Process for heating the column for distillation of the C3 fraction from an FCC unit by means of a circuit of water heated by streams belonging to units placed upstream and/or downstream of the FCC unit

Abstract

The present invention describes a process for heating the reboiler of the propane/propylene separation column situated downstream of an FCC unit and fed with the C3 cut from said FCC unit, a process consisting of heating the water in a hot water circuit by means of one or more process fluids originating from units placed upstream and/or downstream of the FCC unit and called hot fluids, one of these fluids being constituted by the overhead vapours from the fractionation column connected to the mild hydrocracking unit.

Claims

1. A process for heating a reboiler of a propane/propylene separation column system which is fed with a C3 cut from a fluid catalytic cracking unit, said process comprising: heating water in a water circuit heat exchange with one or more process fluids originating from units positioned upstream and/or downstream of said fluid catalytic cracking, and then using the heated water in the water circuit to heat said reboiler of the propane/propylene separation column system, wherein said one or more process fluids are: an overhead vapor stream from a fractionation column of a mild hydrocracking unit positioned upstream of said fluid catalytic cracking, an overhead vapor stream from a stripper of a mild hydrocracking unit positioned upstream of said fluid catalytic cracking unit, and/or effluent from a hydrodesulphurization reactor of a fluid catalytic cracking gasoline hydrotreatment positioned downstream of said fluid catalytic cracking unit, after said effluent undergoes heat exchange with a feedstock of the hydrodesulphurization reactor and with a feedstock of a selective hydrogenation reactor.

2. The process according to claim 1, wherein the water is also heated in the water circuit by at least one fluid selected from the following fluids: an overhead vapor stream from a main fractionation column of said fluid catalytic cracking unit, a vapor stream originating from a stage of a cracked gas compressor, a gasoline stream originating from a debutanizer of said fluid catalytic cracking unit, an upper circulating reflux from a main fractionation column of said fluid catalytic cracking unit, an overhead vapor stream from a gasoline separation column of said fluid catalytic cracking unit, a light cycle oil originating from the main fractionation column of said fluid catalytic cracking unit.

3. The process according to claim 1, wherein said propane/propylene separation column system is also fed with a C3 cut originating from a propylene producing unit.

4. The process according to claim 3, wherein said propylene producing unit is a unit for conversion of olefins to propylene.

5. The process according to claim 1, wherein said propane/propylene separation column system comprises a first propane/propylene separation column having a top and a bottom, and a second propane/propylene separation column having a top and a bottom, wherein liquid from the bottom of the second propane/propylene separation column is pumped to the top of the first propane/propylene separation column, overhead vapor from the second propane/propylene separation column is condensed with cooling water and then sent to a reflux drum of the second propane/propylene separation column, propylene is recovered from the top of the second propane/propylene separation column, and propane is recovered from the bottom of the first propane/propylene separation column, wherein the water heated in the water circuit is heated by heat exchange with said one or more process fluids via heat exchangers which are arranged in parallel, wherein the reboiler of the propane/propylene separation column system that is heated by the water circuit is a reboiler at the bottom of the first propane/propylene separation column, and wherein said water circuit is also used to heat an intermediate reboiler of the first propane/propylene separation column.

6. The process according to claim 1, wherein said water in said water circuit is heated by heat exchange with said overhead vapor stream from said fractionation column of said mild hydrocracking unit.

7. The process according to claim 1, wherein said water in said water circuit is heated by heat exchange with said overhead vapor stream from said stripper of said mild hydrocracking unit.

8. The process according to claim 1, wherein said water in said water circuit is heated by heat exchange with said effluent from said hydrodesulphurization reactor of said fluid catalytic cracking gasoline hydrotreatment.

9. The process according to claim 1, wherein said propane/propylene separation column system comprises a plurality of columns arranged in series, and wherein said reboiler that is heated by said water circuit is in the first column in the series of columns.

10. The process according to claim 9, wherein said reboiler is a bottom reboiler in said first column in the series of columns, and wherein said first column in the series of columns also comprises an intermediate reboiler, and said intermediate reboiler is also heated by said water circuit.

11. The process according to claim 10, wherein the water of said water circuit is cooled in said bottom reboiler from 91 C. to 75 C., and the water of said water circuit is cooled in said intermediate reboiler from 75 C. to 65 C.

Description

BRIEF DESCRIPTION OF THE FIGURES

(1) FIG. 1 is a diagram of the hot water loop process according to the present invention showing the possible different hot fluids. The loop itself has as many exchangers as there are new hot fluids utilized; and

(2) FIG. 2 is a flow chart showing a mild hydrocracking unit, cracked gas processor, FCC unit, an FCC gasoline hydrotreatment unit having HDS reactor(s), a selective hydrogenation (SHU) reactor, a propane/propylene separation column system, and a propylene producing unit, and streams associated therewith, in accordance with the present invention.

BRIEF DESCRIPTION OF THE INVENTION

(3) The present invention can be defined as a process for heating the reboiler of the propane/propylene separation column system situated downstream of an FCC unit and fed with the C3 cut from said FCC unit. The expression column system is used to indicate that the propane/propylene separation can be carried out by means of one or more separation columns arranged in series.

(4) When there is a single column, the reboiler is that of the column considered.

(5) When there are several columns arranged in series, the reboiler is that of the first column in the direction of fluid flow, the top of this first column feeding the bottom of the second column and so on if there are more than two columns.

(6) The process according to the present invention consists of heating the water in a hot water circuit by means of one or more process fluids originating from units placed upstream and/or downstream of the FCC unit and called hot fluids, said hot fluids being chosen, alone or in combination, from the following fluids: overhead vapours from the fractionation column of the mild hydrocracking unit upstream of the FCC unit, overhead vapours from the stripper of the mild hydrocracking unit upstream of the FCC unit, effluent from the hydrodesulphurization (HDS) reactor(s) of the FCC gasoline hydrotreatment unit, if there is one downstream of the FCC unit, after heat exchanges with the feedstock of the HDS reactor(s) and with the feedstock of the selective hydrogenation (SHU) reactor.

(7) The heating of the water in the hot water circuit according to the present invention can optionally be completed by the use of at least one of the following fluids in addition to one of the hot fluids: overhead vapours from the main fractionation column of the FCC unit, vapours originating from the different stages of the cracked gas compressor, gasoline originating from the debutanizer of the FCC unit, upper circulating reflux from the main fractionation column of the FCC unit, overhead vapours from the gasoline separation column of the FCC unit, LCO (light cycle oil) originating from the main fractionation column of the FCC unit.

(8) The process of heating the reboiler of the propane/propylene separation column system situated downstream of an FCC unit according to the present invention, is fed with the C3 cut from said FCC unit to which can be added, according to a variant, a C3 cut originating from another process aimed at producing propylene. By way of example of another process (meaning distinct from the FCC), the process of converting olefins to propylene may be mentioned.

(9) The process of heating the reboiler of the propane/propylene separation column (C-1 A) according to the present invention can be defined more precisely when the propane/propylene separation system is constituted by two columns C-1 A and C-1 B connected in series as follows: the liquid at the bottom of the column C-1 B is pumped then sent to the top of the column C-1 A, the overhead vapours of C-1 B are condensed with cooling water then sent into the reflux tank B of the column C-1 B, the propylene (flow 7) is recovered at the top of C-1 B and the propane (flow 8) at the bottom of C-1 A, the two columns (C-1 A and C-1 B) being situated downstream of an FCC unit.

(10) The process according to the invention is defined thus: the water in the hot water circuit is heated from 65 C. (flow 4a) to 91 C. (flow 4b) via exchangers which are in parallel (E-1, E-2, E-3 etc.) by at least one of the following novel process flows: overhead vapours from the fractionation column of the mild hydrocracking unit upstream of the FCC unit (flow 1) by means of the exchanger E-1, overhead vapours from the stripper of the mild hydrocracking unit upstream of the FCC unit (flow 2) by means of the exchanger E-2, effluent from the HDS reactor(s) of the FCC gasoline hydrotreatment unit (flow 3) by means of the exchanger E-3 if there is an FCC gasoline hydrotreatment unit downstream of the FCC unit. The flow 3 having been used beforehand in order to heat the feedstock of the HDS reactor(s), and the feedstock of the selective hydrogenation (SHU) reactor,
the reboiling of the propane/propylene separation column (C-1 A) being carried out at two levels: with a reboiler at the bottom of the column (E-4), heating the flow 5 by means of the hot water at 91 C. (flow 4b) and returning the water at approximately 75 C. (flow 4c), with an intermediate reboiler (E-5), heating the flow 6 by means of the hot water at approximately 75 C. (flow 4c) and returning the water at 65 C. (flow 4d).

DETAILED DESCRIPTION OF THE INVENTION

(11) The present invention falls within the context of supplying calories to the reboiler of the propane/propylene fractionation column located downstream of the fluid catalytic cracking (abbreviation: FCC) unit.

