Dehydrogenation separation unit with mixed refrigerant cooling

Abstract

To provide a system and method for separating olefinic hydrocarbon and hydrogen in an effluent fluid stream from a dehydrogenation reactor.SOLUTION: The system includes a heat exchanger, which receives and partially condenses the effluent fluid stream so that a mixed phase effluent stream is formed. A primary separation device receives the mixed phase effluent stream, and separates it into a primary vapor stream and a primary liquid product stream. The heat exchanger receives and partially condenses the primary vapor stream so that a mixed phase primary stream is formed. A secondary separation device receives the mixed phase primary stream, and separates it into a secondary vapor stream and a secondary liquid product stream. A heat exchanger receives and warms the secondary vapor stream to provide refrigeration for partially condensing the effluent fluid stream, and a heat exchanger receives and warms the secondary vapor stream to provide refrigeration for partially condensing the primary vapor stream. A mixed refrigerant compression system provides a refrigerant to a heat exchanger to provide refrigeration.SELECTED DRAWING: Figure 1

Description

[Technical field]

[0001] Claiming priority

[0001] This application claims the benefit of U.S. Provisional Application No. 62 / 743,263, filed October 9, 2018, the contents of which are incorporated herein by reference. [Background technology]

[0002]

[0002] Propane dehydrogenation (PDH) separation systems are known in the art. An example of such a system is described in commonly owned U.S. Patent No. 6,333,445, the contents of which are incorporated herein by reference.

[0003]

[0003] Current designs for PDH separation systems require that the reactor effluent vapor stream be compressed to high pressure (approximately 1.2 MPa (12 bar gauge)) using a reactor effluent compressor and then reduced pressure using two generator-mounted or compressor-mounted cryogenic turboexpanders to provide the refrigeration necessary for separation and recovery of the liquid olefin products.

[0004]

[0004] Disadvantages of such prior art systems include the overall process power consumption, the additional cost and maintenance requirements of a turboexpander / generator (or compressor) set, the required high reactor effluent compressor discharge pressure (which increases capital and operating costs), and the lack of flexibility to significantly adjust the olefin and hydrogen separation temperatures. Summary of the Invention [Means for solving the problem]

[0005]

[0005] There are several aspects of the present subject matter that may be implemented separately or together in devices and systems, as described and claimed below. These aspects may be used alone or in combination with other aspects of the subject matter described herein, and the description of these aspects together is not intended to preclude the use of these aspects separately or the claiming of such aspects separately or in different combinations as described in the claims appended hereto.

[0006] In one embodiment, a system for separating olefinic hydrocarbons and hydrogen in an effluent fluid stream from a dehydrogenation reactor includes a main heat exchanger configured to receive and partially condense the effluent fluid stream such that a mixed-phase effluent stream is formed. A primary separation device is in fluid communication with the main heat exchanger to receive and separate the mixed-phase effluent stream into a primary vapor stream and a primary liquid product stream. The main heat exchanger configured to receive and partially condense the primary vapor stream such that a mixed-phase primary stream is formed. A secondary separation device is in fluid communication with the main heat exchanger to receive and separate the mixed-phase primary stream into a secondary vapor stream and a secondary liquid product stream. The main heat exchanger is configured to receive and warm the secondary vapor stream to provide refrigeration for partially condensing the effluent fluid stream and the primary vapor stream. A mixed refrigerant compression system is further configured to provide refrigerant to the main heat exchanger.

