U.S. patent application number 14/068068 was filed with the patent office on 2017-07-20 for compounds and methods for inhibiting corrosion in hydrocarbon processing units.
This patent application is currently assigned to General Electric Company. The applicant listed for this patent is General Electric Company. Invention is credited to Rebika Mayanglambam Devi, Rhomit Ghosh, Manish Joshi, Sathees Kesavan, Muthukumar Nagu, Nimeshkumar Kantilal Patel, Ashok Shankar Shetty, Alagarsamy Subbiah.
Application Number | 20170204339 14/068068 |
Document ID | / |
Family ID | 49547823 |
Filed Date | 2017-07-20 |
United States Patent
Application |
20170204339 |
Kind Code |
A9 |
Subbiah; Alagarsamy ; et
al. |
July 20, 2017 |
COMPOUNDS AND METHODS FOR INHIBITING CORROSION IN HYDROCARBON
PROCESSING UNITS
Abstract
Treatment compositions for neutralizing acidic species and
reducing hydrochloride and amine salts in a fluid hydrocarbon
stream are disclosed. The treatment compositions may comprise at
least one amine with a salt precipitation potential index of equal
to or less than about 1.0. Methods for neutralizing acidic species
and reducing deposits of hydrochloride and amine salts in a
hydrocarbon refining process are also disclosed. The methods may
comprise providing a fluid hydrocarbon stream and adding a
treatment composition to the fluid hydrocarbon stream. The
treatment compositions used may have a salt precipitation potential
index of equal to or less than about 1.0 and comprise either
water-soluble or oil-soluble amines.
Inventors: |
Subbiah; Alagarsamy;
(Bangalore, IN) ; Devi; Rebika Mayanglambam;
(Bangalore, IN) ; Patel; Nimeshkumar Kantilal;
(The Woodlands, TX) ; Nagu; Muthukumar;
(Bangalore, IN) ; Ghosh; Rhomit; (Kolkata, IN)
; Kesavan; Sathees; (Bangalore, IN) ; Shetty;
Ashok Shankar; (Trevose, PA) ; Joshi; Manish;
(Bangalore, IN) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
General Electric Company |
Schenectady |
NY |
US |
|
|
Assignee: |
General Electric Company
Schenectady
NY
|
Prior
Publication: |
|
Document Identifier |
Publication Date |
|
US 20150114884 A1 |
April 30, 2015 |
|
|
Family ID: |
49547823 |
Appl. No.: |
14/068068 |
Filed: |
October 31, 2013 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
|
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13468638 |
May 10, 2012 |
9493715 |
|
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14068068 |
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Current U.S.
Class: |
1/1 |
Current CPC
Class: |
C07C 211/11 20130101;
C10G 2300/4075 20130101; C10G 21/20 20130101; C10G 19/02 20130101;
C07C 211/10 20130101; C10G 19/00 20130101; C07C 211/03 20130101;
C07C 211/34 20130101; C10G 7/10 20130101; C10G 2300/44 20130101;
C10G 75/00 20130101; C10G 2300/80 20130101; C07C 211/09 20130101;
C10G 19/073 20130101; C10G 75/02 20130101; C10G 29/20 20130101;
C10G 75/04 20130101 |
International
Class: |
C10G 21/20 20060101
C10G021/20 |
Claims
1. A treatment composition for neutralizing acidic species and
reducing hydrochloride and amine salts in a fluid hydrocarbon
stream, said treatment composition comprising at least one amine
selected from the group consisting of, 1,2 dimethylpropylamine,
1,4-dimethylpiperazine, N-methyldibutylamine,
N-methyldipropylamine, ethylhexylamine, N-methylpyrrolidine,
di-ethylhydroxylamine, dimethylcyclohexylamine,
diethylpropargylamine, dimethyl-N-propylamine, di-N-propylamine,
N,N,N',N'-tetramethylethylenediamine (TMED), N-methyl piperidine,
2-dimethylamino 2-methyl 1-propanol (DMAMP),
N,N,N',N'-tetramethyldiaminomethane (TMMD), dimethyl tertiary
butanolamine (DMTBA), dimethyl methoxypropylamine (DMMOPA),
furfurylamine, and combinations thereof; and wherein said amine has
a salt precipitation potential index of equal to or less than about
1.0.
2. A method for neutralizing acidic species and reducing deposits
of hydrochloride and amine salts in a hydrocarbon stream comprising
contacting said fluid hydrocarbon stream with a treatment
composition, said treatment composition comprising at least one
amine with a salt precipitation potential index of equal to or less
than about 1.0.
3. The method of claim 2, wherein at least one of said amines is
selected from the group consisting of, 1,2 dimethylpropylamine,
1,4-dimethylpiperazine, N-methyldibutylamine,
N-methyldipropylamine, ethylhexylamine, N-methylpyrrolidine,
di-ethylhydroxylamine, dimethylcyclohexylamine,
diethylpropargylamine, dimethyl-N-propylamine, di-N-propylamine,
N,N,N',N'-tetramethylethylenediamine (TMED), N-methyl piperidine,
2-dimethylamino 2-methyl 1-propanol (DMAMP),
N,N,N',N'-tetramethyldiaminomethane (TMMD), dimethyl tertiary
butanolamine (DMTBA), dimethyl methoxypropylamine (DMMOPA),
furfurylamine, and combinations thereof.
