CN216062029U - Recovery unit of butyl octanol device low pressure evaporator tail gas - Google Patents
Recovery unit of butyl octanol device low pressure evaporator tail gas Download PDFInfo
- Publication number
- CN216062029U CN216062029U CN202122392585.4U CN202122392585U CN216062029U CN 216062029 U CN216062029 U CN 216062029U CN 202122392585 U CN202122392585 U CN 202122392585U CN 216062029 U CN216062029 U CN 216062029U
- Authority
- CN
- China
- Prior art keywords
- pressure
- tail gas
- low
- liquid
- pressure evaporator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Abstract
The utility model discloses a recovery device of tail gas of a low-pressure evaporator of a butanol-octanol device, which comprises a low-pressure evaporator, wherein a gas phase outlet of the low-pressure evaporator is connected with a butyraldehyde receiving tank through a cooler. The device treats tail gas of a low-pressure evaporator of a butanol-octanol device through a compressor and a liquid separating tank, and recovers the tail gas and sends the tail gas to an upstream MTO device.
Description
Technical Field
The utility model belongs to the technical field of butanol and octanol production, and particularly relates to a recovery device for tail gas of a low-pressure evaporator of a butanol and octanol device.
Background
Butanol (butyl alcohol) and octanol (isooctanol is commonly known as octanol, 2-ethylhexanol; 2-ethyl hexanol) are customarily known as butanol and octanol because they can be produced by oxo synthesis in the same set of equipment. Butanol and octanol are important raw materials for synthesizing fine chemical products, and are mainly used for producing plasticizers, solvents, dehydrating agents, defoaming agents, dispersing agents, flotation agents, petroleum additives, synthetic perfumes and the like. Due to its wide use, the yield and the amount of butanol and octanol are also increased year by year.
The general butanol-octanol device comprises a butanol line and an octanol line, wherein propylene and synthesis gas are used as raw materials, mixed butyraldehyde (n-butyraldehyde and isobutyraldehyde) is produced by a low-pressure oxo synthesis method, and the intermediate butyraldehyde is used as the raw material in the subsequent butanol-octanol process; the catalyst used in the oxo process is a complex of rhodium metal and triphenylphosphine, dissolved in butyraldehyde. Butyraldehyde and the catalyst solution are separated by high-pressure and low-pressure evaporation. In the low-pressure evaporation process, a butyraldehyde solution containing a catalyst enters a low-pressure evaporator after being heated by a falling-film evaporator, a gas phase is condensed by a cooler, a liquid phase enters a butyraldehyde receiving tank, a gas phase is discharged to a torch through the butyraldehyde receiving tank, and the discharge amount of the gas phase is adjusted by an adjusting valve to ensure the stability of the system pressure. This portion of the gas phase discharged from the flare, i.e., the tail gas, often carries a portion of the carbon monoxide, hydrogen, propylene, propane, nitrogen, etc. It is generally the case that the tail gas portion cannot be recovered for process reasons and can only be discharged to flare.
Disclosure of Invention
Aiming at the defects of the prior art, the utility model aims to provide a recovery device for tail gas of a low-pressure evaporator of a butanol-octanol device, which solves the problem of tail gas recovery of the low-pressure evaporator in the butanol-octanol device and recycles propylene and propane contained in the originally discharged tail gas as raw materials.
The utility model adopts the following technical scheme:
the utility model provides a recovery unit of butyl octanol device low pressure evaporator tail gas, includes the low pressure evaporator, the gaseous phase export of low pressure evaporator is connected butyraldehyde through the cooler and is received the groove, a serial communication port, the device still include compressor and divide the liquid jar, butyraldehyde receives the tail gas export at groove top to divide into two parallelly connected pipelines, one is connected to the torch, another connects gradually the compressor with divide the liquid jar, divide liquid jar top gaseous phase export to divide into two parallelly connected pipelines, one is connected to the torch, and another is carried to the MTO device.