[0007] In another aspect, a system for separating olefinic hydrocarbons and hydrogen in an effluent fluid stream from a dehydrogenation reactor includes a cold box feed heat exchanger (c) configured to receive and partially condense the effluent fluid stream such that a mixed-phase effluent stream is formed. The system includes a cold box feed heat exchanger. A primary separation device is in fluid communication with the cold box feed heat exchanger to receive and separate the mixed phase effluent stream into a primary vapor stream and a primary liquid product stream. A mixed refrigerant heat exchanger is configured to receive and partially condense the primary vapor stream such that a mixed phase primary stream is formed. A secondary separation device is in fluid communication with the mixed refrigerant heat exchanger to receive and separate the mixed phase primary stream into a secondary vapor stream and a secondary liquid product stream. The mixed refrigerant heat exchanger is configured to receive and warm the secondary vapor stream to provide refrigeration for partially condensing the primary vapor stream. The cold box feed heat exchanger is configured to receive and further warm the secondary vapor stream after it exits the mixed refrigerant heat exchanger to provide refrigeration for partially condensing the effluent fluid stream. A mixed refrigerant compression system is configured to provide refrigerant to the mixed refrigerant heat exchanger.

[0008]

[0008] In yet another aspect, a method for separating olefinic hydrocarbons and hydrogen in an effluent fluid stream from a dehydrogenation reactor includes the steps of partially condensing the effluent fluid stream to form a mixed phase effluent stream; separating the mixed phase effluent stream into a primary vapor stream and a primary liquid product stream; partially condensing the primary vapor stream to form a mixed phase primary stream; separating the mixed phase primary stream into a secondary vapor stream and a secondary liquid product stream; warming the secondary vapor stream to provide refrigeration for partially condensing the effluent fluid stream and the primary vapor stream; and providing refrigerant from a mixed refrigerant compression system to a main heat exchanger. [Brief description of the drawings]

[0009] [Figure 1] 1 is a schematic diagram of a first embodiment of the system of the present disclosure. [Diagram 2]

[0010] FIG. 2 is a schematic diagram of a second embodiment of the system of the present disclosure. [Diagram 3]

[0011] FIG. 13 is a schematic diagram of a third embodiment of the system of the present disclosure. [Figure 4]

[0012] FIG. 13 is a schematic diagram of a fourth embodiment of the system of the present disclosure. [Diagram 5]

[0013] FIG. 13 is a schematic diagram of a fifth embodiment of the system of the present disclosure. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0010]

[0014] The present invention herein is a dehydrogenation separation apparatus that uses a mixed refrigerant (MR) system consisting of a MR compressor with heat exchangers and drums to provide the refrigeration necessary for the separation and recovery of the liquid olefin products. By way of example only, the MR system may use a single mixed refrigerant system or may be a single mixed refrigerant system that is pre-cooled using a second refrigerant.

[0011]

[0015] While achieving the same product recovery as prior art systems, some of the benefits may include: 1) lower power consumption throughout the process; 2) both turbo expander / generator (or compressor) sets are eliminated; 3) the required reactor effluent compressor discharge pressure is significantly reduced, thereby saving capital and operating costs; 4) operation, maintenance, and reliability of the separation system are improved with the MR process compared to the turbo expander process; 5) the MR process allows for a more robust and tolerant design of the main feed heat exchanger; and 6) the MR process provides an independent means to adjust the refrigeration level to the separation system without affecting the recycle effluent compressor.

[0012]

[0016] Since propylene refrigeration is used in many PDH facilities, the MR process described herein uses propylene refrigeration to pre-cool the MR refrigerant and reduce MR compressor power consumption. Pre-cooling also allows the MR component mixture to be simplified, requiring only methane, ethylene (or ethane), and propylene (or propane), although ethylene and propylene are preferred. With no C4 or C5 in the MR mixture, the possibility of reactor catalyst fouling is reduced.

[0013]

[0017] Although the description of the invention presented below is specific to a propane dehydrogenation unit, the same process can be used for butane dehydrogenation.

[0014]

[0018] Referring to FIG. 1, the reactor effluent gas is compressed to approximately 720 kPa (7 The gas is compressed to a pressure of 1.2 bar gauge (0.2 bar gauge) and the heat of compression is removed before entering the cryogenic separation system as cold box vapor feed 8. The gas is delivered to cold box feed heat exchanger 9 where it is partially condensed and then flows to outlet primary separator 10. The vapor and liquid are separated, the liquid stream containing a portion of the C3 olefin product and the vapor stream 17 containing hydrogen and the remaining olefin product.

[0015]

[0019] This vapor stream 17 flows to a mixed refrigerant heat exchanger 11 (MR exchanger) where it is further cooled and partially condensed to the required temperature to achieve the desired product recovery. The partially condensed stream flows to a secondary separator 12 and is separated into a liquid olefin product and a hydrogen-rich vapor stream 21. The hydrogen-rich stream is reheated in the MR exchanger and then split into two streams - recycle gas 13 (which is the hydrogen required for the combined reactor feed) and net vapor 16, which is the remainder of the hydrogen stream and is discharged from the separation system.

[0016]

[0020] The net vapor stream is reheated and refrigeration is recovered in the Fresh Feed heat exchanger, which has a cold end 26 and a warm end 32. The liquid product streams (from the primary separator 10 and the secondary separator 12) are combined to form a combined liquid product stream 18 which flows to the Fresh Feed heat exchangers 26, 32.

[0017]

[0021] The cold box vapor feed 8 ("reactor effluent") is first cooled in the cold box feed exchanger. The feed is cooled primarily by the combined reactor feed 14 and secondarily by a portion 24 of the exhaust net vapor product 16. The combined reactor feed provides the majority of the refrigeration in the cold box feed heat exchanger 9 by combining the recycle gas stream 13 with a cold fresh feed liquid stream 15 (such as propane or n-butane) and vaporizing the combined stream. The cold fresh feed liquid stream 15 is formed from the fresh feed inlet stream 23 which is subcooled in the fresh feed heat exchanger at 26 and 32 before entering the cold box feed heat exchanger 9. Refrigeration for the fresh feed is provided by recovering cold from the C3 olefin product 18 and from a portion of the net vapor product 16.

[0018]

[0022] Flash gas (recycle) 19 is produced by partially warming the separator liquid in the cold end 26 of the fresh feed exchanger. The resulting vapor-liquid mixture 27 is separated in a liquid product tank 28. Vapor from tank 28 is warmed in the warm end 32 of the fresh feed exchanger and flash gas 19 is recycled to the suction of the upstream reactor effluent compressor (see FIG. 1 of U.S. Pat. No. 6,333,445). Liquid product from tank 28 is pumped in and pumped out by pump 34 and additional cold is recovered in the warm end 32 of the fresh feed exchanger.

[0019]

[0023] The overall refrigeration balance for the separation system is provided by the MR compression system, generally shown at 38 in FIG. 1, via final cooling in a mixed refrigerant (MR) exchanger (MRHX) 11. Although a C3 pre-cooled MR system is described here, a single MR system may also be used. FIG. 1 shows a single stage MR compressor 40, followed by an air or water cooler 42, followed by a C3 (propylene) pre-cooler 44. The pre-cooler may utilize as many stages of refrigeration as required to obtain the desired temperature, and two stages are shown for simplicity. The MR refrigerant is separated by separator 46 into vapor phase stream 31 and liquid phase stream 33, respectively, and delivered to the MRHX 11. The MR vapor stream 31 is cooled and condensed in the MRHX 11 and flashed at 35 to produce the coldest refrigerant for the process and the low pressure refrigerant stream 37. The MR liquid stream 33 is further cooled in the MRHX and flashed at 41 and delivered to the low pressure refrigerant stream 37 which joins and mixes with the low pressure refrigerant stream 37 at a warmer temperature. A common refrigerant return stream 47 exits the MRHX as a mixed phase vapor / liquid stream. Before being compressed, the vapor and liquid are separated by separator 48. The liquid is pumped to a higher pressure by pump 49 and the vapor is compressed in compressor 40 to the required discharge pressure. The system uses typical MR compositions appropriate for the specific design conditions.

[0020]

[0024] The heat exchangers illustrated in FIG. 1 and described above may be combined or consolidated into a single main heat exchanger.

[0021]

[0025] Referring to FIG. 2, in a second embodiment of the system, the suction drum for the MR compressor can also be designed to act as a heavy component refrigerant accumulator. The MR system can operate with excess heavy components (such as C3, C4, or C5) in the refrigerant, and the resulting MR is, at least temporarily, a two-phase flow 52 exiting the exchanger 11. These excess heavy components are separated in the compressor suction drum 50 and remain in the drum. The refrigerant vapor flowing to the MR compressor 40 is now at its dew point, and the system automatically operates at dew point conditions. When "make-up" refrigerant is added to the system, the accumulated heavy components will then be balanced with the light components against the dew point at the suction pressure and temperature. If needed, the heavy components can be preferentially removed from the refrigeration system in the suction accumulator or preferentially added and held in the suction drum.

[0022]

[0026] In a third embodiment of the system, illustrated in Figure 3, the reactor effluent gas is compressed to about 720 kPa (7.2 bar gauge) in a REC compressor and the heat of compression is removed by ambient exchanger (air or water) cooling before entering the cryogenic separation system as cold box vapor feed 108. The gas is delivered to main heat exchanger 110 where it is cooled and partially condensed and then flows to primary separator 112. Vapor and liquid are separated, liquid stream 114 containing a portion of the C3 olefin product and vapor stream 116 containing hydrogen and the remaining olefin product. This vapor stream flows back to main heat exchanger 110 where it is further cooled and partially condensed to achieve the desired product recovery. The partially condensed stream 118 flows to secondary separator 122 and is separated into a liquid olefin product 124 and a hydrogen-rich stream 126. The hydrogen-rich vapor stream is reheated in the main heat exchanger and then split at 130 into two streams - recycle gas 132 (which is the hydrogen required for the combined reactor feed 133) and net vapor 134 (which is the remainder of the remaining hydrogen stream and will be discharged from the separation system). The net vapor stream is reheated and refrigeration is recovered in the main heat exchanger.

[0023]

[0027] Warm fresh propane feed 138 is delivered to the main heat exchanger 110 and cooled to the same temperature as the primary separator 112. The cooled fresh propane feed 142 is then mixed with the recycle gas 132 to form the combined reactor feed 133. This stream is reheated and refrigeration is recovered in the main heat exchanger. This provides the majority of the refrigeration for the cryogenic separation system.

[0024]

[0028] The liquid product streams 114 and 124 (from the primary separator 112 and the secondary separator 122) are then passed through the main heat exchangers 116 and 128 at appropriate locations relative to the respective temperatures of those streams. The liquid product stream is fed to the main heat exchanger 110 where it is heated and partially vaporized. The liquid product stream exits the main heat exchanger through a common header to form liquid product stream 146. This orientation of the liquid product stream improves efficiency, reduces piping complexity, and reduces the risk of freezeout.

[0025]

[0029] The partially vaporized mixed C3 liquid product stream 146 is delivered to a liquid product tank 150. Vapor 152 (flash gas) from the liquid product tank is heated in the main heat exchanger and then recycled to the suction of the upstream reactor effluent compressor as flash gas stream 154. Liquid 156 (liquid product) from the liquid product tank is pumped by pump 158 and then heated in the main heat exchanger for additional energy recovery. The warmed liquid product exits the main heat exchanger as C3 product stream 162.

[0026]

[0030] The overall refrigeration balance for the separation system is provided by a mixed refrigerant (MR) system, generally shown at 168. The embodiment of FIG. 3 uses a two-stage MR compressor 172 with air or water intercooling and discharge cooling. The first MR compressor stage discharge 174 is partially condensed at 175 and delivered to an MR interstage drum 176. Vapor 178 is delivered to a second MR compressor stage and liquid 182 is delivered to the main heat exchanger 110. The second MR compressor stage discharge 184 is partially condensed at 185 and separated in an MR accumulator 186. MR accumulator vapor 192 and liquid 194 are delivered to the main heat exchanger 110. The MR accumulator vapor is partially condensed in the main heat exchanger and the resulting stream 196 is delivered to a cold vapor separator drum 202 to improve process efficiency. The cold vapor separator steam 204, cold vapor separator liquid 206, MR accumulator liquid 194, and MR interstage liquid 182 are all condensed and pre-cooled in the main heat exchanger 110. All of these flows exit the exchanger and are flashed through JT valves (by way of example only), and the resulting mixed phase flows are separated and sent back to the main heat exchanger via standpipes 212, 213, 214, and 216 at the appropriate temperature to provide the necessary refrigeration equilibrium for the separation system. Additional details regarding the operation of the MR system 168 are available in commonly owned U.S. Patent Application Publication No. US2014 / 0260415 to Ducote, Jr. et al., the entire contents of which are incorporated herein by reference.

[0027]

[0031] The flashed low pressure MR streams are mixed in the main heat exchanger and exit as a single superheated vapor stream 220 that is delivered to the MR compressor suction drum 224. The system uses a typical MR composition appropriate for the specific design conditions.

[0028]

[0032] The MR system allows for the integration of additional heat transfer equipment, at ambient temperature or cooler, into the main heat exchanger. As an example, FIG. 3 shows the integration of the deethanizer fractionator condenser (deethanizer overhead inlet stream 226 and deethanizer overhead outlet stream 228) into the main heat exchanger. This increases the size of the MR system due to the additional refrigeration load required, but eliminates the need for a separate C3 refrigeration system for the deethanizer fractionator condenser equipment, thereby reducing the overall equipment count for the dehydrogenation plant.

[0029]

[0033] In a fourth embodiment of the system of the present disclosure, illustrated in Fig. 4, an intermediate stage separation device 406 is added to the system of Fig. 1. The mixed-phase MR flow 402 from the MR heat exchanger 11 (starting as a liquid outlet of the separator 46 before entering the MR heat exchanger) is combined with the mixed-phase MR flow 404 from the outlet of the first stage of the compressor 40. The combined flow is directed to the inlet of the separation device 406, and the resulting vapor flow 408 is directed into the inlet of the second stage of the compressor 40. The outlet of the second stage of the compressor 40 is directed to the cooling devices 42 and 44, and the processing of the MR flow then continues as described above with respect to Fig. 1, except that the flow 33 after cooling in the mixed refrigerant heat exchanger 11 and flashing by the valve 41 does not merge with the low pressure refrigerant flow 37. However, in an alternative embodiment, a portion of stream 33 after cooling in mixed refrigerant heat exchanger 11 and flashing through valve 41 may be combined with low pressure refrigerant stream 37 .

[0030]

[0034] In a fifth embodiment of the system of the present disclosure, illustrated in Figure 5, an interstage separation device 506 is added to the system of Figure 2. The mixed-phase MR flow 502 from the MR heat exchanger 11 is combined with the mixed-phase MR flow 504 from the outlet of the first stage of the MR compressor. The combined flow is directed to the inlet of the separation device 506 and the resulting vapor flow 508 is directed into the inlet of the second stage of the MR compressor. The outlet of the second stage of the MR compressor is directed to one or more cooling devices and the processing of the MR flow then continues as described above with respect to Figure 4.

[0031]

[0035] The heat exchangers mentioned in the description may be combined with the use of multi-flow heat exchangers, such as brazed aluminum plate fin heat exchangers, to simplify piping design, plant layout, or performance. Examples of combinations may be a fresh feed-2 exchanger and a fresh feed-1 exchanger, or a cool box feed exchanger and both fresh feed exchangers. Other combinations may be more desirable.

