U.S. patent application number 09/877625 was filed with the patent office on 2002-01-17 for methods for optimal usage and improved valuation of corrosive petroleum feedstocks and fractions (law521).
Invention is credited to Anderson, Michael P., Chimenti, Robert J.L., Halpern, Gerald M., Iannucci, Maureen, Kalamaras, Patricia H..
Application Number | 20020006667 09/877625 |
Document ID | / |
Family ID | 23049439 |
Filed Date | 2002-01-17 |
United States Patent
Application |
20020006667 |
Kind Code |
A1 |
Chimenti, Robert J.L. ; et
al. |
January 17, 2002 |
Methods for optimal usage and improved valuation of corrosive
petroleum feedstocks and fractions (Law521)
Abstract
The invention is a method to improve the prediction of the
corrosivity of organic acids in petroleum crudes, feedstocks and
distillation fractions by providing a more accurate, repeatable,
and rapid means of determining the TAN from the IR spectrum of the
material. The method can be easily practiced in refinery, terminal,
and assay laboratories. It can be used in conjunction with models
and hardware to optimize the usage and improve the valuation of
corrosive feed stocks. The invention can be implemented on-line for
blending optimization. It comprises the steps of irradiating a
heated petroleum sample with IR radiation to produce its IR
absorption spectrum, and predicting the TAN from the spectrum using
a linear, multivariate regression model. The IR TAN value is then
used as input to blending, valuation, and corrosion models.
Inventors: |
Chimenti, Robert J.L.;
(Short Hills, NJ) ; Halpern, Gerald M.;
(Bridgewater, NJ) ; Kalamaras, Patricia H.;
(Milford, NJ) ; Anderson, Michael P.; (The
Woodlands, TX) ; Iannucci, Maureen; (Sierra Madre,
CA) |
Correspondence
Address: |
Ronald D. Hantman
ExxonMobil Research and Engineering Company
(formerly Exxon Research and Engineering Company)
P.O. Box 900
Annandale
NJ
08801-0900
US
|
Family ID: |
23049439 |
Appl. No.: |
09/877625 |
Filed: |
June 8, 2001 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
|
|
09877625 |
Jun 8, 2001 |
|
|
|
09274744 |
Mar 23, 1999 |
|
|
|
Current U.S.
Class: |
436/60 ; 436/164;
436/171 |
Current CPC
Class: |
G01N 33/2876 20130101;
G01N 21/0332 20130101; G01N 21/314 20130101; G01N 2201/1293
20130101; Y10T 436/12 20150115 |
Class at
Publication: |
436/60 ; 436/164;
436/171 |
International
Class: |
G01N 031/00; G01N
033/26; G01N 021/75; G01N 033/03; G01N 021/00; G01N 021/62 |
Claims
1. A method to determine the organic acid content of petroleum
streams comprising: (a) irradiating a sample of said petroleum
stream with IR radiation; (b) determining the absorption spectrum;
and (c) correlating said absorption spectrum with the organic acid
content of said petroleum stream using linear multivariant
regression analysis.
2. The method of claim 1 wherein said organic acid content is in
units of ASTM TAN.
3. The method of claim 1 further comprising the step of heating a
sample of said petroleum stream having boiling points below
1050.degree. F., at a temperature between 25.degree. C. and
125.degree. C. before said irradiating step.
4. The method of claim 3 wherein said temperature is between
40.degree. C. and 100.degree. C.
5. The method of claim 4 wherein said temperature is between
55.degree. C. and 75.degree. C.
6. The method of claim 1 wherein the optical absorbance for every
spectral frequency is between 0 and 2.0 absorbance units.
7. The method of claim 5 wherein the optical absorbance for every
spectral frequency is between 0 and 1.75 absorbance units.
8. The method of claim 3 wherein said sample has boiling points
below 1050.degree. F.
9. The method of claim 3 wherein said sample is a known mixture
having boiling points above and below 1050.degree. F.
10. The method of claim 1 wherein said IR radiation is in the
spectral ranges 1000 and 4800 cm.sup.-1.
11. The method of claim 9 wherein said IR radiation is in the
spectral ranges 1000-1350 cm.sup.-1, 1550-2200 cm.sup.-1, 2400-2770
cm.sup.-1, and 3420-4800 cm.sup.-1.
12. The method of claim 1 further comprising the step of
orthogonalizing the absorption spectrum so as to eliminate
environmental and instrumental contributions.
13. The method of claim 1 further comprising the step of using said
orthogonalized spectra of a set of samples, the calibration
samples, which are representative of the variability of petroleum
feed and process streams, to develop a prediction regression model
to predict the TAN of said streams to an accuracy that renders the
invention useful to the application.
14. The method of claim 13 wherein said number of samples is at
least 8 times the number of regression factors in the model, and
more preferably 10 times the number of regression factors.
15. The method of claim 13 wherein said samples include both whole
crudes and pipestill distillation factions.
16. The method of claim 13 wherein said average prediction error
for a sample set of whole crude and pipestill and laboratory
distillation fractions are less than 0.25 and more preferably less
than 0.15 TAN units.
17. The method of claim 1 utilizing a sufficient number of
calibration samples to achieve a predetermined accuracy.
18. The method of claim 17 wherein said number of calibration
samples exceed 100.
19. The method of claim 17 wherein said number of calibration
samples exceed 400.
20. A method to optimize blending of two or more petroleum
feedstreams having different levels of TAN wherein the feedstream
blend is processed into process streams comprising: (a) blending
said feedstreams in certain proportions to form a feedstream blend;
(b) measuring the TAN level of said feedstream blend and/or said
processed streams using the method of claim 1; (c) comparing the
TAN level of said feedstream blend and/or process streams to a
predetermined TAN level; and (d) adjusting the proportions of said
feedstreams in the blending step so that the TAN level of the
feedstream blend and/or process streams is equal to or less than
said predetermined level.
21. In a method for determining the value of a crude oil, the
improvement which comprises determining the TAN level of the crude
oil by the method of claim 1, valuing the crude oil according to
said TAN level.
