthetic fuel components of a solution. The synthetic gasoline, kerosene and diesel components should be carried out without the esterification to classic methyl esters or biodiesel of the raw algae oils obtained in the first step, but rather be refined directly by catalytic pressurized hydrogen treatments to fuel components, which are then oxygen-free.

Algae contain between 10 and> 30% of recoverable lipids in the form of glycerides. The recovery of these lipids from the dry or wet algae mass requires more effort than z. As the extraction of oil from conventional plant oil suppliers such as rapeseed, sesame, sunflower seeds.

The aim of algal lipid production is to digest the algae cells so that the extractant can easily dissolve out the lipids in the algae cells and the extractant can be recovered easily and with low loss when separating from the lipids. The lipid- and extraction-agent-free algae mass can be further processed to further valuable substances such as feed, dietary supplements, cosmetic additives or biogas plant feed components.

The accessibility of the lipids can be realized with varying effort depending on the algae species. The two most common and cultivated species of algae Spirulina and the green alga Chlorella are different in this sense. The spirulina filamentous algae only have a cell membrane that is relatively easy to overcome. However, chlorella algae have a very robust cell wall.

Occasionally it is possible to produce high amounts of lipid in the algae cell or the biomass with special algae species, but this is not technically effective in mass production. Simple pressing processes, which are successful in the extraction of vegetable oil from oilseeds, do not lead to success, because the cell wall stresses, among other things, can not be overcome. Sometimes a perforation of cell walls and membranes to the destruction and physical dissolution of the cell is necessary. This can be achieved by means of cavitation applications, if the pressure conditions of the process can overcome the cell voltages, generates high diffusion currents or other interfacial penetrating techniques such as ultrasound.

The algae cell digestion is a way to make the ingredients carbohydrates, proteins and lipids available for targeted use.

According to the invention, in the algal cell disruption, 10 to 50% algae dry mass 20 to 40% aqueous algae concentrate and 100% respectively supplemented conditioning agent with a friction energy in the amount of 0.03 to 0.5 kW / kg dry biomass and by heat energy from a low-temperature heat source at 30- 65 ° C treated.

The digested algae biomass is fed with dry contents of 10 to 95% to one of several parallel extractors.

The extractors are operated continuously or discontinuously. In discontinuous operation, the extractors are filled with moist, digested algal biomass up to a first filling volume in the range of 30 to 55% of the nominal volume. Through a mixture of algal powder fine fraction, algae pellets, filler and solvent, an improvement of the mass transfer in the extractor filling can be achieved.

According to the invention digested algal biomass to 45 to 75%, algal pellets to 10-30% and algae powder fine fraction of the same biomass origin to 5 to 25% are mixed mixed as a sealing bed. Alternatively, filler A5 may be added in exchange with pellets or as a proportionate amount. The entire gap volume or the nominal volume of the extractor is filled up with solvent. While the algal pellets are hardly extracted during the elution / extraction, the algae powder content is almost completely eluted by a better macro-liquid flow in the extractor. After extraction, the algae powder is easily separated from the pellets. The pretreated pellets are crushed, ground and subjected to extraction with new pellets or filler. In algal lipid extraction, preference is given to using polar or nonpolar solvents or solvent mixtures consisting of light and medium hydrocarbons such as propane, propylene, butane, butylene pentane, hexane, heptane, ethanol, propanol, ketones, cycloalkanes and aromatic hydrocarbons. The extractor contains filter nipples, filter stockings or filter elements which allow for the dissolution process of fats, oil, resin and lipid components from the algal biomass into the fluid solvent but still effectively prevent their discharge via the outlet of loaded solvents. The extraction can be carried out batchwise in two partial stages. In a first stage, the intimate mixing of pretreated algal biomass is carried out with an extractant. If these processes require the reduction of the apparent viscosity of the suspension, another conditioning agent, such as water, may be added. In a further substep, the suspension is filtered discontinuously or continuously. So that the dissolution processes proceed expediently with moderate heat supply, heating surfaces are arranged in the extractors. To increase the turbulence and to reduce inappropriate concentration gradients between oil and lipid components in the two phases algal biomass and loaded solvent agitators are also used with filter elements in the extractors.

According to the invention, a mixture viscosity of 200 mm ² / s to 3500 mm ² / s, a temperature range of 25-65 ° C and a degree of turbulence corresponding to a Reynolds number> 2500 must be observed during the extraction process.

The solvents to be used must have a selective effect on the substances to be extracted, such as oils, lipids and fats.

Although the classical extractants such as methanol, chloroform or methyl ethyl ketone are good solvents, they should not be used on a large scale because of their difficult technical applicability in the recovery and the risk potential.

Thus, certain lipid groups can be selectively extracted by an appropriate extractant or extractant mixture and unwanted lipid groups, such as. B. phospholipids are suppressed.

The filtrate is fed to an evaporator. By evaporation of the extractant, a concentration of the oil components in the mixture is achieved. The extractant vapors are condensed in a condenser and finally reused for extraction. Only partially condensed extractant fractions are recovered quantitatively in a cryogenic condenser.

The remaining oil phase still contains water from the wet biomass, algae and extractant ingredients. This phase is fed to a vacuum distillation, filtration and / or a gravity separator. In this process stage, the oil-water separation takes place in the occurrence of miscibility gaps between algae oil and water by gravity separation. This is usually when forming a release layer by means of a release layer measurement, based on an oil density of 900-935 kg / m ³ , a phase separation is made.

However, algae boils as an oil-multi-substance mixture seldom produce a separating layer with water, since they can form non-breakable oil-water suspensions. In these cases, by driving off the volatile constituents in a distillation stage, algae crude production must take place in the bottom of this stage.

In the less thermally stable oils or oil components, the use of a vacuum distillation stage at a pressure range of 15 mbar to 250 mbar is necessary to keep the process temperatures low.

Finally, the recovered bottoms product is subjected to filtration to separate oil sludges from the previous process stages. To improve the oil qualities, other filter aids can also be added here. Thus, a prepared algae crude oil is available.

The remaining in the extraction stage low-lipid residual biomass is naturally rich in proteins and carbohydrates. However, they still contain portions of the solvent before it can be used for material, animal or agricultural use.

If the mixture is to be used further energetically, for example, as a feedstock of a biogas plant or fuel in a biomass incineration plant, solvent residues must not be totally removed.

A thermal Biorestmassereinigung means Hordentrocknern, ovens, drying towers, fluidized bed ovens, pressure chambers, vacuum chambers or similar devices with exhaust gas purification finally leads to purified residual biomasses, which is also suitable for agricultural purposes and in livestock as a concentrate content.

When extracting spirulina algae mass, for example, a protein product is produced which consists of 75 to 80% proteins and is in great demand due to the high nutrient content. Such protein-rich residual biomasses should not or only partially or in excess will give in a biogas plant, because relatively little methane and much carbon dioxide and ammonia gas is produced.

The algae crude extracted from the extraction consists of a mixture of glycerides, oils, resins, terpenes, fats and fatty acids. Due to their size, the moles of the ingredients have a high mass of up to about 300 to 1200 g / mol and in addition to carbon and hydrogen they contain up to 12 Ma.% Oxygen. There are also algae species which produce paraffins and lipids of comparatively medium chain length with molecular weights <750 g / mol.

Due to the frequently occurring molecular structure of the algae oil and its ingredients with a large C number, these are hardly suitable directly as gasoline, diesel and kerosene components. Both high boiling temperatures, high pour points and oxygen levels u. a. unfavorable properties preclude direct use as a diesel blend, kerosene or blended components.

Transesterification of the algal oil to methyl ester (glycerides to methyl esters) improves pour point, reduces its viscosity and results in fewer blockages in fuel injection systems. As a diesel and kerosene component, however, methyl ester is hardly or only in very small admixtures suitable since further properties such as the viscosity, the melting point and the dissolving power of motor oils are improved only insufficient.

• – Hydrierung des Algenöls zur Umwandlung der Makromoleküle (Triglyceride) zu Paraffinen,
• – Entfernung des gebundenen Sauerstoffs, Stickstoff, Phosphor, Schwefel aus den Molekülen,
• – milde Spaltung der großen Moleküle mit C-Zahlen größer n-C₁₃ bis n-C₂₄ (Kettenlängenverminderung).

In order to be able to obtain a diesel mixture and kerosene component from the algae oil, the following process steps must be carried out in the pressure-hydrogen treatment:

• Hydrogenation of the algae oil to convert the macromolecules (triglycerides) to paraffins,
• Removal of the bound oxygen, nitrogen, phosphorus, sulfur from the molecules,
• - mild cleavage of the large molecules with C numbers greater than nC ₁₃ to nC ₂₄ (chain length reduction).

The algal crude oil is treated in the catalyst stages at least in two equipped with different catalysts three-phase fixed bed, three-phase moving bed or three-phase fluidized bed reactors, the gas phase of hydrogen-rich gas, the liquid phase an algae oil phase in the molecular weight range from 300 g / mol to 1200 g / mol and the solid phase consists of base metal components and metals produced catalyst pellets. The process pressure is between 1.0 and 17.5 Mpa and the process temperature at 265 to 535 ° C. The gas phase and liquid phase flow through each of the two reactors in series and in series in cocurrent or countercurrent. After leaving the reaction product from the secondary reactor, the hydrogen and gas rich gas phase is separated in the secondary separator and only now fed to the primary reactor mixed with the crude oil. The reactor intermediates are separated from the process water in two separators, After a Kreislauffahrweise the heavy fractions for reprocessing of the crude crude fuel by distillation in the desired synthetic fuel components separated. The reaction process must be of its process parameters, pressure, temperature, hydrogen partial pressure, reactor type, catalyst bed arrangement, circulation mode and catalyst selection designed so that Ausgangsstuffe such as triglycerides as conductive components according to the invention at the outlet of the primary reactor to more than 99.5%. This is a guiding parameter for the total oxygen conversion of the crude oil biocomponents used. Ideally, the catalyst used cuts nC ₁₈ into 2 × nC ₉ . In practice, this is not true. There are many fission products with a distribution of C atom numbers. This means, however, that z. B. having a flash point of + 31 ° C and a density of 718 kg / m ^3, a kerosene / jet fuel component (as aviation turbine fuel) is fit in nC ₉ only in a limited extent. It is advantageous to separate normal and iso-paraffins and to recycle an n-paraffin stream and / or to carry out reactions while avoiding insufficient isomerization conversions in multi-substance reaction systems.

Higher n-paraffins increasingly worsen the pour point, so that the n-paraffins to about ₁₂ nC / nC ₁₃ are still suitable as JET components in smaller and smaller concentrations. Isomers z. As the nonane up to the iC ₁₆ are suitable.

Despite this refinement described above, however, it becomes difficult to achieve the density and calorific value values required of commercial jet fuel JET A1 only by these components. Therefore, it is necessary to achieve the required specification of JET A1 by further cleavage and admixture of other suitable components. The admixing components must have very low pour points and the flash points should be significantly higher than 38 ° C. As blend components, multicomponent mixtures are generally used which are o. G. Own properties. (eg aromatic mixtures and isomer mixtures from refineries).

The crude whey fuel from the secondary separator is fractionated in three distillation stages consisting of stabilization column, algal oil kerosene splitter and algal oil diesel splitter. The top product of the stabilization column is Synthetic Paraffin Ash Petroleum (SPB) and heating gas. The bottoms product is separated into a raw kerosene head product and an algae diesel / middle distillate sump product in the subsequent algae oil kerosene splitter. The diesel / middle distillate sump product is fed to a third distillation stage, algal oil diesel splitter, and fractionated into synthetic paraffinic diesel overhead (SPD) and bottoms to algae heavy ends. The separation conditions in the one to three columns are to be adjusted by the reflux ratio of 1.5 to 7.5, the pressure of 1.25 bar to 11 bar and a temperature range of 45 to 360 ° C.

The crude kerosene head product of the kerosene splitter is to be subjected to paraffin isomerization to achieve separation of the iso and normal paraffin species into synthetic paraffinic kerosene (SPK - iso-paraffin-rich fraction) and algal oil-normal paraffinic component. The algal oil normal paraffinic component is run into the secondary reactor together with the high boiler bottoms product of the diesel splitter to be further isomerized.

embodiments

The invention is based on 1 . 2 . 3 and 4 as well as two embodiments described as follows.

1 and 2 show a process block flow diagram for algae crude oil recovery.

example 1

The algae cell disruption 1a 30% algae dry mass A1, 30% aqueous algae concentrate A2 and 40% conditioning agent A3 or algae pellets A4 are added. By Dissipationsenergiezufuhr done the perforation of the algal cells and their digestion. After a treatment period of 40 minutes and with the aid of low-temperature source B, the digestion process is ended at 45 ° C. and the digested biomass is stopped in an extractor 2 to hand over. The low temperature heat source B for the evaporator 3a and the algae cell digestion 1a Depending on availability, it may come from a storage tank for low-pressure steam, solar or geothermal heat 3b be obtained. The extractor used by way of example 2 consisted of a cylindrical vessel equipped with filter elements containing digested algal cells, pellets and A5 filler.

The filter elements allowed elution of the algal cell constituents by means of an unloaded solvent. The solvent loaded with the oil extraction products was typically in an evaporator 3a transferred, which was heated with a low-temperature heat source B as described above. Solvent vapors enter the condenser 4a for solvent treatment and the cryogenic condenser 4b for solvent recovery. The condensed solvents S were re-used as unloaded product to the extractors 2 fed. Depending on the presence of sufficient cooling or cooling source and solvent to be used, solvent losses of up to 15% can occur.

The liberated or drained liquid extractor 2 was now again heated with an external low temperature heat source to expel residual components of the solvent from the algal constituents. These solvent vapors also became the cryogenic condenser 4b to hand over. From the extractors 2 algae filter cake masses discharged discontinuously were used in the extraction residue treatment and separation 5a separated into a coarse and a fine fraction, wherein the theoretical cut size was set at about 60% of the pellet diameter and / or filler diameter. In the example about 1.5 to 3 mm theoretical Siebmaschenweite were used.

The fines were in the Restbiomassereinigung 5b heated further to partially or completely volatilize solvent components here. End product D is a dry, lipid-free residual biomass that is predominantly proteinaceous and carbohydrate-containing.

The coarse material, which consists of algal pellets and filler, was separated into filler and coarse fraction E. The coarse fraction E became pelleting again 1b the algae cell digestion 1a , or directly to the extractors 2 fed and recycled. The filler A5 was used on the extractors to improve their operation and to fill unwanted extraction spaces.

In the evaporator 3a From time to time, a complete removal of the solvent was carried out so that a water and an oil phase or a water / crude oil mixture remained. In various species of algae, mixtures of oil-water suspensions not separable physically by separation layer formation were also obtained, such as vacuum distillation, gravity separation and filtration 6 were handed over. Here, an anhydrous and solids-free algae crude oil was finally obtained by means of a separating layer formation, an oil skimmer and / or a vacuum distillation. In the example, a simple vacuum distillation was used.

Example 2

The invention is based on a further example and the 3 and 4 described in more detail. 3 and 4 show a basic flow diagram for the conversion and processing of algae crude oil to synthetic, paraffinic hydrocarbon components.

In the primary reactor 7 was the algae crude oil E by means of hydrogen chloride from the secondary separator 11 hydrogenated on a catalyst. Here, the large molecules of Algenrohöls were converted into smaller molecules (paraffins). At the same time bound oxygen, nitrogen and other elements and impurities from the molecules were more or less removed. Forming water, CO, CO ₂ , fission gases and unused hydrogen were in the primary separator 8th separated from the paraffins. The catalytic reaction in the primary reactor 7 leads to an oxygen conversion measured as remaining triglycerides as a guide parameter of the reactants of> 99.5%, which can thus be considered as complete.

In the secondary reactor 10 were those in the primary reactor 7 obtained paraffins on a catalyst with fresh hydrogen J cleaved and isomerized. Heteroatoms should no longer be present here (see also 99.5% conversion of the leading components). The reaction mixture is in the secondary separator 11 separated from hydrogen and fission gases.

In recirculating gas compression and purification 9 became the one in the reactors 7 and 10 required hydrogen compressed to the required operating pressure and fed to the stoichiometric excess of the reactors. After the reaction stage, the reaction gas stream was condensed and the remaining hydrogen-rich and pollutant-rich gases are discharged from the plant for external further processing, discarded or partially or completely freed in a gas purification stage of foreign gases such as H ₂ S, NH ₃ , CO, PH ₃ and CO ₂ ,

After the purification step, the spent hydrogen was supplemented by fresh hydrogen J and recirculated to the reactors. A fresh hydrogen addition J was advantageously first in the secondary reactor 10 performed to recycle gas purification 9 to relieve or to waive certain certain Algenrohölqualitäten and driving styles completely. Subsequently, with the hydrogen-containing exhaust gas stream, the primary reactor 7 supplied with hydrogen.

• – Heizgas K
• – Synthetisches Paraffinisches Benzin L, Hauptkomponenten C₅ bis C₁₂
• – Synthetisches Paraffinisches Kerosin M, Hauptkomponenten C₁₀ bis C₁₄
• – Synthetischer Paraffinischer Diesel N, Hauptkomponenten C₁₄ bis C₁₉
• – Schwersieder O, Heizölkomponenten, Paraffinwachse > C₁₇.

In product stabilization / product separation, the reaction products were from the secondary separator 11 decomposed into the following fractions:

• - Heating gas K
• - Synthetic paraffinic gasoline L, main components C ₅ to C ₁₂
• - Synthetic Paraffinic Kerosine M, main components C ₁₀ to C ₁₄
• - Synthetic Paraffinic Diesel N, main components C ₁₄ to C ₁₉
• - High boilers O, heating oil components, paraffin waxes> C ₁₇ .

In a further process step, the isoparaffin / n paraffin separation was carried out 15 , Isoparaffins could previously be enriched by isomerization reactions in the two reactors.

• – Normalparaffine (geradkettig): 0,489 nm
• – Isoparaffine (verzweigte Ketten): 0,558 nm.

The molecular diameter of typical paraffins is:

• Normal paraffins (straight chain): 0.489 nm
• - Isoparaffins (branched chains): 0.558 nm.

As a result, an enrichment and separation between normal paraffins and isoparaffins was achieved.

If all pores are occupied, the normal paraffins have to be removed (reactivated) either by pressure changes or temperature changes expediently with the aid of a flushing medium. In this way, kerosene cuts with high isoparaffin content can win, which then have enough deep freezing points. The normal paraffin stream was recycled through the secondary reactor.

It is possible to exploit the isomerization capability of the catalyst in the second reaction stage. This has the advantage that no expensive noble metal catalysts are needed and the hydrogen purity may be set lower for the reaction in the isomerization step. This paraffin separation works in both the gas and liquid phases.

LIST OF REFERENCE NUMBERS

1a

Algal cell disruption

1b

pelleting

2

Extractors 1 - n

3a

Evaporator

3b

Storage with low-pressure steam, solar or geothermal energy

4a

Condenser for solvent treatment

4b

Cryogenic condenser for solvent recovery

5a

Extraction residue treatment and separation

5b

Rest biomass cleaning

5c

Füllstoffseparation

6

Oil separation, vacuum distillation and filtration

7

primary reactor

8th

primary separator

9

Recirculation gas cleaning and compressors

10

secondary reactor

11

secondary separators

12

Stabilization column

13

Algae oil kerosene Splitter

14

Algae oil diesel Splitter

15

Isoparaffin / n-paraffin separation

16

capacitor

17

analyzer

A1

Algae dry mass

A2

watery algae concentrate

A3

conditioners

A4

algae pellets

A5

Filler / solvent

B

Heat source (external)

C

cooling medium

D

Residual biomass (dry, lipid-free)

e

coarse fraction

F

Algae powder-fine fraction

G

algae oil

H1

process water

H2

process water

I

mud

J

Fresh hydrogen

K

heating gas

L

Synthetic Paraffinic Gasoline (SPB)

M

Synthetic Paraffinic Kerosene (SPK)

N

Synthetic Paraffinic Diesel (SPD)

O

high boiler

P

bypass

Q

seaweed extract

R

extraction residue

S

Solvent condensate

T

Solvent vapors

U

Rohalgenkraftstoff distillation use

V

Exhaust gas from recycle gas purification

QUOTES INCLUDE IN THE DESCRIPTION

This list of the documents listed by the applicant has been generated automatically and is included solely for the better information of the reader. The list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions.

Cited patent literature

• WO 2010138620 [0003]
• US 2011095225 [0004]
• WO 2010104922 [0005]

Claims (7)

Process for the preparation of synthetic algae gasoline, algal kerosene and algae diesel components comprising the steps: a) pretreatment and conditioning of the algal biomass, b) extraction of the algal biomass, c) solvent recovery with biomass cleaning, oil separation and filtration, d) catalytic pressure-hydrogen treatment, e) distillative treatment of the reaction products, f) isomerization and / or isomeric enrichment of distillation cuts of the reaction products. A method according to claim 1, characterized in that in step a) 10 to 50% Algentrockenmasse 20 to 40% aqueous algae concentrate and 100% each supplemented conditioning agent and algal pellets with a friction energy in the amount of 0.03 to 0.5 kW / kg Biomass and a low-temperature heat of 30 ° C to 65 ° C are treated. Process according to claims 1 and 2, characterized in that in the step b the extractors an open-digested algal biomass to 45 to 75%, algae pellets to 10-30%, algae powder fine fraction of the same biomass origin mixed to 5% -25% mixed as a dense bed , the filler alternatively in exchange with pellets or added proportionally and the mixture with a solvent or solvent mixture consisting of light and medium hydrocarbons such as propane, propylene, butane, butylene, pentane, hexane, heptane, ethanol, propanol, ketones, cycloalkanes and aromatic hydrocarbons , a mixture viscosity of 200 mm ² / s to 3500 mm ² / s, a temperature range of 25 ° C to 65 ° C and a turbulence degree corresponding to a Reynolds number> 2500 is extracted. Process according to claims 1-3, characterized in that in step c, a suspension is filtered discontinuously or continuously, the filtrate in an evaporator at normal boiling point of the selected solvent. Normaldruckdestillation or a vacuum distillation at a pressure range of 15 mbar to 250 mbar and a gravity separator with a separation layer measurement at an oil density of 900-935 kg / m ³ as Algenrohöl after filtration of the oil is formed. A process according to claims 1, characterized in that the algae crude oil according to step d) flows through at least two stages of catalyst equipped with different base catalysts three-phase fixed bed, three-phase moving bed or three-phase fluidized bed reactors, wherein the gas phase from hydrogen-rich gas, the liquid phase a Algenrohölphase In the molecular weight range of 300 g / mol to 1200 g / mol and the solid phase of base metals and metals produced catalyst pellets, the process pressure between 1.0 and 17.5 Mpa and the process temperatures 265-535 ° C, gas phase and liquid phase in cocurrent or countercurrent the reactors 7 and 10 flow one after another and in series, the fresh hydrogen J with a recycle gas after a cycle cleaning and compression 9 with a 0.2 to 5 MPa higher pressure first into a secondary reactor 10 be added, and then after the gas-liquid separation in the secondary separator 11 the gas phase as partially used gas with the algae crude oil G the input of the primary reactor 7 after a gas-liquid separation in the primary separator 8th a circulation procedure takes place until the leading component of the sum of the starting materials of the triglycerides at the outlet of the primary reactor 7 converted to more than 99.5%, which in the analyzer 17 be determined. Process according to claims 1-5, characterized in that, after step e, a crude pulp distillation feedstock U in the three distillation stages consisting of a stabilization column 12 , an algae oil kerosene splinter 13 and an algae oil diesel splitter 14 , is fed to a fractionated separation, the top product of the stabilization column 12 as synthetic paraffinic gasoline (SPB) L and heating gas K its bottom product in the following algae oil kerosene splinters 13 into a raw kerosene head product and an algae diesel / middle distillate sump product, which in turn is the third distillation stage, an algae oil diesel splitter 14 is fed and, in the algal oil-diesel splitter 14 arise as overhead product synthetic paraffinic diesel (SPD) N and the high boiler O in the bottom, the separation conditions in the one to three columns 12 to 14 be set by selecting the reflux ratio of 1.5 to 7.5, the pressure of 1.25 bar to 11 bar and the temperature of 45 ° C to 360 ° C. Process according to claims 1-6, characterized in that after step f the raw kerosene head product of the kerosene splitter 13 an iso / n paraffin separation 15 is introduced and a separation of the iso and normal paraffin species in Synthetic Paraffinic Kerosene M (isoparaffin rich) and normal paraffinic component takes place, which together with the high boiler sump product to the input of the secondary reactor 10 to be led.

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