The device of the utility model separates the tail gas originally discharged by a low-pressure evaporator of a butanol-octanol device and removed from a torch by a compressor and a liquid separating tank, and sends the tail gas to an upstream MTO device as a raw material after the pressure of the tail gas is increased.
Furthermore, a compressor inlet pressure controller is arranged at the front end of the compressor, bypasses are arranged at the front end and the rear end of the compressor, and a compressor inlet pressure regulating valve is arranged on each bypass.
Further, a gas phase outlet of the low-pressure evaporator is provided with a pressure controller, and a tail gas outlet at the top of the butyraldehyde receiving groove is connected to a pipeline of a torch and is provided with a pressure regulating valve.
And further, a pressure controller is arranged at a gas phase outlet at the top of the liquid separation tank, and a liquid separation tank pressure regulating valve is arranged on a pipeline connected to the torch through the gas phase outlet at the top of the liquid separation tank.
Further, a liquid phase outlet at the bottom of the liquid separation tank is connected to a liquid phase outlet at the bottom of the butyraldehyde receiving tank.
Further, the liquid separation tank is provided with a liquid level controller, and a liquid level regulating valve is arranged on a pipeline of which a liquid phase outlet at the bottom of the liquid separation tank is connected to a liquid phase outlet at the bottom of the butyraldehyde receiving tank.
The utility model has the beneficial effects that: according to the recovery device for the tail gas of the low-pressure evaporator of the butanol-octanol device, the tail gas is separated by the compressor and the liquid separating tank, the tail gas is sent to the upstream MTO device as a raw material after the pressure of the tail gas is increased, and the device effectively recovers propylene and propane contained in the originally discharged tail gas and utilizes the propylene and propane as MTO raw materials.
Drawings
FIG. 1 is a schematic structural diagram of a recovery device of tail gas of a low-pressure evaporator of a butanol-octanol device disclosed by the utility model;
in the figure, V-1 is a low-pressure evaporator, E-1 is a circulating water cooler, V-2 is a butyraldehyde receiving tank, PIC-1 is a pressure controller, PV-1 is a pressure regulating valve, V-3 is a liquid separating tank, C-1 is a compressor, PIC-2 is a compressor inlet pressure controller, PIC-3 is a liquid separating tank top outlet pressure controller, PV-2 is a C-1 compressor inlet pressure regulating valve, PV-3 is a liquid separating tank pressure regulating valve, LIC-1 is a liquid separating tank liquid level controller, and LV-1 is a liquid separating tank liquid level regulating valve.
Detailed Description
In order to more clearly illustrate the technical solution of the present invention, a specific implementation manner of the present invention is described below with reference to the accompanying drawings. It is to be understood that the following examples and drawings are merely illustrative of one embodiment of the present invention and are not to be construed as limiting the utility model.
As shown in figure 1, the recovery device for the tail gas of the low-pressure evaporator of the butanol-octanol device comprises a low-pressure evaporator V-1, a butyraldehyde receiving tank V-2, a compressor C-1 and a liquid separating tank V-3, wherein a gas phase outlet of the low-pressure evaporator V-1 is connected with the butyraldehyde receiving tank V-2 through a circulating water cooler E-1, a tail gas outlet at the top of the butyraldehyde receiving tank V-2 is divided into two parallel pipelines, one pipeline is connected with a torch, the other pipeline is sequentially connected with the compressor C-1 and the liquid separating tank V-3, a gas phase outlet at the top of the liquid separating tank V-3 is divided into two parallel pipelines, one pipeline is connected with the torch, and the other pipeline is conveyed to an MTO device.
In the n-butyl octanol device, a tail gas outlet of a butyraldehyde receiving groove V-2 is connected with a torch. The tail gas is pressurized by a compressor C-1, enters a liquid separation tank V-3 for further gas-liquid separation, and is sent to an upstream MTO device as a raw material after the pressure of the tail gas is increased.
And a gas phase outlet of the low-pressure evaporator V-1 is provided with a pressure controller PIC-1, and a tail gas outlet at the top of the butyraldehyde receiving tank V-2 is connected to a pipeline of a torch and is provided with a pressure regulating valve PV-1 which is connected with a control signal of the pressure controller PIC-1.
The front end of the compressor C-1 is provided with a compressor inlet pressure controller PIC-2, the front end and the rear end of the compressor C-1 are provided with bypasses, and the bypasses are provided with compressor inlet pressure regulating valves PV-2 which are connected with control signals of the pressure controller PIC-2.
A gas phase outlet at the top of the liquid separation tank V-3 is provided with a pressure controller PIC-3, a pipeline connected to the torch is provided with a liquid separation tank pressure regulating valve PV-3, and the liquid separation tank pressure regulating valve PV-3 is connected with a control signal of the pressure controller PIC-3; the liquid separation tank V-3 is provided with a liquid level controller LIC-1, a bottom liquid phase outlet is connected to a bottom liquid phase outlet of the butyraldehyde receiving tank V-2, a liquid level regulating valve LV-1 is arranged on a connecting pipeline, and the liquid level regulating valve LV-1 is connected with a control signal of the liquid level controller LIC-1.
Referring to fig. 1, under normal conditions of the original device, liquid from a low-pressure evaporator V-1 cooled by a circulating water cooler E-1 enters a butyraldehyde receiving tank V-2, and the butyraldehyde is discharged by tail gas at the top of the tank V-2, and is regulated and controlled by a pressure regulator PIC-1 which is set to 70kPag and controls a pressure regulating valve PV-1, and a torch is discharged.
After the device is adopted, under the normal working condition, tail gas from a butyraldehyde receiving tank V-2 enters a compressor C-1 through a pressure controller PIC-2 with the set pressure of 65kPag to be pressurized to 0.2MPag, if the inlet of the compressor C-1 is lower than the set pressure of the pressure controller PIC-2, opening a pressure regulating valve PV-2 under the control of a pressure controller PIC-2 to ensure the pressure of the pressure controller PIC-2 to be stable, feeding the pressurized tail gas from a compressor C-1 into a liquid separating tank V-3 for liquid separation, controlling the pressure of the tail gas at the top through the pressure controller PIC-3 to be 0.25MPag, sending to an MTO device, if the pressure is higher than the set value of the pressure controller PIC-3, the pressure controller PIC-3 controls to open the pressure regulating valve PV-3 to ensure that the tail gas enters the torch to ensure the pressure of the pressure controller PIC-3 to be stable; the liquid at the bottom of the liquid separation tank V-3 passes through a liquid level controller LIC-1 to control the opening of a liquid level regulating valve LV-1, and the liquid material is sent to the bottom of a butyraldehyde receiving tank V-2 to be recovered.
The specific working process is as follows:
the driving working condition is as follows:
the butyraldehyde receiving tank V-2 is normally discharged stably through a pressure regulating valve PV-1, and the pressure of the low-pressure evaporator V-1 is stabilized below 0.08Mpag and above 0.06 MPag. Firstly, closing a pressure regulating valve LV-1, normally closing the pressure regulating valve PV-3, opening the pressure regulating valve PV-2 to 50% of opening degree, starting a compressor C-1, slowly and manually closing the pressure regulating valve PV-1 when the pressure of a monitoring pressure controller PIC-3 reaches 0.25MPag, and correspondingly and manually opening the pressure regulating valve PV-3 to ensure that the pressure of the pressure controller PIC-3 is stabilized above 0.03MPag and simultaneously the pressure controller PIC-3 does not exceed 0.28 MPag. When the pressure regulating valve PV-1 is turned down until closed, and the pressure controller PIC-1 shows that 0.07Mpag is stable, the automatic regulation is set, and the set value is 0.08 MPag. The pressure controller PIC-2 is stabilized at 0.65MPag, and an automatic control pressure regulating valve PV-2 is arranged. When the liquid level of the liquid separation tank V-3 slowly increases to 50 percent, the liquid level regulating valve LV-1 is opened.
