CN216024002U - Device for removing trace aromatic hydrocarbon in tail hydrogen through recontacting and disproportionation and transalkylation - Google Patents
Device for removing trace aromatic hydrocarbon in tail hydrogen through recontacting and disproportionation and transalkylation Download PDFInfo
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- CN216024002U CN216024002U CN202120384855.4U CN202120384855U CN216024002U CN 216024002 U CN216024002 U CN 216024002U CN 202120384855 U CN202120384855 U CN 202120384855U CN 216024002 U CN216024002 U CN 216024002U
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Abstract
A device for removing trace aromatic hydrocarbons in disproportionation and transalkylation tail hydrogen by re-contact is characterized by comprising a thermal separation tank, a cold separation tank, a heat exchanger, a tail hydrogen cooler, an oil-gas separation tank, a freezing water pipe and a mixed oil-gas pipe, wherein the top end of the thermal separation tank is provided with a first gas phase conveying pipe, and the bottom end of the thermal separation tank is provided with a first bottom liquid output pipe and a second bottom liquid output pipe; the top of the cold separation tank is provided with a second gas phase conveying pipe and a circulating hydrogen pipe, the middle part of the cold separation tank is provided with a first feeding hole, and the bottom of the cold separation tank is provided with a third bottom liquid output pipe and a fourth bottom liquid output pipe. The method does not need to rely on a reforming device, uses part of the bottom oil of the hot separation tank or the bottom oil of the cold separation tank or the mixed two kinds of oil of the disproportionation and alkyl transfer device as absorption oil to absorb heavy components in the tail hydrogen of the disproportionation, has the removal rate of removing aromatic hydrocarbon up to 80 percent and the removal rate of C5+ petroleum hydrocarbon up to 74 percent, and can effectively recover the aromatic hydrocarbon resources in the tail hydrogen.
Description
Technical Field
The utility model relates to a tail hydrogen treatment device, in particular to a treatment device for tail hydrogen disproportionation and transalkylation.
Background
Hydrogen is an important resource of refining enterprises, so how to efficiently recycle by-products (hydrogen-rich tail gas) in the production process of refining devices is a problem which is always concerned and regarded by relevant professionals. At present, the hydrogen-rich tail gas in the refining device is generally prepared by a Pressure Swing Adsorption (PSA) method, a membrane separation method, a cryogenic separation method and the like, and the Pressure Swing Adsorption (PSA) method is most commonly applied.
The prior tail hydrogen for disproportionation and transalkylation contains a small amount of C5+ petroleum hydrocarbon and trace amount of aromatic hydrocarbon (benzene and toluene and above heavy aromatic hydrocarbon), and if the tail hydrogen is directly fed into a Pressure Swing Adsorption (PSA) device, the tail hydrogen is likely to cause heavy hydrocarbon saturated poisoning of an adsorbent, wherein the benzene and toluene and above heavy aromatic hydrocarbon are most harmful. Although the heavy hydrocarbon saturation poisoning of the adsorbent is reversible, the adsorbent after regeneration is far less effective than the adsorbent before regeneration. Therefore, before the tail hydrogen of disproportionation and transalkylation enters a pressure swing adsorption device, pretreatment is needed, and trace aromatic hydrocarbons (benzene, toluene and the heavy aromatic hydrocarbons above) in the tail hydrogen are removed as much as possible.
See the patent of Chinese utility model with patent number ZL201521096228.1 for reforming and re-contacting device for disproportionated tail hydrogen (publication number: CN205228000U), the scheme of the tail hydrogen conveying pipeline of the patent is as follows: the two ends of the bypass are respectively connected with a compressor and a PSA device of the disproportionation and transalkylation device, the bypass further comprises a tail hydrogen reforming re-contact bypass, the bypass is provided with an evaporator, a gas-liquid separation tank and a regulating valve which are sequentially communicated by pipelines, the two ends of the bypass are respectively connected with the compressor and the PSA device of the disproportionation and transalkylation device, and the tail hydrogen conveying pipeline comprises a tail hydrogen pipeline and a second regulating valve. Its advantage is for effectively eliminating C5's influence, improves the stability of device, and the safe orderly the going on of guarantee production has simple structure, convenient operation's characteristics moreover.
The utility model discloses a method for recovering tail hydrogen of a disproportionation and transalkylation device (publication number: CN109422243A), wherein the tail hydrogen from the disproportionation and transalkylation device is led to an inlet or an outlet of a last-stage air cooler or a water cooler of a reformed hydrogen compressor, or to an inlet or an outlet of a penultimate-stage air cooler or a water cooler of the reformed hydrogen compressor, mixed with compressed gas passing through the reformed hydrogen compressor, then contacted with reformed oil, and sequentially fed into a re-contact refrigerator for cooling and a last-stage re-contact tank for gas-liquid separation, a separated liquid phase is returned to the previous-stage re-contact tank or fed into a product separation unit after cold energy recovery, and the separated gas phase is used as a raw material gas of a pressure swing adsorption device, or one part is used as make-up hydrogen, and the other part is used as the raw material gas of the pressure swing adsorption device to obtain high-purity hydrogen. Its advantage is low cost and high effect on recovering tail hydrogen from disproportionation and alkyl transfer unit.
Both prior art patents rely on a re-contacting device in the reformer to increase the correlation between the two devices, so that the two devices can affect each other when the production of the disproportionation and transalkylation device or the reformer fluctuates. In addition, the disproportionated tail hydrogen is incorporated into the reformed hydrogen and enters a re-contact tank to remove heavy components (C5+ petroleum hydrocarbon (main) and trace amount of aromatic hydrocarbon (secondary)) in the disproportionated tail hydrogen with the absorption oil in reforming. These heavy components are absorbed by the reforming absorber oil and are not returned to the disproportionation and transalkylation unit. Thus, the prior art patents require reforming recontacting devices with sufficient load to accept disproportionated tail hydrogen and may not reduce aromatics losses from the disproportionating and transalkylation units.
SUMMERY OF THE UTILITY MODEL
The first technical problem to be solved by the utility model is to provide a device for removing trace aromatic hydrocarbon in tail hydrogen of disproportionation and transalkylation by re-contact in order to solve the technical situation.
The second technical problem to be solved by the present invention is to provide a device for removing trace aromatics in tail hydrogen of disproportionation and transalkylation without depending on a reforming device, aiming at the above technical current situation.
The technical solution adopted by the present invention to solve the first and second technical problems is: the device for removing trace aromatic hydrocarbon in tail hydrogen by recontacting and disproportionation and transalkylation comprises
The top end of the thermal separation tank is provided with a first gas phase conveying pipe, and the bottom end of the thermal separation tank is provided with a first bottom liquid output pipe and a second bottom liquid output pipe;
the cold separation tank is provided with a second gas phase conveying pipe and a circulating hydrogen pipe at the top, a first feeding hole at the middle part and a third bottom liquid output pipe and a fourth bottom liquid output pipe at the bottom; the first feed inlet is connected with the first gas phase conveying pipe;
the heat exchanger is provided with a second feeding hole, a first discharging hole, a first heat exchange unit and a second heat exchange unit;
the tail gas cooler is provided with a feeding hole and a discharging hole, and the feeding hole of the tail gas cooler is connected with the first discharging hole of the heat exchanger;
the top of the oil-gas separation tank is provided with a fourth gas-phase conveying pipe, the middle of the oil-gas separation tank is provided with a third feeding hole, the bottom of the oil-gas separation tank is provided with a liquid-phase condensing oil pipe, and the fourth gas-phase conveying pipe can be led to the PSA device through the second heat exchange unit; the liquid-phase condensing oil pipe passes through the first heat exchange unit;
a chilled water line passing through the exhaust gas cooler; and
the feed end of the mixed oil-gas pipe is connected with the discharge port of the tail gas cooler, and the discharge end of the mixed oil-gas pipe is connected with the third feed port of the oil-gas separation tank;
the first base liquid output pipe, the third base liquid output pipe and the second gas phase conveying pipe are connected and converged and then enter the second feed port of the heat exchanger, and the second base liquid output pipe, the fourth base liquid output pipe and the oil outlet end of the liquid phase condensation oil pipe are converged.
