CN108147949B - Method for separating benzenediol reaction liquid - Google Patents
Method for separating benzenediol reaction liquid Download PDFInfo
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- CN108147949B CN108147949B CN201611110570.1A CN201611110570A CN108147949B CN 108147949 B CN108147949 B CN 108147949B CN 201611110570 A CN201611110570 A CN 201611110570A CN 108147949 B CN108147949 B CN 108147949B
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- YCIMNLLNPGFGHC-UHFFFAOYSA-N catechol Chemical compound OC1=CC=CC=C1O YCIMNLLNPGFGHC-UHFFFAOYSA-N 0.000 title claims abstract description 103
- 239000012295 chemical reaction liquid Substances 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title description 41
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 114
- QIGBRXMKCJKVMJ-UHFFFAOYSA-N Hydroquinone Chemical compound OC1=CC=C(O)C=C1 QIGBRXMKCJKVMJ-UHFFFAOYSA-N 0.000 claims abstract description 78
- 230000008016 vaporization Effects 0.000 claims abstract description 39
- 239000007788 liquid Substances 0.000 claims abstract description 36
- 239000012808 vapor phase Substances 0.000 claims abstract description 30
- 238000000926 separation method Methods 0.000 claims abstract description 17
- 239000003054 catalyst Substances 0.000 claims abstract description 14
- 238000009834 vaporization Methods 0.000 claims description 35
- 238000006243 chemical reaction Methods 0.000 claims description 14
- 238000005805 hydroxylation reaction Methods 0.000 claims description 11
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 10
- 150000002989 phenols Chemical class 0.000 claims description 4
- 230000006866 deterioration Effects 0.000 abstract description 32
- 239000000463 material Substances 0.000 abstract description 15
- 239000011269 tar Substances 0.000 description 36
- 239000000203 mixture Substances 0.000 description 12
- 230000033444 hydroxylation Effects 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000009835 boiling Methods 0.000 description 3
- KQUXHNRTCORKIG-UHFFFAOYSA-N hydrogen peroxide;phenol Chemical compound OO.OC1=CC=CC=C1 KQUXHNRTCORKIG-UHFFFAOYSA-N 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- RFFLAFLAYFXFSW-UHFFFAOYSA-N 1,2-dichlorobenzene Chemical compound ClC1=CC=CC=C1Cl RFFLAFLAYFXFSW-UHFFFAOYSA-N 0.000 description 2
- GQLFYNLDVCYDKN-UHFFFAOYSA-N 2-hydroperoxyphenol Chemical compound OOC1=CC=CC=C1O GQLFYNLDVCYDKN-UHFFFAOYSA-N 0.000 description 2
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000005235 decoking Methods 0.000 description 2
- 229940079593 drug Drugs 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 239000000975 dye Substances 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000000575 pesticide Substances 0.000 description 2
- 239000005060 rubber Substances 0.000 description 2
- OKIRBHVFJGXOIS-UHFFFAOYSA-N 1,2-di(propan-2-yl)benzene Chemical compound CC(C)C1=CC=CC=C1C(C)C OKIRBHVFJGXOIS-UHFFFAOYSA-N 0.000 description 1
- XKZQKPRCPNGNFR-UHFFFAOYSA-N 2-(3-hydroxyphenyl)phenol Chemical compound OC1=CC=CC(C=2C(=CC=CC=2)O)=C1 XKZQKPRCPNGNFR-UHFFFAOYSA-N 0.000 description 1
- ISPYQTSUDJAMAB-UHFFFAOYSA-N 2-chlorophenol Chemical compound OC1=CC=CC=C1Cl ISPYQTSUDJAMAB-UHFFFAOYSA-N 0.000 description 1
- OMNGOGILVBLKAS-UHFFFAOYSA-N 2-methoxyphenol Chemical compound COC1=CC=CC=C1O.COC1=CC=CC=C1O OMNGOGILVBLKAS-UHFFFAOYSA-N 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 150000005205 dihydroxybenzenes Chemical class 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 235000013599 spices Nutrition 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000002641 tar oil Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/68—Purification; separation; Use of additives, e.g. for stabilisation
- C07C37/685—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/68—Purification; separation; Use of additives, e.g. for stabilisation
- C07C37/70—Purification; separation; Use of additives, e.g. for stabilisation by physical treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/68—Purification; separation; Use of additives, e.g. for stabilisation
- C07C37/70—Purification; separation; Use of additives, e.g. for stabilisation by physical treatment
- C07C37/74—Purification; separation; Use of additives, e.g. for stabilisation by physical treatment by distillation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a separation method of a benzenediol reaction liquid, which comprises the following steps: vaporizing the benzenediol reaction liquid to obtain a first vapor phase condensate, vaporized residual liquid and a first cold neck collecting liquid; steam stripping the vaporized residual liquid by adopting vaporous phenol to obtain a second vapor-phase condensate, steam-stripped residual liquid and a second cold-neck collecting liquid; and rectifying the first vapor phase condensate and the second vapor phase condensate to separate phenol, catechol and hydroquinone. The invention firstly vaporizes the reaction liquid, and separates the tar and the catalyst from the phenol and the benzenediol, the temperature is lower, and the deterioration loss of the materials is reduced; then phenol is used for stripping to extract the residual benzenediol in the tar, so that the content of the benzenediol in the discharged tar is greatly reduced, and the lower loss of taking away is realized under the condition of lower deterioration loss. Then the purpose of separating phenol, catechol and hydroquinone can be achieved by rectification.