4. The method of claim 2, wherein said amine has a pKa equal to or
greater than about 5.0.
5. The method of claim 2, wherein said amine has a salt
precipitation potential index of equal to or less than about
0.5.
6. The method of claim 2, wherein said treatment composition is
added to said fluid hydrocarbon stream in an amount ranging from
about 0.1 to about 1000 ppm by volume of said fluid hydrocarbon
stream.
7. The method of claim 2, wherein a molar ratio of said treatment
composition to any HCl present in said hydrocarbon stream ranges
from about 1:1 to about 5:1.
8. The method of claim 2, wherein said treatment composition
comprises at least one water soluble amine.
9. The method of claim 8, wherein said water-soluble amine is
selected from the group consisting of 1,2 dimethylpropylamine,
1,4-dimethylpiperazine, N-methylpyrrolidine, di-ethylhydroxylamine,
dimethyl-N-propylamine, N,N,N',N'-tetramethylethylenediamine
(TMED), 2-dimethylamino 2-methyl 1-propanol, N-methyl piperidine,
N,N,N',N'-tetramethyldiaminomethane (TMMD), dimethyl tertiary
butanolamine (DMTBA), dimethyl methoxypropylamine (DMMOPA),
furfurylamine, and combinations thereof.
10. The method of claim 9, wherein said treatment composition is
added to said fluid hydrocarbon stream after said fluid hydrocarbon
stream leaves a distillation tower of a hydrocarbon refining
process.
11. The method of claim 2, wherein said treatment composition
comprises at least one oil soluble amine.
12. The method of claim 11, wherein said oil-soluble amine is
selected from the group consisting of N-methyldibutylamine,
N-methyldipropylamine, ethylhexylamine, dimethylcyclohexylamine,
di-ethylpropargylamine, di-N-propylamine, and combinations
thereof.
13. The method of 12, wherein said treatment composition is added
to said fluid hydrocarbon stream after said fluid hydrocarbon
stream leaves a desalter of a hydrocarbon refining process.
14. A method for neutralizing acidic species and reducing deposits
of hydrochloride and amine salts in a hydrocarbon refining process
comprising: (a) contacting a fluid hydrocarbon stream present in
said refining process with a first treatment composition after said
fluid hydrocarbon stream leaves a desalter of said hydrocarbon
refining process, said first treatment composition comprising at
least one oil-soluble amine with a salt precipitation potential
index of equal to or less than about 1.0; and (b) adding a second
treatment composition to said fluid hydrocarbon stream after said
fluid hydrocarbon stream leaves a distillation tower of said
hydrocarbon refining process, said second treatment composition
comprising at least one water-soluble amine with a salt
precipitation potential index of equal to or less than about
1.0.
15. The method of claim 14, wherein at least one water-soluble
amine is a member selected from the group consisting of 1,2
dimethylpropylamine, 1,4-dimethylpiperazine, N-methylpyrrolidine,
di-ethylhydroxylamine, dimethyl-N-propylamine,
N,N,N',N'-tetramethylethylenediamine (TMED), 2-dimethylamino
2-methyl 1-propanol (DMAMP), N-methyl piperidine,
N,N,N',N'-tetramethyldiaminomethane (TMMD), dimethyl tertiary
butanolamine (DMTBA), dimethyl methoxypropylamine (DMMOPA),
furfurylamine, and combinations thereof.
16. The method in claim 15, wherein the neutralizing acid species
comprises 1,4-dimethylpiperazine and/or N-methylpyrrolidine.
17. The method of claim 14, wherein at least one oil-soluble amine
is a member selected from the group consisting of
N-methyldibutylamine, N-methyldipropylamine, ethylhexylamine,
dimethylcyclohexylamine, di-ethylpropargylamine, di-N-propylamine,
and combinations thereof.
18. The method of claim 14, wherein at least one water-soluble
amine has a pKa equal to or greater than about 5.0.
19. The method of claim 14, wherein at least one oil-soluble amine
has a pKa equal to or greater than about 5.0.
20. The method of claim 14, wherein at least one water-soluble
amine has a salt precipitation potential index of equal to or less
than about 0.5.
21. The method of claim 14, wherein at least one oil-soluble amine
has a salt precipitation potential index of equal to or less than
about 0.5.
Description
FIELD OF THE INVENTION
[0001] The present invention relates to the refinery processing of
crude oil. Specifically, it is directed towards the problem of
corrosion of refinery equipment caused by corrosive elements found
in the crude oil.
CROSS REFERENCE TO RELATED APPLICATION
[0002] The present application is a continuation in part of U.S.
patent application Ser. No. 13/468,638, filed May 10, 2012 titled
COMPOUNDS AND METHODS FOR INHIBITING CORROSION IN HYDROCARBON
PROCESSING UNITS, and herein incorporated by reference.
