CN112973594A - Trans-1, 2-dichloroethylene preparation system for crude product alkaline washing absorption - Google Patents
Trans-1, 2-dichloroethylene preparation system for crude product alkaline washing absorption Download PDFInfo
- Publication number
- CN112973594A CN112973594A CN202110179993.3A CN202110179993A CN112973594A CN 112973594 A CN112973594 A CN 112973594A CN 202110179993 A CN202110179993 A CN 202110179993A CN 112973594 A CN112973594 A CN 112973594A
- Authority
- CN
- China
- Prior art keywords
- tower
- condenser
- tank
- storage tank
- regeneration
- 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.)
- Granted
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/013—Preparation of halogenated hydrocarbons by addition of halogens
- C07C17/02—Preparation of halogenated hydrocarbons by addition of halogens to unsaturated hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
- C07B2200/00—Indexing scheme relating to specific properties of organic compounds
- C07B2200/09—Geometrical isomers
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention provides a crude product alkali washing absorbed trans-1, 2-dichloroethylene preparation system, which comprises a synthesis tower, a regeneration tower, a mother liquor storage tank, a regeneration storage tank and a neutralization device, wherein a gas phase inlet at the bottom of the synthesis tower is used for introducing acetylene gas, a liquid phase inlet at the bottom of the synthesis tower is connected with an outlet of a mother liquor tank, a gas phase outlet at the top of the synthesis tower is connected with a synthesis condenser, a gas phase inlet at the bottom of the regeneration tower is used for introducing chlorine gas, a liquid phase inlet at the top of the regeneration tower is connected with the regeneration storage tank, a liquid phase outlet at the bottom of the regeneration condenser is connected with the mother liquor storage tank, the neutralization device comprises a mixer, an oil-water separator, a neutralization liquid storage tank and a soda liquor tank, the oil-water separator is connected with an outlet of the crude product tank, an oil phase outlet of the oil-water separator is connected with an inlet of the mixer, an, reduces the resource consumption of neutralization reaction, recycles the acidic wastewater at the same time and increases the added value.
Description
Technical Field
The invention relates to the technical field of preparation of trans-1, 2-dichloroethylene, in particular to a trans-1, 2-dichloroethylene preparation system for crude product alkali washing absorption.
Background
Trans-1, 2-dichloroethylene (hereinafter referred to as dichloroethylene) is a good solvent and chemical raw material, and is colorless and volatile liquid with slight pungent smell. The main application is as follows: the trans-1, 2-dichloroethylene is a novel environment-friendly organic solvent, and can be used as a solvent for paint, resin, wax, rubber and acetate fiber, a dry cleaning agent, an insecticide, a bactericide, an anesthetic, a low-temperature extractant, a refrigerant and the like. Due to the wide application of trans-1, 2-dichloroethylene, the preparation of the trans-1, 2-dichloroethylene also becomes a very concerned problem in the chemical industry.
In the existing equipment, when the crude synthetic material is rectified, the mother liquor has strong acidity, and the acidity of the mother liquor needs to be adjusted before dehydrogenation and rectification, so the technical problem is not solved in the prior art.
Disclosure of Invention
It is necessary to provide a trans-1, 2-dichloroethylene preparation system with crude alkali washing absorption.
A crude product alkali washing absorbed trans-1, 2-dichloroethylene preparation system comprises a synthesis tower, a regeneration tower, a mother liquor storage tank, a regeneration storage tank and a neutralization device, wherein the synthesis tower and the regeneration tower are packed towers, a tower bottom liquid phase inlet is connected with an outlet of the mother liquor tank, a tower top gas phase outlet of the synthesis tower is connected with a condenser for synthesis, an outlet of the condenser for synthesis is connected with a tower top liquid phase inlet of the synthesis tower through a gas-water separator, an outlet of the condenser for synthesis is also connected with the crude product tank through the gas-water separator so as to input a semi-finished product containing dichloroethylene into the crude product tank, a tower bottom gas phase inlet of the regeneration tower is used for introducing chlorine, a tower top liquid phase inlet of the regeneration tower is connected with the regeneration storage tank, a tower bottom liquid phase outlet of the regeneration tower is connected with the mother liquor storage tank, the regeneration tower is provided with the condenser for regeneration, a tower top gas phase outlet of the regeneration, still set up pre-heater, intensifier between synthetic tower and mother liquor storage tank, the export of the entry linkage mother liquor storage tank of pre-heater, the liquid phase entry at the bottom of the exit linkage intensifier of pre-heater, the liquid phase entry at the bottom of the tower of the top of the tower exit linkage synthetic tower of intensifier, the gaseous phase entry linkage acetylene gas incoming material pipeline of intensifier, neutralization apparatus includes blender, oil water separator, neutralization solution storage tank, lye jar, the export of crude jar is connected to oil water separator, and oil water separator's oil phase exit linkage blender entry deposits alkali lye in the alkali lye jar, and lye jar and blender entry linkage, the exit linkage neutralization solution storage tank of blender, and neutralization solution storage tank export is passed through power pump, pipeline and is discharged neutralization solution.