22. A method to optimize the addition of acid neutralizing agents
to a petroleum feedstream that is processed into process streams
comprising: (a) determining the optical absorbance spectrum of the
feedstream and/or processed streams; (b) predicting the organic
acid content and/or corrosion rate of the feedstream and/or
processed streams from its spectrum; (c) adding the neutralizing
agent in batch or intermittent or continuously mixed flow; (d)
measuring the optical spectrum of the treated feedstream and/or
processed streams; (e) predicting the remaining acid content and/or
the corrosion rate of the treated feedstream and/or processed
streams without removing the neutralized products or unreacted
neutralizing agent; and (f) controlling the amount or blend of
neutralizing agents, and/or the temperature, pressure, mixing, or
flow conditions in the neutralizing process to achieve the target
acid level and/or corrosion rate in the treated feedstream and/or
processed streams.
Description
BACKGROUND OF THE INVENTION
[0001] This invention relates to a method for predicting the
organic acid level in a petroleum feedstream and the use of that
method. Substantial economic benefits derive from the optimal usage
and improved valuation of corrosive feedstocks. Such benefits can
be achieved by means of improved (i.e. more accurate, precise and
rapid) methods for analyzing the corrosive organic acid content of
these feedstocks which, in many cases, can be purchased at
attractive prices. Additional benefits can be achieved through the
use of these improved methods in conjunction with mathematical
models to control process and blending apparatus and to valuate
feedstocks. Applications of the means to obtain the improved
organic acid content value, in conjunction with the models and
control apparatus, are to predict the corrosivity towards process
equipment, the value of a crude or blend for sale or purchase, the
recipe for crude or feed blending to a target corrosivity or
organic acid level, and optimization of processes to reduce the
corrosive organic acid species. The improved method for predicting
the organic acid content is more accurate, repeatable, and rapid
than existing methods and, unlike such existing methods, can be
implemented for batch or continuous on-line operation.
[0002] Currently, producers, materials engineers, plant process
operators and planners, and raw materials purchasers estimate
corrosivity caused by the organic acids in the materials from the
Total Acid Number (TAN), or a parameter derived therefrom, obtained
by a commonly accepted potassium hydroxide titration method, one
example being ASTM D664.
[0003] The ASTM D664 method, while the most commonly used method in
the petroleum industry for determining organic acids in petroleum
streams, is not selective to organic acids. It reports, as acids,
any species that utilizes the potassium titrant in reaction,
complexation, neutralization, or replacement. For example, one
limitation of the current ASTM method is its inaccuracy in
determining the correct acid content when the material has di- and
trivalent metal acid salts, such as calcium naphthenates. Use of
the ASTM TAN method on materials that contain calcium naphthenates
would over-report the TAN since both true acid content as well as
the calcium salts would be reported as TAN. Hence the corrosivity
of the materials, as determined from mathematical models relating
corrosion rates to the TAN value for these materials, would be
over-estimated in such cases.
[0004] This invention includes, in all of its embodiments, a method
to predict the organic acid content from the infra-red (IR)
spectrum of a petroleum feedstock or process fluid. The IR method
reports the organic acid content in units of titratable organic
acid, TAN. The TAN determined by IR, henceforth called IR TAN,
therefore, can be used in applications and models that use TAN as
an input parameter. The IR TAN method is shown to be statistically
equivalent to ASTM TAN and be more accurate than ASTM when calcium
acid salts are present in the materials.
[0005] High TAN crudes can be purchased, in many cases, at
attractive prices. The improved method for TAN measurement, as
incorporated in the present invention, is a key enabler for
reducing feed costs through the increased usage of such
economically attractive materials.
SUMMARY OF THE INVENTION
[0006] The invention is a method to improve the prediction and
control of the corrosivity of organic acids in petroleum crudes,
feedstocks and distillation fractions by providing a more accurate,
repeatable, and rapid means of determining the TAN from the IR
spectrum of the material. The method can be easily practiced in
field, refinery, terminal, and assay laboratories. It can be
implemented on-line for blending optimization in production fields
and in refineries.
[0007] The invention comprises the common steps of irradiating a
heated petroleum sample with IR radiation to produce its IR
absorption spectrum, and predicting the TAN from the spectrum using
a multivariate regression model. The IR TAN value thus obtained is
then used as input to blending, valuation, and corrosion
models.
[0008] Other embodiments of the present invention include using the
method of determining TAN level in methods for valuing crude oil,
blending petroleum feed and distillation sidestreams and optimizing
neutralizing processes.
BRIEF DESCRIPTION OF THE DRAWINGS
[0009] FIG. 1A shows the regions of the absorption bands of the
acid C.dbd.O, aromatic C.dbd.C, and carboxylate ion COO--
functionalities for the distillate residuum fraction of an
untreated (curve a), and two treatment levels (curves b and c) of
the crude oil blend of Example 1, where the treatment comprises the
addition of Ca(OH).sub.2.
[0010] FIG. 1B shows the difference in absorbance of the untreated
blend subtracted from each of the treated blends (curves b and c,
respectively), of Example 1, showing the loss in acid C.dbd.O and
gain in the salt COO-- absorption.
[0011] FIG. 2A shows the fitted values of the IR TAN using the
calibration model and corresponding measured ASTM TAN for 216 plant
and laboratory distillation samples. Plant distillate fractions
from atmospheric and vacuum pipestills and the material boiling at
temperatures greater than 650.degree. F. (650+) are included.
Laboratory distillation fractions include a blend of material
having mid-boiling point temperatures of 650 and 1050.degree. F.
and the total material that boils at temperatures greater than and
less than 650.degree. F., denoted by 650+ and 650-, respectively.
The boiling point range for the lab cuts is 100.degree. F. although
some distillations were carried out with a 50.degree. F. range for
each cut. The Standard Error of Calibration (SEC) for all of the
216 samples is 0.11. The center solid line on the graph is the
parity line.
[0012] FIG. 2B shows the predicted IR TAN and the measured ASTM TAN
for 221 refinery samples using the calibration model shown in FIG.
2A. The Standard Error of Prediction is 0.08. It can be seen that
the predictions are excellent with most of the data points around
the parity line and within the site repeatability of the ASTM
reference method.