Normal working conditions are as follows:
normal operating mode 1: when the pressure of the pressure controller PIC-1 is lower than 0.07MPag, the pressure controller PIC-2 can be reduced by less than 0.065MPag, at the moment, the pressure regulating valve PV-2 can be slowly increased, the outlet circulating gas of the compressor C-1 can be increased, the pressure controller PIC-3 can be higher than 0.25MPag, the pressure regulating valve PV-3 can be controlled to be closed, then the pressure of the pressure controller PIC-2 can be increased to 0.065MPag, and the pressure controller PIC-1 can be increased until the 0.07MPag is stable.
Normal working condition 2: when the pressure of the pressure controller PIC-1 is higher than the set value of 0.07MPag and less than 0.08MPag, the pressure controller PIC-2 is higher than 0.065MPag, the pressure regulating valve PV-2 is slowly turned off at the moment, the outlet circulating gas of the compressor C-1 is reduced, the pressure controller PIC-3 is higher than 0.25MPag, the pressure regulating valve PV-3 is controlled to be turned on, the pressure of the pressure controller PIC-2 is slowly reduced to 0.065MPag at the moment, and the pressure of the pressure controller PIC-1 is reduced to 0.07 MPag.
Normal working condition 3: when the pressure of the pressure controller PIC-1 rises and exceeds 0.08MPag, the pressure regulating valve PV-1 is directly opened, the pressure of the low-pressure evaporator V-1 is directly reduced to be below 0.08MPag, and the normal working condition 2 is reached at the moment, so that the stability is recovered.
And (3) parking working condition:
setting the pressure regulating valves PV-1, PV-2 and PV-3 to be in a manual state, slowly closing the pressure regulating valve PV-3, slowly opening the pressure regulating valve PV-2, slowly opening the pressure regulating valve PV-1 to ensure the stable pressure of the butyraldehyde receiving tank V-2. When the pressure regulating valve PV-3 is completely closed, the pressure controller PIC-2 controls the pressure to be stable, the pressure of the butyraldehyde is stabilized by the groove V-2, and the compressor C-1 is stopped. From which the system stops operating.
The tail gas discharge amount of a butyraldehyde receiving groove V-2 in a low-pressure evaporator of a butanol-octanol device is about 300 kg/h-500 kg/h, the tail gas contains about 13% of propylene and about 73% of propane, and after the device is adopted, 312t/a of propylene is recovered, and 1752t/a of propane is recovered. The butyraldehyde can be further recovered after the tail gas is compressed, and 330 t/a of the butyraldehyde can be expected to be recovered through the bottom of the liquid separation tank V-3.
Claims (6)
1. The utility model provides a recovery unit of butyl octanol device low pressure evaporator tail gas, includes the low pressure evaporator, the gaseous phase export of low pressure evaporator is connected butyraldehyde through the cooler and is received the groove, a serial communication port, the device still include compressor and divide the liquid jar, butyraldehyde receives the tail gas export at groove top to divide into two parallelly connected pipelines, one is connected to the torch, another connects gradually the compressor with divide the liquid jar, divide liquid jar top gaseous phase export to divide into two parallelly connected pipelines, one is connected to the torch, and another is carried to the MTO device.
2. The recovery device of the tail gas of the low-pressure evaporator of the butanol-octanol device as claimed in claim 1, wherein a compressor inlet pressure controller is arranged at the front end of the compressor, bypasses are arranged at the front end and the rear end of the compressor, and a compressor inlet pressure regulating valve is arranged on the bypass.
3. The recovery device of butanol-octanol device low-pressure evaporator tail gas according to claim 1, wherein the gas phase outlet of said low-pressure evaporator is equipped with pressure controller, and the tail gas outlet at the top of said butyraldehyde receiving tank is connected to the pipeline of flare and equipped with pressure regulating valve.