Description
Technical Field
The invention relates to the technical field of preparation of benzenediol, in particular to a separation method of benzenediol reaction liquid.
Background
The benzenediol comprises pyrocatechol and hydroquinone, is an important chemical raw material, and has wide application fields. Wherein, the catechol is used as a basic raw material of fine chemicals and is used in the industries of pesticides, spices, medicines, dyes, polymers and the like; hydroquinone is an important intermediate of photography, rubber, dyes, pesticides and medicines, has wide application range, and expands the application field in recent years.
The traditional industrial production method of catechol and hydroquinone mainly comprises the following steps:
(1) hydrolysis of o-chlorophenol or o-dichlorobenzene;
(2) hydrolysis of guaiacol (o-methoxyphenol);
(3) aniline oxidation process;
(4) diisopropylbenzene oxidation method.
The above process has complex reaction process, more byproducts, serious environmental pollution and high production cost.
In contrast, the phenol hydrogen peroxide hydroxylation method is characterized in that phenol and hydrogen peroxide are used as raw materials, hydroxylation reaction is carried out on ortho-position and para-position through a catalyst, catechol and hydroquinone are synthesized in one step, the method is simpler than the indirect multi-step method, and almost all catechol and hydroquinone more than 1/3 in the world are produced by the phenol hydrogen peroxide hydroxylation method at present. The process route is simple, the raw materials are cheap, the byproducts are water and a small amount of tar, and the environmental pollution is low, so the process enjoys the reputation of a 'clean process', is the latest technology of competitive research and development in the world at present, and is acknowledged as the most promising process for producing the benzenediol in the 21 st century. At present, the international industrial phenol hydrogen peroxide hydroxylation method for synthesizing the o/hydroquinone has been successfully carried out, such as Rhone-Poulenc method, Brichima method, Ube method and the like. However, the conversion rate of the phenol hydroperoxide hydroxylation method is generally low, and the reaction solution comprises water, phenol, catechol, hydroquinone, tar and a catalyst, so that the post-treatment is complicated.
At present, the post-treatment of the reaction liquid of the phenol hydroperoxide hydroxylation method is divided into two procedures: separating reaction liquid and refining benzenediol. The water in the reaction solution forms an azeotrope with phenol, the boiling point (99.5 ℃) of which is very different from the boiling point (182 ℃) of phenol, and can be easily separated in advance by a mature method. After removal of water, the task of the reaction liquid separation is to separate the reaction liquid into three fractions:
and (3) recycling phenol: containing a small amount of water and benzenediol, and returning to the reaction process;
mixing benzenediol: containing a small amount of phenol, and sending to a dihydroxybenzene refining process;
tar oil: containing a small amount of hydroquinone and discharging.
For example, the separation and purification method reported in the patent CNl45086A of the company rona planck: the reaction product after dehydration and concentration is sent to a dephenolizing tower for removing phenol for the first time, the tower bottom material is sent to a decoking tower and an evaporator for removing tar, the distillate material of the decoking tower is sent to a second dephenolizing tower, the material after completely removing phenol is sent to a product refining tower, and catechol and hydroquinone are separated out. In the process, the tar removal evaporator adopts a film evaporator, the tar is discharged from the system before part of phenol and pyrocatechol are removed, and the separated tar contains about 7 percent of hydroquinone.
However, the current reaction liquid separation method has two main problems-deterioration loss and entrainment loss:
phenol, catechol, and hydroquinone have atmospheric boiling points of 182 deg.C, 246 deg.C, and 287 deg.C, respectively, and the aged gum (i.e., tar) is essentially a non-volatile matter, and therefore, separation thereof is not difficult to achieve by rectification separation. But there is a great loss of material in the rectification separation process.
Phenol and benzenediol are heat-sensitive substances and can deteriorate in the rectification process. Experiments show that the quality loss of pure phenol and benzenediol is not large and is below 1 percent when the pure phenol and the benzenediol are rectified at 200 ℃. However, when they coexist with a catalyst and a conventional rubber, deterioration loss is remarkably increased, which is a first problem to be solved in the separation of a reaction liquid. The deterioration loss depends on the heating time and the rectification temperature of the material, and the shorter the heating time is, the lower the rectification temperature is, and the smaller the deterioration loss is.
Meanwhile, the discharged tar contains benzenediol, which causes carrying loss. The quantity of the benzenediol contained in the tar with small volatility depends on the temperature of the rectifying still, and the lower the temperature, the greater the carrying loss.
Therefore, the deterioration loss and the carry-away loss trade off. In order to reduce the carrying loss, the tar removing temperature is high, but the deterioration loss at high temperature is obviously increased, the total loss can be larger, and the deterioration loss and the carrying loss are difficult to be solved, which is an important problem to be solved urgently in the separation of reaction liquid.
Disclosure of Invention
In view of the above, the technical problem to be solved by the present invention is to provide a method for separating a dihydroxybenzene reaction liquid, which has low deterioration loss and low carrying-away loss.
The invention provides a separation method of a benzenediol reaction liquid, which comprises the following steps:
vaporizing the benzenediol reaction liquid to obtain a first vapor phase condensate, vaporized residual liquid and a first cold neck collecting liquid;
steam stripping the vaporized residual liquid by adopting vaporous phenol to obtain a second vapor-phase condensate, steam-stripped residual liquid and a second cold-neck collecting liquid;
and rectifying the first vapor phase condensate and the second vapor phase condensate to separate phenol, catechol and hydroquinone.
Preferably, the pressure of the vaporization is 15 mmHg.
Preferably, the vaporization temperature is 160-200 ℃.
Preferably, the pressure of the stripping is 15 mmHg.
Preferably, the stripping temperature is 160-220 ℃.
Preferably, the diphenol reaction solution is a reaction solution obtained by a hydrogen peroxide hydroxylation reaction of dehydrated phenol.
Preferably, the reaction liquid contains phenol, catechol, hydroquinone, tar and a catalyst.
Compared with the prior art, the invention provides a method for separating a benzenediol reaction liquid, which comprises the following steps: vaporizing the benzenediol reaction liquid to obtain a first vapor phase condensate, vaporized residual liquid and a first cold neck collecting liquid; steam stripping the vaporized residual liquid by adopting vaporous phenol to obtain a second vapor-phase condensate, steam-stripped residual liquid and a second cold-neck collecting liquid; and rectifying the first vapor phase condensate and the second vapor phase condensate to separate phenol, catechol and hydroquinone. The invention firstly vaporizes the reaction liquid, separates the tar and the catalyst from the phenol and the hydroquinone, has lower temperature, reduces the deterioration loss of the materials, and has the deterioration loss rate of the phenol below 0.4 percent, the deterioration loss rate of the catechol below 3 percent and the deterioration loss rate of the hydroquinone below 3.5 percent; and then phenol is used for stripping to extract the residual benzenediol in the tar, so that the content of the benzenediol in the discharged tar is greatly reduced, the residual content of the pyrocatechol is less than 1%, the residual content of the hydroquinone is less than 5%, and the lower loss of taking away is realized under the condition of lower deterioration loss. Then the purpose of separating phenol, catechol and hydroquinone can be achieved by rectification.
Detailed Description
The invention provides a separation method of a benzenediol reaction liquid, which comprises the following steps:
vaporizing the benzenediol reaction liquid to obtain a first vapor phase condensate, vaporized residual liquid and a first cold neck collecting liquid;
steam stripping the vaporized residual liquid by adopting vaporous phenol to obtain a second vapor-phase condensate, steam-stripped residual liquid and a second cold-neck collecting liquid;
and rectifying the first vapor phase condensate and the second vapor phase condensate to separate phenol, catechol and hydroquinone.
The method comprises the steps of vaporizing reaction liquid, condensing to obtain first vapor-phase condensate, vaporized residual liquid and first cold-neck collecting liquid. Wherein the first vapor phase condensate contains a large amount of phenol and benzenediol; the vaporized residual liquid mainly comprises tar, a catalyst and phenol and dihydroxybenzene which are partially carried away along with the tar; the cold-neck collection was phenol.