BACKGROUND OF THE INVENTION
[0003] Hydrocarbon feedstocks such as petroleum crudes, gas oil,
etc., are subjected to various processes in order to isolate and
separate different fractions of the feed stock. In refinery
processes, the feedstock is distilled so as to provide light
hydrocarbons, gasoline, naphtha, kerosene, gas oil, etc.
[0004] The lower, boiling fractions are recovered as an overhead
fraction from the distillation tower. The intermediate components
are recovered as side cuts from the distillation tower. The
fractions are cooled, condensed, and sent to collecting equipment.
No matter what type of petroleum feed stock is used as the charge,
the distillation equipment is subjected to the corrosive activity
of acids such as H.sub.2S, HCl, organic acids, and
H.sub.2CO.sub.3.
[0005] Corrosion in the crude overhead distillation equipment is
mainly due to condensation of hydrogen chlorides formed by
hydrolysis of the magnesium chloride and calcium chloride in crude
oil. Typical hydrolysis reactions may proceed as in Equations I or
II:
MgCl.sub.2+2H.sub.2O2HCl+Mg(OH).sub.2 (I)
CaCl.sub.2+2H.sub.2O2HCl+Ca(OH).sub.2 (II)
[0006] Corrosive attack on the metals normally used in the low
temperature sections of a refinery (i.e., where water is present
below its dew point) is an electrochemical reaction generally in
the form of acid attack on active metals in accordance with
Equations III, IV or V:
At the anode: FeFe.sup.+++2e.sup.- (III)
At the cathode: 2H.sup.++2e.sup.-2H (IV)
At the cathode: 2HH.sub.2 (V)
[0007] The aqueous phase may be water entrained in the hydrocarbons
being processed and/or water added to the process for such purposes
as steam stripping. These waters, regardless of source, are
collectively referred to as brines. Acidity of the condensed water
is due to dissolved acids in the condensate, principally HCl,
organic acids, H.sub.2S, and H.sub.2CO.sub.3. HCl, the most
troublesome corrosive material, is formed by hydrolysis of calcium
and magnesium chlorides originally present in the brines.
[0008] One of the chief points of difficulty with respect to
corrosion occurs above and in the temperature range of the initial
condensation of water. The term "initial condensate" as it is used
herein signifies a phase formed when the temperature of the
surrounding environments reaches the dew point of water. At this
point a mixture of liquid water, hydrocarbon, and vapor may be
present. Such initial condensate may occur within the distillation
tower itself or in subsequent condensers. The top temperature of
the distillation tower is normally maintained above the dew point
of water. The initial aqueous condensate formed contains a high
percentage of HCl. Due to the high concentration of acids dissolved
in the water, the pH of the first condensate is quite low. For this
reason, the water is highly corrosive.
[0009] In the past, highly basic ammonia has been added at various
points in hydrocarbon refining processes in an attempt to control
the corrosiveness of condensed acidic materials Ammonia, however,
has not proven effective with respect to eliminating corrosion
occurring at the initial condensate. It is believed that ammonia
has been ineffective for this purpose because it does not condense
completely enough to neutralize the acidic components of the first
condensate.
[0010] Several amines, including morpholine and methoxypropylamine,
have been used to successfully control or inhibit corrosion that
ordinarily occurs at the point of initial condensation within or
after the distillation tower. These amines or their blends are
added in pure form or as an aqueous solution. The high alkalinity
of these amines serves to raise the pH of the initial condensate
rendering it less corrosive. The amines are added in amounts
sufficient to raise the pH of the liquid at the point of initial
condensation to above 4.0, and in some cases, to between 5.0 and
6.0.
[0011] These amines, however, form hydrochloride salts that deposit
on the inner surfaces of hydrocarbon refining equipment. These
deposits can cause both fouling and corrosion problems and are most
problematic in units that do not use a water wash.
[0012] Some amines and their blends currently used produce less
salt deposits on hydrocarbon refining equipment than the amines
listed above. These amines are also aqueous amines and are
introduced in the distillation tower or downstream of the
distillation tower. These amines include picoline (U.S. Pat. No.
5,211,840) and blends comprising dimethylethanolamine and
dimethylisopropanolamine, (U.S. Pat. No. 4,490,275)
ethylenediamine, monoethanolamine and hexylmethylenediamine (U.S.
Pat. No. 7,381,319). Additional amines include trimethylamine and
N-methylmorpholine and their blends.
BRIEF DESCRIPTION OF THE INVENTION
[0013] It was surprisingly discovered that some amines are more
effective at neutralizing the acidic species in hydrocarbon streams
than ammonia. It was also surprisingly discovered that other amines
are more effective than the comparative amines, trimethylamine and
N-methylmorpholine. These effective amines also are effective at
reducing deposits of amine salt species on the internal surfaces of
hydrocarbon processing equipment.
[0014] Accordingly, a treatment composition is disclosed for
neutralizing acidic species and reducing hydrochloride and amine
salts in a fluid hydrocarbon stream. The treatment composition may
comprise at least one amine with a salt precipitation potential
index ("Salt PPI") of equal to or less than about 1.0. The fluid
hydrocarbon stream may comprise an aqueous portion, or brine. Both
the hydrocarbon stream and any aqueous portion present in the fluid
hydrocarbon stream may be in a liquid phase, a vapor phase, or a
combination thereof.
[0015] Suitable amines include, but are not limited to, 1,2
dimethylpropylamine, 1,4-dimethylpiperazine, N-methyldibutylamine,
N-methyldipropylamine, ethylhexylamine, N-methylpyrrolidine,
di-ethylhydroxylamine, dimethylcyclohexylamine,
diethylpropargylamine, dimethyl-N-propylamine, di-N-propylamine,
N,N,N',N'-tetramethylethylenediamine (TMED), N-methylpiperidine,
2-dimethylamino 2-methyl 1-propanol (DMAMP),
N,N,N',N'-tetramethyldiaminomethane (TMMD), dimethyl tertiary
butanolamine (DMTBA), dimethyl methoxypropylamine (DMMOPA),
furfurylamine, and combinations thereof.
[0016] In another exemplary embodiment, a method for neutralizing
acidic species and reducing hydrochloride and amine salts in a
hydrocarbon stream is disclosed. The method may comprise contacting
a fluid hydrocarbon stream with a treatment composition. The
treatment composition may comprise at least one amine with a Salt
PPI of equal to or less than about 1.0.
[0017] In yet another exemplary embodiment, a method for
neutralizing acidic species and reducing deposits of hydrochloride
and amine salts in a hydrocarbon refining process is disclosed. The
method comprises contacting a fluid hydrocarbon stream present in
the refining process with a first treatment composition after the
fluid hydrocarbon stream leaves the desalter. The first treatment
composition may comprise at least one oil-soluble amine. A second
treatment composition with at least one water-soluble amine may be
added to the fluid hydrocarbon stream as it leaves the distillation
tower. Both the first and second treatment compositions may
comprise at least one amine with a Salt PPI of equal to or less
than about 1.0.
BRIEF DESCRIPTION OF THE DRAWINGS
[0018] FIG. 1 shows a simplified section of a hydrocarbon refining
process; and
[0019] FIG. 2 shows a graph of amines and their salt precipitation
potential indices.
DETAILED DESCRIPTION OF EXEMPLARY EMBODIMENTS
[0020] FIG. 1 (FIG. 1) shows a simplified section of a hydrocarbon
refining process. Crude (1) is fed through a series of heat
exchangers (3) before entering at least one desalter (5). Desalted
crude (7) enters another series of heat exchangers (9) where it is
preheated to about 200 to 700.degree. F. before entering a flash
drum (11), or preflash tower. The lights (13) from the flash drum
may be fed directly to the distillation tower (15). The bottoms
(17) from the flash drum may be fed to a direct-fired furnace (19)
before they are fed to the distillation tower (15). The
distillation tower is often called an atmospheric tower as it
operates slightly above atmospheric pressure, typically around 1 to
3 atmospheres gauge.
[0021] The overhead distillation tower temperature usually ranges
from 200 to 350.degree. F. While in the tower, the crude is
distilled into multiple fractions, also called "sidecuts". The
sidecuts comprise heavy gas oil (21), light gas oil (23), diesel
(25), and kerosene (27). The bottoms (37) exit the distillation
tower for processing elsewhere (not shown). Naphtha vapor (29)
exits the top of the distillation tower and enters a series of heat
exchangers (31). The naphtha vapor then enters at least one
condenser (33). A portion of the condensed naphtha stream is fed
back into the top of the tower as reflux (35).
[0022] Some refining processes may not utilize a flash drum and
instead feed crude directly to a direct-fired furnace. Likewise
some operations have been omitted from FIG. 1 for the sake of
brevity. These and other minor differences in crude refining
processes do not affect the scope of the invention.
[0023] It was surprisingly discovered that some amines are more
effective at neutralizing the acidic species in hydrocarbon streams
than ammonia. It was also surprisingly discovered that other amines
are more effective than the comparative amines, trimethylamine and
N-methylmorpholine. These effective amines are also effective at
reducing deposits of amine salt species on the internal surfaces of
hydrocarbon processing equipment.
[0024] Without limiting this specification to any particular theory
of operation, the overall efficiency of a given amine may be
predicted upon assessment of several factors. One such factor is
the amine-HCl salt precipitation potential index ("Salt PPI"). The
Salt PPI may also be known by those in the art as the salt
volatility index. These indices are merely a comparison of the
precipitation potential of the amine salt to the salt of a typical
neutralizing compound used in hydrocarbon refining, ammonia.
[0025] Salt PPI may be calculated from the equation:
[ p 225 .degree. F ( NH 4 Cl ) p 225 .degree. F ( Amine Cl ) ] + [
p 300 .degree. F ( NH 4 Cl ) p 300 .degree. F ( Amine Cl ) ] 2
##EQU00001##
where p is the vapor pressure at either 225 or 300.degree. F. The
average Salt PPI over the 225 to 300.degree. F. range is selected
because these amines usually have the requisite volatility
characteristics at typical crude overhead operating temperatures.
Namely, such amines are thermally stable at temperatures typical to
the refining process, yet volatile enough to condense with the
initial condensate. As can be seen from the equation, the salt of
the typical neutralizing compound, ammonia, is used as a benchmark.
If one were to substitute the vapor pressure of ammonia for the
vapor pressure of the amine in the equation, the Salt PPI would be
1.0. Effective amines are those that are as good, if not better
than the typical additive, ammonia. Thus, effective amines would
have a Salt PPI of equal to or less than 1.0. Other neutralizers
commonly used in hydrocarbon refining are trimethylamine and
N-methylmorpholine. The Salt PPI of these comparative amines is
equal to, or greater than 0.1. Thus, the most effective amines
would have a Salt PPI of equal to, or less than 0.1. FIG. 2 shows a
graph of amines and their salt precipitation potential indices.
[0026] Accordingly, a treatment composition is disclosed for
neutralizing acidic species and reducing hydrochloride and amine
salts in a fluid hydrocarbon stream. The treatment composition
comprises at least one amine with a salt precipitation potential
index of equal to or less than about 1.0.
[0027] The fluid hydrocarbon stream may comprise an aqueous
portion, or brine. Both the hydrocarbon stream and any aqueous
portion present in the fluid hydrocarbon stream may be in a liquid
phase, a vapor phase, or a combination thereof. Examples of fluid
hydrocarbons include, but are not limited to, crude oil, natural
gas, condensate, heavy oil, processed residual oil, bitumen, coker
oils, coker gas oils, fluid catalytic cracker feeds and slurries,
gas oil, naphtha, diesel fuel, fuel oil, jet fuel, gasoline,
kerosene, crude styrene distillation tower feed, crude ethylbenzene
column feed, pyrolsis gasoline, chlorinated hydrocarbons feed, or
vacuum residual.
[0028] In one exemplary embodiment, at least one amine may have the
structure:
##STR00001##
where R.sub.1, R.sub.2, and R.sub.3 may the same or different and
are H, or alkyls of 1 to 20 carbon atoms. The alkyls may be
straight alkyls, branched alkyls, cycloalkyl rings,
hydroxyl-substituted alkyls, or alkoxy-substituted alkyls. Said
alkyls may be unsaturated. Additionally R.sub.1 and R.sub.2 may be
interconnected by carbon or a combination of carbon and other atoms
such as oxygen to form a nitrogen containing heterocyclic ring.
[0029] Suitable amines include, but are not limited to, acyclic
N-alkylated alkoxy/alkanol tertiary amines which may include
acyclic N-alkylated alkoxy/alkanol tertiary polyamines; cyclic
amines which may include cyclic N-alkylated amines or cyclic
N-alkylated tertiary polyamines or cyclic N-alkylated tertiary
amines; acyclic N-alkylated tertiary amines which may include
acyclic N,N'-alkylated tertiary polyamines; or combinations
thereof. In another embodiment, the acyclic N-alkylated
alkoxy/alkanol tertiary amine may be an acyclic N-dimethylated
alkoxy/alkanol tertiary monoamine. Amines that are exemplary of
this class include 2-dimethylamino 2-methyl 1-propanol (DMAMP),
dimethyl tertiary butanolamine (DMTBA), and dimethyl
methoxypropylamine (DMMOPA). In another embodiment, the cyclic
amine may be a cyclic N-alkylated tertiary polyamine. The cyclic
N-alkylated tertiary amine may be a cyclic N-methylated tertiary
monoamine or diamine. Amines that are exemplary of this class may
have five or six-membered rings and include 1,4-dimethylpiperazine,
N-methylpyrrolidine, and N-methyl piperidine. In yet another
embodiment, the acyclic N,N'-alkylated tertiary amine may be an
acyclic N,N'-polymethylated tertiary diamine. Amines that are
exemplary of this class include
N,N,N',N'-tetramethylethylenediamine (TMED) and
N,N,N',N'-tetramethyldiaminomethane (TMMD). In another embodiment
the R.sub.1 may be a non-carbon atom for example an oxygen as in
the case of an N,N-dialkyl-hydroxylamine.
[0030] In another embodiment, the treatment composition may
comprise at least one amine selected from the group consisting of
1,2 dimethylpropylamine, 1,4-dimethylpiperazine,
N-methyldibutylamine, N-methyldipropylamine, ethylhexylamine,
N-methylpyrrolidine, di-ethylhydroxylamine,
dimethylcyclohexylamine, diethylpropargylamine,
dimethyl-N-propylamine, di-N-propylamine,
N,N,N',N'-tetramethylethylenediamine (TMED), N-methylpiperidine,
2-dimethylamino 2-methyl 1-propanol (DMAMP),
N,N,N',N'-tetramethyldiaminomethane (TMMD), dimethyl tertiary
butanolamine (DMTBA), dimethyl methoxypropylamine (DMMOPA),
furfurylamine, and combinations thereof.
[0031] Another factor indicative of the overall efficiency of a
given amine is the logarithm of the acid dissociation constant,
pKa. Generally, amines with higher pKa values are more efficient
neutralizers. Accordingly, in another embodiment, the treatment
composition may comprise an amine with a pKa equal to or greater
than about 5.0.
[0032] In yet another embodiment, the treatment composition may
comprise an amine with a salt precipitation potential index of
equal to or less than about 0.5. Alternatively, amines may have a
salt precipitation potential index of equal to or less than about
0.1.
[0033] In another exemplary embodiment, a method for neutralizing
acidic species and reducing deposits of hydrochloride and amine
salts in a hydrocarbon stream is disclosed. The method may comprise
contacting a fluid hydrocarbon stream with a treatment composition
comprising at least one amine with a Salt PPI of equal to or less
than about 1.0. The at least one amine may have the structure as
described above.
[0034] In another method, the treatment composition may comprise at
least one acyclic N-alkylated alkoxy/alkanol tertiary amine,
acyclic N-alkylated alkoxy/alkanol tertiary polyamine, cyclic amine
such as cyclic N-alkylated tertiary amine or cyclic N-alkylated
tertiary polyamine, acyclic N,N'-alkylated tertiary polyamine, or
combinations thereof. In another embodiment, the acyclic
N-alkylated alkoxy/alkanol tertiary amine may be an acyclic
N-dimethylated alkoxy/alkanol tertiary monoamine. The cyclic amine
may include cyclic N-alkylated amines, cyclic N-alkylated tertiary
polyamines, or cyclic N-alkylated tertiary amines. In one
embodiment, the cyclic N-alkylated amine may be a cyclic
N-methylated tertiary monoamine or diamine. In yet another
embodiment, the acyclic N,N'-alkylated tertiary amine may be an
acyclic N,N'-polymethylated tertiary diamine.
[0035] In another method, the treatment composition may comprise at
least one amine selected from the group consisting of 1,2
dimethylpropylamine, 1,4-dimethylpiperazine, N-methyldibutylamine,
N-methyldipropylamine, ethylhexylamine, N-methylpyrrolidine,
di-ethylhydroxylamine, dimethylcyclohexylamine,
diethylpropargylamine, dimethyl-N-propylamine, di-N-propylamine,
N,N,N',N'-tetramethylethylenediamine (TMED), N-methyl piperidine,
2-dimethylamino 2-methyl 1-propanol (DMAMP),
N,N,N',N'-tetramethyldiaminomethane (TMMD), dimethyl tertiary
butanolamine (DMTBA), dimethyl methoxypropylamine (DMMOPA),
furfurylamine, and combinations thereof.
[0036] In another method, the treatment composition may comprise an
amine with a pKa equal to or greater than about 5.0. In yet another
method, the treatment composition may comprise an amine with a Salt
PPI of equal to or less than about 0.5. Alternatively, the amine
may have a Salt PPI of equal to or less than about 0.1.
[0037] In one embodiment, a method for neutralizing acidic species
and reducing deposits of hydrochloride and amine salts in a
hydrocarbon stream is disclosed, wherein the treatment composition
may be added to the fluid hydrocarbon stream in an amount ranging
from about 1 ppm to about 1000 ppm by volume of the fluid
hydrocarbon stream. In another method, the treatment composition
may be added at 300 ppm to 900 ppm by volume of the fluid
hydrocarbon stream. Alternatively, the treatment composition may be
added at about 300 ppm to about 700 ppm.
[0038] The above ranges may vary with application, source of the
hydrocarbon stream, and the corrosive species present. The fluid
hydrocarbon stream, for example, may be a stream that exits the
desalter in a hydrocarbon refining process. The fluid hydrocarbon
stream may also be a stream that exits the distillation tower
(fluid overhead stream) of a hydrocarbon refining process. In the
case of the hydrocarbon stream being a stream that exits the
distillation tower, the hydrocarbon stream can contain up to 10%
brine, such as 0.1% to 10% brine by volume. HCl may be present at
about 0.1 ppm to about 2000 ppm by volume relative to the brine and
at about 0.1 ppm to about 200 ppm by volume relative to the
hydrocarbon stream. The molar ratio of the treatment composition to
HCl present in the fluid hydrocarbon stream may range from about
1:1 to about 5:1. Alternatively, the molar ratio may be about
1:1-1.3:1. In one embodiment, the treatment composition may be
added at about 0.1 to about 1000 ppm by volume of the fluid
hydrocarbon stream as it exits the distillation tower. In yet
another embodiment, the treatment composition may be added at about
0.1 to about 200 ppm by volume of the fluid hydrocarbon stream as
it exits the distillation tower. These ranges are effective even if
other corrosive species, such as H.sub.2S, are present in the
hydrocarbon stream.
[0039] It was also surprisingly discovered that the effectiveness
of some amines may be increased by selecting the addition point in
the hydrocarbon refining process. It was also surprisingly
discovered that there was a correlation between the addition point
and the amine's solubility in oil or water. The effectiveness of
oil-soluble amines may be increased by adding them to the fluid
hydrocarbon stream as it leaves the desalter. The effectiveness of
water-soluble amines may be increased by adding them to the fluid
hydrocarbon stream as it leaves the distillation tower.
[0040] Accordingly, another exemplary embodiment discloses a method
where the treatment composition comprises at least one water
soluble amine. In another embodiment, the treatment composition is
added to a fluid hydrocarbon stream after it leaves the
distillation tower of a hydrocarbon refining process (FIG. 1,
B).
[0041] Another exemplary embodiment discloses a method where the
treatment composition comprises at least one oil soluble amine. In
another embodiment, the treatment composition is added to a fluid
hydrocarbon stream after it leaves the desalter of a hydrocarbon
refining process (FIG. 1, A).
[0042] In yet another exemplary embodiment, a method for
neutralizing acidic species and reducing deposits of hydrochloride
and amine salts in a hydrocarbon refining process is disclosed. The
method comprises contacting a fluid hydrocarbon stream present in
the refining process with a first treatment composition after the
fluid hydrocarbon stream leaves the desalter. The first treatment
composition may comprise at least one oil-soluble amine. A second
treatment composition with at least one water-soluble amine may be
added to the fluid hydrocarbon stream as it leaves the distillation
tower. Both the first and second treatment compositions may
comprise at least one amine with a Salt PPI of equal to or less
than about 1.0.
[0043] Another exemplary embodiment discloses a method wherein at
least one water-soluble amine is a member selected from the group
consisting of 1,2 dimethyl propylamine, 1,4-dimethylpiperazine,
N-methylpyrrolidine, di-ethylhydroxylamine, dimethyl-N-propylamine,
N,N,N',N'-tetramethylethylenediamine, 2-dimethylamino 2-methyl
1-propanol, N-methyl piperidine,
N,N,N',N'-tetramethyldiaminomethane (TMMD), dimethyl tertiary
butanolamine (DMTBA), dimethyl methoxypropylamine (DMMOPA), and
furfurylamine. Yet another method discloses a method wherein at
least one oil-soluble amine is a member selected from the group
consisting of N-methyldibutylamine, N-methyldipropylamine,
ethylhexylamine, dimethylcyclohexylamine, diethylpropargylamine,
and di-N-propylamine.
[0044] Other embodiments disclose methods wherein at least one
water-soluble or oil-soluble amine may have a pKa of equal to or
greater than about 5.0. Yet other embodiments disclose methods
wherein at least one water-soluble or oil-soluble amine may have a
Salt PPI of equal to or less than about 0.5. Alternatively, the
Salt PPI may be equal to or less than about 0.1.
Examples
[0045] Several amines were tested to determine their efficiencies
in neutralizing acidic species and reducing deposits of
hydrochloride and amine salts. The neutralization efficiency of
these amines was tested using two-phase titration. For each amine
tested, a titrand (100 ml) was placed in a flask. The titrand was
designed to simulate an initial condensate and comprised 90 vol %
naphtha and 10 vol % acidic water. The titrand was heated to
100.degree. C. and maintained at that temperature while amine
titrant was added to the flask. The resulting pH at different amine
titrant concentrations are summarized in Table 1.
[0046] As shown in Table 1, all of the amines have a pKa greater
than 5.0. Also shown in Table 1, all of the effective amines have a
lower Salt PPI than the ammonia benchmark of 1.0. Other effective
amines have a Salt PPI equal to, or lower than at least one of the
comparative amines.
TABLE-US-00001 TABLE 1 Solubility Salt Neutral. Efficiency pH at
Amines Oil/Water pKa PPI 250 ppm 500 ppm 1000 ppm Effective Amines
Salt PPI less than ammonia benchmark di-N-propyl amine Oil 10.91
0.24 2.2 3.0 7.6 N,N,N',N'- Water 8.97 0.27 4.7 6.7 8.3
tetramethylethylenediamine (TMED) Furfurylamine Water 8.89 0.38 2.6
6.5 8.5 Comparative Amines Trimethylamine (TMA) Water 9.76 0.10 2.6
8.0 8.8 N-methylmorpholine (NMM) Water 7.10 0.18 2.4 5.4 6.8
Effective Amines Salt PPI less than at least one comparative amine
1,2 Dimethyl propyl amine Water 9.90 <0.1 1.4 8.5 9.6
1,4-dimethylpiperazine Water 8.20 <0.1 3.7 5.5 7.6
N-methyldibutylamine Oil 10.31 <0.1 1.9 2.0 5.0
N-methyldipropylamine Oil 10.09 <0.1 2.4 2.8 5.6 Ethyhexylamine
Oil 9.0 <0.1 2.2 2.7 5.3 N-methylpyrrolidine Water 10.32 <0.1
2.2 6.8 8.1 Diethylhydroxylamine Water 5.61 <0.1 2.4 4.1 5.0
Dimethylcyclohexylamine Oil 10.00 0.10 1.8 1.9 5.2
Diethylpropargylamine Oil 7.70 0.12 2.2 3.6 5.9
[0047] A second set of tests were performed using some of the
effective amines above. Additional tertiary amines were also tested
and found to be effective. The additional tertiary amines were
N-methyl piperidine, 2-dimethylamino 2-methyl 1-propanol ("DMAMP")
in an azeotropic solution comprising 80 wt % amine,
N,N,N',N'-tetramethyldiamino methane ("TMMD"), dimethyl tertiary
butanolamine ("DMTBA"), and dimethyl methoxypropylamine ("DMMOPA").
The neutralization efficiency of these amines was tested using
two-phase titration. For each amine tested, a titrand (100 ml) was
placed in a flask. The titrand was designed to simulate an initial
condensate and comprised 90 vol % naphtha and 10 vol % acidic
water. The titrand was heated to 100.degree. C. and maintained at
that temperature while amine titrant was added to the flask. The
tests were repeated 3 times in the second set of tests. The
resulting pH at different amine titrant concentrations are
summarized in Table 2. The data in Table 2 are the averages of the
3 repeated tests.
[0048] As shown in Table 2, all of the amines have a pKa greater
than 5.0. Also shown in Table 2, all of the effective amines have a
lower Salt PPI than the ammonia benchmark of 1.0.
TABLE-US-00002 TABLE 2 Neutral. Efficiency pH at Boiling Solubility
Salt 250 500 1000 Point Amines Oil/Water pKa PPI ppm ppm ppm
.degree. C. Comparative Amines Trimethylamine (TMA) Water 9.76 0.10
2.6 8.0 8.8 2.87 N-methylmorpholine Water 7.10 0.18 2.4 5.4 6.8 116
(NMM) Effective Amines Salt PPI less than at least one comparative
amine 2-Dimethylamino 2- Water 10.2 0.27 2.3 6.3 9.5 98 methyl 2-
propanol (DMAMP) 80% azeotrope soln N,N,N,N- Water 8.97 0.48 4.7
6.7 8.3 122 tetramethylethylene diamine (TMED) N-methyl piperidine
Water 10.08 0.24 2.1 7.5 8.1 107 1,2 Dimethyl propyl Water 9.90
0.30 1.4 8.5 9.6 87 amine 1,4-dimethylpiperazine Water 8.20 0.18
3.7 5.5 7.6 132 N-methylpyrrolidine Water 10.32 0.10 2.2 6.8 8.1 81
N,N,N',N'- Water 0.30 7.54 8.87 9.25 85 tetramethyldiamino- methane
(TMMD) Dimethyl Water 8.9 0.32 150 tertiarybutanolamine (DMTBA)
Dimethyl Water 9.5 0.20 124 methoxypropylamine (DMMOPA)
[0049] Exemplary treatment compositions may have at least one amine
as described above. Alternatively, the exemplary treatment
compositions may have two or more of the amines described above. In
yet another embodiment, the exemplary treatment compositions may
comprise one or more of the amines described above as well as one
or more amines that are known corrosion inhibitors. The treatment
composition may be added to the hydrocarbon stream as 100% actives,
or it may be added in to the hydrocarbon stream in solution with a
carrier. The carrier may be an organic or aqueous solvent,
depending on the amines used and their solubility in oil and water.
The treatment composition may be present in a range from about 5 wt
% to about 95 wt % based on a total weight of the solution. In
another embodiment, the treatment composition may range from about
25 wt % to about 75 wt % based on a total weight of the solution.
Alternatively, the treatment composition may range from about 40 wt
% to about 60 wt %.
[0050] When water-soluble amines are used, the carrier may comprise
water. When oil-soluble amines are used, the carrier may comprise
at least one non-polar organic solvent. Suitable non-polar organic
solvents include, but are not limited to, naphtha, heavy aromatic
naphtha, pentane, cyclopentane, hexane, cyclohexane, benzene, ethyl
benzene, 1,2,4-trimethyl benzene, toluene, xylene, cumene,
1,4-dioxane, chloroform, diethyl ether, and methyl esters of fatty
acids (biodiesel).
[0051] An exemplary treatment composition may have a formulation as
listed in Table 3.
TABLE-US-00003 TABLE 3 Solubility Amines Oil/Water wt %
1,4-dimethylpiperazine Water 30-70 N-methylpyrrolidine Water
30-70
[0052] Another exemplary treatment composition may have a
formulation as listed in Table 4.
TABLE-US-00004 TABLE 4 Solubility Amines Oil/Water wt %
N-methylmorpholine (NMM) Water 45-50 1,4-dimethylpiperazine Water
5-10 N-methylpyrrolidine Water 40-50
[0053] This written description uses examples to disclose the
invention, including the best mode, and also to enable any person
skilled in the art to practice the invention, including making and
using any devices or systems and performing any incorporated
methods. The patentable scope of the invention is defined by the
claims, and may include other examples that occur to those skilled
in the art. Such other examples are intended to be within the scope
of the claims if they have structural elements that do not differ
from the literal language of the claims, or if they include
equivalent structural elements with insubstantial differences from
the literal languages of the claims.
* * * * *