Furthermore, the first gas phase conveying pipe is provided with an air cooler for cooling.
Furthermore, a first valve is arranged on the second gas phase conveying pipe. And a second valve and a third valve are respectively arranged on the connecting pipelines of the first base liquid output pipe and the third base liquid output pipe.
Compared with the prior art, the utility model has the advantages that: the utility model does not need to rely on a reforming device any more, and utilizes part of the bottom oil of a hot separation tank or the bottom oil of a cold separation tank or two kinds of mixed oil of a disproportionation and alkyl transfer device as absorption oil to absorb heavy components (trace aromatic hydrocarbon (main) and C5+ petroleum hydrocarbon (secondary)) in tail hydrogen of disproportionation, and the removal rate (mass) of the removed aromatic hydrocarbon can reach 80 percent, and the removal rate (mass) of the C5+ petroleum hydrocarbon can reach 74 percent. After absorbing heavy components in the tail hydrogen, the absorption oil is converged with the liquid phases of the two product separation tanks to continue other process treatment, so that aromatic hydrocarbon resources can be effectively recovered, and the loss of part of aromatic hydrocarbon in the disproportionation and transalkylation production processes is reduced. Under the conditions of the utility model, the consumption of the chilled water can be greatly reduced, and the chilled water resource can be efficiently utilized.
Drawings
FIG. 1 is a schematic structural diagram of an embodiment.
Detailed Description
The utility model is described in further detail below with reference to the accompanying examples.
As shown in fig. 1, the device for removing trace aromatic hydrocarbons in disproportionation and transalkylation tail hydrogen by re-contact in this embodiment includes a hot separation tank 1, a cold separation tank 2, a heat exchanger 3, a tail gas cooler 6, an oil-gas separation tank 4, a chilled water pipe 36, and a mixed oil-gas pipe 35.
The thermal separation tank 1 has a first gas phase delivery pipe 14 at the top end and a first bottom liquid delivery pipe 12 and a second bottom liquid delivery pipe 13 at the bottom end.
The cold separation tank 2 is provided with a second gas phase conveying pipe 22 and a circulating hydrogen pipe 23 at the top, a first feeding hole 21 at the middle part and a third bottom liquid output pipe 24 and a fourth bottom liquid output pipe 25 at the bottom; the first feed opening 21 is connected to the first gas phase duct 14.
The heat exchanger 3 is provided with a second feeding hole 34, a first discharging hole, a first heat exchange unit 31 and a second heat exchange unit 32. The tail gas cooler 6 is provided with a feeding hole and a discharging hole, and the feeding hole of the tail gas cooler 6 is connected with a first discharging hole of the heat exchanger; the top of the oil-gas separation tank 4 is provided with a fourth gas phase conveying pipe 41, the middle part is provided with a third feeding port 42, the bottom is provided with a liquid phase condensing oil pipe 43, and the fourth gas phase conveying pipe 41 passes through the second heat exchange unit 32 and can be led to a PSA device; the liquid phase condensing oil pipe 43 passes through the first heat exchange unit 31; the chilled water line 36 passes through the off-gas cooler 6.
The feed end of the mixed oil-gas pipe 35 is connected with the discharge hole of the tail gas cooler 6, and the discharge end is connected with the third feed port 42 of the oil-gas separation tank 4.