[0013] FIG. 3 shows the IR and ASTM TAN values for high TAN crudes,
some of which also contain high levels of calcium organic salts, as
described in Example 2, below. Each data point is for a given
sample measured by the two techniques with error bars representing
the repeatability of the IR method. The solid line is the parity
line and the band bounded by the dotted two lines surrounding the
parity line represents values within the ASTM repeatability for the
ASTM D664 method. Sample points lying outside and to the right of
the region bounded by the two dotted lines in the figure are those
for which the ASTM TAN is higher than the IR.
[0014] FIG. 4 shows that large difference between the ASTM and IR
TAN coincides with high Ca levels in the samples. The triangle data
points are the Ca levels in ppm, on the left ordinate axis, plotted
against the ASTM TAN for the sample and sample sequence shown in
FIG. 3. The circle data points are the delta TAN; that is, the
difference between the ASTM and IR TAN measurements, right ordinate
axis, for the same samples.
[0015] FIG. 5 shows the ASTM TAN, on the abscissa, for the same
samples and sample sequence of FIG. 3 plotted against the sum of
the IR TAN and the Ca-equivalent TAN (which is defined as the Ca
(ppm)/357). The solid line is the parity line. The figure shows
that the Ca in these samples can account for the differences
between the measured IR and ASTM TAN.
[0016] FIG. 6 shows that for blends of high acid crudes having high
levels of Ca naphthenates, the TAN values as measured and
calculated, for both the ASTM and IR methods blend linearly. The IR
TAN is lower in value for the blends consistent with the lower
values for the blend components.
[0017] FIG. 7 shows that the absorption cross-section, in
cm.sup.2/mole, of model acids varies in peak position, spectral
width, and dimer-to-monomer ratio. Thus, Beer's law, which
expresses a linear relationship between concentration and spectral
absorption, is not expected to hold for a complex mixture of acids
present in a crude oil. Correspondingly, it is not obvious that a
linear, multivariate model could be used to relate the spectra of
this complex mixture to ASTM TAN with sufficient accuracy to be
useful in the applications.
[0018] FIG. 8 shows that a single model organic acid dissolved in a
white oil to a TAN value of 3.4 changes its spectral absorption
band shape, not just intensity, as a finction of concentration.
Thus, Beer's law is not expected to hold for a complex mixture of
acids present in a crude oil.
[0019] Correspondingly, it is not obvious that a linear,
multivariate model could be used to relate the spectra of this
complex mixture to ASTM TAN. It is, furthermore, not obvious that a
single linear multivariate model for crudes and their distillate
fractions could be developed having sufficient accuracy for
corrosion applications, in view of the non-Beer's law behavior of
the acids. For example, prediction error of 0.1 TAN units, over a
sample set that includes crudes, pipestill and laboratory
distillation cuts, is desirable.
[0020] FIG. 9 shows a method to optimize the blending of high and
low TAN feeds to achieve a target TAN determined from a corrosion
model and safety and equipment reliability constraints.
[0021] FIG. 10 shows a method to optimize the valuation of
corrosive crudes by combining standard inspection qualities with
the improved IR TAN method described herein.
[0022] FIG. 11 shows a method to optimize the blending of crudes
from different wells to achieve a target TAN for shipment by
pipeline or other transportation means.
[0023] FIG. 12 shows a method to optimize a TAN neutralization
process.
DESCRIPTION OF PREFERRED EMBODIMENT
[0024] The novel features of this invention are its selectivity to
organic acids, its ability to quantitate organic acid content in
units of ASTM TAN, and its ability to predict acid content from IR
spectra where the spectral frequency and band shape of the acid's
absorbance changes with feedstock composition.
[0025] A method is described to predict the organic acid content,
in ASTM D669 TAN units of mg KOH/gram of sample, of petroleum crude
oils, laboratory and plant distillation fractions, and petroleum
distillation residua. The method consists of the following:
[0026] 1. For materials having boiling points below 1050.degree.
F., heating an undiluted sample to a temperature of 25 to
125.degree. C., preferably between 40 and 100.degree. C., and more
preferably between 55 and 75.degree. C. in an optical cell having a
path length of 0.005 to 0.1 cm, preferably 0.01 to 0.03 cm, and
more preferably 0.0175 to 0.0225 cm, so as to insure that the
optical absorbance for every spectral frequency used in the model
is between the values of 0 and 2.0 absorbance units, and preferably
between 0 and 1.75 absorbance units, for every sample. The
temperature is controlled to approximately .+-.26 C for all
measurements. Similarly the optical path length is fixed for all
measurements.
[0027] 2. For residua having boiling points above 1050.degree. F.,
preparing and heating a mixture of known proportions of the crude
or a distillation fraction boiling below 1050.degree. F. (diluent
fraction) and the fraction boiling above 1050.degree. F. in the
same optical cell as described above may be more convenient due to
the high viscosity of the residuum fraction. Determination of the
IR TAN for the residua is obtained by the difference between the IR
TAN for the mixture and diluent fraction weighted according to
their weight fractions. The use of a lower boiling fraction of the
same crude as a diluent fraction avoids, to a greater extent, any
mixture incompatibility, inhomogeneity, and precipitation that may
occur if common reagent solvents are used.
[0028] 3. Irradiate the heated sample with infra-red radiation in
the spectral frequency ranges from 1000 to 4800 cm.sup.-1 and
preferably in the ranges 1000-1350 cm.sup.-1, 1550-2200 cm.sup.-1,
2400-2770 cm.sup.-1, 3420-4800 cm.sup.-1, and obtain the infra-red
absorption spectrum of said sample.
[0029] 4. Eliminate the major environmental and instrumental
contributions to the measured spectrum by orthogonalizing the
measured spectrum in each of the above mentioned frequency ranges
to that of atmospheric air, dissolved water, and to orthonormal
polynomials on each of the above mentioned frequency ranges
representing the major instrumental contributions that are
independent of the sample composition. The resulting spectra,
called the conditioned spectra, are used as inputs in a
multi-variate regression model.
[0030] 5. Obtain the IR TAN value by multiplying the absorption at
each spectral frequency used in the model by a calibration value
for that frequency and summing up said products over all of the
frequencies in the above-mentioned ranges.
[0031] 6. The calibration values for each spectral frequency of the
model are obtained by applying linear, multi-variate regression
techniques to a data set consisting, in part, of the conditioned IR
absorption spectra of samples for which the ASTM TAN had been
obtained. The data set also consists of samples containing
naphthenic acids having insignificant levels of alkaline-earth acid
salts and samples of these same materials to which known amounts of
calcium has been used to neutralize varying levels of the acids.
The data set also consists of samples of materials which have
naphthenic acids and contain significant levels of calcium almost
entirely in the form of calcium acid-salts, such as certain crude
oils. In the latter cases, the ASTM TAN levels are corrected for
the presence of the calcium acid salts which are reported as TAN,
and the corrected values are used in the regression model. The
corrected ASTM TAN may be taken as the difference between the
measured ASTM TAN and the calcium concentration, expressed in ppm,
divided by 357. Thus a calcium concentration of 357 ppm as
naphthenate would result in a corrected value of TAN which is 1 TAN
unit less than the measured ASTM TAN.
[0032] The features of this invention include its selectivity to
organic acids, its quantitation of organic acid content in ASTM TAN
units, and the use of a linear multivariate model to predict acid
content of a sample from its IR spectrum.
[0033] 1. Acid Prediction from IR Spectra is an Application of
Linear, Multi-variate Correlation
[0034] The invention makes use of a non-obvious application of
multivariate modeling methods to quantify the acid content in terms
of ASTM TAN. Linear, multivariate prediction methods using spectra
as input are normally applied where there is no variation in the
spectral frequency position or shape of the absorption band of the
molecular functionality that is relevant to the predicted
parameter. If linear multi-variate regression models using the
spectral frequencies as independent variables are to apply, it is
assumed that there is a characteristic frequency and absorption
band for that functionality and, furthermore, that its contribution
to the absorption spectrum of the sample changes in only in
amplitude, not shape or position, as a function of its
concentration within the sample.
[0035] There are several reasons why the absorption frequencies of
the naphthenic acids would not be considered suitable as
independent variables for a linear, multi-variate regression model.
First, the C.dbd.O absorption band of the acid COOH group is
actually composed of C.dbd.O vibrations of a hydrogen-bonded acid
dimer, and of an acid monomer, located at approximately 1709 and
1760 cm.sup.-1, respectively. The dimer and monomer forms of the
acid are in thermal equilibrium, with relative concentrations
dependant upon the dissociation constant and temperature. Under
measurement conditions, the spectra are strong functions of
temperature, the temperature dependencies being different for
different acids, for the same acid diluted in different hydrocarbon
liquids, and for the same acid diluted to different levels in the
same hydrocarbon liquid. Consequently, the shape and frequency
position of the absorption cross-section for different acids vary
depending upon the interactions with the non-acid portion of the
molecule and with temperature.
[0036] As an example of the first case FIG. 7, shows the absorption
cross-section in cm.sup.2 per mole for several model acid compounds
diluted in the same white oil matrix at a fixed temperature. It can
be seen that the strength and position of the bands vary with the
molecular structure.
[0037] In addition to the variation of the C.dbd.O absorption band
due to intramolecular interactions, intermolecular interaction with
other molecules that comprise the hydrocarbon matrix will also
affect the position and shape of the bands. Thus, the Beer-Lambert
law does not generally hold for organic acids. FIG. 8 curve (a)
shows the absorbance per mm, absorptivity, of a single acid,
cyclopentylacetic acid, diluted in a white oil to a TAN value of
3.4. Chloroform, a non-polar solvent, was added to dilute the TAN
further by up to a factor of 100. The absorption band for each of
the samples should differ only in amplitude and not in shape if
Beer's law was valid for the acid. It is clear from curves (b)-(g)
in FIG. 8 that the interaction with the solvent alters the
absorption characteristics of the acid C.dbd.O.
[0038] A consequence of the non-Beer's Law behavior is the
inability of a few-frequency, multi-linear regression model, to
predict the acid content with sufficient accuracy for corrosion
applications. This invention recognizes that the use of a
multivariate principal component model transforms the measured
spectral frequencies into new variables that in sufficient number
can account for this non-Beer's Law behavior with sufficiently high
accuracy to be of utility for corrosion applications. For similar
reasons, the determination of acid reduction by peak or integrated
band intensity ratios are less accurate than the approach
disclosed.
[0039] For example, in the principal component regression model
shown in FIGS. 2A and 2B, 10 non-sequential component variables
were used, including component number 17, in order of decreasing
eigenvalue, to result in a prediction error over the whole suite of
petroleum crudes and pipestill and laboratory distillates, of less
than 0.11 TAN units. A total of 216 samples that spanned the
variability of the application was used, resulting in over 10
samples per regression component.
[0040] 2. Prediction of Organic Acid Content as ASTM TAN from IR
Spectra
[0041] Materials engineers and process operators have historically
used ASTM TAN values to estimate the corrosivity of petroleum crude
and distillate fractions. The instant invention predicts the ASTM
TAN value of a sample from its IR spectrum. This was accomplished
by developing a relationship between the IR spectrum and the ASTM
TAN of 216 calibration samples consisting of a wide range of
petroleum crude oils and distillate fractions, to enable this
relationship to be used to predict the ASTM TAN of future
samples.
[0042] An IR transmission cell having CaF.sub.2 windows and an
optical path length of 200 microns was maintained at a temperature
of 65.+-.2.degree. C. and used to obtain the spectra of the
samples. A Fourier transform IR spectrometer was used to obtain the
spectra at approximately 1 cm.sup.-1 resolution.
[0043] Only selected regions of the spectra were used to develop
the calibration model. These regions are 4800-3420 cm.sup.-1,
2770-2400 cm.sup.-1, 2200-1550 cm.sup.-1 and 1350-1000 cm.sup.-1.
Although the major absorbance of the acid functionality occurs in
the 1800-1650 cm.sup.-1 region, the additional spectral frequencies
are critical to obtain the required accuracy and statistical
measures of the quality of the model and its predictions. An
example is the ability of the model to detect when a sample is a
model outlier and its TAN, predicted by IR, may not be
accurate.
[0044] The measured spectra in the above-mentioned spectral
frequency ranges were conditioned to eliminate effects of
instrumental and environmental variations which were independent of
the acid content and chemical composition of the samples. The
conditioning was independently applied to each frequency
region.
[0045] The conditioned spectra of the calibration samples were
correlated against their TAN values as determined by the ASTM D664
method. The correlation consisted of a principal component
regression of spectral scores vs. ASTM D664 TAN values.
[0046] The IR TAN for the 500 calibration samples is shown in FIG.
2A. The samples have ASTM TAN values in the range 0-5. The Standard
Error of Calibration was 0.09.
[0047] IR TAN predictions were carried out of 221 refinery samples
including crude oils, and distillation fractions. The results are
shown in FIG. 2B. The Standard Error of Prediction is 0.08.
[0048] The IR method is more repeatable than the ASTM technique.
For example, using Arab light crude, the repeatability of the IR
TAN is 0.008, while the ASTM method claims 0.024.
[0049] 1. Selectivity to Organic Acids
[0050] The standard test method for Total Acid Number of petroleum
feeds is ASTM D664-89. While the scope of this method, as stated by
ASTM, is for petroleum products, it is commonly applied in the
industry for crude oils and other hydrocarbon feedstocks, and for
process liquids and distillation fractions, as an indicator of
organic acid corrosivity. The method, however, is not selective to
organic acids. Other constituents that may be present, including
inorganic acids, esters, phenolic compounds, lactones, resins,
salts of heavy metals, salts of ammonia and other weak bases, acid
salts of polybasic acids, are titrated by the test method and
reported as acid number. If present in petroleum feedstocks and
process fluids, these constituents may result in ASTM TAN values
which over-estimate the organic acid content. Consequently, the
corrosivity may be over-estimated if a corrosion model is used to
relate the TAN of the material to its corrosivity, assuming these
other constituents are not corrosive.
[0051] Salts of alkaline earth metals, such as calcium may be
present in petroleum liquids as the result of natural occurrence or
as reaction products of upstream treatment to neutralize part of
the acid. Calcium salts of naphthenic acids are titrated and
reported as acids by the ASTM method. The IR absorption due to acid
carbonyl (C.dbd.O) and carboxylate anion (COO--) functionalities
can be separately detected and, consequently, forms the basis for
the selective prediction of organic acid content.
EXAMPLE 1
Selectivity to Organic Acids when CaO is Added to the Sample
[0052] The following example illustrates the ability of the IR to
differentiate between acids and salts. A crude blend was treated to
reduce the organic acid by the addition of CaO, based on ASTM TAN
of the untreated crude. The addition of CaO produces soluble
Ca-salts of the acids having low volatility. Upon distillation of
the treated crude blend, these salts, therefore, tend to
concentrate in the residuum fraction. Consequently, it may be
anticipated that the ASTM method applied to this fraction will
report a TAN value at levels comparable to or higher than that of
the untreated crude fraction, due to the inability of the method to
distinguish between acids and Ca-salts of these acids. The acid
content of the residuum fraction on the other hand is expected to
be reduced from its untreated levels.
[0053] Application of the ASTM and IR TAN methods to these resid
fractions result in the TAN determinations shown in Table 1. It can
be seen that the ASTM TAN values are at the same level or higher as
the treat increased, from B to C while the IR TAN significantly
decreases with treat level, as anticipated. It can be concluded
that the IR gives a more reliable estimate of the organic acid
TAN.
1TABLE 1 ASTM TAN IR TAN RESID FRACTION (mg KOH/g sample) (mg KOH/g
sample) A Untreated crude 2.17 2.22 B Treat on crude blend 1.94
0.69 C Treat on crude blend 3.12 0.14
[0054] These conclusions are confirmed by the IR spectra of the
untreated and treated residuum fractions. FIG. 1A shows the regions
of the absorption bands of the acid C.dbd.O, aromatic C.dbd.C, and
COO-- carboxylate ions of the Ca salts for the distillate residuum
fraction of an untreated crude oil blend (curve A), the crude oil
blend treated to level B (curve b), and level C (curve c), where
treat C is greater than treat B. The organic acid C.dbd.O band is
reduced in curves b and c from curve a, with increasing treat. The
carboxylate ion of the Ca salt on the other hand can be seen to
increase in curves b and c with increasing treat. The selectivity
of the IR absorbance can be more clearly displayed in FIG. 1B,
where the absorbance of the untreated material is subtracted from
the B and C treated materials, curves b and c, respectively,
showing the loss in acid C=O and gain in the salt COO--
absorption.
EXAMPLE 2
IR TAN Provides More Accurate Quantitation of Organic Acids Than
ASTM TAN for High TAN Crudes Containing Organic Acid Salts of
Calcium
[0055] This example illustrates the application of the IR TAN
invention to petroleum crude oils that contain relatively high
levels of naphthenic acids and their calcium salts. This example
shows that the true TAN of these crudes, as determined by the
instant invention, are lower than those obtained by using the ASTM
method. This is supported by showing that the calcium in the
samples exist almost entirely as acid salts and account for the
differences between the ASTM and IR TAN determinations.
[0056] This example also shows that the IR TAN of mixtures of these
high TAN crudes blend linearly with the TAN values of the
individual components weighted by their weight fraction, and that
the TAN values of these blends, as determined by the IR, are lower
than those obtained by ASTM. These results demonstrate that the IR
TAN method can be used to blend crudes more accurately to a target
TAN level for applications of the sale and purchase of crude
mixtures, and for the planning of refinery processing. For example,
the IR TAN method can be implemented at a pipeline or tanker
terminals to control blending of the crudes to the target TAN
level.
[0057] ASTM and IR TAN of high TAN crudes from three production
fields, designated by B, K, and M, and zones designated by A, M, Y
and 0, 1, 2, 3, have been determined and the results shown in
columns 3 and 4 of Table 2, and their differences ASTM-IR, are
shown in column 4. The data are presented in order of decreasing
ASTM TAN.
2TABLE 2 TAN and Ca Measurements on the B, M, K Crude Samples TAN
Ca (ppm) SAMPLE ASTM IR ASTM-IR Acid digest. Xylene dilut. B/M2
7.13 6.71 0.42 158.0 160.0 B/A1 6.25 5.87 0.38 43.0 42.7 B/A2 6.24
5.92 0.32 43.0 42.6 B/M3 5.88 5.29 0.59 78.0 78.1 K/M1 5.47 4.13
1.34 809.0 803.0 K/M3 5.38 3.67 1.71 834.0 756.0 K/Y0 5.28 3.82
1.46 670.0 596.0 K/M1 4.97 3.24 1.73 953.0 907.0 B/M1 4.28 3.78
0.50 76.0 72.7 K/M1 3.86 2.86 1.00 406.0 379.0 B/M1 3.82 3.42 0.40
35.0 28.9 K/Y0 1.75 1.47 0.28 14.0 14.2 M/M1 1.30 1.25 0.05 2.4 2.7
M/M1 0.51 0.39 0.12 2.5 1.5 K/A1 0.05 0.11 -0.06 11.0 8.6 K/A1 0.03
0.03 0.00 13.0 10.2
[0058] Also shown in the table are the results of calcium analyses
using the method of Inductively Coupled Plasma (ICP) analysis. Two
methods were used to introduce the samples into the plasma. One
involved acid digestion of the remaining ash after combustion of
the sample. The second involved dilution of the sample with xylene.
The acid digestion method determines the total Ca in the sample,
while the xylene dilution technique determines soluble Ca as well
as insoluble Ca species having particle sizes below about 3
microns. The errors in the reported Ca values for each method are
less than 5% relative.
[0059] The two measurements of the Ca level for each of the samples
are given in the table. The similar values obtained by the acid
digestion and xylene dilution methods are consistent with the Ca
existing predominantly as soluble organic species in these samples,
due to the exclusion of insoluble Ca with particle size >3
microns from the ICP in the xylene method.
[0060] FIG. 3 shows a parity plot of the ASTM and IR TAN
measurements (solid circles), with error bars corresponding to the
repeatability of the IR method. The parity line (solid line) is
shown at the center of a band which is defined by the two dashed
lines corresponding to the 6% repeatability of the ASTM TAN
measurement. The IR TAN values that fall within his band agree with
and are statistically equivalent to the ASTM values. Examples are
the samples having the four highest and five lowest ASTM TAN values
listed in Table 1. These samples have, then, the smallest
differences between the ASTM and IR TAN values.
[0061] The samples, however, whose points lie outside and to the
right of the band are considered as "outliers" in the sense that
they are not well predicted by the IR model when compared with the
ASTM values. It can be seen from Table 1 that the largest
difference between the ASTM and IR is for the K/M1 having an ASTM
TAN of S and an IR TAN of 3.2. It will be shown, in the following,
that the IR TAN values of the "outlier" samples shown in FIG. 3 are
closer to the true TAN values than those obtained using the ASTM
method.
[0062] The reason for the inaccuracy of the ASTM method is that the
potassium, added as the potassium hydroxide (KOH) titrant, replaces
part or all the calcium that is present as acid salts in the
crudes. The ASTM method utilizes potentiometic detection, which, as
practiced, does not distinguish the acid and salt titration
end-points. Consequently, the consumption of KOH in replacement of
Ca in the salts is reported as acid.
[0063] Evidence supporting the notion that the titration of organic
Ca salts is the source of the difference between the ASTM and IR
TAN is shown in FIG. 4. The Ca content of the samples (left
ordinate axis) is plotted against the ASTM TAN. The difference
(delta TAN) between the ASTM and IR TAN (right ordinate axis) is
also plotted against the ASTM TAN for the corresponding samples.
The coincidence of high Ca and delta TAN can be clearly seen.
[0064] It can be shown that 357 ppm of Ca is required to form the
salt of 1 TAN of acid. If all of the Ca in the samples is in the
form of acid salts, the ASTM method would report, for these Ca
species a TAN value of Ca(ppm)/357(ppm). The reported ASTM TAN for
a given sample would comprise the sum of its free acid and
"Ca-equivalent" TAN contributions.
[0065] FIG. 5 shows the sum of the IR and Ca-equivalent TAN on the
ordinate plotted against the ASTM TAN. The excellent agreement
supports the assertion that nearly all of the Ca is present as acid
salts and these salts are the source of the erroneously high values
of TAN reported by the ASTM method.
[0066] Blends of the B, M, and K crudes were prepared according to
the recipes given in Table 3. The ASTM and IR TAN of the blends
were calculated from the measurements on the crude components and
the blend recipes. Specific gravity data were required since the
TAN is determined on a weight basis and the blend recipes were
given on a volume fraction basis.
3TABLE 3 B, M, K, Crude Blends Field: K B M BLEND COMPONENT Zone:
Y0 M1 A1 M3 M1 M2 M3 A1 A2 M1 Specific gravity 0.941 0.941 0.941
0.941 0.934 0.934 0.934 0.934 0.934 0.908 ASTM TAN 5.28 5.47 0.05
5.38 4.28 7.13 5.88 6.25 6.24 0.51 IR TAN 3.82 4.13 0.11 3.67 3.78
6.71 5.29 5.87 5.92 0.39 1 Volume frac. 0.13 0.13 0.22 0.00 0.06
0.06 0.04 0.01 0.01 0.32 ASTM TAN 0.71 0.74 0.01 0.00 0.27 0.45
0.23 0.08 0.08 0.16 (calc.) IR TAN (calc.) 0.52 0.56 0.02 0.00 0.24
0.43 0.20 0.08 0.08 0.12 2 Volume frac. 0.16 0.16 0.21 0.04 0.05
0.05 0.02 0.01 0.01 0.32 ASTM TAN 0.83 0.87 0.01 0.19 0.19 0.32
0.14 0.04 0.04 0.16 (calc.) IR TAN (calc.) 0.60 0.66 0.02 0.13 0.17
0.31 0.13 0.04 0.04 0.12 3 Volume frac. 0.21 0.21 0.15 0.05 0.05
0.05 0.02 0.00 0.00 0.25 ASTM TAN 1.12 1.16 0.01 0.29 0.23 0.39
0.10 0.03 0.03 0.12 (calc.) IR TAN (calc.) 0.81 0.88 0.02 0.20 0.20
0.37 0.09 0.03 0.02 0.09 4 Volume frac. 0.24 0.24 0.11 0.07 0.05
0.05 0.01 0.00 0.00 0.22 ASTM TAN 1.28 1.33 0.01 0.36 0.23 0.38
0.07 0.02 0.02 0.11 (calc.) IR TAN (calc.) 0.93 1.00 0.01 0.25 0.21
0.36 0.06 0.02 0.02 0.08 5 Volume frac. 0.26 0.26 0.09 0.09 0.05
0.05 0.01 0.01 0.01 0.18 ASTM TAN 1.39 1.44 0.00 0.47 0.22 0.37
0.06 0.03 0.03 0.09 (calc.) IR TAN (calc.) 1.00 1.09 0.01 0.32 0.19
0.35 0.06 0.03 0.03 0.07 6 Volume frac. 0.27 0.27 0.08 0.11 0.06
0.06 0.01 0.00 0.00 0.15 ASTM TAN 1.43 1.48 0.00 0.57 0.23 0.39
0.05 0.00 0.00 0.08 (calc.) IR TAN (calc.) 1.04 1.12 0.01 0.39 0.21
0.37 0.05 0.00 0.00 0.06 7 Volume frac. 0.27 0.27 0.10 0.13 0.06
0.06 0.01 0.00 0.00 0.12 ASTM TAN 1.43 1.48 0.00 0.68 0.24 0.40
0.04 0.00 0.00 0.06 (calc.) IR TAN (cal) 1.03 1.12 0.01 0.46 0.21
0.38 0.04 0.00 0.00 0.04
[0067]
4TABLE 4 IR and ASTM TAN on B, M, K, Crude Blends ASTM TAN IR TAN
Blend calc. meas. calc. meas. 1 2.74 2.66 2.24 2.07 2 2.80 2.72
2.21 2.05 3 3.47 3.32 2.70 2.52 4 3.81 3.75 2.94 2.82 5 4.12 4.14
3.16 3.06 6 4.24 4.21 3.23 3.12 7 4.34 4.34 3.31 3.20
[0068] The specific gravity and volume fractions were used to
obtain target weights of the components. The ASTM and IR TAN values
for the components, shown in Table 3, were calculated from the
actual weights of the components used to make the blends. The
calculated (from the sum of the component values in Table 3) and
measured TAN for the blends are shown in Table 4 and the results
displayed in FIG. 6.
[0069] Both IR and ASTM TAN blend linearly as evidenced by the
small differences between the measured and calculated TAN of the
blends. In addition, the true TAN values of the blends, as
determined by the IR method, is significantly less than the values
obtained by the ASTM method.
[0070] The true TAN values, as determined by IR, are lower than
those obtained using the ASTM method on the same samples. The Ca in
the crude samples appear to exist almost entirely as acid salts and
account for the differences between ASTM and IR TAN measurements.
Finally, studies on crude mixtures show that TAN blends linearly
and the TAN values of the blends, determined by IR, are lower than
those obtained by ASTM.
[0071] The conclusions show that the IR TAN method may be used to
determine and report the TAN of these crudes. Commercial Fourier
Transform IR hardware has been developed that is suitable for this
application. Consequently, the IR TAN method can be implemented at
the pipeline, tanker, or refinery to control blending of the crudes
to a target TAN.
EXAMPLE 3
IR TAN Provides Accurate Quantitation of Organic Acids For Low TAN
Crudes Containing Inorganic Ca-Salts
[0072] A sample of low acid North Sea crude, Y, was determined to
have an ASTM TAN of 1.4 and an IR TAN of 0.14, a factor of 10
lower. The ASTM value was suspect due to unusually high
concentrations of Na (720 ppm) and Ca (446 ppm). If the Ca titrated
is as acid, the ASTM test will result in a reported TAN of 1.25,
due just to the Ca. When the calculated 1.25 Ca-equivalent TAN is
added to the IR TAN value of 0.14, the calculated 1.39 result is
consistent with the ASTM measured TAN of 1.4.
[0073] The crude was water-washed to remove water-soluble inorganic
salts. An analysis of the washed crude confirmed the removal of
nearly all of the Na (0.99 ppm) and Ca (0.59 ppm). A second IR
measurement was performed on the washed crude yielding the same
result (0.14) as on the original sample. A second ASTM measurement
gave <0.1, consistent with the IR TAN.
[0074] The Y crude contained mostly water-soluble inorganic salts.
Thus, with the removal of these inorganic salts, the ASTM TAN was
significantly reduced and are comparable to the IR TAN which is
unaffected by such salts.
[0075] Applications
[0076] The invention provides: the capability to accurately,
precisely and rapidly determine the TAN of crudes, blends, and
distillation fractions; the means to monitor and control the
blending and the neutralization of organic acid species in
corrosive crudes; the means of determining, monitoring, and
controlling TAN in plant laboratories, on-line in refineries and at
pipeline and transport terminals, and remotely for spot checks
at-line, such as at storage vessels. Specifically,
[0077] 1. The present invention can be used, in conjunction with
corrosion models, to select and blend raw material and process unit
feeds and products so that the TAN of the components and/or blend
meet a target value consistent with safe and economical operations
in the context of corrosion management. In a related application,
the invention can also be used to monitor the TAN of process
streams in order to maintain instantaneous and time-averaged TAN
values within a limit as determined by plant corrosion experience.
These applications are driven by the economic advantage of
maximizing the usage of higher TAN feeds that are often
lower-priced.
[0078] An example of this feed blending application is shown in
FIG. 9. Feed Tank 1 (FT 1) contains single high TAN crude, or a
blend of two or more high TAN crudes. Feed Tank 2 (FT2) contains a
single low-to-medium TAN crude, or a blend of two or more such
crudes. These Feed Tanks are connected to a mixing valve (MV) whose
output TAN (TANB) is determined at a measuring point (MP) by the
on-line IR TAN analyzer (A) embodying the present invention. TANB
is supplied to a control system (CS) along with a desired target
TAN (TANT) determined by a target model (TM) based on corrosion
experience and safety and reliability constraints. A signal from
the control system is fed back to the mixing valve to vary the
amounts of material from both feed tanks until the target TAN is
obtained (i.e., when TANT-TANB=0), thereby minimizing feed
costs.
[0079] 2. The invention can be used by supply personnel, planners,
and assay database managers to valuate candidate raw materials
(e.g. crudes) and make purchasing and pricing decisions based on
the corrosivity of such materials as inferred by their TAN. When
embodied in a transportable analyzer configuration, the invention
can provide on-the-spot evaluations of raw material TAN prior to
the commitment to purchase of large quantities.
[0080] FIG. 10 shows an example where a crude sample (S) is
collected from a storage or shipboard tank (T) and the IR spectrum
obtained by a portable FT-IR TAN analyzer (A). The TAN value, along
with other valuation parameters such as yield, sulfur and metals
content, and gravity, is provided as input to a mathematical model
(M) that calculates a range of values, in dollars per barrel, for
example, for the crude price.
[0081] As an alternative to collecting a sample, a portable
analyzer can be used with an optical probe (P), which can be
inserted into the crude. The spectrum is obtained via an optical
fiber (F) linking the analyzer to the probe. The probe heats the
sampled portion of crude so as to obtain the spectrum at the same
temperature as that of the calibration samples used to build the IR
TAN model.
[0082] 3. This invention can be used to monitor the crude TAN from
different wells within a given field or from several fields and
blend these crudes to a target TAN for transport and sale. The
monitoring and blending can be carried out on-line or at-line at
pipelines, tankers, or blending stations. It has been shown earlier
that the crude TAN blends in proportion to the TAN values weight
fraction of its components.
[0083] FIG. 11 shows the means for on-line blending of crudes
produced from 3 different wells (W1, W2, and W3) directly into a
pipeline (PL). A portion of the output from W1, W2, and W3 is
switched, on demand from the analyzer (A), by valves V1, V2, V3,
respectively, to a filter (F) which removes water and solids that
melt above the sample measurement temperature. The filtered crude
flows into the FT-IR analyzer (A), which heats the sample, and
determines its TAN (TAN1, TAN2, and TAN3) from its IR spectrum. The
main output from W1, W2, and W3 flows into a mixing valve system
(MVS), that includes means to determine the specific gravity and
volumetric flow rate of each of the flows, and that controls the
weight fraction of each to produce the blend (B), which enters the
pipeline (PL). A portion of the blend is switched, on demand from
the analyzer (A), by valve (VB), to the filter (F) and the analyzer
(A) that determines its blend TAN (TANB). The blend and target TAN
values (TANB and TANT) are transmitted to the control system (CS)
that controls the mixing valve system (MVS), according to a control
algorithm that includes well depletion and other production factors
and economics, to adjust the flows of W1, W2, and W3 to make the
difference between the blend and target TAN zero.
[0084] 4. The invention can be used to monitor and control TAN
reduction processes, such as neutralization of the corrosive
organic species. For example, a method to optimize a neutralization
process is shown in FIG. 12. In this embodiment the invention
serves as both a feed-forward and feed-back controller to optimize
the neutralization process. The hydrocarbon feed in this example
may be, but is not limited to, a whole or topped crude, and the
neutralizing agent may be, but is not limited to, an oxide,
hydroxide, or hydrate of calcium.
[0085] The target levels of organic acids for petroleum feeds and
processed fractions are currently measured by a potassium hydroxide
titration, such as ASTM D664, and reported as Total Acid Number
(TAN). Corrosion rates in process equipment are estimated from
these TAN values using corrosion model. Instantaneous or averaged
TAN limits for the feed and processed fractions are generally
established corresponding to critical corrosion rates.
[0086] TAN values obtained by such methods are unreliable when the
hydrocarbon contains oxides, hydroxides, hydrates, and salts of
certain metals, such as calcium. These species may be native to the
crude or may be present in neutralizing agents. Consequently,
existing methods cannot be used to reliably optimize neutralizing
processes without first separating these species or their reaction
products from the hydrocarbon. The model-based IR method described
below is the preferred optical absorbance method to be used in this
invention. It is selective to acids, insensitive to acid type and
interactions with other constituents in the untreated or treated
feed, can be implemented on-line, and is sufficiently rapid to
enable process control and optimization.
[0087] The invention may be described with reference to FIG. 12. In
this embodiment the invention serves as both a feed-forward and a
feed-back controller to optimize the neutralization process. The
hydrocarbon feed in this example may be, but is not limited to, a
whole or topped crude, and the neutralizing agent may be, but is
not limited to, an oxide, hydroxide, or hydrate of calcium.
[0088] An infrared spectrum of the feed is measure at point A prior
to its entering the mixing valve through which water (desalter
water) is typically added for desalting. The spectrum signal is
input to the IR TAN and/or corrosion rate model from which a TAN
value and/or corrosion rate, respectively, for the feed is
predicted. The TAN/corrosion rate value is compared with the
relevant feed TAN and/or corrosion rate control limit values in the
analyzer and a feed rate of neutralizing agent is estimated by the
analyzer. The process controller sets the neutralizing agent
control valve to provide this initial feed of neutralizing agent to
the mixing valve. The feed/neutralizing agent/desalter water
mixture is introduced into the desalter. The temperature, pressure,
and residence time of the mixture in the desalter are such as to
both effectively reduce the salt and water content of the mixture
and to neutralize the acid to the targeted value of TAN and/or
corrosion rate.
[0089] An IR spectrum of the treated feed is obtained, at point B,
upon its emergence from the desalter. The spectrum signal is used
with the relevant prediction model to estimate the TAN and/or
corrosion rate of the treated feed. The difference between the
predicted and target values of the TAN and/or corrosion rate value
is used by the process controller to correct the setting of the
neutralizing agent control valve so as to achieve the target value.
The entire feed-forward and feed-back process control sequence can
be repeated to provide, on-line optimization of the neutralization
process.
[0090] If the control limit (sidestream TAN and/or corrosion rate
control limit) is determined based upon the TAN and/or corrosion
rate caused by a sidestream or fraction of a processing unit, such
as single or multiple stage pipestill rather than feed TAN and/or
corrosion rate, infrared spectrum needs to be acquired of the
limiting sidestream, shown as point C, for example. Alternatively,
and more preferably the sidestream TAN and/or corrosion rate can be
predicted from a measurement of the untreated and treated feed. By
obvious extension, other or additional points in the processing
equipment, such as the furnace outlet can similarly be monitored
and provide relevant control limits.
* * * * *