METHOD FOR IMPROVING PROPYLENE RECOVERY FROM FLUID CATALYTIC CRACKER UNIT
20180002255 · 2018-01-04
Assignee
Inventors
Cpc classification
C07C7/005
CHEMISTRY; METALLURGY
B01D53/145
PERFORMING OPERATIONS; TRANSPORTING
C07C7/11
CHEMISTRY; METALLURGY
C10G7/02
CHEMISTRY; METALLURGY
International classification
C07C7/11
CHEMISTRY; METALLURGY
Abstract
The present invention relates to a method for treating a cracked stream stemming from a fluid catalytic cracker unit (FCCU) in order to improve propylene recovery. The present invention also relates to the corresponding installation to implement the method.
Claims
1. Method for treating a cracked stream stemming from a fluid catalytic cracker unit (FCCU) comprising the following steps: compressing and partly condensing the gas stream from the main fractionator column overhead receiver of the FCCU; separating the partly condensed gas stream in order to recover an upstream liquid and an upstream gas; heating the upstream liquid; introducing this heated liquid into an upstream stripper for recovering at the top of the stripper a stream rich in C2 compounds and at the bottom a first liquid stream rich in C3+ hydrocarbons; introducing the first liquid stream rich in C3+ into a first heat exchanger and then into a second heat exchanger; introducing the liquid recovered from the second heat exchanger into a stabilizer column for recovering at the top of the stabilizer column a stream rich in C3 and C4 hydrocarbons and from the side of the stabilizer column a liquid stream rich in C5 and C6 hydrocarbons and from the bottom of the stabilizer column a liquid stream rich in C5, C6 and C7+ hydrocarbons; introducing the liquid stream rich in C5 and C6 hydrocarbons into the first heat exchanger; introducing a liquid stream from stabilizer column bottom into a primary absorber and introducing the upstream gas into a primary absorber for recovering at the top of the primary absorber a first gas stream; and at the bottom of the primary absorber a second liquid stream; introducing lean oil from FCCU main fractionator into a sponge absorber; cooling the first gas stream from primary absorber and introducing it into a propylene absorber; cooling the liquid stream rich in C5 and C6 hydrocarbons from the first heat exchanger; introducing the liquid stream rich in C5 and C6 hydrocarbons recovered from the first heat exchanger into the propylene absorber; recovering a bottom liquid rich in C3 hydrocarbons at the bottom of the propylene absorber and a top gas poor in C3 hydrocarbons at the top of the propylene absorber; introducing the top gas recovered at the top of the propylene absorber into the sponge absorber, preferably to recover a fuel gas and a rich oil.
2. Method according to claim 1, comprising a further step of mixing the liquid rich in C3 hydrocarbons, from the propylene absorber with the stream resulted from the compression and partial condensation of the gas stream from the main fractionator before the separation of the resulting stream into the upstream liquid and the upstream gas.
3. Method according to claim 1 further comprising the step of introducing the liquid rich in C5 and C6 hydrocarbons recovered from the first heat exchanger into a second heat exchanger before its introduction into the propylene absorber, advantageously with cooling water.
4. Method according to claim 1 further comprising the step of introducing the liquid rich in C5 and C6 hydrocarbons recovered from the second heat exchanger into a third heat exchanger before its introduction into the propylene absorber.
5. Method according to claim 1, comprising the following steps of: introducing the stream rich in C3 and C4 hydrocarbons into a condenser; cooling the stream retrieved from this condenser; separating the obtained stream into a liquid stream which is introduced into the stabilizer column and into a liquid stream sent to a LPG (Liquefied Petroleum Gas) treating unit to recover LPG.
6. Method according to claim 1, wherein the stream rich in C2 is mixed with the stream resulted from the compression and partial condensation of the gas stream from the main fractionator overhead receiver before the separation of the resulting stream into the upstream liquid and the upstream gas.
7. Method according to claim 1, wherein the second liquid fraction is mixed with the stream resulted from the compression and partial condensation of the gas stream from the main fractionator before the separation of the resulting stream into the upstream liquid and the upstream gas.
8. Method according to claim 1, wherein the bottom liquid rich in C3 from the propylene absorber is mixed with the stream resulting from the compression and partial condensation of the gas stream from the main fractionator before the separation of the resulting stream into the upstream liquid and the upstream gas.
9. Method according to claim 1, wherein a gas stream from PRU rich in propylene is mixed with the stream resulting from the compression and partial condensation of the gas stream from the main fractionator before the separation of the resulting stream into the upstream liquid and the upstream gas.
10. Method according to claim 5, wherein the first gas stream is cooled before being introduced into the propylene absorber.
11. An installation for treating a cracked stream stemming from a fluid catalytic cracker unit (FCCU) comprising: means for compressing and partly condensing a gas stream from the main fractionator column receiver of the FCCU (1); means for separating the partly condensed gas stream to recover an upstream liquid and an upstream gas; for heating the upstream liquid; a stripper column and means for introducing the heated upstream liquid into the stripper in order to recover at the top of the stripper a stream rich in C2 compounds and at the bottom of the stripper a first liquid stream rich in C3+ hydrocarbons; a first heat exchanger and means for introducing into this first heat exchanger the first liquid stream rich in C3+ hydrocarbon; a stabilizer column and means for introducing the liquid stream rich in C3+ hydrocarbons from the first heat exchanger into the stabilizer column to recover from the side of the stabilizer column a first liquid stream rich in C5 and C6 hydrocarbons and at the top of the stabilizer column a gas stream rich in C3 and C4 hydrocarbons; means for introducing the first liquid stream rich in C5 and C6 hydrocarbons into the first heat exchanger; means for cooling the liquid stream rich in C5 and C6 hydrocarbons from the first heat exchanger; a primary absorber and means for introducing to said primary absorber a liquid stream rich in C5, C6 and C7+ hydrocarbons from stabilizer column and the upstream gas from the separator for recovering at the top of the primary absorber a first gas stream and at the bottom of the primary absorber a liquid stream; a propylene absorber and means for introducing to this propylene absorber the cooled liquid stream rich in C5 and C6 hydrocarbons; a sponge absorber and means for introducing to this sponge absorber a lean oil; means for cooling the first gas stream from the primary absorber; means for introducing into the propylene absorber the first gas stream from the primary absorber for recovering at the top of the propylene absorber a gas stream poor in C3 hydrocarbons and at the bottom of the propylene absorber a liquid stream rich in C3 hydrocarbons; means tier introducing into the sponge absorber the gas stream poor in C3 hydrocarbons recovered at the top of the propylene absorber.
12. Installation according to claim 11 further comprises a second heat exchanger and means for introducing into said second heat exchanger the liquid stream rich in C5 and C6 hydrocarbons recovered from the first heat exchanger and advantageously with cooling water.
13. Installation according to claim 11 further comprises a third heat exchanger and means for introducing into said third heat exchanger the liquid stream rich in C5 and C6 hydrocarbons ecovered from the second heat exchanger and advantageously a cold propylene stream.
14. Installation according to claim 11 further comprises a fourth heat exchanger and means for introducing into this fourth heat exchanger the liquid rich in C5, C6 and C7+ hydrocarbons and the liquid stream rich in C3+ hydrocarbons recovered from the first heat exchanger before introduction of the resulting stream rich in C3+ hydrocarbons into the stabilizer column.
15. Installation according to claim 11 further comprises a treatment unit of the liquid stream rich in C3 and C4 hydrocarbons from the stabilizer column comprising: a condenser and means for introducing into this condenser the liquid stream rich in C3 and C4 hydrocarbons; a heat exchanger (4-8) and means for introducing into this heat exchanger the stream retrieved from the condenser; separation means for separating the obtained stream into a liquid stream which is introduced into the stabilizer column and a liquid stream sent to a LPG treating unit to recover LPG.
16. Installation according to claim 11 further comprises means for recycling and mixing the stream rich in C2 compounds with the stream resulting from the compression and partial condensation of the gas stream from the main fractionator before the separation of the resulting stream into the upstream liquid and the upstream gas.
17. Installation according to claim 11 further comprises means for recycling and mixing the liquid stream from the primary absorber with the stream resulting from the compression and partial condensation of the gas stream from the main fractionator before the separation of the resulting stream into the upstream liquid and the upstream gas.
18. Installation according to claim 11 further comprises heat exchanger and means for introducing into this heat exchanger the gas stream from the primary absorber before introduction into the propylene absorber.
Description
[0094] The invention will be better understood upon reading the description which follows, only given as an example and made with reference to the appended drawing wherein
[0095] In all of the following, a same reference designates a stream flowing in a conduit and the conduit which conveys this stream. Moreover, unless indicated otherwise, the pressures are meant to be in relative bars.
[0096] The installation according to the invention is illustrated in
[0097] In this installation, the propylene absorber 15 is in between the primary absorber 13 and the sponge absorber 16. The method according to the invention starts by providing a gas stream 101 having wide range of hydrocarbons from C1 to C7+ with impurities like nitrogen, CO.sub.2, H.sub.2S, water vapour etc. from the main fractionator column overhead receiver of an FCCU 1. The gas stream 101 has generally a temperature comprised between 30 and 50° C., preferably between 38 and 43° C., and a pressure generally comprised between 0.5 and 2.5 barg, especially between 1.0 and 2.0 barg. Its molar content in propylene is generally comprised between 15 and 50 mol %, preferably between 25 and 45 mol %. The gas stream 101 is compressed and partially condensed into a compressor/condenser 2. The pressure of the compressed gas stream is for example comprised between 14 barg and 16 barg and the liquid molar content is higher than 70 mol %, preferably comprised between 70 and 80 mol %. The resulting stream is introduced into a separator 3 which enables to recover an upstream liquid 102 and an upstream gas 103. The separator 3 is preferably a high pressure receiver, operating for example at a pressure higher than 14 barg. The upstream liquid 102 is pumped, thanks to a pump 4, and heated into a heat exchanger 5, advantageously with stabilizer column bottom stream 107. The resulting heated stream, preferably at a temperature comprised between 50 and 70° C., preferably between 55 and 65 ° C., is introduced into an upstream stripper 6 for recovering at the top of the stripper a stream 104 rich in C2 compounds and at the bottom of the stripper a liquid stream 105 rich in C3+ hydrocarbons. The stripper 6 generally operates at a pressure comprised between 14 and 17 barg, preferably between 15 and 16 barg. The molar content of C3+ hydrocarbons in stream 104 is generally lower than 45 mol %. The molar content of Cl, C2 hydrocarbons in stream 104 is for example comprised between 20 and 50 mol %, preferably between 30 and 40 mol %. The stream 104 is generally at a temperature comprised between 50 and 70° C., preferably between 60 and 65 ° C. The stream 105 is generally at a temperature comprised between 85 and 110° C., preferably between 95 and 100 ° C. The molar content of C3+ hydrocarbons in stream 105 is generally higher than 95 mol %, preferably higher than 99 mol %. The stream 104, rich in C2 compounds, is optionally recycled and mixed with the stream from the compressor/condenser 2. The liquid stream 105 rich in C3+ hydrocarbon is introduced into a first heat exchanger 7 and optionally into a second heat exchanger 8 to be heated at a temperature more than 105° C., the resulting stream is introduced into an upstream stabilizer column 9 for recovering a side liquid stream 106 rich in C5 and C6 hydrocarbons and a second bottom liquid stream 108 rich in C5, C6 and C7+ hydrocarbons and a gas stream 110 rich in C3 and C4 hydrocarbons. The stabilizer column generally operates at a pressure comprised between 10.5 and 12.5 barg, preferably between 11 and 12 barg. The molar content of C3 hydrocarbons in stream 106 and in stream 107 is practically nil (lower than 10 ppm). The molar content of C5 and C6 hydrocarbons in stream 106 is generally higher than 93 mol %. The molar content of C7+ hydrocarbons in stream 106 is generally lower than 22 mol %©. The molar content of C5 and C6 hydrocarbons in stream 110 is generally lower than 1 mol %. The molar content of C3 and C4 hydrocarbons in stream 110 is generally higher than 98 mol %. The liquid stream 107 is introduced into the second heat exchanger 8 to be cooled at a temperature comprised between 90 and 120° C., preferably between 100 and 110° C., and the resulting stream can be separated into two streams—a stabilized gasoline stream 108 for storage and a recycle gasoline stream 109 which can be introduced for example into the primary absorber 13. Stream 107 can also be used in heat exchanger 5 to heat stream 102. Stream 106 is introduced into the first heat exchanger 7 and the resulting stream is introduced into a cooler 10 thanks to a pump 11 and the resulting cooled stream 106 at a temperature lower than 50° C., preferably lower than 42 ° C., is introduced into a heat exchanger 