[0032]

[0036] While preferred embodiments of the present invention have been shown and described, it will be apparent to those skilled in the art that changes and modifications can be made in those embodiments without departing from the scope of the invention.

Claims

1. 1. A system for separating olefinic hydrocarbons and hydrogen in an effluent fluid stream from a dehydrogenation reactor, comprising: a. a main heat exchanger configured to receive and partially condense an effluent fluid stream such that a mixed-phase effluent stream is formed; b. a separation system configured to receive and separate the mixed-phase effluent stream into a separated vapor stream comprising hydrogen and a separated liquid stream comprising olefinic hydrocarbons; c. a splitter configured to receive the separated vapor flow and split it into a recycle gas flow and a net vapor flow; d. a junction configured to receive and combine at least a portion of the propane flow and the recycle gas flow, the propane flow being independent of the effluent fluid flow, to form a combined flow; e. a main heat exchanger configured to receive and warm the net vapor flow, the combined flow, and the separated liquid flow to provide refrigeration in the main heat exchanger; f. a mixed refrigerant compression system configured to provide refrigeration in the main heat exchanger; Equipped with the main heat exchanger includes a warm end receiving the effluent fluid flow and a cold end at which the mixed-phase effluent flow exits the main heat exchanger; The system further comprises a propane feed expansion device configured to receive and expand a feed stream comprising propane, the feed stream being independent of the effluent fluid stream such that an expanded feed stream is generated; the main heat exchanger is also configured to receive and warm the expanded feed fluid stream at the warm end to provide cooling to the effluent fluid stream. system.

2. the main heat exchanger includes a primary refrigeration passage; The mixed refrigerant compression system comprises: i) a suction separation device configured to receive a mixed-phase refrigerant flow from the primary refrigeration passage of the main heat exchanger; ii) a compressor having an inlet in fluid communication with the suction separation device; iii) a first stage cooling device having an inlet in fluid communication with an outlet of the compressor; iv) a discharge separation device having an inlet in fluid communication with an outlet of the first stage cooling device and a vapor outlet in fluid communication with the primary refrigeration passage of the main heat exchanger; The system of claim 1 , comprising:

3. further comprising a second stage cooling device; the compressor is a two-stage compressor including a first stage having a compressor first stage inlet in fluid communication with an outlet of the suction separation device such that the compressor first stage inlet receives fluid from the outlet of the suction separation device, and a compressor first stage outlet in fluid communication with the inlet of the first stage cooling device such that the inlet of the first stage cooling device receives fluid from the compressor first stage outlet; an intermediate stage separation device having an intermediate stage separation device inlet in fluid communication with an outlet of the first stage cooling device such that the intermediate stage separation device inlet receives fluid from the outlet of the first stage cooling device; the compressor also includes a second stage having a compressor second stage inlet in fluid communication with the interstage separation device outlet of the interstage separation device such that the compressor second stage inlet receives fluid from the interstage separation device outlet, and a compressor second stage outlet in fluid communication with the inlet of the second stage cooling device such that the second stage inlet receives fluid from the compressor second stage outlet. The system of claim 2.

4. The discharge separation device includes a liquid outlet and further comprises a junction; the junction is configured to receive and combine discharge steam from a steam outlet of the discharge separation device and discharge liquid from a liquid outlet of the discharge separation device; The system of claim 2 , wherein the junction has a junction outlet in fluid communication with the primary refrigeration passage of the main heat exchanger.

5. The system of claim 2 , wherein the discharge separation device includes a liquid outlet in fluid communication with the primary refrigeration passage of the main heat exchanger.

6. 3. The system of claim 2, wherein the main heat exchanger includes a mixed refrigerant cooling passage configured to receive and combine a mixed refrigerant from the vapor outlet of the discharge separation device, and further comprises a first expansion device configured to receive and expand condensed mixed refrigerant from the mixed refrigerant cooling passage and direct the expanded mixed refrigerant to the primary refrigeration passage.