The invention realizes the recycling of the mother liquor, the regeneration process and the synthesis process are continuous reaction processes, the synthesis reaction of the dichloroethylene and the regeneration of the mother liquor are mutually supplemented without mutual influence, the whole process for producing the dichloroethylene does not need to be stopped or interrupted, the structure of equipment is optimized, and the production efficiency is high.
In the invention, the dichloroethylene in the crude product tank is subjected to first light low-temperature rectification treatment through the light component removal tower to remove light impurities, then is subjected to second heavy high-temperature rectification through the rectification tower to remove heavy impurities, gas-phase dichloroethylene is distilled from the top of the rectification tower and is stored in the finished product tank after being condensed, and the content of the dichloroethylene obtained through the secondary treatment can reach 0.999%.
The scheme temporarily stores light impurities distilled from the light component removing tower and high boiling point impurities distilled from the rectifying tower to a certain amount, and then the light impurities and the high boiling point impurities are rectified and separated again by the batch tower, so that light phase substances are recycled into the light component removing tower, enter the system again and are separated and utilized by multiple times of rectification, and the high boiling point impurities are collected by the collecting tank independently.
This scheme is because the acid water is from the mother liquor, and other impurity can not introduced to the retrieval and utilization to the mother liquor storage tank again of the acid water after here will separating, and need not independent processing acid water, realizes the inside cyclic utilization of system, reduces enterprise environmental protection pressure.
Drawings
Fig. 1 is a schematic connection diagram of the present apparatus.
In the figure: a synthesis tower 10, a condenser 11 for synthesis, a production control valve 111, an acetylene gas incoming pipeline 112, an acetylene recycling pipeline 113, a crude product tank 12, a preheater 13, a tower top temperature detector 14, a tower bottom temperature detector 15, a controller 16, an input control valve 17, a reinforcer 18, a regeneration tower 20, a condenser 21 for regeneration, a mother liquor storage tank 30, a tail gas pipeline 31, a regeneration storage tank 40, a balance pipeline 41, a first condenser 42, a second condenser 43, a light component removal tower 50, a dehydrogenation buffer tank 51, a light component temporary storage tank 52, a transition buffer tank 53, a rectification tower 60, a rectification buffer tank 61, a heavy component temporary storage tank 62, a finished product tank 63, a batch tower 70, a batch buffer tank 71, a collection tank 72, a first tail gas absorption pipeline 73, a second tail gas absorption pipeline 74, a third tail gas absorption pipeline 75, a reinforced condenser 76, a mixer 81, an oil-water separator 82, a neutralizing liquid storage tank 83, a crude product tank 12, an alkali liquor tank 84 and an acid water return pipe 85.
Detailed Description
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to these drawings without creative efforts.
Referring to fig. 1, an embodiment of the present invention provides a system for preparing trans-1, 2-dichloroethylene absorbed by crude alkali washing, including a synthesis tower 10, a regeneration tower 20, a mother liquor storage tank 30, a regeneration storage tank 40, a light component removal tower 50, a rectification tower 60, a batch tower 70, and a neutralization device, where the synthesis tower 10 and the regeneration tower 20 are packed towers, a tower bottom liquid phase inlet is connected to an outlet of the mother liquor tank, a tower top gas phase outlet of the synthesis tower 10 is connected to a synthesis condenser 11, an outlet of the synthesis condenser 11 is connected to a tower top liquid phase inlet of the synthesis tower 10 through a gas-water separator, an outlet of the synthesis condenser 11 is further connected to a crude product tank 12 through a gas-water separator, so as to input a semi-finished product containing dichloroethylene into the crude product tank 12, the tower bottom gas phase inlet of the regeneration tower 20 is used for introducing chlorine gas, the tower top liquid phase inlet of the regeneration tower 20 is connected to the regeneration storage tank 40, the regeneration tower 20 is provided with a regeneration condenser 21, the gas phase outlet at the top of the regeneration tower 20 is connected with the regeneration condenser 21, and the outlet of the regeneration condenser 21 is connected with the crude product tank 1 through a gas-water separator.
A balance pipeline 41, a first condenser 42 and a second condenser 43 are further arranged between the regeneration storage tank 40 and the crude product tank 12, the balance pipeline 41 is connected between the inlet of the first condenser 42 and the regeneration storage tank 40, the gas-phase outlet of the first condenser 42 is connected with the inlet of the second condenser 43, the liquid-phase outlet of the first condenser 42 and the liquid-phase outlet of the second condenser 43 are connected with the crude product tank 12, a tail gas pipeline 31 is further arranged between the mother liquor storage tank 30 and the regeneration condenser 21, a preheater 13 and a reinforcer 18 are further arranged between the synthesis tower 10 and the mother liquor storage tank 30, the inlet of the preheater 13 is connected with the outlet of the mother liquor storage tank 30, the outlet of the preheater 13 is connected with the liquid-phase inlet at the bottom of the reinforcer 18, the outlet at the top of the reinforcer 18 is connected with the liquid-phase inlet at the bottom of the synthesis tower.
The crude product tank 12 is connected with a light component removal tower 50 and a rectifying tower 60 through pipelines and a power pump, the light component removal tower 50 is a packed tower, a dehydrogenation buffer tank 51, a light temporary storage tank 52 and a transition buffer tank 53 are further arranged on the light component removal tower 50, the crude product tank is connected with the dehydrogenation buffer tank 51, the dehydrogenation buffer tank 51 is connected with a tower bottom liquid phase inlet of the light component removal tower 50, a tower top gas phase outlet of the light component removal tower 50 is connected with a condenser for dehydrogenation, the condenser for dehydrogenation is connected with the light temporary storage tank 52, and a tower bottom liquid phase outlet of the light component removal tower 50 is connected with the transition buffer tank 53.
The rectifying tower 60 is a packed tower, a rectifying buffer tank 61 and a heavy temporary storage tank 62 are arranged on the rectifying tower 60, the finished product tank 63, the transition buffer tank 53 is connected with the rectification buffer tank 61, the rectification buffer tank 61 is connected with the tower bottom inlet of the rectification tower 60, the gas phase outlet at the tower top of the rectification tower 60 is connected with a rectification condenser, the rectification condenser is connected with the finished product tank 63, the tower bottom outlet of the rectification tower 60 is connected with a heavy buffer tank, the tower top temperature of the lightness-removing tower 50 is lower than the boiling point temperature of trans-1, 2-dichloroethylene, the tower top temperature of the rectification tower 60 is higher than the boiling point temperature of trans-1, 2-dichloroethylene, the intermittent tower 70 is a packed tower, the intermittent tower 70 is further provided with an intermittent buffer tank 71 and a collection tank 72, the light tank and the heavy temporary storage tank are connected with the intermittent buffer tank 71, the intermittent buffer tank 71 is connected with the tower bottom inlet of the intermittent tower 70, and the gas phase outlet.
The neutralization device comprises a mixer 81, an oil-water separator 82, a neutralization solution storage tank 83 and an alkaline solution tank 84, wherein the oil-water separator 82 is connected with the outlet of the crude product tank 12, the oil phase outlet of the oil-water separator 82 is connected with the inlet of the mixer 81, alkaline solution is stored in the alkaline solution tank 84, the alkaline solution tank 84 is connected with the inlet of the mixer 81, the outlet of the mixer 81 is connected with the neutralization solution storage tank 83, and the outlet of the neutralization solution storage tank 83 conveys the neutralization solution to the dehydrogenation buffer tank 51 through a power pump and a pipeline. An acid water return pipe 85 is also provided between the oil-water separator 82 and the mother liquor storage tank.
In the invention, the dichloroethylene in the crude product tank is subjected to first light low-temperature rectification treatment by the light removal tower 50 to remove light impurities, and then is subjected to second heavy high-temperature rectification by the rectification tower 60 to remove heavy impurities, gas-phase dichloroethylene is distilled from the top of the rectification tower 60 and is stored in the finished product tank 63 after being condensed, and the content of the dichloroethylene obtained by the secondary treatment can reach 0.999%. This scheme is when realizing, through control lightness-removing tower inner tower top temperature, makes it be less than the dichloroethylene boiling point, distills off light impurity and collects alone, and heavy component such as dichloroethylene gets into the rectifying column rectification once more, and control rectifying column top temperature is higher than the dichloroethylene boiling point, makes dichloroethylene be gaseous phase discharge to the condensation is collected, and other heavy components are collected alone. According to the scheme, the light impurities and the heavy impurities are discharged in batches by performing rectification twice above and below the boiling point of the dichloroethylene, so that the purity of the dichloroethylene is ensured to reach 0.999.
The scheme temporarily stores light impurities distilled from the light component removing tower and high boiling point impurities distilled from the rectifying tower to a certain amount, and then the light impurities and the high boiling point impurities are rectified and separated again by the batch tower 70, the light phase substances are recycled into the light component removing tower and enter the system again to be rectified and separated for a plurality of times, and the high boiling point impurities are collected by the collecting tank 72 independently.
In this scheme, carry out acid-base neutralization to the crude through neutralization apparatus, alkali lye adopts low concentration alkali lye usually, in order to reduce the violent degree of neutralization reaction, adopts oil water separator 82 to separate acid water and oil phase in advance, and the acid water passes through the pipeline retrieval and utilization to mother liquor jar by the reutilization, has reduced the resource consumption of neutralization reaction, also recycles the acid waste water here simultaneously, increases the added value. This scheme is because the acid water is from the mother liquor, and other impurity can not introduced to the retrieval and utilization to the mother liquor storage tank again of the acid water after here will separating, and need not independent processing acid water, realizes the inside cyclic utilization of system, reduces enterprise environmental protection pressure.
In the invention, acetylene is used as a raw material prepared in the preceding step, the raw material and the catalyst mother liquor in the mother liquor storage tank 30 enter the synthesis tower 10, the raw material and the catalyst mother liquor react to generate a crude product containing dichloroethylene, the mother liquor deprived of a chloride ion is discharged into the regeneration storage tank 40, the liquid in the regeneration storage tank 40 is pumped into the regeneration tower 20, chlorine is introduced into the regeneration tower 20, one chloride ion in the chlorine is absorbed by the mother liquor lacking the chloride ion, the regeneration of the mother liquor is realized, the regenerated mother liquor is stored in the mother liquor storage tank 30 and is pumped into the synthesis tower 10 again for use, a part of dichloroethylene still exists at the top of the regeneration tower 20 and is condensed and refluxed into the crude product tank 12 by the regeneration condenser 21, thereby the conversion rate of the dichloroethylene in the system is improved, and the yield of the dichloroethylene in the crude product. A part of dichloroethylene still exists at the top of the regeneration tower 20, and is condensed and refluxed to the crude product tank 12 by a regeneration condenser 21. The mother liquor is copper chloride solution with copper chloride content not lower than 98%, and the mother liquor with one chloride ion being deprived is cuprous chloride solution with cuprous chloride content not lower than 98%.
The invention realizes the recycling of the mother liquor, the regeneration process and the synthesis process are continuous reaction processes, the synthesis reaction of the dichloroethylene and the regeneration of the mother liquor are mutually supplemented without mutual influence, the whole process for producing the dichloroethylene does not need to be stopped or interrupted, the structure of equipment is optimized, and the production efficiency is high.
The scheme is that a tail gas pipeline 31 is arranged on the mother liquor storage tank 30 and is used for absorbing gas which is discharged into the mother liquor storage tank 30 in the regeneration process of the regeneration tower 20, the entrained gas is discharged into a regeneration condenser 21 along the tail gas pipeline 31, and the gas is condensed and then separated and sent into a tail gas treatment system.
This scheme still sets up balanced pipeline 41, first condenser 42, second condenser 43 for regeneration storage tank 40, the mother liquor temperature of discharging from the synthetic tower 10 like regeneration storage tank 40 is higher, and inside its part secretly carries partial gaseous dichloroethylene, gets into regeneration storage tank 40 inside, causes the big problem of regeneration storage tank 40 internal pressure easily, and this scheme discharges gaseous dichloroethylene into first condenser 42 and second condenser 43, and the dichloroethylene after the condensation gets into in crude jar 12 to improve the conversion of dichloroethylene in the synthetic tower 10. The first condenser 42 and the second condenser 43 adopt a series reinforcement mode, so that the substance which is not cooled in the first condenser is secondarily condensed by the second condenser, and the gas-phase ethylene dichloride is fully collected. This scheme still sets up balanced pipeline, first condenser, second condenser for the regeneration storage tank, and is higher at the synthetic tower exhaust mother liquor temperature, and it is inside to smuggle partial gaseous dichloroethylene secretly, gets into inside the regeneration storage tank, causes the big problem of regeneration storage tank internal pressure easily, and this scheme emits gaseous dichloroethylene into first condenser and second condenser, and the dichloroethylene after being condensed gets into in the crude jar to improve the conversion of dichloroethylene in the synthetic tower.
The scheme is that the mother liquor storage tank is provided with a tail gas pipeline for absorbing gas which is discharged into the mother liquor storage tank in the regeneration process of the regeneration tower and is entrained along the tail gas pipeline, the entrained gas is discharged into a regeneration condenser, the gas is condensed and then separated and sent into a tail gas treatment system, meanwhile, part of gas-phase dichloroethylene is also entrained in the gas and is discharged into the regeneration condenser along the tail gas pipeline, and the condensed gas enters a crude product tower.
The intensifier 18 is a packed tower, the acetylene gas enters the post-preheating mother liquor to be premixed in the intensifier 18, the acetylene gas and the preheated mother liquor begin to react, the mixture at the outlet of the intensifier 18 enters the synthesis tower to be further mixed and reacted, the arrangement of the intensifier 18 can lead the materials to be contacted and reacted in advance, the materials are contacted and reacted fully, the material reaction time is prolonged, the acetylene gas and the synthesis tower are fully mixed in advance, the reaction begins in advance, and the full preparation is made for the reaction in the synthesis tower.
Further, an acetylene recycling pipeline 113 is arranged for the second condenser, the other end of the acetylene recycling pipeline 113 is connected with an acetylene gas incoming pipeline 112, and a pipeline for connecting the second condenser is arranged on a gas-liquid separator of the condenser for synthesis. The gas phase remained in the gas-liquid separator and not condensed enters a second condenser, the gas-phase dichloroethylene is condensed and then enters a crude product tank, and part of acetylene gas flows back along an acetylene recycling pipeline 113 for secondary utilization. The scheme does not need to arrange a gas phase balance port for the second condenser, and can recycle the gas phase, thereby improving the utilization rate of acetylene.
According to the scheme, the mother liquor is preheated in advance before entering the synthesis tower 10, the preheating temperature is 88-93 ℃, the preheated mother liquor enters the synthesis tower 10, the required heat is less, the time point of the synthesis reaction of the mother liquor and acetylene gas can be advanced, the time required by the synthesis reaction is shortened, and the reaction efficiency is improved.
Further, a tower top temperature detector 14 and a tower bottom temperature detector 15 are arranged at both the tower top and the tower bottom of the synthesis tower 10, a controller 16 (of course, the controller 16 does not control the on-off of the acetylene input pipeline, and the pipeline is only used as a carrier for installing the controller 16) and an input control valve 17 are arranged on a pipeline for inputting acetylene, a recovery control valve 111 is arranged on a pipeline for connecting the synthesis condenser 11 and the crude product tank 12, and the controller 16 is connected with the tower top temperature detector 14, the tower bottom temperature detector 15, the input control valve 17 and the recovery control valve 111. The scheme forms an interlocking control system by a temperature controller 16 and a temperature detector, the temperature controller 16 adopts the existing equipment in the prior art, a tower top temperature detector 14 is used for detecting the temperature at the top of the synthesis tower 10, a tower bottom temperature detector 15 is used for detecting the temperature at the bottom of the synthesis tower 10, when the real-time temperature detected by the tower top temperature detector 14 is higher than the set value, which indicates that the content of high boiling point heavy components in the product produced at the tower top is higher, multiple times of reflux condensation separation are needed, the controller 16 controls the extraction control valve 111 to close and controls the input control valve 17 to close, otherwise, when the real-time temperature detected by the tower top temperature detector 14 is lower than the set value, which indicates that the content of dichloroethylene in the product produced at the tower top is higher, at this time, the controller 16 controls the extraction control valve 111 to be intermittently opened to extract the semi-finished product, and controls the input control valve 17 to be opened to input acetylene gas. The controller can be realized by adopting a switch circuit in the prior art.
