Patent Application
20190119580
The present invention pertains to a process for controlling corrosion in petroleum refining units by reducing buildup of hydrochloride salts and minimizing fouling of the apparatus.
Hydrocarbon feedstocks such as petroleum crudes, gas oil, etc. are subjected to various processes in order to isolate and separate different fractions of the feedstock. In refinery processes, the feedstock is distilled so as to provide the various valuable fractions, e.g., light hydrocarbons, gasoline, naphtha, kerosene, gas oil, etc. The lower boiling fractions are recovered as an overhead fraction from the distillation and vacuum columns. The intermediate components are recovered as side cuts from the distillation column. The fractions are cooled, condensed, and sent to collecting equipment. No matter what type of petroleum feedstock is used as the charge, the distillation equipment is subjected to the corrosive activity of acids such as H2S, HCl, organic acids, and H2CO3. The problem of corrosion caused by these acid gases as water condenses in the overhead condensing systems of distillation and vacuum columns is well known. The consequent presence of acidic water leads to the undesirable corrosion of metallic equipment, often rapidly.
The general mechanism of this corrosion is an oxidation of metal atoms by aqueous hydrogen ions. The rate of corrosion is directly related to the concentration of aqueous hydrogen ions. A particularly difficult aspect of the problem is that the corrosion occurs above and in the temperature range of the initial condensation of water. The term “initial condensate” as used herein indicates a phase formed when the temperature of the surrounding environment reaches the dew point of water. At this point a mixture of liquid water, hydrocarbon, and vapor may be present. The initial condensate may occur within the distilling unit itself or in subsequent condensers and other equipment. The top temperature of the fractionating column is normally maintained above the dew point of water. The initial aqueous condensate formed contains a high percentage of HCl. The chlorine comes from salts in the crude, and recently the salt content of crude oil (especially Opportunity Crudes) being used in refineries has increased, generating more chlorides. Due to the high concentration of acids dissolved in the water, the pH of the first condensate can be rather low. Thus, as noted, the condensed water can be highly corrosive. It is important that the first condensate is made less corrosive.
Conventionally, highly basic ammonia has been added at various points in the system in an attempt to inhibit the corrosiveness of condensed acidic materials. However, ammonia has not been effective to eliminate corrosion occurring at the initial condensate due to its volatility. In one non-limiting view, ammonia may be ineffective because it does not condense completely enough to neutralize the acidic components of the first condensate.
Amines such as morpholine and methoxy propylamine have been used successfully to control or inhibit corrosion that occurs at the point of initial condensation within or after the distillation unit. Adding amines to the petroleum fractionating system raises the pH of the initial condensate rendering the material substantially less corrosive. The amine inhibitor can be added to the system either in pure form or as an aqueous solution. In some cases, sufficient amounts of amine inhibitors are added to raise the pH of the liquid at the point of initial condensation to above 4.5; in some cases to between 5.5 and 6.5. Other highly basic (pKa>8) amines have been used, including ethylenediamine, monoethanolamine and hexamethylene diamine.
However, the use of these highly basic amines for treating the initial condensate has a problem relating to the resultant hydrochloride salts of these amines which tend to form deposits in distillation columns, column pumparounds, overhead lines, overhead heat exchangers and other parts of the system. These deposits occur after the particular amine has been used for a period of time, sometimes in as little as one or two days. These deposits can cause both fouling and corrosion problems and are particularly problematic in units that do not use a water wash.
Thus, it would be desirable if a process could be devised that neutralizes acid environments in distillation overheads of hydrocarbon processing facilities that minimizes or reduces deposits of hydrochloride and amine salts.
The present invention is a process for controlling corrosion in an overhead system of a refining unit comprising water vapor/condensate and petroleum products comprising the step of adding to the system an amine compound and an alcohol, preferably wherein the amount of the amine compound and the alcohol independently range from 1 to 10,000 ppm based on the petroleum products.
In one embodiment of the process disclosed herein the amine compound is an alkylamine, an alkanolamine, or mixtures thereof, preferably dimethylethanolamine (DMEA), dimethylisopropanolamine (DMIPA), ethylenediamine (EDA), methoxypropylamine (MOPA), monoethanolamine (MEA), dimethylaminopropylamine (DMAPA), morpholine, or trimethylamine (TMA).
In one embodiment, the process disclosed herein above wherein the alcohol is a polyol, polyether diol, polyether triol, or mixtures thereof.
In one embodiment the process disclosed herein above the alcohol is a polyol based on ethylene glycol reacted with ethylene oxide, a polyol based on ethylene glycol reacted with propylene oxide, or a polyol based on ethylene glycol reacted with ethylene oxide and propylene oxide, or mixtures thereof.
In one embodiment of the process disclosed herein above the alcohol is a polyol based on glycerol reacted with ethylene oxide, a polyol based on glycerol reacted propylene oxide, a polyol based on glycerol reacted butylene oxide, a polyol based on glycerol reacted ethylene oxide and/or propylene oxide and/or butylene oxide, or mixtures thereof.
In one embodiment of the process disclosed herein above the alcohol is ethylene glycol, diethylene glycol, triethylene glycol, tetraethylene glycol, glycerol, polyethylene glycol, polypropylene glycol, polytetramethylene glycol, or mixtures thereof.
In one embodiment of the process disclosed herein above the amine compound and the alcohol are added to the system separately.
In one embodiment of the process disclosed herein above the amine compound and the alcohol are added to the system together.
In one embodiment the process disclosed herein above further comprises the step of adding the amine compound and the alcohol to the system at a rate sufficient to maintain the pH of water condensate in the system at a pH of equal to or greater than 4, more preferably equal to or greater than 5.
Methods and compositions are disclosed for neutralizing acid environments and controlling corrosion in distillation overhead systems of petroleum product processing facilities, including, but not limited to distillation columns, vacuum distillation columns, preflash towers, and the like. The neutralizer composition comprises an amine compound and an alcohol.
For decades, refiners have struggled with providing adequate neutralization in overhead systems without forming corrosive salts. Ammonia and several amines have been tried to control corrosion with random successes and failures. The neutralizer compositions of the invention will allow reduction of fouling tendency of the corrosive salts without changing the neutralization power of ammonia and amines.
The water vapor/condensate coming out of the overhead of the crude distillation unit (CDU) in the refinery is very acidic primarily due to the presence of acidic components, such as hydrochloric acid (HCl), which is formed when the crude oil passes through a heating furnace (composed of metal chlorides such as MgCl2, CaCl2, etc.) prior to entering the CDU. Water vapor and HCl rise to the top of the distillation tower along with the light components of the crude oil such as liquefied petroleum gas and naphtha. This stream passes through an overhead line and then enters a condenser, after which the water stream will be separated from naphtha and off-gas and sent to a water treatment unit. The acidic HCl stream (often having a pH less than 2) is highly corrosive and needs to be neutralized (preferably to a pH of 4 or greater, more preferably 5 or greater). The neutralizing composition is added to the overhead system, traditionally, neutralizers are injected into the overhead system between the CDU and the condenser.
In one embodiment of the present invention, the neutralizing composition may be added to the overhead system upstream of the aqueous dew point. This addition point is usually the overhead line off of the distillation column or the vapor line off of a dry first condensing stage accumulator.
It will be appreciated that it is not necessary for corrosion in distillation overheads or other equipment to completely cease for the method of this invention to be considered successful. Indeed, the inventive method should be considered operative if corrosion is inhibited to a measurable extent. In the context of this invention, the term “controlling corrosion” is defined to include any cessation, prevention, abatement, reduction, suppression, lowering, controlling or decreasing of corrosion, rusting, oxidative decay, etc. Similarly, the term “neutralize” refers to such corrosion inhibition by reducing the acidity of the chemicals or components in the system such as by raising pH, but does not require adjusting pH to be 7, but rather raising of pH and moving from acidity to basicity to some measurable extent. Furthermore, the nature of the metal surfaces protected in the methods of this invention is not critical. The metals in which the system operates may include, but are not necessarily limited to iron alloys, copper alloys, nickel alloys, titanium alloys, and these metals in unalloyed form as well, etc.
The first component of the neutralizing composition is an amine compound, preferably one or more alkylamine or alkanolamine, preferably dimethylethanolamine (DMEA), dimethylisopropanolamine (DMIPA), ethylenediamine (EDA), methoxypropylamine (MOPA), monoethanolamine (MEA), dimethylaminopropylamine (DMAPA), morpholine, and trimethylamine (TMA). The one or more alkylamine or alkanolamine is added in an amount of from 1 ppm to 10,000 ppm based on the petroleum products.
Preferably the amine compound is added in an amount of equal to or greater than 1 ppm, preferably equal to or greater than 1 ppm, more preferably equal to or greater than 10 ppm, and more preferably equal to or greater than 100 ppm based on the petroleum products. Preferably the amine compound is added in an amount of equal to or less than 5,000 ppm, preferably equal to or less than 1,000 ppm, and more preferably equal to or less than 500 ppm based on the petroleum products.
The second component of the neutralizing composition is an alcohol. Any suitable alcohol may be used. Preferably, the alcohol is a polyol, polyether diol, polyether triol, or mixtures thereof. In one embodiment, the alcohol s a polyol based on ethylene glycol reacted with ethylene oxide, a polyol based on ethylene glycol reacted with propylene oxide, a polyol based on ethylene glycol reacted with butylene oxide or a polyol based on ethylene glycol reacted with ethylene oxide and/or propylene oxide and/or butylene oxide, or mixtures thereof. In another embodiment, the alcohol is s a polyol based on glycerol reacted with ethylene oxide, a polyol based on glycerol reacted propylene oxide, a polyol based on glycerol reacted ethylene oxide and propylene oxide, or mixtures thereof. In yet another embodiment, the alcohol is ethylene glycol, diethylene glycol, triethylene glycol, tetraethylene glycol, glycerol, polyethylene glycol, polypropylene glycol, polytetramethylene glycol, or mixtures thereof. The one or more alcohol is added in an amount of from 1 ppm to 10,000 ppm based on the petroleum products.
Preferably alcohol is added in an amount of equal to or greater than 1 ppm, preferably equal to or greater than 1 ppm, more preferably equal to or greater than 10, and more preferably equal to or greater than 100 ppm based on the petroleum products. Preferably the alcohol is added in an amount of equal to or less than 5,000 ppm, preferably equal to or less than 1,000 ppm, and more preferably equal to or less than 500 ppm based on the petroleum products.
It will be appreciated that it is difficult to predict what the optimum dosage rate would be in advance for any particular system. The dosage will depend upon a variety of complex, interrelated factors including, but not necessarily limited to, the exact nature of the stream being fractionated, the temperature and pressure of the distillation conditions, the particular amine blends used, etc. In one non-limiting embodiment of the invention, the dosage rate will be determined on a case-by-case basis depending upon the acid content of the system. It may be desirable to use computer modeling to determine the optimum rate. Nevertheless, to provide some understanding of expected or possible dosage rates, the amount of the amine compound and alcohol may independently range from 1 to 10,000 ppm, based on the petroleum products. In another non-limiting embodiment, the amount of the amine compound and alcohol may independently range from 1 to 500 ppm.
The desired pH range for all points in the system is from 4 to 8.5, and in another non-limiting embodiment may be from 5 to 7. Alternatively, to give another idea of expected dosage rates, the neutralizing composition may be added to the system at a rate sufficient to maintain the pH of water condensate in the system at a pH of equal to or greater than 4.0. In another non-limiting embodiment, the neutralizing composition may be added to the system at a rate sufficient to maintain the pH of equal to or greater than 5.0.
The solubility of the monoethanolamine hydrochloride (MEA.HCl) and or ethylenediamine hydrochloride (EDA.2HCl) in diethylene glycol or glycerol is determined as follows: to 10 g of diethylene glycol or glycerol is added an excess amount of the salt and the reaction mixture is stirred rigorously for at least 1 h at the desired temperature. The stirring is then stopped and the reaction mixture is allowed to settle. The solubility of the salt in ethylene glycol or glycerol is calculated from the chloride concentration measured by Ion Chromatography. The viscosity of the saturated solution is measured on a Stabinger Viscometer.
The solubility of MEA.HCl and EDA.2HCl in diethylene glycol at different temperatures is shown in
At 25° C., the solubility of MEA.HCl and EDA.2HCl in glycerol is determined to be 44.5 wt % and 12.8 wt %, respectively. The viscosity of the room temperature saturated solution of MEA.HCl in glycerine and EDA.2HCl in glycerine at different temperatures is shown in
| Number | Date | Country | Kind |
|---|---|---|---|
| 102016000044341 | Apr 2016 | IT | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/US2017/029760 | 4/27/2017 | WO | 00 |