7. 10. The system of claim 1, wherein the mixed refrigerant compression system comprises a mixed refrigerant consisting essentially of methane, ethylene and propane.

8. The main heat exchanger is also configured to receive and warm the combined flow at the warm end to provide cooling to the effluent fluid flow. The system of claim 1 .

9. The system of claim 1 , wherein the separation system comprises a single separation device.

10. The system of claim 1 , wherein the junction is external to the main heat exchanger.

11. 2. The system of claim 1, wherein the splitter is configured to receive the separated steam flow as a superheated steam flow and split into a recycle steam flow and a net steam flow, both of the recycle steam flow and the net steam flow being superheated hydrogen-rich steam flows.

12. The system of claim 1 , wherein the splitter is configured to receive the separated steam flow and split it into a recycle steam flow and a net steam flow having a matching hydrogen composition.

13. The system of claim 1 , wherein the main heat exchanger is a single heat exchanger.

14. A method for separating olefinic hydrocarbons and hydrogen in an effluent fluid stream from a dehydrogenation reactor in a system, comprising: a. partially condensing an effluent fluid stream in a main heat exchanger to form a mixed-phase effluent stream; b. separating the mixed-phase effluent stream into a separated vapor stream comprising hydrogen and a separated liquid stream comprising an olefin product; c. dividing the separated vapor stream into a recycle gas stream and a net vapor stream; d. combining at least a portion of said recycle gas stream with a propane stream independent of said effluent fluid stream to form a combined stream; e. warming the net vapor stream, the combined stream, the separated liquid stream, and a refrigerant stream to provide refrigeration for partially condensing the effluent fluid stream; Including, the main heat exchanger includes a warm end receiving the effluent fluid flow and a cold end at which the mixed-phase effluent flow exits the main heat exchanger; The system further comprises a propane feed expansion device configured to receive and expand a feed stream comprising propane, the feed stream being independent of the effluent fluid stream such that an expanded feed stream is generated; the main heat exchanger is also configured to receive and warm the expanded feed fluid stream at the warm end to provide cooling to the effluent fluid stream. method.

15. 15. The method of claim 14, wherein the refrigerant stream used in step e. comprises a mixed refrigerant.

16. 16. The method of claim 15, wherein the step of partially condensing the effluent fluid stream is accomplished using both the mixed refrigerant and a stream comprising propane and a portion of the separated vapor stream.

17. 16. The method of claim 15, wherein the mixed refrigerant is composed primarily of methane, ethylene and propane.

18. 1. A system for separating olefinic hydrocarbons and hydrogen in an effluent fluid stream from a dehydrogenation reactor, comprising: a. a main heat exchanger configured to receive and partially condense an effluent fluid stream such that a mixed-phase effluent stream is formed; b. a separation system configured to receive and separate the mixed-phase effluent stream into a separated vapor stream comprising hydrogen and a separated liquid stream comprising olefinic hydrocarbons; c. a splitter configured to receive the separated vapor flow and split it into a recycle gas flow and a net vapor flow; d. a junction configured to receive and combine at least a portion of the propane flow and the recycle gas flow, the propane flow being independent of the effluent fluid flow, to form a combined flow; e. a main heat exchanger configured to receive and warm the net vapor flow, the combined flow, and the separated liquid flow to provide refrigeration in the main heat exchanger; f. a refrigerant compression system configured to provide refrigeration in the main heat exchanger; Equipped with the main heat exchanger includes a warm end receiving the effluent fluid flow and a cold end at which the mixed-phase effluent flow exits the main heat exchanger; The system further comprises a propane feed expansion device configured to receive and expand a feed stream comprising propane, the feed stream being independent of the effluent fluid stream such that an expanded feed stream is generated; the main heat exchanger is also configured to receive and warm the expanded feed fluid stream at the warm end to provide cooling to the effluent fluid stream. system.

19. The system of claim 18 , wherein the separation system comprises a single separation device.

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