CA1228317A - Process for fluid catalytic cracking of hydrocarbons - Google Patents
Process for fluid catalytic cracking of hydrocarbonsInfo
- Publication number
- CA1228317A CA1228317A CA000432477A CA432477A CA1228317A CA 1228317 A CA1228317 A CA 1228317A CA 000432477 A CA000432477 A CA 000432477A CA 432477 A CA432477 A CA 432477A CA 1228317 A CA1228317 A CA 1228317A
- Authority
- CA
- Canada
- Prior art keywords
- cracking
- catalyst
- suspension
- hydrocarbons
- fluid catalytic
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
- C10G11/04—Oxides
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
PROCESS FOR THE FLUID CATALYTIC CRACKING OF HYDROCARBONS
ABSTRACT OF THE DISCLOSURE
The fluid catalytic cracking of hydrocarbons process covered by this invention consists of:
a) preparing a suspension made up of a hydrocarbon, meant to act as a dispersion agent, a cracking additive and a cracking catalyst;
b) mixing said suspension into the fresh charge stream to be introduced into the reactor;
c) making such mixture of such suspension and fresh charge stream undergo cracking.
The process of this invention has been found to be quite efficient in the processing of charges of hydrocarbons of high metal content, and enables catalyst losses to be brought down by about 50 to 80%.
ABSTRACT OF THE DISCLOSURE
The fluid catalytic cracking of hydrocarbons process covered by this invention consists of:
a) preparing a suspension made up of a hydrocarbon, meant to act as a dispersion agent, a cracking additive and a cracking catalyst;
b) mixing said suspension into the fresh charge stream to be introduced into the reactor;
c) making such mixture of such suspension and fresh charge stream undergo cracking.
The process of this invention has been found to be quite efficient in the processing of charges of hydrocarbons of high metal content, and enables catalyst losses to be brought down by about 50 to 80%.
Description
~22831~
The present invention relates to a process for the fluid catalytic cracking of hydrocarbons whereby hydrocarbon charges contaminated with high contents of metal can be processed.
: The cracking process concerned consists of pro-paring a suspension made up of a hydrocarbon, a crack-in additive, and a cracking catalyst, constantly mixing said suspension with a fresh stream of hydrocarbons, and marina the mixture undergo cracking.
Under the usual fluid catalyst cracking processes-referred to hereinafter as FCC - the catalyst is brought into contact with the charge and the mixture flows through a riser where the cracking reactions take place towards the reactor. At the reactor the catalyst is separated, usually by means of cyclones, from the output of the reaction, the latter going on to the distilling stage and the catalyst to be stripped and then to the regenerator.
m e steam stripping treatment withdraws the weaker compounds adsorbed at the surface of the gala-lust, while treatment in the regenerator burns out the ooze also lying on the surface of the catalyst, active middle portions of which become obstructed, thus bringing about a drop in catalytic action.
The particles of the catalyst dragged or carried away by combustion gases are also reassured by means of " ~28317 cyclones lying within the regenerator. After having been regenerated, the catalyst rejoins the process, to meet up with a fresh stream of coarse.
The output which goes on to be distilled is led Jo a fractionator where it is broken up into gases, naphtha, light gas oil, heavy ohs oil, clarified oil and slurry oil. Such slurry oil will also contain particles of the catalyst, carried away by the reaction products upon separation from the catalyst at reactor outlet.
Though the latest FCC units are equipped with sets of one or more stage cyclones, catalyst losses in such units are still considerable.
The fluid catalytic cracking process covered by this invention makes use of a catalyst charging method (described further on) which enables a drastic cut to be made in such losses.
cause of the oil crisis, efforts have been world-wide towards developing processes to make ever greater use of such oil as is available. Thus cracking processes have come into being which enable use to be made of the heavier fractions of crude as a raw material for such processes, while at the same time catalysts that are more active and less susceptible to being poisoned than those used in the seventies are being developed. ____ ~;2283~
3 .
It is a well-known fact that the presence of certain metals, such as No and V, in the charge to be cracked, represents a serious obstacle when the usual catalysts are employed, since such metals soon poison them. Furthermore, in the heavier cuts of crude the proportion of such metals is considerably greater than in the lighter cuts.
-To overcome this trouble research ha been undertaken towards finding a way of lessening the o effect of such poisons upon the catalysts then known.
