CN111099952B - Method for cooling, washing and recovering heat of propane dehydrogenation device reactor effluent - Google Patents
Method for cooling, washing and recovering heat of propane dehydrogenation device reactor effluent Download PDFInfo
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- CN111099952B CN111099952B CN201811250997.0A CN201811250997A CN111099952B CN 111099952 B CN111099952 B CN 111099952B CN 201811250997 A CN201811250997 A CN 201811250997A CN 111099952 B CN111099952 B CN 111099952B
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- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
- C07C5/333—Catalytic processes
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Abstract
The present disclosure relates to a process for cooling scrubbing and heat recovery of the reactor effluent of a propane dehydrogenation unit. The method disclosed by the invention utilizes the washing oil to wash the reactor effluent, can effectively remove heavy components in the reaction effluent, can not need to use a large-scale water-cooling heat exchanger to cool the reactor effluent due to the great improvement of the heat exchange quantity, saves water consumption and investment, and also fundamentally solves the problems that the large-scale water-cooling heat exchanger is easy to leak and the reactor effluent is easy to coke; meanwhile, the washed washing oil can provide a heat source for hot users in the system, so that waste heat is utilized more fully, and the purposes of energy conservation and consumption reduction are achieved.
Description
Technical Field
The disclosure relates to the field of propane dehydrogenation production devices, in particular to a cooling washing and heat recovery method for propane dehydrogenation device reactor effluent.
Background
The catalytic dehydrogenation of propane to produce Propylene (PDH) is a special process for producing propylene. The technology for preparing propylene by catalytic dehydrogenation of propane has been developed for nearly 40 years and has been industrially applied in the early 90 s of the 20 th century. In recent years, PDH technology has been developed in a long way through continuous improvement and perfection, and industrial application thereof is becoming mature. The successful catalytic dehydrogenation of propane has been developed mainly from 5 processes: 1) the Oleflex process by UOP corporation; 2) the Catofin process by Lummus corporation; 3) the STAR process by Uhde corporation; 4) PDH technology from Linde-BASF corporation; 5) the FBD process of the company Snamprogetti-Yarsintez. By the end of 2017, a total of 29 PDH devices are running in the world, and the total energy exceeds 1300 million tons of propylene per year. The industrial application apparatus mainly uses an Oleflex process from UOP or a Catofin process from Lummus.
The Catofin process uses Cr series catalyst which is easy to coke, but the Lummus company develops a fixed bed reactor which can adapt to frequent regeneration and a process, and solves the coking problem. The Oleflex process and STAR process use Pt-based catalysts in order to obtain better stability and lower coking rate, and to extend the reaction-regeneration cycle as long as possible.
In the propane dehydrogenation production device, gas-phase effluent from a reaction unit mainly contains components such as hydrogen, C3, C2 and methane, the temperature of the gas-phase effluent is about 135-140 ℃, the gas-phase effluent is cooled to about 43 ℃ through a large water-cooling heat exchanger, the effluent enters a contact cooler, heavy components in the effluent are absorbed and dissolved by a liquid-phase solvent, and the gas-phase effluent goes to two-stage compression from the upper part of the contact cooler. The first section outlet gas enters the second section compression inlet after being cooled by the inter-section cooler.
In order to remove scale and coke from the effluent cooler, compressor intercooler, and outlet cooler, and to improve heat exchange and compressor efficiency, an on-line cleaning system is typically provided. Fresh solvent is added to the process side inlet of each heat exchanger through a solvent injection pump which is operated intermittently, and the solvent which absorbs heavy components is collected into a suction tank, an intersegmental tank and a discharge tank of a reaction effluent compressor and is collected into a solvent injection tank for recycling. The spent solvent may be discharged by a solvent injection pump for disposal outside the home.
The defects of the original flow include that the design flow of a solvent distribution/collection system is complex, the heat is not reasonably utilized, water cooling facilities are arranged before, between and after reaction effluents enter a compressor, and the water consumption and the energy consumption are high. Heavy oil in the reactor effluent is easy to coke in the system, thereby causing problems such as blockage and the like.
Disclosure of Invention
The purpose of the present disclosure is to provide a cooling washing and heat recovery method for propane dehydrogenation unit reactor effluent, which can effectively wash propane dehydrogenation unit reactor effluent, avoid coking, and reduce system energy consumption.