12 to be cooled at a temperature comprised between 20 and 40° C., preferably between 28 and 32° C., with a stream of cold propylene 113, preferably from a propylene recovering unit (PRU). A cooled stream 106 is recovered; this stream has generally at a temperature lower than 40° C., preferably lower than 31° C. Stream 106 is introduced into a propylene absorber 15 and a hot stream of propylene 114, generally at a temperature between 20 and 35° C., preferably between 28 and 30 ° C., which can be sent back to a propylene recovery unit. Recycle Gasoline stream 109 from the stabilizer column bottom is introduced into a primary absorber 13 for recovering a first gas stream 111 and a liquid stream 112 which can be recycled, thanks to a pump 22, and mixed with the stream 101 from the compressor/condenser 2. The gas stream 111 is preferably cooled to a temperature advantageously lower than 40° C. in a heat exchanger 14, preferably with water, before being introduced into the bottom of propylene absorber 15 for recovering at the bottom a liquid fraction 115 rich in C3 hydrocarbons which is preferably recycled and mixed with the stream 101 from the compressor/condenser 2, and at the top a gas stream 116. The propylene absorber generally operates at a pressure comprised between 12.5 and 14 barg, preferably between 12.9 and 13.5 barg. The molar content of C3 and C4 hydrocarbons in stream 115 is generally greater than 10 mol %, preferably greater than 13 mol %. The molar content of C3 hydrocarbon in stream 116 is generally lower than 10 mol %, preferably lower than 7 mol %. The gas stream 116 is then introduced into a sponge absorber 16, which generally operates at a pressure comprised between 12.5 and 14 barg, preferably between 13 and 13.6 barg, a lean oil is also introduced into the sponge absorber 16 for recovering a fuel gas 118 which can be sent to sweetening and a rich oil 119 which can be recycled to the main fractionator column of the FCCU. The stream 110 rich in C3 and C4 hydrocarbons can be introduced into a stabilizer condenser 17, which generally operates at a pressure comprised between 10.5 and 12 barg, preferably between 11 and 11.3 barg, the resulting stream being introduced into a stabilizer receiver and then separated into two stream, LPG stream 120 which can be sent, thanks to a pump 20 to a LPG treating unit, and a liquid stream 121 which is recycled thanks to reflux pump 21 to the stabilizer column 9. The C3 and C4 molar content of stream 110 is advantageously higher than 98 mol %.
[0098] Examples of temperature, pressure and flow rates are given for a particular embodiment in the following table:
TABLE-US-00001 Temperature Pressure Flow rate Flow (° C.) (barg) (kmol/h) 101 40 1.4 1778 101 after 2 40 13.2 4480 102 40 13.1 3457 102 after 4 40 20 3457 102 after 5 60 19.5 3457 103 40 13.1 1023 104 62 14.9 833 105 98 15.3 2624 105 after 7 92 11.6 2624 105 after 8 109 11.4 2624 106 140 11.5 300 106 after 7 93 11.3 300 106 after 10 40 11 300 106 after 11 40 13.1 300 106 after 12 30 12.9 300 107 183 11.6 1018 107 after 8 110 11.4 1018 107 after 5 64 11.2 1018 107 after 23 40 11 1018 108 40 11 695 109 40 11 323 109 after 24 40 13.5 323 110 59 11.2 3130 110 after 17 55 11.1 3130 110 after 18 40 10.9 3130 110 after 19 40 10.9 3130 111 55.5 13.4 519 111 after 14 40 13.2 519 112 54.4 13.8 1529 113 21 22.4 575 114 29 22.2 575 115 38 13.2 364 116 43 12.9 455 117 40 12.9 85 118 51.6 12.7 405 119 60 12.9 135 120 40 10.9 1304 121 40 11.3 1825 122 38 32.5 23
[0099] Results of the method according to the invention are detailed in the following table.
TABLE-US-00002 Propylene absorber operating parameters Pressure (top) Hg/cm2g 12.9 Temperature (Top/Bot) ° C. 43/38 Absorbent inlet temperature ° C. 30 Gas inlet temperature ° C. 40 Conventional scheme Invention Propylene potential from Kmol/h 591.03 591.03 FCCU Total propylene loss kmol/h 33.42 16.97 % overall propylene recovery % 94.35 97.13 Propylene product flow rate Kg/h 23493 24206 (99.8% pure)
The provision of a propylene absorber greatly increases the propylene recovery by more than 2.5% with a low investment.
[0100] The method and installation according to the invention are particularly efficient and easy to operate, allowing an upgrade of existing installation and/or conception of very profitable new installations.