Further, still set up first tail gas absorption pipeline 73 for the condenser for dehydrogenation tower, still set up second tail gas absorption pipeline 74 for light temporary storage tank, still set up third tail gas absorption pipeline 75 for the condenser for rectifying column, first tail gas absorption pipeline 73, second tail gas absorption pipeline 74, third tail gas absorption pipeline 75 are collected in strengthening condenser 76, and the export of strengthening condenser 76 is connected with intermittent buffer tank 71. The whole retrieval and utilization of tail gas are absorbed in this scheme, are separated by batch column rectification, and inside the retrieval and utilization system, tail gas need not to arrange outward.
The modules or units in the device of the embodiment of the invention can be combined, divided and deleted according to actual needs.
The above disclosure is only illustrative of the preferred embodiments of the present invention, which should not be taken as limiting the scope of the invention, but rather the invention can be embodied in other specific forms without departing from the spirit or essential characteristics thereof. It will be understood by those skilled in the art that all or a portion of the above-described embodiments may be practiced and equivalents thereof may be resorted to as falling within the scope of the invention as claimed. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.
Furthermore, it should be understood that although the present description refers to embodiments, not every embodiment may contain only a single embodiment, and such description is for clarity only, and those skilled in the art should integrate the description, and the embodiments may be combined as appropriate to form other embodiments understood by those skilled in the art.
Claims (9)
1. A trans-1, 2-dichloroethylene preparation system for crude product alkali washing absorption is characterized in that: the device comprises a synthetic tower, a regeneration tower, a mother liquor storage tank, a regeneration storage tank and a neutralization device, wherein the synthetic tower and the regeneration tower are packed towers, a liquid phase inlet at the bottom of the tower is connected with an outlet of a mother liquor tank, a gas phase outlet at the top of the synthetic tower is connected with a condenser for synthesis, an outlet of the condenser for synthesis is connected with a liquid phase inlet at the top of the synthetic tower through a gas-water separator, an outlet of the condenser for synthesis is also connected with a crude product tank through the gas-water separator so as to input a semi-finished product containing dichloroethylene into the crude product tank, a gas phase inlet at the bottom of the regeneration tower is used for introducing chlorine gas, a liquid phase inlet at the top of the regeneration tower is connected with the regeneration storage tank, a liquid phase outlet at the bottom of the regeneration tower is connected with the mother liquor storage tank, the regeneration tower is provided with a regeneration condenser, a gas phase outlet at the top, The exit of enhancer, the entry linkage mother liquor storage tank of pre-heater, the liquid phase entry at the bottom of the exit linkage enhancer of pre-heater, the liquid phase entry at the bottom of the top of the tower exit linkage synthetic tower of enhancer, the gaseous access connection acetylene gas incoming material pipeline of enhancer, neutralization apparatus includes blender, oil water separator, neutralization liquid storage tank, lye tank, the export of crude jar is connected to oil water separator, oil water separator's oil phase exit linkage blender entry, deposits alkali lye in the lye tank, lye tank and blender access connection, the exit linkage neutralization liquid storage tank of blender, and the export of neutralization liquid storage tank is passed through power pump, pipeline and will be neutralized liquid and discharge.
2. The system for the production of trans-1, 2-dichloroethylene with crude caustic wash absorption according to claim 1, wherein: the top and bottom of the synthetic tower are provided with a top temperature detector and a bottom temperature detector, a pipeline for inputting acetylene is provided with a controller and an input control valve, a pipeline for connecting the condenser for synthesis and the crude product tank is provided with a production control valve, and the controller is connected with the top temperature detector, the bottom temperature detector, the input control valve and the production control valve.