In order to achieve the above objects, the present disclosure provides a cooling scrubbing and heat recovery method for propane dehydrogenation unit reactor effluent, the method comprising the steps of:
s1, enabling the reactor effluent and the washing oil to respectively enter an effluent contact cooler for countercurrent contact washing, and respectively obtaining washing oil containing heavy components and gas phase effluent from the bottom and the top of the effluent contact cooler;
s2, enabling the washing oil containing the heavy components to serve as a heat medium to enter a hot user of the propane dehydrogenation device for heat exchange, and enabling part of the washing oil after heat exchange with the hot user to enter a washing oil recovery device for removing the heavy components for regeneration to obtain regenerated washing oil;
s3, dividing the regenerated washing oil into a first regenerated washing oil and a second regenerated washing oil, and enabling the first regenerated washing oil to enter a washing oil cooler for cooling and then return to the effluent contact cooler of the step S1 as circulating washing oil for carrying out the contact washing;
s4, the gas phase effluent of the step S1 enters a reactor effluent compressor for compression and then enters a separation device for separation.
Optionally, step S4 includes: enabling the gas phase effluent to enter a reactor effluent compressor, performing first-stage compression, then performing heat exchange with the second regenerated washing oil, then entering an intersegmental cooler for cooling, and enabling the cooled gas phase effluent to enter a separation device for separation after second-stage compression;
and enabling the second regenerated washing oil after heat exchange with the first section of compressed outlet gas and the washing oil containing heavy components to enter the hot user for heat exchange together as a heat medium.
Optionally, the method further comprises: and a bypass is arranged at the inlet of the washing oil recovery device, so that the regenerated washing oil is mixed with the washing oil from the bypass, and the mixed washing oil is divided into the first regenerated washing oil and the second regenerated washing oil.
Optionally, the heat user of the propane dehydrogenation unit of step S2 includes a deethanizer reboiler and/or a depropanizer reboiler of the separation unit.
Optionally, the method for removing heavy components and regenerating in step S2 includes: adsorbing to remove heavy components, filtering to remove heavy components or distilling to remove heavy components.
Optionally, the method further comprises replenishing the inlet line of the wash oil cooler with fresh wash oil in step S3.
Optionally, the temperature of the reactor effluent is 120-140 ℃; the temperature of the gas phase effluent in the step S1 is 35-58 ℃, and the temperature of the heavy component-containing washing oil in the step S1 is 120-140 ℃.
Optionally, the temperature of the washing oil after heat exchange with the hot user in the step S2 is 40-100 ℃; the washing oil entering the washing oil recovery device accounts for 10-50% of the total weight of the washing oil after heat exchange with a hot user.
Optionally, the temperature of the first regenerated washing oil cooled in the step S3 is 33-43 ℃.
Optionally, the outlet temperature of the first-stage compression is 105-135 ℃, and the inlet temperature of the second-stage compression is 35-58 ℃; the temperature of the second regenerated washing oil after heat exchange is 100-120 ℃.
Through the technical scheme, the reactor effluent is washed by using the washing oil, heavy components in the reactor effluent can be effectively removed, and the reactor effluent can be cooled without using a large water-cooling heat exchanger due to the great improvement of the heat exchange amount, so that the water consumption and the investment are saved, and the problems that the large water-cooling heat exchanger is easy to leak and the reactor effluent is easy to coke are fundamentally solved; meanwhile, the washed washing oil can provide a heat source for users in the system, so that waste heat is utilized more fully, and the purposes of energy conservation and consumption reduction are achieved.
Additional features and advantages of the disclosure will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the disclosure and are incorporated in and constitute a part of this specification, illustrate embodiments of the disclosure and together with the description serve to explain the disclosure, but do not constitute a limitation of the disclosure. In the drawings:
FIG. 1 is a process flow diagram of one embodiment of the presently disclosed method for cooling scrubbing and heat recovery of a propane dehydrogenation unit reactor effluent.
Detailed Description
The following detailed description of the embodiments of the disclosure refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present disclosure, are given by way of illustration and explanation only, not limitation.
In the present disclosure, the use of directional words such as "up and down" generally means up and down in the normal use state of the device, unless stated to the contrary. The "inner and outer" are with respect to the outline of the device itself.
The present disclosure provides a method for cooling washing and heat recovery of reactor effluent of a propane dehydrogenation unit, comprising the steps of:
s1, enabling the reactor effluent and the washing oil to respectively enter an effluent contact cooler for countercurrent contact washing, and respectively obtaining washing oil containing heavy components and gas phase effluent from the bottom and the top of the effluent contact cooler;
s2, enabling the washing oil containing the heavy components as a heat medium to enter a hot user of the propane dehydrogenation device for heat exchange, and enabling part of the washing oil after heat exchange with the hot user to enter a washing oil recovery device for removing the heavy components for regeneration to obtain regenerated washing oil;
s3, dividing the regenerated washing oil into a first regenerated washing oil and a second regenerated washing oil, and enabling the first regenerated washing oil to enter a washing oil cooler for cooling and then return to the effluent contact cooler of the step S1 as circulating washing oil for contact washing;
and S4, the gas phase effluent of the step S1 enters a reactor effluent compressor for compression and then enters a separation device for separation.
The method disclosed by the invention washes the reactor effluent by using the washing oil, can effectively remove heavy components in the reaction effluent, can not need to use a large-scale water-cooling heat exchanger to cool the reactor effluent due to the great improvement of the heat exchange quantity, saves water consumption and investment, and also fundamentally solves the problems that the large-scale water-cooling heat exchanger is easy to leak and cokes due to high temperature; meanwhile, the washed washing oil can provide a heat source for hot users in the system, so that waste heat is utilized more fully, and the purposes of energy conservation and consumption reduction are achieved.
In the process of the present disclosure, the temperature of the reactor effluent from the upstream propane dehydrogenation reactor may be 120 to 140 ℃; in order to improve the washing and de-weighting effects and the cooling effects, preferably, the temperature of the gas-phase effluent in the step S1 can be 35-58 ℃, preferably 40-43 ℃, and the temperature of the washing oil containing the heavy component in the step S1 can be 120-140 ℃, preferably 129-133 ℃.
In the method disclosed by the disclosure, the temperature of the washed washing oil containing heavy components is increased, and heat can be provided for a hot user in the system, for example, the temperature of the washing oil after heat exchange with the hot user in the step S2 can be 40-100 ℃, and is preferably 65-80 ℃; the proportion of the washing oil entering the washing oil recovery device to the total weight of the washing oil after heat exchange can be adjusted within a large range, for example, 10-50%.
Further, to ensure that the wash oil is circulated within the system, in one embodiment, a wash oil pump may be provided at the liquid phase outlet of the effluent contact cooler for delivering wash oil containing heavy components, the head of the wash oil pump preferably being sufficient to overcome the on-way drag drop of the wash oil to the hot user, the wash oil recovery unit, and back to the effluent contact cooler.
In the method of the present disclosure, the first regenerated washing oil may be cooled by a cooler and then returned to the contact cooler, and the first regenerated washing oil and the reactor effluent are subjected to contact washing and cooling in the contact cooler, and in order to ensure the washing and cooling effect, the temperature of the first regenerated washing oil cooled in step S3 may be 33 to 43 ℃.
To further prevent the problem of reactor effluent coking during separation compression due to high temperatures, step S4 may include, in one embodiment: the gas phase effluent enters a reactor effluent compressor, exchanges heat with second regenerated washing oil after first-stage compression, then enters an intersegmental cooler for cooling, and the cooled gas phase effluent enters a separation device for separation after second-stage compression; and the second regenerated washing oil after heat exchange and the washing oil containing heavy components are used as a heat medium to enter a heat user for heat exchange. In the embodiment, through the design of heat exchange between a part of regenerated washing oil (namely, second regenerated washing oil) and the effluent at the first-stage outlet of the compressor, the temperature of the effluent at the first-stage outlet can be reduced from 140-130 ℃ to below the temperature easy to coke, so that the condition of the downstream easy to coke is improved, the solvent dosage and the operation cost in the prior art are saved, and the heat carried by the second regenerated washing oil after heat exchange can be used for a reboiler of a downstream process, so that the heat in the system is further effectively utilized, and the energy consumption of the system is reduced.
In the process of the present disclosure, the reactor effluent compressor may be conventional in the art, for example, comprising a first-stage suction tank, a first-stage compressor, an effluent compressor interstage cooler, a second-stage suction tank, and a second-stage compressor connected in series, and a cycle oil heat exchanger may be disposed between the first-stage compressor and the interstage cooler to exchange heat between the gas-phase effluent of the first-stage compression outlet and the second regenerated wash oil.
In the method disclosed by the invention, in order to avoid coking of the compressor section, the outlet temperature of the first section of compression can be 105-135 ℃; the inlet temperature of the two-stage compression can be 35-58 ℃; the temperature of the second regenerated washing oil after heat exchange with the first-stage compressed outlet gas can be 100-120 ℃.
In the method disclosed by the disclosure, a bypass can be arranged at an inlet of the washing oil recovery device, so that the washing oil subjected to heat exchange by a user in the system is divided into two parts, one part of the washing oil subjected to heat exchange is sent to the washing oil recovery device to be recovered and removed with heavy components, and the other part of the washing oil is used as a bypass adjusting pipeline of the recovery device and is mixed with the recovered and regenerated washing oil to obtain the first regenerated washing oil and the second regenerated washing oil. In this embodiment, the amount of wash oil entering the recovery unit can be adjusted by the bypass depending on the plant feed composition, the washing method and the operating conditions, thereby allowing the recovery unit to achieve lower overall energy consumption while meeting the washing requirements.
In the method of the present disclosure, the heat user of the propane dehydrogenation unit of step S2 may be a conventional heat-consuming device in the system, and may include a reboiler of a separation device, which may include, for example, a deethanizer reboiler, a depropanizer reboiler, and the like.
In the method of the present disclosure, the wash oil recovery device may be of a type conventional in the art, that is, a device for removing heavy components from the wash oil, and the method of regenerating the recovery device by removing heavy components may be conventional in the art, and preferably may include: adsorption to remove heavy components, filtration to remove heavy components, or distillation to remove heavy components, e.g., vacuum distillation; wherein the meaning of heavy components is well known to those skilled in the art and includes, for example, at least one of tar, dimethyl disulfide, aromatics, heavy aromatics, dimethyl isobutylene, dipentene, and carbonic acid polymers.
In the method according to the present disclosure, in order to secure the washing capacity and the circulation amount of the washing oil, in one embodiment, fresh washing oil may be supplemented to the inlet line of the washing oil cooler of step S3.
The present disclosure is further illustrated by the following examples, but is not to be construed as being limited thereby.
Examples
As shown in fig. 1, the reactor effluent entering the effluent contact cooler is about 135-140 ℃, 35-41 ℃ washing oil is used in the effluent contact cooler to be in countercurrent contact with gas phase effluent, heavy components in the effluent are dissolved by the washing oil and then discharged from the bottom of the effluent contact cooler, the washing oil is sent to a hot user hot side such as a reboiler of a deethanizer, partial flow of the cooled washing oil (with the temperature of 60-85 ℃) containing the heavy components is sent to a washing oil recovery system, and the circulating washing oil quantity and the recovered washing oil quantity are controlled by FC 1; after heavy components are removed by a recovery device, the obtained regenerated washing oil is mixed with the washing oil which circularly flows back and then is divided into first regenerated washing oil and second regenerated washing oil, the first regenerated washing oil is cooled by a cooler and then returns to an effluent contact cooler, the second regenerated washing oil is sent to a circulating oil heat exchanger to exchange heat with a product at the first section outlet of the compressor, the temperature of the first section outlet of the compressor is 130 ℃, the temperature of the first section outlet of the compressor is 85 ℃ after entering the circulating oil heat exchanger to exchange heat, and then the second section of the compressor is subjected to second-section compression after being cooled to 42 ℃ by an intersegmental cooler; the flow to the effluent contact cooler (first regeneration wash oil) is controlled by the effluent contact cooler overhead vapor phase temperature control (TC3) loop, and the flow to the circulating oil heat exchanger (second regeneration wash oil) is controlled by the flow to the effluent contact cooler (FC 2). The wash oil to the effluent contact cooler (first regenerated wash oil) is cooled by the wash oil cooler 5 to around 40 c with circulating water so that the effluent contact cooler overhead gas phase effluent temperature reaches the compressor required inlet temperature, about 43 c. The outlet temperature of the second regenerated washing oil after heat exchange by the circulating oil heat exchanger is 110 ℃, and the second regenerated washing oil is mixed with the washing oil containing heavy components flowing out of the bottom of the effluent contact cooler and then sent to a system heat user for heat exchange.
By adopting the cooling washing and heat recovery method for the reactor effluent of the propane dehydrogenation device, the reaction effluent can be effectively cooled without adopting a large water-cooling heat exchanger, the cooling water consumption is saved, and heat can be provided for a system heat user, so that the device investment and the operation cost are greatly reduced; the reaction effluent is not easy to coke in the process of de-heavy and cooling treatment, so that the dosage of the solvent for avoiding coking is saved, and the operation cost is reduced.
The preferred embodiments of the present disclosure are described in detail with reference to the accompanying drawings, however, the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present disclosure within the technical idea of the present disclosure, and these simple modifications all belong to the protection scope of the present disclosure.
It should be noted that the various features described in the foregoing embodiments may be combined in any suitable manner without contradiction. To avoid unnecessary repetition, the disclosure does not separately describe various possible combinations.
In addition, any combination of various embodiments of the present disclosure may be made, and the same should be considered as the disclosure of the present disclosure as long as it does not depart from the gist of the present disclosure.
Claims (7)
1. A process for cooling scrubbing and heat recovery of the effluent from a propane dehydrogenation unit reactor, the process comprising the steps of:
s1, enabling the reactor effluent and the washing oil to respectively enter an effluent contact cooler for countercurrent contact washing, and respectively obtaining washing oil containing heavy components and gas phase effluent from the bottom and the top of the effluent contact cooler;
s2, enabling the washing oil containing the heavy components to serve as a heat medium to enter a hot user of the propane dehydrogenation device for heat exchange, and enabling part of the washing oil after heat exchange with the hot user to enter a washing oil recovery device for removing the heavy components for regeneration to obtain regenerated washing oil;
s3, dividing the regenerated washing oil into a first regenerated washing oil and a second regenerated washing oil, and enabling the first regenerated washing oil to enter a washing oil cooler for cooling and then return to the effluent contact cooler of the step S1 as circulating washing oil for carrying out the contact washing;
s4, enabling the gas-phase effluent obtained in the step S1 to enter a reactor effluent compressor for compression and then enter a separation device for separation;
a bypass is arranged at the inlet of the washing oil recovery device, so that the regenerated washing oil is mixed with the washing oil from the bypass, and the mixed washing oil is divided into first regenerated washing oil and second regenerated washing oil;
the temperature of the reactor effluent is 135-140 ℃; the temperature of the gas phase effluent in the step S1 is 40-43 ℃, and the temperature of the heavy component-containing washing oil in the step S1 is 129-133 ℃; and the temperature of the first regenerated washing oil cooled in the step S3 is 33-43 ℃.
2. The method of claim 1, wherein step S4 includes: enabling the gas phase effluent to enter a reactor effluent compressor, firstly exchanging heat with the second regenerated washing oil after first-stage compression, then entering an intersegmental cooler for cooling, and enabling the cooled gas phase effluent to enter a separation device for separation after second-stage compression;
and enabling the second regenerated washing oil after heat exchange with the first section of compressed outlet gas and the washing oil containing heavy components to enter the hot user for heat exchange together as a heat medium.
3. The process of claim 1, wherein the hot user of the propane dehydrogenation unit of step S2 comprises a deethanizer reboiler and/or a depropanizer reboiler of the separation unit.
4. The method of claim 1 wherein the step S2 for removing heavy components for regeneration comprises: adsorbing to remove heavy components, filtering to remove heavy components or distilling to remove heavy components.
5. The method of claim 1, further comprising replenishing an inlet line of the wash oil cooler with fresh wash oil in step S3.
6. The method according to claim 1, wherein the temperature of the washing oil after heat exchange with the hot user in the step S2 is 40-100 ℃; the washing oil entering the washing oil recovery device accounts for 10-50% of the total weight of the washing oil after heat exchange with a hot user.
7. The process according to claim 2, wherein the outlet temperature of the first stage of compression is 105 to 135 ℃ and the inlet temperature of the second stage of compression is 35 to 58 ℃; the temperature of the second regenerated washing oil after heat exchange with the first section of compressed outlet gas is 100-120 ℃.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6388155B1 (en) * | 2000-08-01 | 2002-05-14 | Abb Lummus Global Inc. | Styrene dehydrogenation reactor effluent treatment |
| US7687677B1 (en) * | 2006-09-29 | 2010-03-30 | Uop Llc | Process for recovering thermal energy from a reactor effluent stream |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20160090336A1 (en) * | 2014-09-25 | 2016-03-31 | Uop Llc | Removal of aromatic contaminants in olefin stream from paraffin dehydrogenation |
| CN108349837B (en) * | 2015-11-06 | 2021-06-11 | 环球油品公司 | Reactor effluent scrubbing to remove aromatics |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6388155B1 (en) * | 2000-08-01 | 2002-05-14 | Abb Lummus Global Inc. | Styrene dehydrogenation reactor effluent treatment |
| US7687677B1 (en) * | 2006-09-29 | 2010-03-30 | Uop Llc | Process for recovering thermal energy from a reactor effluent stream |
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