The first bottom liquid output pipe 12 is connected with the third bottom liquid output pipe 24 and the second gas phase delivery pipe 22, and then enters the second feed inlet 34 of the heat exchanger 3, and the second bottom liquid output pipe 13 is connected with the fourth bottom liquid output pipe 25 and the oil outlet end of the liquid phase condensation oil pipe 43.
An air cooler 15 for cooling is arranged on the first gas phase delivery pipe 14. The second gas-phase transport pipe 22 is provided with a first valve 51. The connecting pipeline of the first bottom liquid output pipe 12 and the third bottom liquid output pipe 24 is respectively provided with a second valve 52 and a third valve 53.
The method for removing the trace aromatic hydrocarbon by adopting the device is characterized in that the mass ratio of the absorbed oil to the tail hydrogen in the material entering the second feeding hole 34 is 1: 1-4: 3; the hydrogen flow rate in the second gas phase conveying pipe 22 is 5-15%, and the hydrogen flow rate in the circulating hydrogen pipe 23 is 85-95%; the temperature of the mixed oil gas in the discharge hole of the tail gas cooler 6 is not higher than 15 ℃; the return water temperature in the freezing water pipe 36 is between 10 and 15 ℃; the temperature of the condensed oil after heat exchange in the liquid-phase condensed oil pipe 43 is not lower than 50 ℃; the temperature of tail hydrogen after heat exchange in the fourth gas phase conveying pipe 41 is not higher than 50 ℃; the temperature of the freezing water in the freezing water pipe 36 is 5-15 ℃.
The mixture or single material of the bottom liquid of the hot separating tank 1 and the bottom liquid of the cold separating tank 2 is taken as absorption oil and tail hydrogen of a disproportionation and transalkylation device to be converged and then enters a multi-stream heat exchanger 3, and the other stream is converged with the liquid phase output by the cold separating tank 2 and condensed oil after heat exchange and then enters a subsequent fractionation unit for treatment. And after the gas phase output from the top of the hot separation tank 1 enters an air cooler 15 for cooling, the gas phase is input from the middle part of the cold separation tank 2 for secondary gas-liquid separation.
The liquid phase output from the bottom discharge port of the cold separation tank 2 is divided into two streams, one stream is used as absorption oil to be converged with tail hydrogen, and the other stream is converged with the liquid phase output from the bottom of the hot separation tank 2 and condensed oil after heat exchange. The gas phase output from the top is divided into two streams, one stream is used as circulating hydrogen, and the other stream is used as tail hydrogen of a disproportionation and transalkylation device and is converged with absorption oil to enter a multi-stream heat exchanger 3.
The temperature of the mixed oil gas is not higher than 50 ℃ after the mixed oil gas is cooled for the second time by the multi-stream heat exchanger 3, the mixed oil gas is cooled to below 15 ℃ by the tail hydrogen cooler 6, and the mixed oil gas enters the oil gas separation tank 4 from the middle part of the oil gas separation tank 4 for gas-liquid separation. The condensed oil exchanges heat with the liquid-phase condensed oil output from the bottom of the oil-gas separation tank 4 for the first time, and the temperature of the condensed oil after heat exchange is not lower than 50 ℃; exchanging heat with the gas-phase-removed tail hydrogen output from the top of the oil-gas separation tank 4 for the second time, wherein the temperature of the heat-exchanged removed tail hydrogen is not higher than 50 ℃; and the mixed oil gas after heat exchange enters a tail hydrogen cooler 6 to be continuously cooled, and exchanges heat with chilled water, and the return water temperature of the chilled water is 10-15 ℃.
The mixed oil gas enters the oil-gas separation tank 4 from the middle part of the oil-gas separation tank 4. After gas-liquid separation, the liquid-phase condensed oil is output from the bottom of the oil-gas separation tank 4 and then enters a multi-stream heat exchanger for heat exchange, and then is converged with the bottom liquid of the heat separation tank and the bottom liquid of the cold separation tank 2; and after gas phase removal, tail hydrogen is output from the top of the oil-gas separation tank 4 and enters a multi-stream heat exchanger for heat exchange, and then is purified by a PSA device.
Claims (4)
1. A device for removing trace aromatic hydrocarbon in tail hydrogen through re-contact disproportionation and transalkylation is characterized by comprising
The heat separation tank (1) is provided with a first gas phase conveying pipe (14) at the top end and a first bottom liquid output pipe (12) and a second bottom liquid output pipe (13) at the bottom end;
the cold separation tank (2) is provided with a second gas phase conveying pipe (22) and a circulating hydrogen pipe (23) at the top, a first feeding hole (21) at the middle part and a third bottom liquid output pipe (24) and a fourth bottom liquid output pipe (25) at the bottom; the first feed port (21) is connected with the first gas phase conveying pipe (14);
the heat exchanger (3) is provided with a second feeding hole (34), a first discharging hole, a first heat exchange unit (31) and a second heat exchange unit (32);
the tail gas cooler (6) is provided with a feeding hole and a discharging hole, and the feeding hole of the tail gas cooler (6) is connected with the first discharging hole of the heat exchanger;
the top of the oil-gas separation tank (4) is provided with a fourth gas-phase conveying pipe (41), the middle of the oil-gas separation tank is provided with a third feeding port (42), the bottom of the oil-gas separation tank is provided with a liquid-phase condensing oil pipe (43), and the fourth gas-phase conveying pipe (41) can pass through the second heat exchange unit (32) and can be led to a PSA device; the liquid-phase condensed oil pipe (43) passes through the first heat exchange unit (31);
a freezing water pipe (36) passing through the exhaust gas cooler (6); and
the feed end of the mixed oil-gas pipe (35) is connected with the discharge hole of the tail gas cooler (6), and the discharge end of the mixed oil-gas pipe is connected with the third feed hole (42) of the oil-gas separation tank (4);
the first bottom liquid output pipe (12), the third bottom liquid output pipe (24) and the second gas phase conveying pipe (22) are connected and converged and then enter a second feeding hole (34) of the heat exchanger (3), and the second bottom liquid output pipe (13) is converged with a fourth bottom liquid output pipe (25) and an oil outlet end of the liquid phase condensation oil pipe (43).
2. The device for removing the trace aromatic hydrocarbons in the tail hydrogen generated by disproportionation and transalkylation through re-contact as claimed in claim 1, wherein the first gas phase transport pipe (14) is provided with an air cooler (15) for cooling.
3. The apparatus for removing trace aromatic hydrocarbons from disproportionation and transalkylation tail hydrogen as claimed in claim 1, wherein the second gas phase transport pipe (22) is provided with a first valve (51).
4. The apparatus for removing trace aromatics in tail hydrogen generated by disproportionation and transalkylation by re-contact as claimed in claim 1, wherein the connecting pipeline between the first bottom liquid output pipe (12) and the third bottom liquid output pipe (24) is provided with a second valve (52) and a third valve (53), respectively.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120384855.4U CN216024002U (en) | 2021-02-20 | 2021-02-20 | Device for removing trace aromatic hydrocarbon in tail hydrogen through recontacting and disproportionation and transalkylation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120384855.4U CN216024002U (en) | 2021-02-20 | 2021-02-20 | Device for removing trace aromatic hydrocarbon in tail hydrogen through recontacting and disproportionation and transalkylation |
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| Publication Number | Publication Date |
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| CN216024002U true CN216024002U (en) | 2022-03-15 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202120384855.4U Active CN216024002U (en) | 2021-02-20 | 2021-02-20 | Device for removing trace aromatic hydrocarbon in tail hydrogen through recontacting and disproportionation and transalkylation |
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| CN (1) | CN216024002U (en) |
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- 2021-02-20 CN CN202120384855.4U patent/CN216024002U/en active Active
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