(12) The invention consists of heating the water in a hot water circuit with process fluids from units placed upstream and/or downstream of the FCC unit, optionally in addition to the usual process fluids from the FCC unit already described in the prior art.

(13) The hot water circuit making possible the supply of calories to the reboiler of the propane/propylene fractionation column is described in FIG. 1 according to the invention.

(14) FIG. 1 shows the high-pressure propane/propylene fractionation column, generally constituted by 2 columns (C-1 A and C-1 B) given the high number of trays (between 200 and 300) and the usual height restrictions associated with the siting of industrial columns (approximately 100 metres maximum).

(15) The liquid at the bottom of the column C-1 B is pumped then sent to the top of the column C-1 A.

(16) The overhead vapours of C-1 B are condensed with cooling water then sent into the reflux drum B.

(17) The propylene (flow 7) is recovered at the top of C-1 B and the propane (flow 8) at the bottom of C-1 A.

(18) In the process according to the invention, the water in the hot water circuit is heated from 65 C. (flow 4a) to 91 C. (flow 4b) via exchangers which are in parallel (E-1, E-2, E-3 etc.) by the following new process flows: overhead vapours from the fractionation column of the mild hydrocracking unit upstream of the FCC unit (flow 1) by means of the exchanger E-1, overhead vapours from the stripper of the mild hydrocracking unit upstream of the FCC unit (flow 2) by means of the exchanger E-2, effluent from the HDS reactor(s) of the FCC gasoline hydrotreatment unit (flow 3) by means of the exchanger E-3, if there is an FCC gasoline hydrotreatment unit downstream of the FCC unit. The flow 3 having been used beforehand for heating the feedstock of the HDS reactor(s), and the feedstock of the selective hydrogenation (SHU) reactor.

(19) The fluids in the hot water circuit can also be made up with the process fluids from the FCC unit described in the prior art via the operation F.

(20) The reboiling of the propane/propylene separation column (C-1 A) is carried out at two levels: with a reboiler at the bottom of the column (E-4), heating the flow 5 by means of the hot water at 91 C. (flow 4b), and returning the water at approximately 75 C. (flow 4c), with an intermediate reboiler (E-5), heating the flow 6 by means of the hot water at approximately 75 C. (flow 4c) and returning the water at 65 C. (flow 4d).

(21) In the process according to the invention, it is possible to further heat hot water and thus obtain a reboiling of the propane/propylene fractionation column without consuming low-pressure steam.

(22) Furthermore, the process fluids from the units upstream and downstream of the FCC unit, making it possible to heat the water, have a generally higher temperature than the process fluids from the FCC unit (Table 1 below).

(23) As a result, the difference in temperature between the hot and cold flows in the exchangers (E-1, E-2, E-3 etc.) heating the hot water is greater, which reduces the cost of said exchangers, and therefore the cost of the hot water circuit.

(24) TABLE-US-00001 TABLE 1 Temperatures of the process fluids capable of heating the water of the hot water circuit Temperature Process flow ( C.) New Overhead vapours from the fractionation 120 to 140 flow column (mild hydrocracking unit) according Overhead vapours from the stripper (mild 150 to 180 to the hydrocracking unit) invention Effluent from the HDS reactor(s) (FCC >120 gasoline hydrotreatment unit) Flow Overhead vapours from the main fractiona- 100 to 120 known tion column (FCC unit) from the Gasoline originating from the debutanizer 120 to 180 prior art (FCC unit) Upper circulating reflux of the main fractiona- 120 to 140 tion column (FCC unit) Overhead vapours from the gasoline separation 110 to 130 column (FCC unit) LCO originating from the main fractionation >160 column (FCC unit)

(25) All these flows, new or already known from the prior art, are capable of heating the water circulating in the hot water loop used for reboiling the propane/propylene separation column according to a variant configuration depending on the power necessary for reboiling the propane/propylene fractionation column as well as on the availability of the flow.

(26) The process according to the present invention is implemented as soon as use is made either of the overhead vapour from the fractionation column connected to the mild hydrocracking unit, or of the overhead vapour from the stripper connected to the mild hydrocracking unit, or also of the hot effluent from the HDS reactor(s) (when such a unit exists). Any combination of these three flows, used in part or in full, falls within the scope of the present invention.

(27) The flows having a high temperature are preferred in order to minimize the area of the exchangers utilized. However, any combination of fluids (new or forming part of the prior art), as soon as at least one new fluid among the three preceding ones is used in the hot water loop, must be understood as forming part of the present invention.

(28) Example According to the Invention

(29) A mild hydrocracking unit processing 458 t/h of vacuum distillate (79% originating from vacuum fractionation and 21% originating from a coking unit) produces 304 t/h of residue. The reaction section of the mild hydrocracking unit comprises 3 reactors in series and 7 catalytic beds. The average temperature of each bed is 403 C. during the lifetime of the catalyst. The partial hydrogen pressure is 85 bar (abs) and the hourly space velocity (HSV) is 0.31 h.sup.1.

(30) The residue of the mild hydrocracking unit is sent into an FCC unit operating under severe conditions and with the addition of ZSM-5 to the catalyst in order to maximize the propylene yield.

(31) The propylene yield of the FCC unit is 9% by weight relative to the feedstock.

(32) The FCC unit comprises a LPG (liquefied petroleum gas) fractionation section constituted by a depropanizer, a deethanizer and a high-pressure propane/propylene fractionation column in order to obtain propylene with a purity of 99.6 mol. %.

(33) A C3 cut originating from a coking unit (13 t/h) is added to the LPG originating from the FCC at the inlet to the LPG fractionation section.

(34) The propane/propylene separation column has a feed of 47 t/h the composition by mass of which is as follows: 66% propylene, 33% propane and less than 1% C4+.

(35) The pressure at the bottom of the propane/propylene fractionation column is 22 bar (abs).

(36) The heating power necessary for reboiling the propane/propylene separation column is 52 MW (MW is the abbreviation of megawatt i.e. 10.sup.6 watt).

(37) There is no FCC gasoline hydrotreatment unit downstream of the FCC unit as the sulphur content of the gasoline originating from the FCC unit is less than 10 ppm.

(38) The process fluids from the FCC unit available for heating the water in the hot water circuit are shown in Table 2 below.

(39) The log mean temperature difference (LMTD) is shown for each exchange. The greater the LMTD value, the smaller the exchange surface area will be.

(40) TABLE-US-00002 TABLE 2 Flows available for heating the water in the hot water circuit (according to the prior art) inlet outlet Available process fluids T T Duty LMTD from the FCC unit ( C.) ( C.) (MW) ( C.) Overhead vapours from the 100 70 20 6.8 main fractionation column Gasoline originating from 158 70 11 23.9 the debutanizer Total 31

(41) Only 31 MW of the 52 MW necessary can be supplied inside the FCC unit.

(42) In this example: there is no gasoline separation column, the gasoline at the bottom of the debutanizer first heats the feedstock of the debutanizer then the hot water, the upper circulating reflux from the main fractionation cannot be used, as it heats the reboiler of the deethanizer, the LCO cannot be used as it heats the feedstock of the debutanizer.

(43) In total, 21 MW of low-pressure steam is therefore necessary in order to complete the heating of the reboiler of the propane/propylene fractionation column.

(44) Table 3 below shows the process fluids available for heating the water in the hot water circuit according to the invention.

(45) TABLE-US-00003 TABLE 3 Flows available for heating the water in the hot water circuit (according to the invention) inlet outlet Available process T T Duty LMTD fluids (unit) ( C.) ( C.) (MW) ( C.) Flow Overhead vapours from 100 70 20 6.8 according the main fractionation to the column (FCC unit) prior art Gasoline originating 158 70 11 23.9 from the debutanizer (FCC unit) New flow Overhead vapours from 121 88 34 26.3 according the fractionation to the column (mild hydro- cracking unit) invention Overhead vapours from 150 70 8 21.9 the stripper (mild hydrocracking unit) Total 73

(46) Table 3 shows that the heating power available for heating the water (73 MW) is greater than that required (52 MW). The exchanges with the greatest temperature differences (LMTD) are preferred as they are less costly. In this example, the propane/propylene separation column can be reboiled entirely by means of a hot water circuit comprising the following exchanges for heating the water: overhead vapours from the fractionation column of the mild hydrocracking unit/hot water (34 MW), gasoline originating from the debutanizer/hot water (11 MW), overhead vapours from the stripper of the mild hydrocracking unit/hot water (8 MW).

(47) The hot water no longer needs to be heated by the overhead vapours from the main fractionation column of the FCC unit. This exchange has been dispensed with as it had the smallest temperature difference (LMTD) and therefore the highest exchange surface/exchanged power ratio.