- m is led to substances nowadays known as cracking pass- -vapors or additives. The presence of such substances on the reaction medium enables high No and V content hydrocarbon charges to be processed.
It was found that compounds containing B, Sun, To, Sub, My, Bit W, To, In, Go and others have such powers. Nowadays there is a trade in products for such purpose. Meanwhile further passivation process technic quest have been described in publications on the subject.
Jo Fresh processes directed towards the more effective use of crude, plus such Tahitian have led to other discoveries in recent years.
One of the purposes of the process of the present invention is that of providing a process for the fluid catalytic cracking of hydrocarbons in which catalyst losses can be drastically reduced, by about 50 to 80%.
lZ283~7 . "
Another purpose of the process invented is that of enabling catalyst fines (particles of G-40 microns on size) to play their part in cracking reactions.
A further purpose of the process invented is what of enabling metal contaminated hydrocarbon charges to be processed.
Such purposes were achieved thanks to the change made in the way of supplying the coolest to the process. Instead of employing the usual method of replace it in catalyst losses, namely, by means of a pressurized silo leading to the regenerator, in this invention the catalyst is supplied wet, directly to the reaction medium;
By supplying the process with wet virgin catalyst, that is, by means of a suspension within a hydrocarbon, there is the advantage to be gained of enabling catalyst - fines to play a part in the cracking reaction.
The process invented enables stricter control to be kept over the quantities of catalyst and of cracking additive (if any) which it is intended to add to the stream of the charge.
The catalyst is suspended in a stream of a hydra-carbon, for instance, heavy vacuum gas oil, heavy recycle gas oil, LOO or FCC diesel, naphtha, FCC fuel oil, etc., said suspension being mixed with the charge or else directly injected into the riser, after which ~ZZ83~7 the cracking takes place. When the charge is contami-noted with metals, a cracking additive is incorporated to inhibit any poisoning of the catalyst. The basis of such additives is usually antimony and there are several kinds on the market.
This invention resides in a process for the fluid catalytic cracking of hydrocarbons, which comprises the following steps:
a) preparing a suspension comprising (i) a hydrocarbon and (ii) a virgin cracking catalyst or a virgin cracking catalyst and a cracking additive;
b) continuously mixing said suspension with a stream of a hydrocarbon feed stock having a density of from 10 to 25 APT to form a joint charge; and c) subjecting said joint charge to cracking, said process being conducted in the substantial absence of added water.
The invention further provides a process for the fluid catalytic cracking of hydrocarbons comprising:
(a) preparing a suspension comprising (i) a hydrocarbon and (ii) a virgin cracking catalyst or a virgin cracking catalyst and a cracking additive;
(b) directly and continuously injecting said suspension into a riser unit; and (c) subjecting said hydrocarbon to cracking, said process being conducted in the lZZ8317 - pa -substantial absence of added water.
An alternative process would be to inject the catalyst suspension directly into the riser and then make it undergo cracking.
To determine the quantities of the suspension to be added to the process from time to time, certain operational aspects have to be considered.
The method of checking on the degree of metal contamination of the catalyst by measuring hydrogen and methane produced during the process is a well-known one.
When the catalyst is poisoned by I and V, dehydrogenation and the creation of coke reactions take place at the .
12283'17 .
same time, being catalyzed by such metals. Therefore, a sign that the catalyst is being contaminated is that there is a higher proportion of hydrogen in the fuel gas.
Usually, what is done is to control catalytic action by making piecemeal replacements o, tune spent catalyst with regenerated or even virgin catalyst and also by striving to keep the relationship between the hydrogen and the methane present in the fuel gas within bounds regarded as acceptable. It is worth-whole keeping such bounds as low as possible.
For the purpose of comparing performance under the process invented with that under processes already described in publications, a suspension was prepared, as yet on an experimental scale, containing the gala-lust, and according to methods described further on, and the invented process was carried out. Afterwards, merely for the sake of comparison, a know cracking process was completed.
It was found that when the method invented is employed, and whether or not a cracking additive is added to the catalyst suspension, catalyst losses are substantially less.
It was also found that when the method of the present invention is employed, less cracking additive has to be used to arrive at the same hydrogen/methane ratio in the ~228317 fuel gas, other variables in the operation being the same. This means that about half as much cracking additive has to be employed.
