CN112850945A

CN112850945A - Dust-containing phenol water separation process and separation method

Info

Publication number: CN112850945A
Application number: CN202011568110.XA
Authority: CN
Inventors: 傅敏燕; 丁烙勇
Original assignee: SHANGHAI ZEMAG MINDAC MACHINERY EQUIPMENT CO LTD
Current assignee: SHANGHAI ZEMAG MINDAC MACHINERY EQUIPMENT CO LTD
Priority date: 2020-12-25
Filing date: 2020-12-25
Publication date: 2021-05-28

Abstract

The invention discloses a dust-containing phenol-water separation process and a separation method, belonging to the field of phenol-water separation, wherein the process comprises a primary tar separator, a buffer tank, a multiplication separator A, a filter and a settling tank which are sequentially connected according to the flow direction of phenol-water; the multiplication separator A comprises a separator tank body, and an overflow partition plate A, an overflow partition plate B and an overflow partition plate C are sequentially arranged in the separator tank body to divide a suspension separation zone with a feeding gradually-expanding opening, a cyclone and a tar opening, a filler zone with fillers, a special plate group zone with folded plates and an outlet zone with a water phase outlet and an oil phase outlet; the overflow partition plates A and B are sealed at the lower part of the separator tank body, the bottom of the overflow partition plate B is provided with a through hole, and the overflow partition plate C is sealed at the middle part of the separator tank body. The method comprises at least five-stage separation (the highest effective separation can be achieved by eight stages in one-time pass), so that micro oil drops in the phenol water can be effectively removed, and the influence of filter operation on a subsequent phenol ammonia recovery working section can be avoided.

Description

Dust-containing phenol water separation process and separation method

Technical Field

The invention relates to the field of phenol water treatment of pressurized fixed bed gasification, in particular to a dust-containing phenol water separation process and a separation method.

Background

In the BGL gasification technology, the dust-containing phenol water from the gasification section is usually separated from coal dust, dissolved gas, tar and oil in the phenol water by adopting the processes of cooling, decompression expansion and gravity settling, and the separation process comprises four-stage separation of a primary tar separator, an oil separator, a settling tank and a filter (a buffer tank does not have the separation function).

The traditional dust-containing phenol water separation process adopts a four-stage separation procedure, the oil content of the separated phenol water is still higher, the separation effect is poorer, and the adaptability is also poorer. And because the effect of separating dust from the dust-containing phenol water in the primary tar separator is poor, the dust which is not fully removed influences the separation of the oil separator on the oil, and even the bottom of the buffer tank is deposited with the dust-containing tar.

In fact, when the dust-containing phenol water is separated and treated, the dust-containing tar is separated quickly, so that a large amount of dust-containing tar is deposited, an outlet of the dust-containing tar is blocked, and part of the dust-containing tar is brought out to downstream equipment, so that the separation function of the downstream equipment is influenced.

In addition, because the filter is subjected to pressure drop increase and even blockage after long-term use, the filter needs to be subjected to back flushing operation, impurities in the filter medium are removed by using nitrogen and heated back flushing water at 80 ℃, but the back flushing operation causes periodic increase of the temperature of phenol water in a boundary region, and the operation of a deacidification tower in a downstream phenol ammonia recovery section is influenced. Aiming at the working condition of gasifying the easily pulverized materials, the dust content in the phenol water containing dust is greatly increased, and the traditional process is not suitable.

Disclosure of Invention

Aiming at the problem that the effect of separating dust and tar from dust-containing phenol water in the prior art is not ideal, the invention aims to provide a dust-containing phenol water separation process and a separation method.

In order to achieve the purpose, the technical scheme of the invention is as follows:

on one hand, the invention provides a dust-containing phenol-water separation process, which comprises a primary tar separator, a buffer tank, a multiplication separator A, a filter and a settling tank which are sequentially connected through a pipeline according to the flow direction of phenol-water;

wherein the multiplying separator A comprises:

the separator comprises a separator tank body, wherein one side of the separator tank body is provided with a feeding gradually-expanding opening, and the top and the bottom of the other side of the separator tank body are respectively provided with a light phase outlet and a heavy phase outlet;

the overflow separation plate A, the overflow separation plate B and the overflow separation plate C are sequentially arranged in the separator tank body according to the medium flow direction so that the separator tank body is divided into a suspension separation area, a filling area, a special plate group area and an outlet area;

the cyclone is arranged in the suspension separation zone, and the feed divergent opening is opposite to the tangential direction of the cyclone so as to lead the inflowing phenol water to be centrifugally separated;

the tar port is arranged at the lowest part of the conical bottom of the suspension separation zone and is positioned between the cyclone and the overflow partition plate A;

a filler packed within the filler zone to increase the size of oil droplets in the phenol water; and

a special plate set disposed within the special plate set region to increase a size of oil droplets in the phenol water;

wherein the overflow separation plate A closes the lower part of the cross section of the separator tank body to allow the phenol water to overflow through the upper part of the overflow separation plate A, the overflow separation plate B closes the lower part of the cross section of the separator tank body and the bottom of the overflow separation plate B is provided with a flow hole to allow the light phase to overflow through the upper part of the overflow separation plate B and the heavy phase to pass through the flow hole, and the overflow separation plate C closes the middle part of the cross section of the separator tank body to allow the light phase and the heavy phase to overflow through the upper part and the lower part of the overflow separation plate C respectively.

Preferably, there are at least two buffer tanks, the at least two buffer tanks are connected in series or in parallel through a pipe valve assembly, the pipe valve assembly includes a first state and a second state which can be switched with each other, wherein the at least two buffer tanks are connected in series when the pipe valve assembly is in the first state, and the at least two buffer tanks are connected in parallel when the pipe valve assembly is in the second state.

Further, the diapire of buffer tank is the concave surface in order to collect the dirty tar that subsides, just install in the buffer tank and be used for striking off the scraper blade that the dirty tar that adheres on the diapire in the buffer tank, the scraper that is used for scraping the floating oil on the liquid level is still installed to upper portion in the buffer tank, the outer wall mounting of buffer tank has steam coil.

Further, a medicine feeding tank and a multiplication separator B which are sequentially connected between the multiplication separator A and the filter according to the flowing direction of the phenol water are also included; wherein the medicine adding tank is used for separating the combined oil in the phenol water by adding a medicine, and the multiplying separator B is used for separating the oil phase separated from the combined oil.

Preferably, the dosing tank comprises a dosing tank body, and a stirrer, a dosing device and a pH value adjusting device which are arranged on the dosing tank body.

Further, still be provided with the returning charge device between multiplication separator B and the filter, the returning charge device is used for returning the phenol water to when the bound oil content in the phenol water is higher than predetermined threshold multiplication separator A and/or the preliminary tar separator.

In another aspect, the invention also provides a dust-containing phenol water separation method, which comprises the following steps,

step S1, introducing the dust-containing phenol water into a primary tar separator to preliminarily remove dust-containing tar and tar in the phenol water;

step S2, introducing the phenol water treated by the primary tar separator into a buffer tank for buffering and temporary storage, and further removing dust-containing tar and tar in the phenol water;

step S3, introducing the phenol water treated by the buffer tank into a multiplication separator A, increasing the size of oil droplets in the phenol water by the multiplication separator A and separating the oil droplets from the phenol water;

step S4, introducing the phenol water treated by the multiplication separator A into a filter, and further removing suspended particles and tar in the phenol water; and

and step S5, introducing the phenol water treated by the filter into a settling tank for standing and storage.

Preferably, the dust-containing tar discharged by the primary tar separator and the buffer tank is sent to a centrifuge for centrifugal treatment to obtain dust-containing tar, tar and water, wherein the dust-containing tar and the materials are mixed and returned to the furnace or are mixed and then pumped back to the furnace, the tar is introduced into a clean tar oil groove for recovery, and the water is sent to a tar sewage groove; and introducing the tar overflowed from the buffer tank into a clean tar tank for recycling.

Further, before the phenol water treated by the multiplication separator A is passed into a filter, the method also comprises the following steps,

step 31, adding water to PAM and PAC according to the mass ratio of 1:1.5 to dissolve the PAM and the PAC into liquid, adding 10-30 times of clear water to dilute the liquid, and adjusting the pH value to 8-9.5;

step 32, when the turbidity of the phenol water is 300mg/L, adding 1-10kg of medicament into a medicament adding tank according to the proportion of adding the medicament per kiloton, and stirring to separate the combined oil in the phenol water introduced into the medicament adding tank into an oil phase and a water phase;

and step 33, introducing the phenol water after the medicament treatment into a multiplication separator B, and increasing the size of oil droplets in the phenol water through the multiplication separator B and separating the oil droplets from the phenol water.

Further, the phenol water after being treated by the multiplication separator B and before being introduced into the filter also comprises the following steps,

step 34, detecting the content of bound oil in the phenol water treated by the multiplier separator B;

step 35, judging whether the content of the bound oil in the phenol water is higher than a preset threshold value, if so, carrying out the next step, and if not, introducing into a filter;

and step 36, returning the phenol water treated by the multiplication separator B to the multiplication separator A for treatment again, adjusting the proportion of the medicament to be added into the medicament adding tank, or returning the phenol water treated by the multiplication separator B to the initial tar separator for separation again.

Preferably, when the easily pulverized material is gasified and the dust entrainment in the phenol water from the gasification section is greatly increased, the phenol water flowing out of the primary tar separator is connected to the multiplication separator A to enhance the separation effect of the dust-containing tar; then sequentially passes through a buffer tank, a filter and a settling tank.

Adopt above-mentioned technical scheme, its beneficial effect lies in:

1. firstly, the oil separator is removed, so that the device and the method avoid the influence of dust-containing tar on the oil separator when the device and the method separate the dust-containing phenol water, and simultaneously, the oil phase in the dust-containing phenol water can still be effectively separated due to the arrangement of the multiplication separator A;

2. due to the arrangement of the tar port on the multiplier separator A, on one hand, the oil phase in the phenol water can be amplified, so that the oil phase can be separated more easily, on the other hand, the dust-containing tar which is not separated and treated in time can be discharged from the tar port in time in the rapid treatment process, and the influence of the dust-containing tar on subsequent equipment is avoided;

3. the filter is placed in front of the settling tank, so that when the filter performs backwashing operation, backwashing water cannot obviously influence the temperature of the settling tank with a large volume due to the arrangement of the settling tank, and the operation of a deacidification tower of a downstream phenol-ammonia recovery section is ensured;

4. due to the arrangement of the primary tar separator, the buffer tank, the multiplication separator A, the filter and the settling tank which are sequentially connected, the separation stage number of the phenol water containing dust is increased to 5, the dust and the oil are fully separated, the quality of the finally obtained phenol water is ensured, a good foundation is laid for the treatment of a downstream working section, the effect of separating the dust and the oil is improved by increasing the separation stage number, and the separation is shortened and improved by multiplying the separator;

5. the arrangement of the chemical adding tank and the multiplying separator B ensures that the combined oil which is difficult to remove by physical means is separated into oil phase and water phase by adding the chemical, and then the decomposed oil phase is removed by the multiplying separator B;

6. the arrangement of the material returning device ensures that the oil phase content in the phenol water exceeds the standard, the oil phase can be pumped to an upstream multiplication separator A or a primary tar filter for retreatment and retreatment after the adjustment of the dosage;

7. the separation process flow and the separation technology can be flexibly and pertinently adjusted through the serial and parallel connection of the two buffer tanks, the two multiplication separators and the plurality of filters, and the phenol water quantity fluctuation and the raw material fluctuation can be better coped with.

Drawings

FIG. 1 is a schematic structural view of an embodiment of a first aspect of the process for separating dust-laden phenol water according to the present invention;

FIG. 2 is a schematic diagram of the arrangement of multiplier separator A in the first aspect of the process for separating dust-laden phenol water according to the present invention;

FIG. 2.1 is a schematic structural view of an overflow partition plate A in the present invention;

FIG. 2.2 is a schematic structural view of an overflow partition plate B in the present invention;

FIG. 2.3 is a schematic structural view of an overflow partition plate C in the present invention;

FIG. 3 is a schematic structural view of a tubular valve assembly in an embodiment of a second aspect of the process for separating water from dust-laden phenol of the present invention;

FIG. 4 is a schematic structural view of an embodiment of a third aspect of the process for separating water containing dust phenol according to the present invention;

FIG. 5 is another schematic structural view of an embodiment of the third aspect of the process for separating water containing dust phenol according to the present invention;

FIG. 6 is a flow diagram of a fourth embodiment of a process for separating water from dust-laden phenol of the present invention;

FIG. 7 is a flow chart showing the operation of the method for separating dust-laden phenol water according to the present invention when the bound oil content in the phenol water does not reach the standard.

In the figure, 1-initial tar separator, 2-buffer tank, 21-stirring shaft, 22-scraper, 23-scraper, 3-multiplication separator A, 31-separator tank body, 311-suspension separation zone, 312-packing zone, 313-special plate group zone, 314-outlet zone, 32-feeding gradually-expanding mouth, 33-light phase outlet, 34-heavy phase outlet, 351-overflow partition plate A, 352-overflow partition plate B, 353-overflow partition plate C, 36-cyclone, 37-tar mouth, 38-packing, 39-special plate group, 4-filter, 5-settling tank, 6-medicine feeding tank, 7-multiplication separator B, 8-pipe valve component, 81-tee joint A, 82-tee joint B, 83-stop valve A, 84-stop valve B, 85-stop valve C, 86-first bypass pipeline, 87-second bypass pipeline, 9-view mirror, 10-return pump and 11-sampling port.

Detailed Description

The following further describes embodiments of the present invention with reference to the drawings. It should be noted that the description of the embodiments is provided to help understanding of the present invention, but the present invention is not limited thereto. In addition, the technical features involved in the embodiments of the present invention described below may be combined with each other as long as they do not conflict with each other.

It should be noted that in the description of the present invention, the terms "upper", "lower", "left", "right", "front", "rear", and the like indicate orientations or positional relationships based on structures shown in the drawings, and are only used for convenience in describing the present invention, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.

In the technical scheme, the terms "first" and "second" are only used for referring to the same or similar structures or corresponding structures with similar functions, and are not used for ranking the importance of the structures, or comparing the sizes or other meanings.

In addition, unless expressly stated or limited otherwise, the terms "mounted" and "connected" are to be construed broadly, e.g., the connection may be a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; the two structures can be directly connected or indirectly connected through an intermediate medium, and the two structures can be communicated with each other. To those skilled in the art, the specific meanings of the above terms in the present invention can be understood in light of the present general concepts, in connection with the specific context of the scheme.

Examples of the first aspect of the invention

A dust-containing phenol-water separation process is shown in figure 1 and comprises a primary tar separator 1, a buffer tank 2, a multiplication separator A3, a filter 4 and a settling tank 5 which are sequentially connected through pipelines according to the flow direction of phenol-water. The multiplied separator a3 is used for separating the tiny oil from the phenol water.

Since the phenol water discharged from the gasification reaction section usually contains coal dust, oil and tar, a series of separation steps are required to obtain phenol water which can be used continuously. And typically also needs to be cooled down by a cooler and expanded down by an expander before entering the separation unit provided in this embodiment.

The dust-containing phenol water after cooling and depressurization enters the primary tar separator 1, and in the embodiment, the primary tar separator 1 is a central driving type primary tar separator, and the structure and the principle of the primary tar separator are not described in detail in the embodiment. Through the separation effect of initial tar separator 1, can be with the dirty tar and the tar initial separation of the dirty phenol aquatic, wherein, dirty tar enters into centrifuge and carries out centrifugal treatment to finally obtain phenol water, tar and dirty tar, tar then lets in clean tar groove and retrieves, and phenol water flows to downstream equipment along with the pipeline.