The vaporization is preferably carried out under a negative pressure, the pressure of vaporization preferably being 15 mmHg.
The vaporization temperature is preferably 160-200 ℃, more preferably 170-190 ℃, and most preferably 180 ℃.
The vaporization method is not particularly limited in the present invention, and may be a vaporization method known to those skilled in the art. Preferably, continuous thorough mixing is employed to minimize the partial pressure of hydroquinone in the vapor phase in contact with the tar and to reduce the residual content of hydroquinone in the tar.
The vaporization is preferably carried out in a vaporization kettle.
The tar and the catalyst are separated from the phenol and the hydroquinone in the vaporization process, the vaporization temperature is low, the deterioration loss of the materials is reduced, and experimental results show that the deterioration loss rate of the phenol is below 0.4%, the deterioration loss rate of the catechol is below 3%, and the deterioration loss rate of the hydroquinone is below 3.5%.
Then the vaporized residual liquid obtained in the vaporization process is stripped, preferably vaporous phenol is used as a stripping agent, and is contacted with the vaporized residual liquid for stripping, so that the residual benzenediol is extracted from the tar. Respectively obtaining a second vapor phase condensate, a stripping residual liquid and a second cold neck collecting liquid.
Wherein the second vapor phase condensate mainly contains phenol and dihydroxybenzene carried away with tar; the stripping residual liquid mainly contains residual tar and catalyst; the second cold-neck collection was phenol.
The cold neck collection liquid is a liquid phase collected by a cold neck collection bottle.
The stripping is preferably carried out under negative pressure, the pressure of stripping preferably being 15 mmHg.
The temperature of the steam stripping is preferably 160-220 ℃, more preferably 170-210 ℃, and most preferably 180-200 ℃.
The stripping method of the present invention is not particularly limited, and may be a stripping method known to those skilled in the art. Countercurrent stripping, or total mixing stripping is preferred, as long as vapor-liquid contact is enhanced.
The stripping is preferably carried out in a stripping vessel.
The invention adopts a stripping mode to extract the residual benzenediol in the tar, thereby greatly reducing the content of the benzenediol in the discharged tar, ensuring that the residual content of the pyrocatechol is less than 1 percent and the residual content of the hydroquinone is less than 5 percent, and further having lower loss of taking away.
Meanwhile, before rectification, the invention removes the catalyst and tar in the phenol and benzenediol system, improves the purity and reduces the deterioration loss.
Then the purpose of separating phenol, catechol and hydroquinone can be achieved by rectification.
Specifically, the vapor phase condensate obtained in the vaporization and stripping process enters a rectifying tower to separate phenol and benzenediol. The pressure of the rectification is preferably 15mmHg to facilitate the connection of the equipment.
Because of the high vacuum degree, a (0 ℃) cold well is preferably arranged behind the condenser and in front of the vacuum pump to capture phenol, and the captured phenol is in a solid state.
Because tar and catalyst are non-volatile, the present invention adopts the simplest vaporization to remove them from the reaction solution. The low vaporization temperature results in a higher concentration of benzenediols in the vaporized raffinate. The invention adopts phenol stripping to the vaporized residual liquid, greatly reduces the content of the benzenediol in the discharged tar, realizes lower loss of taking away under the condition of low deterioration loss, and reduces the loss of the benzenediol discharged along with the tar to below 3 percent. In the invention, because the rectification separation of phenol and benzenediol is carried out after tar and catalyst are removed, the deterioration loss of materials in the rectification process becomes extremely small.
In order to further illustrate the present invention, the following will describe the method for separating the reaction solution of benzenediol in accordance with the present invention in detail with reference to the examples.
Example 1
180.1g of the reaction liquid obtained by the hydroperoxide hydroxylation of dehydrated phenol was continuously vaporized in a 100ml vaporization vessel at a vaporization pressure of 15mmHg and a vaporization temperature of 180 ℃. As a result of the vaporization, 166.8g of vapor-phase condensate, 8.3g of vaporized residue and 4.6g of cold-neck condensate were obtained.
The composition of the individual streams and the mass balance of the individual components are shown in Table 1, where Table 1 shows the composition of the individual streams and the mass balance of the individual components obtained by vaporization. Wherein the loss rate of phenol in the vaporization process is 0.39%, the deterioration loss rate of catechol is 2.6%, and the deterioration loss rate of hydroquinone is 3.4%.
8.3g of the vaporized residue obtained in the vaporization were continuously stripped with 120g of phenol in a 100ml stripping vessel at a stripping pressure of 15mmHg and a stripping temperature of 180 ℃. As a result of the stripping, 166.8g of vapor-phase condensate, 8.3g of stripped residue and 4.6g of cold-neck condensate were obtained.
The compositions of the individual streams and the mass balance of the individual components are shown in Table 2, and Table 2 shows the compositions of the individual streams and the mass balance of the individual components obtained by steam stripping. As can be seen from Table 2, the resulting stripped residue tar contained no phenol, a residual catechol concentration of 0.7% and a residual hydroquinone concentration of 3.9%.
TABLE 1 composition of the individual streams of material obtained by vaporization and the material balance of the individual components
TABLE 2 composition of the stripped stocks and material balance of the components
As can be seen from tables 1 and 2, the total phenol deterioration loss rate in the above vaporization and stripping processes was 3.4%, catechol deterioration loss rate was 3.4%, hydroquinone deterioration loss rate was 4.9%, the entrainment loss of catechol with the discharge of tar was 0.3%, and the entrainment loss of hydroquinone with the discharge of tar was 2%.
Example 2
180.1g of the reaction liquid obtained by the hydroperoxide hydroxylation of dehydrated phenol was continuously vaporized in a 100ml vaporization vessel at a vaporization pressure of 15mmHg and a vaporization temperature of 180 ℃. As a result of the vaporization, 167.9g of vapor-phase condensate, 8.2g of vaporized residue and 3.7g of cold-neck condensate were obtained.
The composition of the individual streams and the mass balance of the individual components are shown in Table 3, where Table 3 shows the composition of the individual streams and the mass balance of the individual components obtained by vaporization. As can be seen from Table 3, the loss rate of phenol in the vaporization process was 0.39%, the deterioration loss rate of catechol was 2.5%, and the deterioration loss rate of hydroquinone was 3.4%.
8.2g of the vaporized residue obtained in the vaporization were continuously stripped with 60.5g of phenol in a 100ml stripping vessel at a stripping pressure of 15mmHg and a stripping temperature of 180 ℃. As a result of the stripping, 59.9g of vapor-phase condensate, 5.4g of stripped residue and 3.3g of cold-neck condensate were obtained. The compositions of the individual streams and the mass balances of the individual components are shown in Table 4, where Table 4 shows the compositions of the individual streams and the mass balances of the individual components obtained by stripping.
As can be seen from Table 4, the stripped residue tar contained no phenol, with a residual catechol concentration of 0.7% and a residual hydroquinone concentration of 4.9%.
TABLE 3 composition of the individual streams of material obtained by vaporization and the material balance of the individual components
TABLE 4 composition of the stripped stocks and material balance of the components
As can be seen from tables 3 and 4, the total phenol deterioration loss rate in the vaporization and stripping processes was 3.7%, the catechol deterioration loss rate was 3.2%, the hydroquinone deterioration loss rate was 4.8%, the entrainment loss of catechol with the discharge of tar was 0.3%, and the entrainment loss of hydroquinone with the discharge of tar was 2.6%.
As can be seen from the above examples, the present invention first removes tar and catalyst from the reaction solution of the hydroxylation of hydrogen peroxide of phenol by means of vaporization-stripping, and then separates phenol and benzenediol by means of rectification to complete the crude separation of the reaction solution. Lower entrainment losses are achieved with lower deterioration losses.
The above description of the embodiments is only intended to facilitate the understanding of the method of the invention and its core idea. It should be noted that, for those skilled in the art, it is possible to make various improvements and modifications to the present invention without departing from the principle of the present invention, and those improvements and modifications also fall within the scope of the claims of the present invention.
Claims (3)
1. The separation method of the benzenediol reaction liquid is characterized by comprising the following steps of:
vaporizing the benzenediol reaction liquid to obtain a first vapor phase condensate, vaporized residual liquid and a first cold neck collecting liquid;
steam stripping the vaporized residual liquid by adopting vaporous phenol to obtain a second vapor-phase condensate, steam-stripped residual liquid and a second cold-neck collecting liquid;
rectifying the first vapor phase condensate and the second vapor phase condensate to separate phenol, catechol and hydroquinone;
the pressure of the vaporization is 15 mmHg;
the vaporization temperature is 160-200 ℃;
the pressure of the stripping is 15 mmHg;
the stripping temperature is 160-220 ℃.
2. The separation method according to claim 1, wherein the reaction solution of the benzenediol is a reaction solution obtained by a hydrogen peroxide hydroxylation reaction of dehydrated phenol.
3. The separation method according to claim 2, wherein the reaction solution contains phenol, catechol, hydroquinone, tar and a catalyst.
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