3. The system for the production of trans-1, 2-dichloroethylene with crude caustic wash absorption according to claim 1, wherein: still set up balanced pipeline, first condenser, second condenser between regeneration storage tank and crude jar, balanced pipeline connects between the entry of first condenser and regeneration storage tank, and the gaseous phase export of first condenser and the entry linkage of second condenser, and the liquid phase export of first condenser and the liquid phase export of second condenser connect crude jar, still sets up the tail gas pipeline between mother liquor storage tank and the condenser for regeneration.
4. The system for the production of trans-1, 2-dichloroethylene with crude caustic wash absorption according to claim 3, wherein: and an acetylene recycling pipeline is also arranged for the second condenser, the other end of the acetylene recycling pipeline is connected with an acetylene gas incoming pipeline, and a gas-liquid separator of the condenser for synthesis is provided with a pipeline for connecting the second condenser.
5. The system for the production of trans-1, 2-dichloroethylene with crude caustic wash absorption according to claim 4, wherein: the system is also provided with a light component removing tower and a rectifying tower, a crude product tank is connected with the light component removing tower and the rectifying tower through a pipeline and a power pump, the light component removing tower is a packed tower, the light component removing tower is also provided with a dehydrogenation buffer tank, a light temporary storage tank and a transition buffer tank, the crude product tank is connected with the dehydrogenation buffer tank, the dehydrogenation buffer tank is connected with a tower bottom liquid phase inlet of the light component removing tower, a tower top gas phase outlet of the light component removing tower is connected with a dehydrogenation condenser, the dehydrogenation condenser is connected with the light temporary storage tank, a tower bottom liquid phase outlet of the light component removing tower is connected with the transition buffer tank, the rectifying tower is a packed tower, the rectifying tower is also provided with a rectifying buffer tank, a heavy temporary storage tank and a finished product tank, the transition buffer tank is connected with the rectifying buffer tank, the rectifying buffer tank is connected with a tower bottom inlet of the rectifying tower, a tower top gas phase outlet of the rectifying tower is connected with a, the tower top temperature of the light component removal tower is lower than the boiling point temperature of trans-1, 2-dichloroethylene, and the tower top temperature of the rectification tower is higher than the boiling point temperature of trans-1, 2-dichloroethylene.
6. The system for the production of trans-1, 2-dichloroethylene with crude caustic wash absorption according to claim 5, wherein: the system is further provided with an intermittent tower which is a packed tower and is also provided with an intermittent buffer tank and a collecting tank, the light temporary storage tank and the heavy temporary storage tank are connected with the intermittent buffer tank, the intermittent buffer tank is connected with an inlet at the bottom of the intermittent tower, and a gas phase outlet of the intermittent tower is connected with the collecting tank through a condenser.
7. The system for the production of trans-1, 2-dichloroethylene with crude caustic wash absorption according to claim 6, wherein: an acid water return pipe is also arranged between the oil-water separator and the mother liquor storage tank.
8. The system for the production of trans-1, 2-dichloroethylene with crude caustic wash absorption according to claim 4, wherein: still set up first tail gas absorption pipeline for the condenser for dehydrogenation tower, still set up second tail gas absorption pipeline for the jar is kept in to the light, still set up third tail gas absorption pipeline for the condenser for the rectifying column, first tail gas absorption pipeline, second tail gas absorption pipeline, third tail gas absorption pipeline are collected in strengthening the condenser, and the export of strengthening the condenser is connected with intermittent buffer jar.