Furthermore, it was discovered that lower hydrogen/
methane ratios within the fuel gas could be arrived at than those under the usual kind of process, regardless of what quantity of cracking additive might be employed in the usual process. This means that under the usual process the hydrogen/methane ratio in the fuel gas cannot be brought down below a given f guru no matter what quantity of cracking additive be employed.
Therefore the fluid catalytic cracking process covered by this invention has proved to be more efficient than those previously described in publications.
The invented process will next be described in terms of the drawing which is appended to this specification so as to make it clearer though such description must in no way be construed as a limitation of the process.
The single drawing figure is a schematic representation of the invention.
The cracking reactor is shown under 1 and consists of the riser unit and the product separator, the catalyst regenerator, under I, and the tank for preparing the suspension, under 3.
~228317 To the mixing tank (3), provided with a mechanic eel stirrer (4), a hydrocarbon I is added, which is to act as the dispersing medium for the catalyst, plus a cracking additive (6), if needed, and a virgin catalyst (7), in suitable proportions. The suspension stream thus secured for the catalyst (8) is being continually mixed with the stream of the fresh charge (9), which gives rise to a joint charge stream (10), which is led into the cracking reactor (1), more specifically, into the riser.
The stream of reaction products (11) is separated and led to the fractionator - not shown in the figure -while the stream of spent catalyst (12) is led to the regenerator (2), in which regeneration of the catalyst will take place.
A stream of combustible gas (13) is introduced into the regenerator (2) to burn up the coke deposited upon the spent catalyst, which gives rise to a stream of combustion gases (14), which is then withdrawn from the regenerator (2). From the regenerator a stream of regenerated catalyst (15) also runs back to the process and joins up with the stream of the combined charge (10) which enters the cracking reactor (1).
In carrying out this invention heavy gas oil was so ~Z283~7 - pa -employed as the charge and as the dispersing agent, and air as the combustible gas.
An alternative process under the invention consists of preparing a suspension of the catalyst in a hydrocarbon (8), either with or without cracking additive, and injecting such suspension continuously into the riser, that is, without going through the stage of having to mix it with the stream of fresh charge (9).
The usual method which was employed for the sake of comparison was as follows.
X
lZ28317 g The catalyst stored in a silo was transferred to the regenerator by pressurizing the silo and the catalyst was added continuously to the process. The cracking additive was diluted with gas oil in a drum and continuously injected into the stream of the charge, in quantities big enough to arrive at the desired results. The mixture so secured was made to undergo cracking.
In order to bear out results arrived at on the workbench a prototype unit was put up for trials.
Such trials were meant to arrive at more reliable figures than those ascertained at a work bench scale, amongst others, those for catalyst losses, as well as ideal operating conditions and a study comparing usual process with that invented.
The examples given below show the results of such trials which are not however to be regarded as limits of the invention.
he catalysts that can be used for the process invented are the usual ones, e.g.: low alumina, high alumina, zealots, etc.
Operating conditions followed for the trials were also the ones that usually apply.
Throughout the trials the quality of the charge was kept the same.
' 1 ! ' .
EXAMPLE I
The purpose of this example is to check the efficiency of the feed system under the process invented as compared with that for the usual process.
In tests 1 and 2 the catalyst was replaced continuously as provided for in the usual method, that is from the silo to the regenerator. In tests 3 and 4 the invented method was employed, namely:
A suspension of the catalyst in gas oil was prepared in a mixing tank provided with a mechanical stirrer. Such suspension was fed continuously. to the process, along with the charge.
he charge used for such tests was a heavy gas oil derived from Leon crudely the catalyst used was high alumina In all the tests, replacement was exactly equal to quantity of catalyst lost.
'rABLE (I) Ten Charge (m Davy) Replacement (tons/dzy) 1 153 0.45
The present invention relates to a process for the fluid catalytic cracking of hydrocarbons whereby hydrocarbon charges contaminated with high contents of metal can be processed.
: The cracking process concerned consists of pro-paring a suspension made up of a hydrocarbon, a crack-in additive, and a cracking catalyst, constantly mixing said suspension with a fresh stream of hydrocarbons, and marina the mixture undergo cracking.
Under the usual fluid catalyst cracking processes-referred to hereinafter as FCC - the catalyst is brought into contact with the charge and the mixture flows through a riser where the cracking reactions take place towards the reactor. At the reactor the catalyst is separated, usually by means of cyclones, from the output of the reaction, the latter going on to the distilling stage and the catalyst to be stripped and then to the regenerator.
m e steam stripping treatment withdraws the weaker compounds adsorbed at the surface of the gala-lust, while treatment in the regenerator burns out the ooze also lying on the surface of the catalyst, active middle portions of which become obstructed, thus bringing about a drop in catalytic action.
The particles of the catalyst dragged or carried away by combustion gases are also reassured by means of " ~28317 cyclones lying within the regenerator. After having been regenerated, the catalyst rejoins the process, to meet up with a fresh stream of coarse.
The output which goes on to be distilled is led Jo a fractionator where it is broken up into gases, naphtha, light gas oil, heavy ohs oil, clarified oil and slurry oil. Such slurry oil will also contain particles of the catalyst, carried away by the reaction products upon separation from the catalyst at reactor outlet.
Though the latest FCC units are equipped with sets of one or more stage cyclones, catalyst losses in such units are still considerable.
The fluid catalytic cracking process covered by this invention makes use of a catalyst charging method (described further on) which enables a drastic cut to be made in such losses.
cause of the oil crisis, efforts have been world-wide towards developing processes to make ever greater use of such oil as is available. Thus cracking processes have come into being which enable use to be made of the heavier fractions of crude as a raw material for such processes, while at the same time catalysts that are more active and less susceptible to being poisoned than those used in the seventies are being developed. ____ ~;2283~
3 .
It is a well-known fact that the presence of certain metals, such as No and V, in the charge to be cracked, represents a serious obstacle when the usual catalysts are employed, since such metals soon poison them. Furthermore, in the heavier cuts of crude the proportion of such metals is considerably greater than in the lighter cuts.
-To overcome this trouble research ha been undertaken towards finding a way of lessening the o effect of such poisons upon the catalysts then known.
- m is led to substances nowadays known as cracking pass- -vapors or additives. The presence of such substances on the reaction medium enables high No and V content hydrocarbon charges to be processed.
It was found that compounds containing B, Sun, To, Sub, My, Bit W, To, In, Go and others have such powers. Nowadays there is a trade in products for such purpose. Meanwhile further passivation process technic quest have been described in publications on the subject.
Jo Fresh processes directed towards the more effective use of crude, plus such Tahitian have led to other discoveries in recent years.
One of the purposes of the process of the present invention is that of providing a process for the fluid catalytic cracking of hydrocarbons in which catalyst losses can be drastically reduced, by about 50 to 80%.
lZ283~7 . "
Another purpose of the process invented is that of enabling catalyst fines (particles of G-40 microns on size) to play their part in cracking reactions.
A further purpose of the process invented is what of enabling metal contaminated hydrocarbon charges to be processed.
Such purposes were achieved thanks to the change made in the way of supplying the coolest to the process. Instead of employing the usual method of replace it in catalyst losses, namely, by means of a pressurized silo leading to the regenerator, in this invention the catalyst is supplied wet, directly to the reaction medium;
By supplying the process with wet virgin catalyst, that is, by means of a suspension within a hydrocarbon, there is the advantage to be gained of enabling catalyst - fines to play a part in the cracking reaction.
The process invented enables stricter control to be kept over the quantities of catalyst and of cracking additive (if any) which it is intended to add to the stream of the charge.
The catalyst is suspended in a stream of a hydra-carbon, for instance, heavy vacuum gas oil, heavy recycle gas oil, LOO or FCC diesel, naphtha, FCC fuel oil, etc., said suspension being mixed with the charge or else directly injected into the riser, after which ~ZZ83~7 the cracking takes place. When the charge is contami-noted with metals, a cracking additive is incorporated to inhibit any poisoning of the catalyst. The basis of such additives is usually antimony and there are several kinds on the market.
This invention resides in a process for the fluid catalytic cracking of hydrocarbons, which comprises the following steps:
a) preparing a suspension comprising (i) a hydrocarbon and (ii) a virgin cracking catalyst or a virgin cracking catalyst and a cracking additive;
b) continuously mixing said suspension with a stream of a hydrocarbon feed stock having a density of from 10 to 25 APT to form a joint charge; and c) subjecting said joint charge to cracking, said process being conducted in the substantial absence of added water.
The invention further provides a process for the fluid catalytic cracking of hydrocarbons comprising:
(a) preparing a suspension comprising (i) a hydrocarbon and (ii) a virgin cracking catalyst or a virgin cracking catalyst and a cracking additive;
(b) directly and continuously injecting said suspension into a riser unit; and (c) subjecting said hydrocarbon to cracking, said process being conducted in the lZZ8317 - pa -substantial absence of added water.
An alternative process would be to inject the catalyst suspension directly into the riser and then make it undergo cracking.
To determine the quantities of the suspension to be added to the process from time to time, certain operational aspects have to be considered.
The method of checking on the degree of metal contamination of the catalyst by measuring hydrogen and methane produced during the process is a well-known one.
When the catalyst is poisoned by I and V, dehydrogenation and the creation of coke reactions take place at the .
12283'17 .
same time, being catalyzed by such metals. Therefore, a sign that the catalyst is being contaminated is that there is a higher proportion of hydrogen in the fuel gas.
Usually, what is done is to control catalytic action by making piecemeal replacements o, tune spent catalyst with regenerated or even virgin catalyst and also by striving to keep the relationship between the hydrogen and the methane present in the fuel gas within bounds regarded as acceptable. It is worth-whole keeping such bounds as low as possible.
For the purpose of comparing performance under the process invented with that under processes already described in publications, a suspension was prepared, as yet on an experimental scale, containing the gala-lust, and according to methods described further on, and the invented process was carried out. Afterwards, merely for the sake of comparison, a know cracking process was completed.
It was found that when the method invented is employed, and whether or not a cracking additive is added to the catalyst suspension, catalyst losses are substantially less.
It was also found that when the method of the present invention is employed, less cracking additive has to be used to arrive at the same hydrogen/methane ratio in the ~228317 fuel gas, other variables in the operation being the same. This means that about half as much cracking additive has to be employed.
Furthermore, it was discovered that lower hydrogen/
methane ratios within the fuel gas could be arrived at than those under the usual kind of process, regardless of what quantity of cracking additive might be employed in the usual process. This means that under the usual process the hydrogen/methane ratio in the fuel gas cannot be brought down below a given f guru no matter what quantity of cracking additive be employed.
Therefore the fluid catalytic cracking process covered by this invention has proved to be more efficient than those previously described in publications.
The invented process will next be described in terms of the drawing which is appended to this specification so as to make it clearer though such description must in no way be construed as a limitation of the process.
The single drawing figure is a schematic representation of the invention.
The cracking reactor is shown under 1 and consists of the riser unit and the product separator, the catalyst regenerator, under I, and the tank for preparing the suspension, under 3.
~228317 To the mixing tank (3), provided with a mechanic eel stirrer (4), a hydrocarbon I is added, which is to act as the dispersing medium for the catalyst, plus a cracking additive (6), if needed, and a virgin catalyst (7), in suitable proportions. The suspension stream thus secured for the catalyst (8) is being continually mixed with the stream of the fresh charge (9), which gives rise to a joint charge stream (10), which is led into the cracking reactor (1), more specifically, into the riser.
The stream of reaction products (11) is separated and led to the fractionator - not shown in the figure -while the stream of spent catalyst (12) is led to the regenerator (2), in which regeneration of the catalyst will take place.
A stream of combustible gas (13) is introduced into the regenerator (2) to burn up the coke deposited upon the spent catalyst, which gives rise to a stream of combustion gases (14), which is then withdrawn from the regenerator (2). From the regenerator a stream of regenerated catalyst (15) also runs back to the process and joins up with the stream of the combined charge (10) which enters the cracking reactor (1).
In carrying out this invention heavy gas oil was so ~Z283~7 - pa -employed as the charge and as the dispersing agent, and air as the combustible gas.
An alternative process under the invention consists of preparing a suspension of the catalyst in a hydrocarbon (8), either with or without cracking additive, and injecting such suspension continuously into the riser, that is, without going through the stage of having to mix it with the stream of fresh charge (9).
The usual method which was employed for the sake of comparison was as follows.
X
lZ28317 g The catalyst stored in a silo was transferred to the regenerator by pressurizing the silo and the catalyst was added continuously to the process. The cracking additive was diluted with gas oil in a drum and continuously injected into the stream of the charge, in quantities big enough to arrive at the desired results. The mixture so secured was made to undergo cracking.
In order to bear out results arrived at on the workbench a prototype unit was put up for trials.
Such trials were meant to arrive at more reliable figures than those ascertained at a work bench scale, amongst others, those for catalyst losses, as well as ideal operating conditions and a study comparing usual process with that invented.
The examples given below show the results of such trials which are not however to be regarded as limits of the invention.
he catalysts that can be used for the process invented are the usual ones, e.g.: low alumina, high alumina, zealots, etc.
Operating conditions followed for the trials were also the ones that usually apply.
Throughout the trials the quality of the charge was kept the same.
' 1 ! ' .
EXAMPLE I
The purpose of this example is to check the efficiency of the feed system under the process invented as compared with that for the usual process.
In tests 1 and 2 the catalyst was replaced continuously as provided for in the usual method, that is from the silo to the regenerator. In tests 3 and 4 the invented method was employed, namely:
A suspension of the catalyst in gas oil was prepared in a mixing tank provided with a mechanical stirrer. Such suspension was fed continuously. to the process, along with the charge.
he charge used for such tests was a heavy gas oil derived from Leon crudely the catalyst used was high alumina In all the tests, replacement was exactly equal to quantity of catalyst lost.
'rABLE (I) Ten Charge (m Davy) Replacement (tons/dzy) 1 153 0.45
2 285 0.66
3 239 . 0.13
4 255 0.20 ordinary comparison of test 3 against test 2 . shows a drop of 80.3% in ca~al~st~replaced, in the former.
12;283~7 , - EXAMPLE II
In these tests the intention was to discover optimum operating conditions for tune process. Runs were done in which the usual process turn 5) was come pared with that of the invention (run reaction temperature, catalyst/oil ratio, and combined charge ratio were all kept as steady as possible. A cork nod charge of 1.0 means that no recycling was done.
Table II shows average results of the runs.
TABLE (II) Runs _ 5 6 charge (m day) 186 - 186 charge temperature (C) 165 169 circulation of catalyst (ton/min.) 3.0 2.4 catalyst/oil ratio 22.8 18.3 reaction temperature (C) 492 490 dense stage 607 623 regenerator temperature diluted (SUE stage 612 628 cyclone 639 combined charge ratio 1.0 1.0 hydrogen/methane ratio in fuel gas 3.17 2.72 cracking additive (kg/day~* 24 8 replacement catalyst (kg/day)200 100 * antimony type commercial ad Five replacement exactly equal to catalyst lost -The above serves to show that, under the process of the present invention, catalyst losses were half as much. It should also be noted that even with only a third of the additive the hydrogen/methane ratio was lower, Which means that the cracking additive was more efficiently used.
EXP~IPLE III
The object of this example was to find out if by raising the quantity of cracking additive employed, as in the usual catalyst replacement method, the hydrogen/carbon (H2/Cl) ratio would become lower than that arrived at under the process invented.
, under the process invented a clue ratio of 2.7 was arrived at and 2.7k~ of Sub pox day was used.
Doses of Sub were worked out in terms of the common-coal cracking additive employed. Table III shows the results secured.
TABLE (III) kg Sb/day ~2/C
1.80 3.8 2.76 3.17 3.50 3.3 4.00 3.5 - Under the usual process no matter what quantity of additive was used the Ho/ old not be brought down to below 3.17.
12;283~7 , - EXAMPLE II
In these tests the intention was to discover optimum operating conditions for tune process. Runs were done in which the usual process turn 5) was come pared with that of the invention (run reaction temperature, catalyst/oil ratio, and combined charge ratio were all kept as steady as possible. A cork nod charge of 1.0 means that no recycling was done.
Table II shows average results of the runs.
TABLE (II) Runs _ 5 6 charge (m day) 186 - 186 charge temperature (C) 165 169 circulation of catalyst (ton/min.) 3.0 2.4 catalyst/oil ratio 22.8 18.3 reaction temperature (C) 492 490 dense stage 607 623 regenerator temperature diluted (SUE stage 612 628 cyclone 639 combined charge ratio 1.0 1.0 hydrogen/methane ratio in fuel gas 3.17 2.72 cracking additive (kg/day~* 24 8 replacement catalyst (kg/day)200 100 * antimony type commercial ad Five replacement exactly equal to catalyst lost -The above serves to show that, under the process of the present invention, catalyst losses were half as much. It should also be noted that even with only a third of the additive the hydrogen/methane ratio was lower, Which means that the cracking additive was more efficiently used.