The phenol water treated by the primary tar separator 1 overflows to a buffer tank 2. In this embodiment, the bottom of the buffer tank 2 has a concave area for storing settled dust-containing tar, and the bottom of the buffer tank 2 is a concave area, for example, conical, for storing settled dust-containing tar, so that after phenol water enters the buffer tank 2, heavy dust-containing tar can be settled at the bottom by standing and storing. In order to prevent the dust-containing tar from adhering to the bottom of the buffer tank 2, in the present embodiment, a scraper 22 for scraping off the dust-containing tar adhering to the bottom wall of the buffer tank 2 is installed in the buffer tank 2, for example, a stirring shaft 21 may be installed in the buffer tank 2, the stirring shaft 21 may be rotatably installed at the center of the buffer tank 2 by a bracket fixed on the buffer tank 2, and the scraper 22 is fixedly installed on the stirring shaft 21 so that the scraper 22 can completely or partially scrape off the dust-containing tar adhering to the bottom wall of the buffer tank 2 along with the rotation of the stirring shaft 21. Meanwhile, the stirring shaft 21 can be provided with stirring blades so as to ensure that the dust-containing tar in the buffer tank 2 is uniformly settled. In addition, the bottom of the stirring shaft 21 is configured to have a gap of 8-10cm in the bottom of the example buffer tank 2 to prevent the bottom of the stirring shaft 21 from being adhered to fail to operate.

In order to prevent the dust-containing tar from being solidified on the bottom wall of the surge tank 2, in this embodiment, a steam coil is attached to the outer bottom wall of the surge tank 2, and the bottom wall of the surge tank 2 is heated by the steam coil, so that the dust-containing tar adhered thereto is always kept in a fluid state.

In this embodiment, a scraper 23 for scraping off the floating oil on the liquid surface is installed at the upper portion in the buffer tank 2, and preferably, the scraper 23 is fixedly installed on the stirring shaft 21. Correspondingly, an overflow port is arranged on the side wall of the buffer tank 2, so that the floating oil scraped together by the scraper 23 flows out of the buffer tank 2 through the overflow port, and the oil content in the phenol water is reduced.

After the two separation steps, the impurities in the phenol water are mainly oil, and the size of the liquid drops of the oil liquid is small and is difficult to remove under normal conditions. The present embodiment provides a multiplier separator a3, which can gather and enlarge small-sized oil droplets in the phenol water to float out of the water.

Specifically, as shown in fig. 2, the multiple separator a3 includes a separator tank 31, the separator tank 31 is cylindrical or elongated as a whole, a feed gradually expanding mouth 32 for feeding liquid is provided on the left side in the length direction, and a light phase outlet 33 and a heavy phase outlet 34 are provided on the top and bottom on the right side in the length direction, respectively.

An overflow partition plate a351, an overflow partition plate B352 and an overflow partition plate C353, which are sequentially arranged in the medium flow direction, are provided in the separator tank 31. Due to the arrangement of the overflow partition plate a351, the overflow partition plate B352, and the overflow partition plate C353, the separator tank 31 is divided into the suspension separation zone 311, the packing zone 312, the special plate group zone 313, and the outlet zone 314.

The feeding flaring 32 is arranged at the left side of the suspension separation zone 311, a cyclone 36 is also arranged in the suspension separation zone 311, and the feeding flaring 32 is opposite to the tangential direction of the cyclone 36 so as to enable the phenol water flowing into the separator tank 31 to be centrifugally separated. Meanwhile, the bottom of the suspension separation zone 311 is also provided with a recessed area for collecting the dust-containing tar discharged by the cyclone, the recessed area is provided with a tar port 37, and the tar port 37 is located between the cyclone 36 and the overflow partition plate a351, so that the dust-containing tar centrifugally separated by the cyclone 36 can flow out from the tar port 37, and the dust-containing tar is prevented from entering the next area. In this embodiment, the inlet to outlet area ratio of the feed flare 32 is set to 1:2.5, and the diameter of the swirler 36 is set to be at least 1.5 times the diameter of the outlet of the feed flare 32.

Packing 38 is filled in packing region 312, packing 38 is filled in packing region 312 to increase the size of oil droplets in the phenol water, and packing 38 may be loose fibers, structured packing, or random packing.

A special plate group 39 is disposed within the special plate group zone 313 and the special plate group 39 is disposed within the special plate group zone 313 to increase the size of oil droplets in the phenol water. The special plate group 39 comprises a plurality of folded plates which are arranged in a stacked mode with certain gaps between the folded plates, and a certain inclination angle is formed between the folded plates and the flowing direction of the phenol water, so that the folded plates can partially block the phenol water but allow the phenol water to pass through, and oil drops among tiny oil drops collide with each other and are gathered into oil drops with larger sizes through the blocking effect; in the flowing direction of the phenol water, a plurality of groups of special plate groups 39 can be arranged to further increase the gathering effect on oil drops, so that suspended oil drops in the phenol water are gathered into large liquid drops as much as possible to be separated from the water, the gap between the folded plate and the folded plate of the upstream special plate group 39 is larger, the gap between the folded plate and the downstream special plate group 39 is smaller, so that the separation effect is gradually improved, and the gap between the folded plate of the most upstream special plate group 39 is at least 2 times of the gap between the folded plate of the most downstream special plate group 39. Since the dust-containing tar has a density > medium oil density > water density, the water phase flows out from the light phase outlet 33, and the separated oil phase flows out from the heavy phase outlet 34.

In this embodiment, the overflow partition plate a351, the overflow partition plate B352, and the overflow partition plate C353 do not close the separator tank 31. Specifically, the overflow partition plate a351 is semicircular or largely semicircular and is closely fixed at the lower part of the cross section of the separator tank 31 so that the phenol water to be separated and treated overflows from the upper part of the overflow partition plate a351, and the overflow partition plate a351 mainly plays a certain role in blocking the phenol water, as shown in fig. 2.1; the overflow separation plate B352 is semicircular and is fixed closed at the lower part of the cross section of the separator tank 31, and the bottom of the overflow separation plate B352 is provided with a flow hole for the light phase (oil phase) to overflow from the upper part of the overflow separation plate B352 and possible heavy phase (e.g. tar dust entrained) to pass through, as shown in fig. 2.2; the overflow partition plate C353 is a circular plate having cutouts at both the upper and lower ends thereof and is closed in the middle of the cross section of the separator tank 31, so that the light phase and the heavy phase overflow through the upper and lower portions of the overflow partition plate C353, respectively, and then the light phase (aqueous phase) flows out from the light phase outlet 33 and the heavy phase (oil phase) flows out from the heavy phase outlet 34, as shown in fig. 2.3.

The phenol water treated by the multiplier separator A3 is pumped into a filter 4 for filtration to further remove suspended particles, tar and oil possibly carried in the phenol water. In the present embodiment, the filter 4 is divided into 3 layers including a coke layer (filter medium), a sand layer, and a support stone layer. During filtering, the phenol water flows out after sequentially passing through the coke layer, the sand layer and the support stone layer.

The phenol water treated by the filter 4 is then stored in the settling tank 5 in a centralized manner, and at the moment, standing separation can be carried out by depending on the larger capacity of the settling tank 5, so that a very small amount of particles and oil contained in the phenol water are settled and floated out of the phenol water, and final separation is carried out. The volume of the settling tank 5 is usually more than 10000 cubic meters, and the settling tank can play a role in buffering and settling to separate tar and oil which may exist in the settling tank 5 by depending on the storage capacity of the settling tank 5 (the phenol water intake water can be stored for three days under the condition that the phenol water separation section can only enter and leave).

Under normal working conditions, the phenol water containing dust with 2-8g/L of dust content and 8-15g/L of oil content is treated by the separation device of the embodiment, and is discharged from the settling tank 5 after detection, wherein the dust content cannot be detected and is lower than the detection precision of the detection device, the oil content is 0.25g/L at most, and the oil exists basically in the form of bound oil.

Examples of the second aspect of the invention

It differs from the embodiment of the first aspect in that: in this embodiment, at least two buffer tanks 2 are provided, and at least two buffer tanks 2 are connected in series or in parallel. It can be understood that when the phenol water overflowing from one buffer tank 2 contains more particles and oil and affects the subsequent treatment, the settling effect of the phenol water in the buffer tank 2 needs to be correspondingly improved.

And the at least two buffer tanks 2 are connected in series or in parallel, so that the settling effect of the phenol water in the buffer tanks 2 can be improved. Both are to make the phenol water stay in the buffer tank 2 for a longer time, thereby improving the settling effect of the phenol water. The purpose of improving the settling effect of the phenol water can be realized by the technical personnel in the field no matter in a series connection or parallel connection mode. Particularly, the parallel connection can increase the separation path and the residence time due to the working condition that the amount of the phenol water containing dust is greatly increased, and the series connection can improve the separation effect.

It will also be appreciated that the separation apparatus of this embodiment further comprises a tubular valve assembly comprising a first state and a second state which are switchable with respect to each other, wherein in the first state the tubular valve assembly at least two buffer tanks 2 are connected in series; when the pipe valve assembly is in the second state, at least two buffer tanks 2 are connected in parallel.

The present embodiment exemplifies the case where the number of buffer tanks 2 is two. As shown in fig. 3, a spool valve assembly 8 may be provided that includes two tees (tee a81 and tee B82) and three shut-off valves (shut-off valve a83, shut-off valve B84 and shut-off valve C85). Wherein, two buffer tanks 2 are firstly connected in series between two tees through pipelines, and two buffer tanks 2 are connected through a balance pipe, and the balance pipe is provided with a sight glass 9 and a sampling port 11.

The water inlet end of the upstream tee joint A81 is only provided with one phenol water overflow port connected with the primary tar separator 1, the water outlet end of the downstream tee joint B82 is only provided with one feeding gradually expanding port connected with the multiplication separator A3, and a stop valve A83 is arranged on a balance pipe connected between the two buffer tanks 2. The buffer tank 2 at the upstream is also connected with one water inlet end of the tee joint B82 at the downstream through a first bypass pipeline 86, and a stop valve B84 is installed on the first bypass pipeline 86; one outlet end of the upstream tee joint a81 is connected to the downstream buffer tank 2 via a second bypass line 87, and a shut-off valve C85 is installed on the second bypass line 87. When the two buffer tanks 2 are required to be connected in series during use, the stop valve B84 and the stop valve C85 are closed, and the stop valve A83 is opened. When two buffer tanks 2 are required to be connected in parallel, the stop valve A83 is closed, and the stop valve B84 and the stop valve C85 are opened. When only one buffer tank 2 is required to be used independently, the stop valve A83 and the stop valve C85 are closed, and the stop valve B84 is opened to use the buffer tank 2 at the upstream; alternatively, the stop valve a83 and the stop valve B84 are closed and the stop valve C85 is opened, i.e., the downstream buffer tank 2 can be used. For convenience of control, the shut-off valve is preferably a valve that can be electrically controlled, such as an electromagnetic valve or an electrically operated valve.

It will be appreciated that it is sometimes necessary to return the material in the downstream buffer vessel 2 to the upstream buffer vessel 2, and therefore in one embodiment a pipe is provided between the two buffer vessels 2, the pipe being provided with a pump for pumping the material in the downstream buffer vessel 2 to the upstream buffer vessel 2.

Similarly, the filters 4 are also similar, in another embodiment, at least two filters 4 are provided, at least two filters 4 are connected in series or in parallel, when connected in series, the filtering effect can be improved, when connected in parallel, the filtering amount can be improved, and one of the two schemes can be selected by a person skilled in the art to use according to needs. In another embodiment, a filter connection pipe valve assembly may be further provided, the filter connection pipe valve assembly including a first state and a second state switchable with each other, wherein the filter connection pipe valve assembly in the first state connects the at least two filters in series, and the filter connection pipe valve assembly in the second state connects the at least two filters in parallel, and in this embodiment, the filter connection pipe valve assembly may have the same structure as the pipe valve assembly in the above-described embodiment.

Examples of the third aspect of the invention

The present embodiment is an improvement of any of the above embodiments. It can be seen from the first embodiment that the oil in the phenol water is in addition to oil droplets, and has bound oil, which cannot be removed by simple physical separation methods, thereby affecting the treatment of the subsequent process.

Therefore, the separation apparatus in this embodiment further includes a chemical feed tank 6 and a multiplier separator B7 connected in series between the multiplier separator a3 and the filter 4 in the flow direction of phenol water, as shown in fig. 4. The dosing tank 6 is used for separating the combined oil in the phenol water by adding a medicament, and the dosing tank 6 comprises a dosing tank body, and a stirrer, a dosing device and a pH value adjusting device which are arranged on the dosing tank body, wherein the rotating speed of the stirrer is generally 20-50 rpm. And multiplier separator B7, which is used to separate the oil phase from the bound oil, has the same structure as multiplier separator A3 described above.

The method for removing the bound oil in the phenolic water by the medicament comprises the following steps: a) adjusting the pH value of the medicament to 8-9.5 by using soda ash; b) adding water into the PAM and PAC (the mass ratio is 1:1.5) medicaments to dissolve the PAM and PAC medicaments into liquid, adding 10-30 times of clear water to dilute the liquid into the liquid with the required concentration, and adding and stirring the liquid and the clear water by using a dosing device of a dosing tank for use; c) the dosage can be determined according to different turbidity degrees of raw water, and the dosage is 1-10kg per kiloton when the turbidity degree of the raw water is generally 100-300 mg/L; d) and the tiny oil drops are gathered and amplified by a second multiplication separator, and then can be separated from the phenol water.

In this example, the chemical is one or more of PAM, PAC, and soda ash, and when mixed into the phenol water, the chemical can effectively break the bonds in the bound oil, and decompose the chemical into water and oil. After the treatment of the medicine adding tank 6, the combined oil in the phenol water is converted into oil and water phases to exist independently, so that the tiny oil drops in the phenol water can be separated from the phenol water after being gathered and amplified by the multiplying separator B7.

When in use, sodium carbonate is properly added according to the requirement to adjust the pH value to 8-9.5, and the adding ratio of PAM to PAC is generally 1:1 to 1: 2; the total dosage is generally 0.1-0.3 ppm.

The method for removing the bound oil in the phenolic water by the medicament comprises the following steps:

1. mixing the medicament solid product according to the proportion of 1: 3 adding water to dissolve the mixture into liquid, and then adding 10-30 times of clear water to dilute the mixture into the required concentration for use;

2. the dosage can be determined according to different turbidity degrees of raw water, and the dosage is 10-20kg per kiloton when the turbidity degree of the raw water is generally 100-300 mg/L.

It can be understood that the content of the bound oil in the phenol water is not constant, and the content of the bound oil in the phenol water is usually changed, so that the adding ratio of the medicament is particularly important, and the removal effect of the bound oil in the phenol water cannot reach the standard due to wrong adding ratio of the medicament, so that the adding ratio of the medicament needs to be adjusted. In another embodiment, a material returning device is further arranged between the multiplying separator B7 and the filter 4, and the material returning device is used for returning the phenol water to the multiplying separator A3 and/or the primary tar separator 1 when the bound oil content in the phenol water is higher than a preset threshold value. The material returning device specifically comprises a material returning pump 10 and related pipelines and valves.

Usually, a sensor for detecting the content of the bound oil in the phenol water is installed on the water outlet side of the multiplied separator B7, i.e., the light phase outlet side thereof, and the data detected by the sensor is processed to be a value of the content of the bound oil, and when the value is higher than a preset threshold value, it indicates that the content of the bound oil is too high, i.e., the treatment of the bound oil in the phenol water by the pharmaceutical agent is not thorough. At this time, the material returning pump 10 works, the water inlet end of the material returning pump is connected with the light phase outlet of the multiplication separator B7, the water outlet end of the material returning pump is connected with the inlet of the multiplication separator A3, the phenol water with unqualified combined oil separation can be returned and treated again, the adding proportion of the medicament only needs to be adjusted during the treatment again until the content of the combined oil in the phenol water detected by the sensor reaches the standard, namely, the content of the combined oil in the phenol water is lower than the preset threshold value, and at this time, the downstream valve is opened to allow the phenol water.

It can be understood by those skilled in the art that when the content of the bound oil in the phenol water detected by the sensor is far higher than the preset threshold and exceeds the agent processing capacity, the return device, i.e. the water outlet of the return pump 10, is directly connected to the primary tar separator 1, so that the phenol water with the content of the bound oil not reaching the standard is separated again. Therefore, the water outlet of the material returning pump 10 can be respectively connected with the multiplication separator A3 and the primary tar separator 1 in two schemes, so as to respectively solve the problems of the two situations; and the water outlet of the material returning pump 10 can be also reversed through a three-way valve, so that the material returning pump has the capability of supplying water to two directions, and the problems of the two conditions can be solved in one scheme.

Since the phenol water is supplied to the filter 4 and the filtration treatment is performed by a pump, the pump for supplying the phenol water to the filter 4 and the return pump 10 for returning the phenol water can be integrated into one, and the water outlet of the pump is led to the filter 4, the multiplier-type separator a3 and the preliminary tar separator 1 by using two three-way valves.

For the same reason, the material returning pump 10 can also be used to return the material in the downstream buffer tank 2 to the upstream buffer tank 2, i.e. a three-way valve is also arranged at the inlet end of the material returning pump 10, so that the material returning pump has two incoming water directions, as shown in fig. 5.

Under normal working conditions, the phenol water containing dust, the dust content of which is 2-8g/L and the oil content of which is 8-15g/L, is treated by the separation device of the embodiment, and is discharged from the settling tank 5 through detection, wherein the dust content cannot be detected, the dust content is lower than the detection precision of the detection device, the oil content is 0.05g/L, and the dust content cannot be detected by the detection device under normal conditions.

Examples of the fourth aspect of the invention

There is provided a dust-containing phenol water separation method, which is applied to the separation device provided in the above embodiment, as shown in fig. 6, and comprises the following steps:

step S1, introducing the dust-containing phenol water into a primary tar separator to preliminarily remove dust-containing tar in the phenol water;

the dust-containing phenol water is obtained from a waste heat boiler of a gasification section, and can be introduced into a primary tar separator after cooling, temperature reduction, expansion, pressure reduction and flash evaporation, the primary tar separator primarily removes dust-containing tar and sends the dust-containing tar into a centrifugal machine for centrifugal treatment to obtain dust-containing tar, tar and water, wherein the dust-containing tar and materials are mixed and returned to the furnace or are sent back to the furnace through a pump after blending, the tar is introduced into a clean tar tank for recovery, and the water is sent to a tar sewage tank. The phenol water overflowing from the primary tar separator flows to the next step for treatment.

Step S2, introducing the phenol water treated by the primary tar separator into a buffer tank for buffering and temporary storage, and further removing dust-containing tar and medium oil in the phenol water;

phenol water is through first tar separator processing back, and the overflow goes into the buffer tank in, because the buffer tank has certain volume, phenol water can stop storage period wherein just can overflow once more and go out, consequently utilizes this period of time, can make the dirty dust tar in phenol water can take place to subside for the phenol water that overflows from the buffer tank obtains the sedimentation separation, and the dirty dust tar of subside at buffer tank toper bottom is then scraped by the scraper blade, and drops into centrifuge and carries out centrifugal treatment. And the phenol water overflowing from the buffer tank enters the next step of treatment, and the tar overflowing from the buffer tank is introduced into a clean tar tank for recycling.

the phenol water overflowing from the buffer tank has a greatly reduced content of particles and oil, and the oil exists in the form of tiny oil droplets, which are generally difficult to separate from the phenol water. At the moment, the multiplication separator A is dependent on the characteristic that the multiplication separator A can gather and amplify the micro oil drops, so that the micro oil drops in the phenol water are gathered into large liquid drops through the blocking and gathering effects of the internal loose fiber bed and the special plate group, and the oil phase with lower density flows out from the light phase outlet and the phenol water with higher density flows out from the heavy phase outlet by utilizing the principle of different densities. The phenol water flowing out of the light phase outlet of the multiplication separator A is sent to the next step for treatment by a pump.

Step S4, introducing the phenol water treated by the multiplication separator A into a filter, and further removing suspended particles and tar in the phenol water;

after the treatment of the multiplied separator A, the phenol water is sent to a filter, such as a dual-medium filter, under the pumping action of a pump, and suspended particles and oil drops in the phenol water are continuously adsorbed and filtered by the filter.

The settling tank is used for storing the filtered phenol water, and the large volume of the settling tank is used for enabling the phenol water to stay for a long time, so that the phenol water can be finally settled while being stored, and particles and oil are further separated.

In the embodiment, the filter is arranged at the upstream of the settling tank, so that when the filter performs backwashing operation, the temperature fluctuation of phenol water output by the settling tank is greatly reduced by utilizing the temperature of a large amount of phenol water and backwashing water stored in the settling tank, and the influence of the backwashing water of the filter on the deacidification tower in the downstream phenol ammonia recovery working section is reduced.

In addition, the method of the embodiment also utilizes the buffer tank to carry out sedimentation treatment on the phenol water, and utilizes the conical bottom to store the settled dust-containing tar, so that the quality of the phenol water obtained at the downstream is better.

And the multiplied separator A is put into use, so that oil drops with small sizes in the phenol water can be gathered and amplified, and then are removed, and the separation effect on the phenol water is further improved.

However, considering that the dust entrainment amount in the phenol water increases when the easily pulverized material is gasified, so that only the primary tar separator cannot achieve a good dust separation effect, in one embodiment, the phenol water flowing out of the primary tar separator is connected to the multiplier separator a to enhance the separation effect of the dust-containing tar, and then passes through the buffer tank, the filter and the settling tank in sequence. That is, the order of operation of the buffer tank and the multiplying separator a is reversed. During specific implementation, add the bypass of multiplication separator A, its import one side is through the tube coupling primary tar separator, and its aqueous phase export one side is through the tube coupling buffer tank, respectively disposes the stop valve on the pipeline, when needing to open, open the stop valve can.

Under the maximum working condition, the phenol water containing dust, the dust content of which is 5-15g/L and the oil content of which is 20-50g/L, is treated by the separation device after the operation sequence is adjusted, and is detected to be discharged from the settling tank 5, wherein the dust content cannot be detected, the detection precision of the detection device is lower, the oil content is 0.7g/L at most, and most of the oil except a small amount of micromolecule free oil exists in the form of bound oil.

Examples of the fifth aspect of the invention

There is provided a method for separating dust-containing phenol water which is an improvement over the fourth embodiment. As shown in fig. 7, the following steps are added between step S3 and step S4, that is, before the phenol water is introduced into the filter, the following steps are also included:

in this step, add the medicine jar including adding the medicine jar body and installing agitator, charge device and pH valve adjusting device on adding the medicine jar body make it possess and add the medicine function simultaneously, can also stir.

And step S33, introducing the phenol water after being treated by the medicament into a multiplication separator B, and increasing the size of oil droplets in the phenol water by the multiplication separator B and separating the oil droplets from the phenol water.

Since the agent has separated the bound oil into oil and water phases, the oil phase, which has been separated from the bound oil, can be efficiently removed by adding a multiplying separator B downstream.

It is understood that, in order to grasp the adding ratio of the chemical agent, after the step S32 and before the phenol water is introduced into the filter, the following steps are further included:

step S34, detecting the content of the bound oil in the phenol water treated by the multiplication separator B;

and a sensor arranged on the outlet side of the light phase of the multiplying separator B detects the phenol water discharged from the outlet of the light phase of the multiplying separator B, and a detection signal of the sensor is processed to obtain a combined oil content value.

Step S35, judging whether the content of the bound oil in the phenol water is higher than a preset threshold value, if so, carrying out the next step, otherwise, introducing the phenol water into a filter;

and step S36, the phenol water treated by the multiplication separator B is returned to the multiplication separator A for treatment again, the ratio of the medicament to be added into the medicament adding tank is adjusted, or the phenol water treated by the multiplication separator B is returned to the initial tar separator for separation again.

The implementation of the method of the embodiment can not only effectively remove the bound oil in the phenol water, but also adjust the adding proportion of the medicament in time when the removal effect of the bound oil fluctuates, and rework and retreat the phenol water when the medicament can not remove the bound oil, thereby ensuring that the oil content in the phenol water entering the downstream step is reduced to the minimum.

The embodiments of the present invention have been described in detail with reference to the accompanying drawings, but the present invention is not limited to the described embodiments. It will be apparent to those skilled in the art that various changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, and the scope of protection is still within the scope of the invention.

Claims

1. A dust-containing phenol-water separation process is characterized in that: the device comprises a primary tar separator, a buffer tank, a multiplication separator A, a filter and a settling tank which are sequentially connected through a pipeline according to the flowing direction of phenol water;

wherein the multiplying separator A comprises:

2. The process of claim 1 for separating water containing dust phenol, characterized in that: the buffer tanks are at least two, the at least two buffer tanks are connected in series or in parallel through pipe valve assemblies, each pipe valve assembly comprises a first state and a second state which can be switched with each other, the at least two buffer tanks are connected in series when the pipe valve assemblies are in the first state, and the at least two buffer tanks are connected in parallel when the pipe valve assemblies are in the second state;

the diapire of buffer tank is the concave surface in order to collect the dirt-laden tar that subsides, just install in the buffer tank and be used for striking off the scraper blade that the dirt-laden tar of adhesion was gone up to the diapire in the buffer tank, the scraper that is used for scraping the floating oil on the liquid level is still installed to upper portion in the buffer tank, the outer bottom wall mounting of buffer tank has steam coil.

3. The process for separating dust-laden phenol water according to any one of claims 1 to 2, characterized in that: the device also comprises a dosing tank and a multiplying separator B which are sequentially connected between the multiplying separator A and the filter according to the flowing direction of the phenol water; wherein the medicine adding tank is used for separating the combined oil in the phenol water by adding a medicine, and the multiplying separator B is used for separating the oil phase separated from the combined oil.

4. The process of claim 3 for separating water containing dust phenol, characterized in that: the medicine feeding tank comprises a medicine feeding tank body, and a stirrer, a medicine feeding device and a pH value adjusting device which are arranged on the medicine feeding tank body.

5. The process of claim 3 for separating water containing dust phenol, characterized in that: the device comprises a multiplication separator A and/or a primary tar separator, wherein a filter is arranged in the device, a material returning device is further arranged between the multiplication separator B and the filter, and the material returning device is used for returning the phenol water to the multiplication separator A and/or the primary tar separator when the bound oil content in the phenol water is higher than a preset threshold value.

6. A dust-containing phenol water separation method is characterized in that: comprises the following steps of (a) carrying out,

7. The process of claim 6, wherein the separation of the dust-laden phenol water comprises: sending the dust-containing tar discharged by the primary tar separator and the buffer tank into a centrifuge for centrifugal treatment to obtain dust-containing tar, tar and water, wherein the dust-containing tar and the material are mixed and returned to the furnace or are mixed and then pumped into the furnace, the tar is introduced into a clean tar oil groove for recovery, and the water is sent to a tar sewage groove; and introducing the tar overflowed from the buffer tank into a clean tar tank for recycling.

8. The process of claim 6, wherein the separation of the dust-laden phenol water comprises: before the phenol water treated by the multiplication separator A is introduced into a filter, the method also comprises the following steps,

9. The process of claim 8, wherein the separation of the dust-laden phenol water comprises: the phenol water after being treated by the multiplication separator B and before being introduced into the filter further comprises the following steps,

10. The process of claim 6, wherein the separation of the dust-laden phenol water comprises: when easily pulverized materials are gasified and the dust entrainment amount in the phenol water from a gasification section is greatly increased, the phenol water flowing out of the primary tar separator is connected to a multiplication separator A to enhance the separation effect of the dust-containing tar; then sequentially passes through a buffer tank, a filter and a settling tank.