4. The recovery device of the tail gas of the low-pressure evaporator of the butanol-octanol device as claimed in claim 1, wherein a pressure controller is arranged at the top gas phase outlet of the liquid separation tank, and a liquid separation tank pressure regulating valve is arranged on a pipeline connecting the top gas phase outlet of the liquid separation tank to a torch.
5. The recovery device of butanol-octanol device low pressure evaporator tail gas according to claim 1, wherein said liquid separation tank bottom liquid phase outlet is connected to butyraldehyde receiving tank bottom liquid phase outlet.
6. The recovery device of tail gas of a low-pressure evaporator of a butanol-octanol device as claimed in claim 5, wherein the liquid separation tank is provided with a liquid level controller, and a liquid level regulating valve is arranged on a pipeline connecting a liquid phase outlet at the bottom of the liquid separation tank to a liquid phase outlet at the bottom of the butyraldehyde receiving tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122392585.4U CN216062029U (en) | 2021-09-30 | 2021-09-30 | Recovery unit of butyl octanol device low pressure evaporator tail gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122392585.4U CN216062029U (en) | 2021-09-30 | 2021-09-30 | Recovery unit of butyl octanol device low pressure evaporator tail gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216062029U true CN216062029U (en) | 2022-03-18 |
Family
ID=80637088
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202122392585.4U Active CN216062029U (en) | 2021-09-30 | 2021-09-30 | Recovery unit of butyl octanol device low pressure evaporator tail gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN216062029U (en) |
-
2021
- 2021-09-30 CN CN202122392585.4U patent/CN216062029U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7707852B2 (en) | Process for recovering lower carbon olefins from product gas for production of olefins | |
| CN216062029U (en) | Recovery unit of butyl octanol device low pressure evaporator tail gas | |
| CN112178455A (en) | LPG (liquefied petroleum gas) small storage tank gasification control system and gasification control method thereof | |
| CN103160351A (en) | Method and device used for utilizing hydrate method to recover methane in low concentration coal bed gas | |
| CN109506131B (en) | Associated gas treatment plant slug flow trapping system and method | |
| CN207108870U (en) | The retracting device of butanol heavy constituent raffinate in a kind of butyl octanol unit | |
| CN102603455A (en) | Process and device for recovering C2 materials in ethylene device | |
| CN2682324Y (en) | Air separation device having cold quantity recovering apparatus | |
| CN111732982B (en) | Natural gas dewaxing method and device | |
| CN112239390B (en) | Ethylene cryogenic recovery system | |
| US20130092602A1 (en) | Continuous Reaction System Comprising Subcritical Or Supercritical Liquid As Solvent And Reactant As Solid | |
| CN111017956B (en) | System for recycling low-temperature methanol washing air and operation method | |
| CN209116630U (en) | The centrifugal ammonia ice maker device of self-operated type drain | |
| CN215109726U (en) | Device for replacing steam jet pump dilution gas with non-permeable gas | |
| CN219222087U (en) | Product gas conveying system of propane dehydrogenation device | |
| CN209815992U (en) | Device for unpowered recovery of hydrogen in purge gas of dimethyl oxalate hydrogenation reaction | |
| CN112178457A (en) | System and method for controlling liquid conveying stoppage of low-pressure flash gas pipeline in oil field | |
| CN218961788U (en) | Low-temperature oil washing device | |
| CN215462103U (en) | Shutdown and material returning transformation system for gas separation device | |
| CN209685645U (en) | Nonyl phenol device high and low pressure system controls improvement system | |
| CN219079406U (en) | System for adjusting hydrogen-carbon ratio in synthesis gas | |
| CN213113237U (en) | Natural gas dewaxing device | |
| CN109082296A (en) | Naphtha reforming device reforms hydrogen compressor outlet and cuts liquid recovery system | |
| CN207108867U (en) | Propylene recovery, the device of propane in a kind of butyl octanol unit tail gas | |
| CN1272618A (en) | Method for extracting concentrated hydrogen gas by utilizing separation of aqua compound |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |