PROCESS TO OBTAIN FUEL FROM BIOMASS IN FLUID CATALYTIC CRACKING

Abstract

The present invention relates to a process for obtaining fuel from biomass which comprises the introduction of the catalyst (3) in the base of an cracking section (4), wherein said catalyst (3) at high temperature comes in contact with a gas stream of light hydrocarbons rich in hydrogen (1), wherein the catalyst (3) and hydrocarbon (1) then come in contact with a lignocellulosic liquid stream (2) in the same cracking section (4), creating the reaction mixture (5) that, soon after, comes into contact with the main stream containing the traditional fossil load of a FCC (6) in a second cracking section (7).

Claims

1. Process to obtain fuels from biomass in a fluid catalytic cracking (FCC) characterized by introducing the catalyst (3) in the base of a cracking section (4), wherein said catalyst (3), at an elevated temperature, is in contact with a gas stream of light hydrocarbons rich in hydrogen (1), wherein the catalyst streams (3) and hydrocarbons (1) then are in contact with a lignocellulosic liquid stream (2) in the same cracking section (4) causing the reaction mixture (5) which then is in contact with the main stream containing the traditional fossil load of FCC (6) at a second cracking section (7).

2. Process according to claim 1, characterized by further separating the product stream (8) obtained by the catalytic cracking process of hydrocarbon streams and subjected to a hydrotreatment step to obtain high octane fuel.

3. Process according to claim 2, characterized by the step of hydrotreating employing a temperature between 350 ° C. and 390 ° C. and, as a catalyst, a metal oxide totally or partially converted into sulfides (active phase) and supported on y-alumina (y-A1203).

4. Process according to claim 1, characterized by the first reaction section (4) employing the following conditions: temperature in the range 500° C. to 800° C., preferably from 500° C. to 700° C., pressure between atmospheric pressure 400 kPa and preferably in the range of 200 kPa to 400 kPa, a catalyst/biomass ratio in the range from 10 to 40 and contact time in the range between 0.1 and 0.9 seconds.

5. Process according to claim 1, characterized by the second reaction section (7) employing the following conditions: speed space in the range between 200 h -1 and 400 h -1, the contact time in the range between 1.5 and 3.0 seconds, temperature in the range between 500° C. and 620° C. and a catalyst/hydrocarbons ratio in a range between 5 and 20.

6. Process, according to claim 1, characterized in that the lignocellulosic liquid stream (2) is derived from the pulp and paper industry, in particular obtained by the Kraft route.

7. Process, according to claim 1, characterized in that the lignocellulosic liquid stream (2) is obtained by fast pyrolysis processing units.

8. Process, according to claim 1, characterized in that the biomass correspond to 0.1 to 10% by weight, preferably 2% by weight relative to the total amount of load added to the FCC.

9. Process, according to claim 1 characterized by the traditional fossil load FCC (6) is selected among petroleum refinery streams, preferably rich in hydrogen, and the hydrogen content of at least 10% by weight of the compound.

10. Process, according to claim 1 characterized in that the gas stream of light hydrocarbons rich in hydrogen (1) is propane, butane, ethane or any stream from natural gas or internal oil streams generated within the petroleum refinery, rich in pentanes and hexanes, present in light naphthas.

11. Process, according to claim 10, characterized in that the stream (1) corresponds to 0.1 to 10% by weight, preferably 5% by weight relative to the total amount of filler added to the FCC.

12. Process, according to claim 1 characterized in that the catalyst (3) used in cracking is a solid acid catalyst.

13. Process, according to claim 12, characterized in that the acid catalyst is a zeolitic catalyst.

Description

BRIEF DESCRIPTION OF THE FIGURES

[0022] The detailed description below makes reference to the accompanying FIG. 1, which illustrates, in simplified terms, the process for obtaining lignocellulosic fuels in a FCC riser type reactor according to the present invention.

DETAILED DESCRIPTION OF THE INVENTION

[0023] The present invention is characterized by a process for the production of fuel, particularly high-octane gasoline with RON (“Research Octane Number”) above 90 and/or MON (“Motor Octane Number”) above 75.

[0024] In the process of obtaining the lignocellulosic fuel under the present invention, a gaseous stream of light hydrocarbons rich in hydrogen (1) is added to the base of a riser-type catalytic cracking reactor (4) which further receives a lignocellulosic liquid stream (2) and regenerated catalyst (3), at elevated temperature, constituting a first reaction section (4). The reaction medium thus generated (5) comes into contact with the main fossil load of the FCC (6) generating a second reaction section (7). The reaction products (8) are then removed from the reactor and the catalyst (11) is sent to a rectification section (10) with steam (9) or other inert gas to remove hydrocarbons still present between the catalyst particles. The catalyst coated with coke generated in the reaction section (4) and (7), also called spent catalyst (15) is sent to the regeneration section (12) for combustion of the coke with air (13), generating combustion products (14).

[0025] More specifically, in the process of the present invention, the catalyst (3) is introduced at the base of the cracking section (4), wherein said catalyst (3), at elevated temperature, is in contact with a gas stream of light hydrocarbons rich in hydrogen (1) at a temperature between 500° C. to 800° C. and atmospheric pressure to about 400 kPa, wherein the catalyst (3) and hydrocarbon (1) streams then come into contact with a lignocellulosic liquid stream (2) in the same cracking section (4) causing the reaction mixture (5) which then comes in contact with the main stream containing the traditional fossil load of FCC (6) at a second cracking section (7).

[0026] In the first reaction section (4) there is the depolymerization of lignin by the zeolitic catalyst (3) under high temperature, preferably in the range between 500° C. to 700° C. and low pressures, preferably in the range of 200 kPa at 400 kPa, catalyst ratio/biomass in the range of 10 to 40 and contact time in the range between 0.1 and 0.9 seconds. This reaction section (4) is where the compound rich in hydrogen is added. The function of the gaseous stream containing hydrocarbons rich in hydrogen (1) added to the catalyst lift of the FCC riser reactor is to mitigate the deficiency in hydrogen of lignocellulosic liquid stream (2), desirable for the optimization of the yield of liquid streams (8) by adding hydrogen thereto.

[0027] In the second reaction section (7) there is catalytic cracking of hydrocarbons at a space velocity in the range between 200 h.sup.−1 and 400 h.sup.−1, contact time in the range between 1.5 and 3.0 seconds in a temperature range between 500° C. and 620° C. and catalyst/hydrocarbon ratio in the range between 5 and 20. In this section there are also donation/hydrogen transfer reactions of fossil load for the renewable load. This combination leads to the production of high octane gasoline with RON above 90 and MON above 75.

[0028] Examples of lignocellulosic liquid streams (2) which can be used in the process are those from agriculture and pulp and paper industry waste, in particular materials obtained by Kraft route, and lignocellulosic materials obtained by processing in fast pyrolysis units, more specifically bio-oil, a material which is rich in sugars and lignin.

[0029] In the process, the lignocellulosic liquid stream (2) corresponds to 0.1 to 10% by weight, preferably 2% by weight relative to the amount of total load added to the FCC.

[0030] Meanwhile the fossil hydrocarbon stream employed as load (6) can be selected from the chains of petroleum refining. However, such stream should preferably be rich in hydrogen, and the hydrogen content of at least 10% by weight of the compound.

[0031] As the gas stream of light hydrocarbons rich in hydrogen (1) can be used as propane, butane, ethane or any stream from natural gas or internal oil streams generated inside the petroleum refinery as rich in pentanes and hexanes present in light naphthas. This light hydrocarbon stream (1) corresponds to 0.1 to 10% by weight, preferably 5% by weight relative to the amount of total load added to the FCC.

[0032] The catalysts (3) which can be used in the catalytic cracking process of the present invention are catalysts typical for catalytic cracking reactions, that is, solid catalysts with acid characteristics. Among the catalysts most often used, we can mention those whose main component is zeolite, a crystalline aluminosilicate, also called zeolite catalysts.

[0033] Loads consisting of biomass, such as those defined in the present invention, when subjected to the FCC, using solid acid catalysts such as zeolites containing faujasites, lead to depolymerization of the lignin present in such load, generating a product stream rich in aromatic and phenolic compounds in the naphtha range (8).

[0034] Ideally, the product stream (8), rich in aromatics and phenolic compounds will subsequently be subjected to a hydrotreating step, which is the setting and adjustment of its properties by removing oxygen compounds, leading to the production of a high octane fuel with a high content of monoaromatic substituted compounds.

[0035] In the hydrotreating step of the aromatic-rich stream (8), a temperature between 350° C. and 390° C. is employed, using metal oxides, fully or partially converted to sulfides (active phase) and supported on y-alumina (y-Al.sub.2O.sub.3) as a catalyst.

[0036] Therefore, after the cracking and hydrotreating steps a high octane fuel is produced, due to the presence of aromatic compounds with a boiling point between 90° C. and 220° C.

[0037] Below some results obtained in tests performed in a FCC unit are presented in the examples.

EXAMPLE 1

[0038] Propane, a hydrogen donor compound was injected into a catalytic reactor with a flow rate of 0.5 L/min in order to generate a reference for comparison purposes. The reaction temperature was maintained at 540° C. The results shown in Table 1 (Test A) are typical of propane processing at moderate reaction temperatures, around 540° C.

[0039] Accordingly, there was no conversion of propane into other compounds.

EXAMPLE 2

[0040] Acetone (propanone), a hydrogen acceptor compound representing the renewable load of a lignocellulosic base, was injected into the base of a catalytic reactor at a flow of 200 g/h with the intention of generating a second reference for comparison purposes. The reaction temperature was maintained at 540° C. The results are shown in Table 1 (Test B). Large quantities of water, carbon monoxide and carbon dioxide were generated. The coke yield is relatively high.

EXAMPLE 3

[0041] Propane was introduced in a catalytic reactor with a flow rate of 0.5 L/min, with an injection of acetone at a flow rate of 200 g/h as stated by the present invention. The reaction temperature was maintained at 540° C. The results are shown in Table 1 (Test C).

TABLE-US-00001 TABLE 1 General conditions and results of tests performed in a FCC unit. Tests A B C General conditions Propane flow rate, L/min 0.5 0 0.5 Acetone flow rate, g/h 0 200 200 Temperature of the 540 540 540 reactor, ° C. Pressure of the reactor, 260 260 260 kPa Process results Gaseous 99.9 50.5 51.5 hydrocarbons <C4, % m/m Liquid hydrocarbons + 0.1 0.2 0.6 C5, % m/m Coke, % m/m 0.0 3.5 0.5 Carbon monoxide, % 0.0 1.2 1.0 m/m Carbon dioxide, % m/m 0.0 0.6 0.5 Water, % m/m 0.0 44.0 45.9

[0042] In comparison to example 2, in example 3, much lower yields of coke and larger yields of gaseous hydrocarbons are obtained, indicating the effectiveness of the invention.

EXAMPLE 4

[0043] A bio-oil stream, receiving hydrogen, was injected in a catalytic reactor with a flow rate of only 60 kg/h flow due to the difficulties caused by processing pure bio-oil in catalytic cracking units. The characteristics of a bio-oil stream (renewable) can be found in Table 2. The catalyst used in testing was an FCC commercial equilibrium catalyst containing ZSM-5.

[0044] The results shown in Table 3 were obtained from processing this stream. There is great production of water and carbon monoxide and carbon dioxide quantities are high. The coke yield is about 11.4% wt. for these operating conditions. The final liquid product is only 17.6% wt.

TABLE-US-00002 TABLE 2 Analysis Unit Result Carbon (C) % wt.. 41.9 Hydrogen (H) % wt.. 7.1 Nitrogen (N) % wt.. 0.23 Oxygen (0) by difference % wt.. Water (Karl Fischer Method) % wt.. 26.5 Acidity mgKOH/g 57.1 Solids % wt.. 0.02 Ph 2.6 Micro Carbon Residue % wt.. 16.2 Ash % wt.. <0.1 Carbonyl content mg BuO/g 202 lower heating value (LHV) MJ/kg 15.0 Density 20/4° C. 1.19 Viscosity 60° C. cSt 15

TABLE-US-00003 TABLE 3 Test 263-048 Reaction Temperature, ° C. 540 Load Temperature, ° C. 50 Normalized yield, % wt.. Coke 11.4 Fuel Gas (H.sub.2, C1-C2) 1.2 Ethane 0.4 CO 7.9 CO.sub.2 2.2 LPG (C3 and C4) 1.0 Propylene 0.6 Liquid products 17.6 Water 58.7 Total 100.0

EXAMPLE 5

[0045] A hydrocarbon stream rich in hydrocarbons with 6 carbon atoms, a hydrogen donor, was injected into a catalyst reactor with a flow rate of 100 kg/h. The reaction temperature was maintained at 500 ° C. The hydrocarbon stream characteristics are shown in Table 4. In the test A commercial equilibrium FCC catalyst containing ZSM-5 was used was used as a catalyst.

TABLE-US-00004 TABLE 4 Relative area % n-Hexane 35.6 3-methyl-pentane 23.1 2-methyl-pentane 20.2 3-methyl-trans-2-pentene, 5.4 methyl cyclopentane 4.0 2,3-dimethyl butane 2.9 other hydrocarbons to C7 8.8 Total 100.0

[0046] The results shown in Table 5 (Test A) were obtained from the processing of this stream. There is no production of water and the amounts of carbon monoxide and carbon dioxide are negligible. The coke yield is around 0% wt. for these operating conditions. The final product is mainly composed of hydrocarbons of the gasoline range (92% wt.).

EXAMPLE 6

[0047] The hydrocarbon stream rich in n-hexane was injected with the bio-oil in three ratios in a catalytic cracking reactor 10% wt., 20% wt. and 30% wt., Tests B, C and D of Table 4, respectively.

[0048] There is production of water, carbon monoxide and carbon dioxide due to deoxygenation reactions carried out in the riser reactor and due to the hydrogen donation of the donor stream to the receiving stream. The coke yield increased as the ratio of bio-oil in the load increases. Furthermore, there is a decrease in gasoline yields, accompanied by the rising yields of LCO and decant oil.

TABLE-US-00005 TABLE 5 Bio-oil % wt. 0 10 20 30 Normalized yields % wt. Coke % wt. 0.0 2.1 4.3 6.5 Fuel Gas (H2, C1-C2) 0.4 0.5 0.7 1.0 % wt. LPG (C3-C4) % wt. 6.7 2.1 1.5 1.6 Gasoline (C5-220° C.) 92.0 90.7 83.6 72.9 % wt. LCO (220° C.-344° C.) 0.6 0.6 1.1 1.7 % wt. Decant oil (+344° C.) 0.3 0.3 0.5 1.0 % wt. Water % wt. 0.0 2.2 5.6 10.2 CO % wt. 0.0 1.2 2.1 4.0 CO.sub.2 % wt. 0.0 0.3 0.6 1.1 Total 100.0 100.0 100.0 100.0

[0049] Table 6 shows the theoretical yields obtained by linear extrapolation of the actual yields of Table 4, if 100% bio-oil were processed. There is no reduction in coke yield, which remains around 21% wt. in all cases. On the other hand, the yield of gasoline is 78.7% wt. when calculated as 10% bio-oil, however decreases drastically to only 28.4% wt. when the calculation is made from 30% wt. bio-oil. That is, there is a significant drop in gasoline yield as the ratio of the donor hydrogen stream decreases. The amount of total liquid products decreased from 79.7% wt. to only 35.3% wt. for the calculation made from 30% wt. This difference is caused by the transfer of hydrogen of the hydrocarbon donor stream C6 to the acceptor stream poor in hydrogen, bio-oil, indicating the importance of the donor stream and the effectiveness of the invention.

TABLE-US-00006 TABLE 6 TEST B TEST C TEST D Bio-oil % wt. 10 20 30 Normalized yields % wt. Coke % wt. 21.3 21.4 21.8 Fuel Gas (H2, 1.6 1.9 2.6 C1-C2) % wt. LPG (C3-C4) % −39.4 −19.1 −10.3 wt. Gasoline (C5- 78.7 50.1 28.4 220° C.) % wt. LCO (220° C.- 0.7 2.8 4.3 344° C.) % wt. Decant oil 0.3 1.4 2.7 (+344° C.) % wt. Water % wt. 22.5 28.2 33.7 CO % wt. 11.8 10.6 13.4 CO.sub.2 % wt. 2.5 2.7 3.4 Total 100.0 100.0 100.0