EXP~IPLE III
The object of this example was to find out if by raising the quantity of cracking additive employed, as in the usual catalyst replacement method, the hydrogen/carbon (H2/Cl) ratio would become lower than that arrived at under the process invented.
, under the process invented a clue ratio of 2.7 was arrived at and 2.7k~ of Sub pox day was used.
Doses of Sub were worked out in terms of the common-coal cracking additive employed. Table III shows the results secured.
TABLE (III) kg Sb/day ~2/C
1.80 3.8 2.76 3.17 3.50 3.3 4.00 3.5 - Under the usual process no matter what quantity of additive was used the Ho/ old not be brought down to below 3.17.
Claims (6)
1. Process for the fluid catalytic cracking of hydrocarbons which comprises the following steps:
a) preparing a suspension comprising (i) a hydrocarbon and (ii) a virgin cracking catalyst or a virgin cracking catalyst and a cracking additive;
b) continuously mixing said suspension with a stream of a hydrocarbon feedstock having a density of from 10° to 25° API to form a joint charge; and c) subjecting said joint charge to cracking, said process being conducted in the substantial absence of added water.
a) preparing a suspension comprising (i) a hydrocarbon and (ii) a virgin cracking catalyst or a virgin cracking catalyst and a cracking additive;
b) continuously mixing said suspension with a stream of a hydrocarbon feedstock having a density of from 10° to 25° API to form a joint charge; and c) subjecting said joint charge to cracking, said process being conducted in the substantial absence of added water.
2. A process for the fluid catalytic cracking of hydrocarbons comprising:
a) preparing a suspension comprising (i) a hydrocarbon and (ii) a virgin cracking catalyst or a virgin cracking catalyst and a cracking additive;
b) directly and continuously injecting said suspension into a riser unit; and c) subjecting said hydrocarbon to cracking, said process being conducted in the substantial absence of added water.
a) preparing a suspension comprising (i) a hydrocarbon and (ii) a virgin cracking catalyst or a virgin cracking catalyst and a cracking additive;
b) directly and continuously injecting said suspension into a riser unit; and c) subjecting said hydrocarbon to cracking, said process being conducted in the substantial absence of added water.
3. Process for the fluid catalytic cracking of hydrocarbons as in claims 1 or 2, said process steps being effected such as to bring about a drop in catalyst losses of from about 50% to 80%.
4. Process for the fluid catalytic cracking of hydrocarbons as in claims 1 or 2, wherein catalyst particles of less than 40 microns in size are employed.
5. The process of claim 1, wherein said cracking is carried out with cracking additives that contain B, Sn, Te, Sb, Mn, Bi, W, Tl, In or Ge.
6. The process of claim 2, wherein said cracking is carried out with cracking additives that contain B, Sn, Te, Sb, Mn, Bi, W, Tl, In or Ge.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| BR8204113A BR8204113A (en) | 1982-07-15 | 1982-07-15 | HYDROCARBON FLUID CATALYTIC CRACKING PROCESS |
| BRPI8204113 | 1983-06-14 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1228317A true CA1228317A (en) | 1987-10-20 |
Family
ID=4031341
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000432477A Expired CA1228317A (en) | 1982-07-15 | 1983-07-14 | Process for fluid catalytic cracking of hydrocarbons |
Country Status (9)
| Country | Link |
|---|---|
| JP (1) | JPS601283A (en) |
| AR (1) | AR231303A1 (en) |
| BR (1) | BR8204113A (en) |
| CA (1) | CA1228317A (en) |
| DE (1) | DE3325027C2 (en) |
| FR (1) | FR2530261B1 (en) |
| GB (1) | GB2124249B (en) |
| IT (1) | IT8348683A0 (en) |
| MX (1) | MX162315A (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4666584A (en) * | 1983-12-09 | 1987-05-19 | Exxon Research And Engineering Company | Method for passivating cracking catalyst |
| US4504381A (en) * | 1983-12-09 | 1985-03-12 | Exxon Research And Engineering Co. | Passivation of cracking catalysts with cadmium and tin |
| US4522704A (en) * | 1983-12-09 | 1985-06-11 | Exxon Research & Engineering Co. | Passivation of cracking catalysts |
| JPH03283312A (en) * | 1990-03-30 | 1991-12-13 | Tokai Rubber Ind Ltd | Terminal portion of tape wire |
| US7753992B2 (en) | 2006-06-19 | 2010-07-13 | Basf Corporation | Methods of manufacturing mercury sorbents and removing mercury from a gas stream |
| US8906823B2 (en) | 2007-09-24 | 2014-12-09 | Basf Corporation | Pollutant emission control sorbents and methods of manufacture and use |
| US8685351B2 (en) | 2007-09-24 | 2014-04-01 | Basf Corporation | Pollutant emission control sorbents and methods of manufacture and use |
Family Cites Families (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2843460A (en) * | 1953-04-07 | 1958-07-15 | Standard Oil Dev Co | Contacting of gases with fluidized solids |
| US3850582A (en) * | 1969-12-10 | 1974-11-26 | Exxon Research Engineering Co | Apparatus for controlled addition of fluidized particles to a processing unit |
| JPS4926921B1 (en) * | 1970-03-19 | 1974-07-13 | ||
| US3849291A (en) * | 1971-10-05 | 1974-11-19 | Mobil Oil Corp | High temperature catalytic cracking with low coke producing crystalline zeolite catalysts |
| US3770615A (en) * | 1971-10-22 | 1973-11-06 | Grace W R & Co | Fluid catalytic cracking process with addition of molecular sieve catalyst-liquid mixture |
| US4259175A (en) * | 1978-10-10 | 1981-03-31 | Union Oil Company Of California | Process for reducing sox emissions from catalytic cracking units |
| US4218306A (en) * | 1979-01-15 | 1980-08-19 | Mobil Oil Corporation | Method for catalytic cracking heavy oils |
| JPS5836035B2 (en) * | 1979-07-24 | 1983-08-06 | フイリツプス ペトロリユ−ム コンパニ− | Method for controlling introduction of metal passivating agent in catalytic cracking method |
| US4269696A (en) * | 1979-11-08 | 1981-05-26 | Exxon Research & Engineering Company | Fluid coking and gasification process with the addition of cracking catalysts |
| US4377470A (en) * | 1981-04-20 | 1983-03-22 | Ashland Oil, Inc. | Immobilization of vanadia deposited on catalytic materials during carbo-metallic oil conversion |
| US4427535A (en) * | 1981-11-02 | 1984-01-24 | Hydrocarbon Research, Inc. | Selective operating conditions for high conversion of special petroleum feedstocks |
-
1982
- 1982-07-15 BR BR8204113A patent/BR8204113A/en not_active IP Right Cessation
-
1983
- 1983-07-07 GB GB08318438A patent/GB2124249B/en not_active Expired
- 1983-07-11 FR FR8311540A patent/FR2530261B1/en not_active Expired
- 1983-07-11 AR AR293580A patent/AR231303A1/en active
- 1983-07-11 DE DE3325027A patent/DE3325027C2/en not_active Expired - Fee Related
- 1983-07-12 MX MX197999A patent/MX162315A/en unknown
- 1983-07-13 IT IT8348683A patent/IT8348683A0/en unknown
- 1983-07-14 JP JP58128686A patent/JPS601283A/en active Granted
- 1983-07-14 CA CA000432477A patent/CA1228317A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| AR231303A1 (en) | 1984-10-31 |
| JPS6345757B2 (en) | 1988-09-12 |
| IT8348683A0 (en) | 1983-07-13 |
| FR2530261B1 (en) | 1986-04-18 |
| BR8204113A (en) | 1984-02-21 |
| MX162315A (en) | 1991-04-24 |
| DE3325027C2 (en) | 1993-11-18 |
| JPS601283A (en) | 1985-01-07 |
| GB8318438D0 (en) | 1983-08-10 |
| GB2124249B (en) | 1986-02-19 |
| GB2124249A (en) | 1984-02-15 |
| DE3325027A1 (en) | 1984-01-19 |
| FR2530261A1 (en) | 1984-01-20 |
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