9. The system for the production of trans-1, 2-dichloroethylene with crude caustic wash absorption according to claim 1, wherein: the mother liquor adopts cupric chloride, and the mother liquor deprived of a chloride ion is cuprous chloride.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110179993.3A CN112973594B (en) | 2021-02-08 | 2021-02-08 | Trans-1, 2-dichloroethylene preparation system for crude product alkaline washing absorption |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110179993.3A CN112973594B (en) | 2021-02-08 | 2021-02-08 | Trans-1, 2-dichloroethylene preparation system for crude product alkaline washing absorption |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112973594A true CN112973594A (en) | 2021-06-18 |
| CN112973594B CN112973594B (en) | 2022-07-12 |
Family
ID=76392812
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110179993.3A Active CN112973594B (en) | 2021-02-08 | 2021-02-08 | Trans-1, 2-dichloroethylene preparation system for crude product alkaline washing absorption |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112973594B (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3301910A (en) * | 1963-02-22 | 1967-01-31 | Uddeholms Ab | Production of trichloroethylene and tetrachloroethylene |
| CN101747141A (en) * | 2009-12-22 | 2010-06-23 | 南通天海化工助剂有限公司 | Technology for producing trans-1,2-dichloroethylene |
| CN104876792A (en) * | 2015-05-21 | 2015-09-02 | 山东海益化工科技有限公司 | Method for producing high-purity chloropropene |
| CN108299153A (en) * | 2018-04-09 | 2018-07-20 | 浙江巨化技术中心有限公司 | A kind of preparation method of trans- 1,2- dichloroethylene |
| CN210595277U (en) * | 2019-10-08 | 2020-05-22 | 中化重庆涪陵化工有限公司 | System for utilize synthetic ammonia gas-liquid separation's aqueous ammonia production monoammonium phosphate |
-
2021
- 2021-02-08 CN CN202110179993.3A patent/CN112973594B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3301910A (en) * | 1963-02-22 | 1967-01-31 | Uddeholms Ab | Production of trichloroethylene and tetrachloroethylene |
| CN101747141A (en) * | 2009-12-22 | 2010-06-23 | 南通天海化工助剂有限公司 | Technology for producing trans-1,2-dichloroethylene |
| CN104876792A (en) * | 2015-05-21 | 2015-09-02 | 山东海益化工科技有限公司 | Method for producing high-purity chloropropene |
| CN108299153A (en) * | 2018-04-09 | 2018-07-20 | 浙江巨化技术中心有限公司 | A kind of preparation method of trans- 1,2- dichloroethylene |
| CN210595277U (en) * | 2019-10-08 | 2020-05-22 | 中化重庆涪陵化工有限公司 | System for utilize synthetic ammonia gas-liquid separation's aqueous ammonia production monoammonium phosphate |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112973594B (en) | 2022-07-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102826950B (en) | Process method for circularly utilizing waste water produced by butadiene preparation through butene oxidative dehydrogenation | |
| CN108840310B (en) | Device and process for producing hydrogen chloride by deep analysis from dilute hydrochloric acid | |
| CN111302899A (en) | Device and method for recovering ammonia and tert-butyl alcohol in cyclohexanone ammoximation production process | |
| CN105555772A (en) | Alkylene oxide separation systems, methods, and apparatuses | |
| CN104649887B (en) | Production method of chloroacetic acid and method for recovering catalysts in production process of chloroacetic acid | |
| CN110922292B (en) | Preparation method of chloromethane | |
| CN110272348A (en) | Recovery process for organic silicon waste acid containing tri-n-butylamine, siloxane and aluminum chloride | |
| CN108641023A (en) | A kind of mercuryless Production of PVC technique | |
| CN112973594B (en) | Trans-1, 2-dichloroethylene preparation system for crude product alkaline washing absorption | |
| CN104119201A (en) | Dry separation and purification system and purification method for fluorine-containing alkane | |
| CN112961026B (en) | Acetylene purification linkage control type trans-1, 2-dichloroethylene preparation system | |
| CN214528777U (en) | Intermittent secondary absorption type trans-1, 2-dichloroethylene preparation system | |
| CN214514487U (en) | Material reinforced mixed trans-1, 2-dichloroethylene production device | |
| CN212102637U (en) | Ammonia and tert-butyl alcohol recovery device in cyclohexanone ammoximation production process | |
| CN214514486U (en) | Trans-1, 2-dichloroethylene preparation system | |
| CN114249676A (en) | Method and device for purifying and separating methyl mercaptan | |
| CN214528776U (en) | Improved integrated trans-1, 2-dichloroethylene preparation device | |
| CN110156555B (en) | Fuel oil recovery process | |
| CN214514610U (en) | Catalyst regeneration integration trans-1, 2-dichloroethylene preparation facilities | |
| CN111978184A (en) | Retrieve device of methylamine in follow NMP crude | |
| CN217940146U (en) | Trans-1,2-dichloroethylene production system | |
| CN220513452U (en) | Piperidine separation and purification system | |
| CN216777944U (en) | Device system for continuously recovering triethylamine from triethylamine hydrochloride solution | |
| CN215828661U (en) | Ethylene carbonate device exhaust gas system material recovery unit | |
| CN211987148U (en) | Fractionating device for mixed acid of phosphoric acid, acetic acid and nitric acid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |