AHNER PAUL (US)
ABHARI RAMIN (US)
AHNER PAUL (US)
| WO2001064610A1 | 2001-09-07 | |||
| WO2003004584A1 | 2003-01-16 |
| US20060106255A1 | 2006-05-18 | |||
| US3909451A | 1975-09-30 | |||
| US3531543A | 1970-09-29 |
1. A process for producing one or more middle distillate fuels, comprising:
(a) separating a synthetic crude into a light fraction and heavy fraction
(b) hydrotreating the light fraction to form a hydrotreated light fraction;
(c) hydrocracking or hydroisomerizing the heavy fraction to form a hydrocracked light fraction
(d) combining the hydrotreated and hydrocracked light fractions to form a combined light fraction;
(e) separating an LPG fraction from the combined light fraction; and
(f) dehydrogenating and oligomerizing all or a portion of the light olefins.
2. The method of claim 1 , wherein the synthetic crude is formed by a Fischer- Tropsch process.
3. The process of claim 2 wherein the Fischer-Tropsch process uses an FT-feedstock selected from the group consisting of coal, petroleum coke, natural gas, petroleum reside and biomass.
4. The process of claim 1 or 2 wherein hydrocracking includes forming a heavy fraction that is dehydrocyclized to produce aromatic compounds which will increase the density and change the seal swell characteristics of the final product(s).
5. The method of claim 2 further including providing a hydrocarbon feedstock and converting the feedstock to a gaseous mixture comprising hydrogen and carbon monoxide.
6. The method of claim 5 further including converting at least a portion of the gaseous mixture to the synthetic crude.
7. The method of claim 1, wherein separating the combined light fraction comprises separating a portion comprising LPG, naphtha portion or light distillate cut.
8. The method of claim 7 further including dehydrogenating the LPG fraction to light olefins. o
9. The method of claim 8 further including catalytically converting the naphtha to a BTX aromatic portion.
10. The method of claim 8, further including alkylating the BTX aromatic portion with a portion of the light olefins.
11. A product produced by any of the preceding claims wherein the product includes paraffins, chemical intermediates, kerosene, jet fuel and diesel fuel.
12. The product of claim 11 further comprising petroleum- or bio-based fuels in any desirable amount. |
PROCESS TO PRODUCE MIDDLE DISTILLATE CROSS REFERENCE TO RELATED APPLICATIONS
This Application claims priority to U.S. Provisional Application No. 60/828,373, filed on October 5, 2006.
FEDERALLY SPONSORED RESEARCH Not applicable.
REFERENCE TO MICROFICHE APPENDIX Not applicable.
FIELD OF INVENTION
The invention relates to a process for the production of middle distillates from synthetic naphtha.
BACKGROUND OF THE INVENTION
Iso-paraffinic synthetic fuels (or "synfuels" for short) generally lack one or more desirable fuel attributes. For gasoline, this includes low octane values. In the case of jet fuel, these include lower density and lack of seal-swelling properties. Lack of seal-swelling properties means that a fuel tank equipped with nitrile rubber closure gasket used for conventional petroleum fuels ("petro-fuels") will leak if filled with an iso-paraffinic synfuel. These differences with petro-fuels can limit use of iso- paraffinic synfuels. One solution has been to blend these synfuels with petro-fuels. However, blending with petro-fuels generally downgrades the synfuel 's low emission qualities. Particulate emissions are attributed to naphthalene-type molecules in crude oil.
Since aromatic hydrocarbons have higher density and can impart seal swelling properties, alkyl benzenes of jet fuel boiling range may be used as blend stocks for corresponding iso-paraffinic synfuels to solve the seal-swell and density issues without affecting their desirable low particulate emission qualities. In the case of gasoline, the alkyl-benzenes are known to increase synfuel octane value.
Synthesis of alkyl aromatics via olefins and benzene has industrially important applications, such as manufacture of cumene and detergent-range linear alkyl benzenes. Alkyl benzenes having alkyl groups with from about 4 to about 9 carbon atoms may also be used as chemical intermediates or as fuel blend stocks.
Traditional processes for manufacturing alkyl aromatic components employ different catalysts and reactors for the benzene and olefin components used to make the alkyl benzene products. For example catalytic reforming may be used to convert paraffϊnic feedstock to benzene by dehydrocyclization. Olefin production is typically achieved by dehydrogenation of the paraffins. Thus, the combination of two processes to make these components is capital-intensive.
Consequently, a simpler process for the preparation of alkyl benzenes and synthetic fuels would be useful.
SUMMARY OF THE INVENTION
A process for producing one or more middle distillate fuels is described. An embodiment of the described process includes (a) dehydrogenating/aromatizing a paraffϊnic naphtha stream into a composition containing olefins and aromatic hydrocarbons (b) subjecting the olefins and aromatic components to aromatic alkylation, and (c) separating the alkyl aromatics of middle distillate range.
In some embodiments the synthetic naphtha is a product of the Fischer- Tropsch process. Selected Fischer-Tropsch processes employ synthesis gas derived from coal, petroleum coke, natural gas, petroleum residue and biomass. In other embodiments, the synthetic naphtha may be the co-product of hydroprocessing glycerides (mono-, di-, and tri-), and fatty acids present in vegetable oils, animal fats, and restaurant greases.
Embodiments of the invention also include products produced by one or more of the methods described herein, particularly wherein the products include chemical intermediates, gasoline, kerosene, jet fuel and diesel fuel. Products further comprising petroleum- or bio-based fuels in any desirable amount are also contemplated.
BRIEF DESCRIPTION OF THE DRAWING
Figure 1 depicts a process for selectively converting paraffinic components according to one embodiment of the invention.
DETAILED DESCRIPTION OF THE INVENTION
The terms "middle distillate product(s)" and "middle distillate" refer to hydrocarbon mixtures with a boiling point range that corresponds substantially with that of kerosene and gas oil fractions obtained in a conventional atmospheric
distillation of crude oil material. The middle distillate boiling point range may include temperatures between about 65 degrees C and about 315 degrees C, with a fraction boiling point between about 93 degrees C and about 182 degrees C.
The term "middle distillate fuel" means jet fuel, kerosene, diesel fuel, gasoline, and combinations thereof.
The term "BTX" means Benzene, Toluene, Xylene, or a mixture of any of Benzene, Toluene, and Xylene.
The term "C x ", where x is a number greater than zero, refers to a hydrocarbon compound having predominantly a carbon number of x. As used herein, the term C x may be modified by reference to a particular species of hydrocarbons, such as, for example, C 5 olefins. In such instance, the term means an olefin stream comprised predominantly of pentenes but which may have impurity amounts, i.e. less than about 10%, of olefins having other carbon numbers such as hexene, heptene, propene, or butene.
The term "light fraction" generally indicates a hydrocarbon comprised primarily of C 2 to C 24 hydrocarbons; preferably C 2 -C 9 in some cases.
The term "light fraction" generally indicates a hydrocarbon comprised primarily of hydrocarbons having a carbon number greater than about C 24 , but in some cases the heavy fraction contains C 10 + fractions.
Naphtha fractions described herein generally have a boiling range of 30 to 250 degrees F and contains alkanes in the C 5 to C 9 range.
LPG fractions generally refer to hydrocarbons having from 2 to 5 carbon atoms, but in most cases 3 and 4.
It has surprisingly been found that using certain noble metal catalyst systems naphtha range paraffins that do not cyclize to an aromatic will dehydrogenate to form olefins which will react in the alkylation step to form alkylated aromatics in the middle distillate boiling range. In particular, commercially available tin/platinum-on- alumina catalysts convert n-hexane to benzene and convert C 7 paraffins to linear internal olefins with high selectivity. Thus, the conversion of naptha-range n-paraffϊn feed to a composition suitable for aromatic alkylation.
One such process is schematically represented in Figure 1. In Figure 1, an n- paraffm naphtha feed 201 is provided to a dehydrogenation unit 202 equipped with a tin/platinum-on-alumina catalyst. The product of the dehydrogenation unit 202 is fed to aromatic alkylation unit 203. Homogeneous Lewis acid catalysts such as
aluminum trichloride or boron trifluoride, and heterogeneous zeolite catalysts, may be employed to carryout the aromatic alkylation reaction. Alkylated-benzenes and unconverted C 6 -Cg products are provided to a separator 204 configured to separate C 10 + products from lower carbon products, including the unconverted C 6 -Cg fraction. Conventional distillation is well suited for this application. The separated unconverted fraction may be recycled to the dehydrogenation unit 202.
When the paraffinic naphtha is the byproduct of a middle distillate synfuel process, this method can be employed to maximize Cio+ product yield and modify the product properties such as density and seal swell.
Example 1:
Commercial Sn/Pt-on-alumina dehydrogenation catalyst from Englehard Corporation comprising 0.65-0.85 wt. percent Sn, 0.40-0.58 wt. percent Li, 0.30-0.45 wt. percent Pt is used. The catalyst has a particle size of 1.58-2.54 mm and a surface area of 140-180 m 2 /g according to BET-N 2 surface area measurements. Tube-in-tube glassware is used in a reactor with about 0.1 g of catalyst in the inside tube. Slits in the bottom tube allow for bottom-up feed flow. The reactor is placed in a furnace and heated to about 232 degrees C under a flow of hydrogen suitable for catalyst activation. After 30 minutes of activation, hydrocarbon recirculation is started. Results from n-hexane, n-heptane, and n-octane are presented in Tables I-III respectively. Table I
Table II
Table III
Reactor Conditions
Catalyst 0.1192 g
Reactor temp 232 degrees C n-Cg lO torr
H 2 200 torr
He 790 ton-
Products (wt. percent) Batch Cycle Time (min)
30 min 50 min
Variations, modifications and additions to this invention will be readily apparent to one skilled in the art and such modifications and additions would be fully within the scope of the invention, which is not limited by the claims.
We Claim: