CN211734024U - Recycling system of quenching water in methanol-to-olefin process - Google Patents
Recycling system of quenching water in methanol-to-olefin process Download PDFInfo
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- CN211734024U CN211734024U CN202020139700.XU CN202020139700U CN211734024U CN 211734024 U CN211734024 U CN 211734024U CN 202020139700 U CN202020139700 U CN 202020139700U CN 211734024 U CN211734024 U CN 211734024U
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Abstract
The utility model relates to a recycling system of quench water in methanol-to-olefin technology, including one-level membrane filter, sedimentation tank and KMPR filter, one-level membrane filter is arranged in receiving methanol-to-olefin technology quench water to the separation is filtrating and concentrate, filtrating direct retrieval and utilization, the sedimentation tank is used for receiving the concentrate to carry out natural cooling and settlement with the concentrate and handle, the KMPR filter is used for receiving the concentrate that handles through the sedimentation tank to with the concentrate separation for producing water and mud, produce water direct retrieval and utilization, mud directly discharges into sludge treatment system. The utility model discloses the water recovery rate is high, but high temperature operation, and online backwash improves system operating stability by a wide margin.
Description
Technical Field
The utility model relates to a methanol-to-olefin process water treatment technology, in particular to a recycling system of quench water in a methanol-to-olefin process.
Background
Mto (methanol to olefins) is a short term for a process of preparing olefins from methanol, and refers to a process of preparing low-carbon olefins (ethylene and propylene) from methanol by catalytic reaction. The reaction generally adopts a fluidized bed reactor, the produced product gas contains various impurities, the product gas (ethylene and propylene) is cleaned and primarily cooled by a quench tower and a water scrubber, and because the product gas contains residual catalyst and byproducts such as mixed alkane, aromatic hydrocarbon, coke and the like, the cleaned water needs to be filtered and cooled to remove suspended matters in the water and then returns to the production system for recycling.
The quenching water mainly washes the reaction gas, so that the main components of the impurities are similar to the components in the reaction gas. Meanwhile, because the fluidized bed reactor is adopted, the catalyst is easy to wear, the particle size of the normal catalyst is 70um, the worn catalyst is recovered through three-stage cyclone in the operation process, and fine powder with the particle size of 0-10um of the catalyst is difficult to separate and recover through cyclone and enters the quenching water. The reaction gas is subjected to heat removal in a quenching tower, and catalyst fine powder and generated acid gas are washed away. The solid content of a water system is increased due to the large loss of the catalyst, and the normal operation of a pump, a quench tower and a heat exchanger is directly influenced after the catalyst is mixed with byproducts such as mixed alkane, aromatic hydrocarbon, coke and the like, so that equipment needs to be cleaned regularly, and the production stability is influenced.
In order to ensure the stability of the water system, patent US6166282 discloses an MTO fluidized bed reactor, in which a set of cyclones is installed at the top of the reactor to reduce the loss of catalyst. US0234281 discloses a set of multiple solid-liquid cyclones or hydrocyclones operating in combination for recovering the catalyst. Patents CN101352621A and CN102093153A disclose a counter current washing and micro cyclone separator coupling device for recovering catalyst. Patent CN205031975U discloses an apparatus for purifying quench water and wash water using a metal sintered filter element. The utility model has the defects of low filtration precision, incomplete separation of catalyst and organic by-products, low backwater quality, low water recovery rate and the like. Patent CN103951098A discloses an apparatus for treating quench water and wash water using a ceramic membrane in combination with a three-phase separator. The utility model discloses a separate oil, water, catalyst completely, nevertheless the rate of recovery of oil, water, catalyst is all not high, simultaneously because the characteristic of ceramic membrane, there are investment and running cost height in practical application, shortcomings such as poor stability.
At present, the most important problem of quenching water treatment is to solve the problem of water recycling, and no proper technical scheme for solving the water recycling exists in the prior art.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a recycling system of quench water in methanol-to-olefin process to solve the problem of the reuse of reclaimed water in the present quench water treatment.
The utility model discloses a metal membrane system can high temperature online processing quench water, concentrates the retrieval and utilization problem of solving quench water, realizes the water recovery rate more than 95% through the second grade system, realizes high flux treatment under the high temperature condition, reduces investment cost by a wide margin, simultaneously because the special construction and the material characteristic of metal membrane, through online high temperature backwash and stable face velocity of flow, can guarantee the stability of system.
The purpose of the utility model can be realized through the following technical scheme:
the utility model provides a recycling system of quench water in methanol-to-olefin technology, including one-level membrane filter, sedimentation tank and KMPR filter, one-level membrane filter is arranged in receiving methanol-to-olefin technology quench water to the separation is filtrating and concentrate, filtrating direct retrieval and utilization, the sedimentation tank is used for receiving the concentrate to carry out natural cooling and settlement with the concentrate and handle, the KMPR filter is used for receiving the concentrate that handles through the sedimentation tank to with the concentrate separation for producing water and mud, produce water direct retrieval and utilization, mud directly discharges into sludge treatment system.
The utility model discloses an in the embodiment, still be provided with one-level membrane filter charge pump before the one-level membrane filter, one-level membrane filter charge pump is connected with one-level membrane filter for in getting methanol to olefin technology quench water pump into one-level membrane filter.
The pipelines at the feed liquid membrane feeding side and the filtrate side are both connected with steam pipelines.
In an embodiment of the present invention, a first-stage membrane filter circulating pump is further connected between the first-stage membrane filter feed pump and the first-stage membrane filter.
In an embodiment of the utility model, be connected with the KMPR charge pump on the pipeline between sedimentation tank and the KMPR filter, the KMPR charge pump is used for the concentrated solution pump income KMPR filter of handling through the sedimentation tank.
The utility model discloses an in an embodiment, the mud pipeline is all drawn forth with the bottom of sedimentation tank to the KMPR filter, set up the sludge pump on the mud pipeline, the mud pipeline is used for connecting the sludge dewatering tower.
In one embodiment of the present invention, the primary membrane filter is a metal membrane filter.
In one embodiment of the present invention, the membrane module of the primary membrane filter is coated with TiO2The metal film of the layer, the filtration precision of the metal film is 20-100nm, and the diameter of the filtration channel is 11-19 mm.
In an embodiment of the utility model, the KMPR filter includes the membrane pond, sets up the membrane module that is used for carrying out the separation to the concentrate that handles through the sedimentation tank in the membrane pond to and the product water pipeline of drawing forth from the membrane pond, the membrane module in the membrane pond sets up a set of or multiunit.
In an embodiment of the present invention, the water production line is provided with a KMPR water production pump.
In one embodiment of the utility model, an aeration device is arranged at the bottom of the membrane pool.
Compared with the prior art, the utility model has the advantages of it is following and beneficial effect:
(1) the water recovery rate is high (> 95%), and the total discharge amount of pollutants and sewage is greatly reduced;
(2) the membrane module can run at high temperature and carry out online backwashing, and each membrane module is provided with an independent circulating pump, so that the flow velocity of the membrane surface is ensured, and the running stability of the system is greatly improved.
(3) The service life of the equipment is long, the flux is high, the system investment is low, and the economy is high;
(4) high filtering precision and high quality of reuse water.
Drawings
FIG. 1 is a schematic diagram showing the structure of a system for recycling quench water in a methanol-to-olefin process according to an embodiment;
FIG. 2 is a schematic cross-sectional view of a metal membrane filter;
fig. 3 is a schematic view of a metal membrane filter structure.
Detailed Description
Detailed description of the preferred embodiments
A recycling system of quenching water in a methanol-to-olefin process refers to fig. 1 and comprises a primary membrane filter 3, a sedimentation tank 4 and a KMPR filter 6, wherein the primary membrane filter 3 is used for receiving the quenching water in the methanol-to-olefin process and separating the quenching water into filtrate and concentrated solution, the filtrate can be directly recycled, the sedimentation tank 4 is used for receiving the concentrated solution and naturally cooling and settling the concentrated solution, the KMPR filter 6 is used for receiving the concentrated solution treated by the sedimentation tank 4 and separating the concentrated solution into produced water and sludge, the produced water can be directly recycled, and the sludge is directly discharged into a sludge treatment system.
In the embodiment, a primary membrane filter feeding pump 1 is further arranged in front of the primary membrane filter 3, and the primary membrane filter feeding pump 1 is connected with the primary membrane filter 3 and is used for pumping quenching water in the methanol-to-olefin process into the primary membrane filter 3; and a primary membrane filter circulating pump 2 is also connected between the primary membrane filter feeding pump 1 and the primary membrane filter 3.
In this embodiment, a KMPR feed pump 5 is connected in line between the sedimentation tank 4 and the KMPR filter 6, and the KMPR feed pump 5 is used for pumping the concentrate treated by the sedimentation tank 4 into the KMPR filter 6.
In the embodiment, sludge pipelines are led out from the KMPR filter 6 and the bottom of the sedimentation tank 4, a sludge pump 8 is arranged on the sludge pipelines, and the sludge pipelines are used for connecting with a sludge dewatering tower.
In this embodiment, the KMPR filter 6 is an immersed membrane filtration system, and includes a membrane tank, membrane modules disposed in the membrane tank for separating the concentrated solution processed by the sedimentation tank 4, and a water production line led out from the membrane tank, the water production line is provided with a KMPR water production pump 7, the membrane modules in the membrane tank are provided with one or more groups, and the bottom of the membrane tank is provided with an aeration device. The membrane component adopts hollow fiber type membrane filaments and adopts a curtain type or column type structure.
Referring to fig. 1, a method for recycling quenching water in a methanol-to-olefin process includes the following steps:
quenching water in the methanol-to-olefin process enters a first-stage membrane filter 3, the first-stage membrane filter 3 separates the quenching water into filtrate and concentrated solution, the filtrate can be directly reused in a quenching water tower,
the concentrated solution enters a KMPR filter 6 for separation, the KMPR filter 6 separates the concentrated solution into produced water and sludge, the produced water can be directly recycled in a quenching water tower, and the sludge is directly discharged into a sludge treatment system; under the process condition, the concentration of the first-stage membrane filter 3 is more than 10 times, the water reuse rate is more than 90%, 10% of concentrated solution enters the KMPR filter 6, and the water yield of the KMPR filter 6 is 5-7% of the total water inflow of the quenching water, so that under the process, the total water reuse rate of the system is more than 95%, the solid content in return water is less than 30mg/L, and the total sludge discharge amount is about 2-3%.
In this embodiment, the operating conditions of the primary membrane filter 3 are: the filtration temperature is preferably 80-130 ℃, more preferably 85-110 ℃, the filtration mode adopts cross-flow filtration, the cross-flow rate is preferably 0.2-6m/s, more preferably 0.5-1.5m/s, and the transmembrane pressure difference is preferably 0.1-1MPa, more preferably 0.2-0.4 MPa.
In this embodiment, the operating conditions of the KMPR filter 6 are: the filtration temperature is preferably 5 to 50 ℃, more preferably 30 to 45 ℃, and the aeration rate is preferably 10 to 100Nm3/h, more preferably 30 to 60Nm3/h。
In the embodiment, the operation process of the method for recycling the quenching water in the methanol-to-olefin process also comprises the backwashing of the first-stage membrane filter 3 and the KMPR filter 6,
the cleaning operation conditions for the primary membrane filter 3 are as follows: conventional chemical cleaning, or filtrate backwashing, or steam backwashing or steam flushing, or a combination of a plurality of cleaning modes, wherein the filtrate backwashing pressure is preferably 0.1-1MPa, more preferably 0.2-0.4MPa, the backwashing period is preferably 20-120min, more preferably 30-60min, and the backwashing time is preferably 5-60s, more preferably 10-30 s; the steam backwashing operation conditions are as follows: backwashing by using low-pressure steam, wherein the backwashing pressure is 1-6bar, the backwashing time is 1-10min, and the backwashing period is 20-120 min; the steam flushing conditions were: introducing 1-10bar steam into the concentrated solution side of the filter, and washing for 1-60min for 1-24 hr.
The backwashing operating conditions for the KMPR filter 6 were: backwashing with the filtrate, wherein the backwashing pressure is preferably 0.01-0.1MPa, more preferably 0.03-0.08MPa, the backwashing period is preferably 30-240min, more preferably 60-150min, and the backwashing time is preferably 5-60s, more preferably 20-40 s.
In this embodiment, under the process that the concentrated solution enters the KMPR filter 6 for separation, the concentrated solution first enters the sedimentation tank 4, the sedimentation tank 4 is used for receiving the concentrated solution, and naturally cooling and settling the concentrated solution, and the concentrated solution treated by the sedimentation tank 4 enters the KMPR filter 6 for treatment.
In this embodiment, the sedimentation tank 4 cools the concentrate naturally to a temperature of <50 ℃, the bottom sludge is discharged into a sludge dewatering tower for treatment by a sludge discharge pump 8, and the supernatant is sent to a KMPR filter 6.
In the embodiment, under the process that the concentrated solution enters the KMPR filter 6 for separation, the quenching water in the process of preparing olefin from methanol enters the first-stage membrane filter circulating pump 2 under the driving of the first-stage membrane filter feeding pump 1, and then is sent to the first-stage membrane filter 3, wherein the first-stage membrane filter circulating pump 2 is used for ensuring the membrane surface flow rate of the first-stage membrane filter 3; the supernatant in the sedimentation tank 4 is fed to a KMPR filter 6 by a KMPR feed pump 5.
In the above embodiment, the membrane module of the primary membrane filter 3 is coated with TiO on the surface2The metal film of the layer, the filtration precision of the metal film is 20-100nm, and the diameter of the filtration channel is 11-19 mm. The first-stage membrane filter 3 is a conventional membrane filter, and the membrane component is coated with TiO on the surface2The metal film of the layer, the filtration precision of the metal film is 20-100nm, and the diameter of the filtration channel is 11-19 mm.
In the above embodiment, the primary membrane filter 3 is structured as shown in fig. 2 and 3, the membrane tubes are arranged in the cavity like a tubular heat exchanger, and each metal tube is individually welded to the flower plates at both ends. The membrane component adopts a structure that the surface is coated with TiO2The metal film of the layer, the filtration precision of the metal film is 20-100nm, and the diameter of the filtration channel is 11-19 mm. In the primary membrane filter 3, the membrane tubes are arranged in the cavity in a similar tube type heat exchanger mode, and each metal tube is independently welded on the flower plates at two ends to form a sealing mode different from other membrane components. Wall thickness of membrane tube<2mm, the supporting layer of the membrane tube is made of metal, the metal comprises stainless steel, hastelloy and the like, and the surface coating is made of TiO2And (5) film layer. The membrane assembly with the structure has the advantages that the flow of the filtrate from the membrane surface to the filtrate end is shorter, the deep pollution is reduced, and the backwashing effect is better. The temperature resistance range is better, and the temperature impact resistance and the mechanical impact resistance are stronger. Steam cleaning can be achieved.
In the above embodiment, the water temperature of the quenching water in the methanol-to-olefin process is greater than 80 ℃, and the solid content is 150-700 mg/L. The quenching water in the methanol-to-olefin process mainly contains a catalyst and a small amount of organic by-products. Wherein the catalyst powder is mainly present in the form of solid particles. The catalyst powder can be separated by a first-stage membrane filter, and the filtrate can be directly recycled.
The present invention will be described in detail below with reference to the accompanying drawings and specific embodiments.
Example 1
Referring to the process scheme shown in FIG. 1, quenching water with a water temperature of 80 ℃ and a solid content of 700mg/L is used. Under the push of a feeding pump 1 of the primary membrane filter, the mixture enters a circulating pump 2 of the primary membrane filter and then is sent to the primary membrane filter 3, the aperture of a metal membrane in the primary membrane filter 3 is 100nm, and the mixture works under the conditions that transmembrane pressure difference is 0.1MPa, membrane surface flow rate is 6m/s and permeation side backpressure is 0.2 MPa; the filtrate is directly returned to the quenching water tower for reuse. Periodically backwashing the membrane with filtrate, wherein the backwashing pressure is 0.2MPa, the backwashing period is 60min, and the backwashing time is 60 s; the steam flushing pressure is 10bar, the flushing time is 1min, and the flushing period is 1 hour. The primary membrane filter 3 is concentrated by 10 times, the concentrated solution enters the sedimentation tank 4, the concentrated solution is naturally cooled to the temperature of 30 ℃, the sludge at the bottom is discharged into the sludge dewatering tower for treatment through the sludge discharge pump 8, the supernatant is sent into the KMPR filter 6 through the KMPR feeding pump 5, the air is introduced into the bottom of the KMPR filter 6 for aeration, the aeration rate is 10Nm3H is used as the reference value. And returning the clear liquid to the quenching water tower for recycling through a KMPR water producing pump 7 on the water producing side after passing through the KMPR filter 6, and backwashing the KMPR filter every 240min for 60s at the backwashing pressure of 0.01 MPa. The sludge is concentrated by 2 times, and the sludge at the bottom of the KMPR filter 6 is sent to a sludge dewatering tower for treatment through a sludge pump 8. The primary membrane filter and the KMPR filter were chemically cleaned every 12-15 hours of operation.
The quality of the filtrate, the recovery rate of each stage of water and the total recovery rate are as follows:
| ss content of filtrate | mg/L | 15 |
| Water recovery rate of first-stage membrane filter | ％ | 90 |
| KMPR water recovery | ％ | 50 |
| Total water recovery | ％ | 95 |
Example 2
Referring to the process scheme shown in FIG. 1, the quenching water is cooled to 130 ℃ and has a solid content of 150 mg/L. Under the push of a feeding pump 1 of the primary membrane filter, the mixture enters a circulating pump 2 of the primary membrane filter and then is sent to the primary membrane filter 3, the aperture of a metal membrane in the primary membrane filter 3 is 20nm, and the mixture works under the conditions that transmembrane pressure difference is 0.2MPa, membrane surface flow rate is 1.5m/s and permeation side backpressure is 0.2 MPa; the filtrate is directly returned to the quenching water tower for reuse. Periodically carrying out steam backwashing on the membrane, wherein the backwashing pressure is 0.2MPa, the backwashing period is 120min, and the backwashing time is 10 min; and (3) periodically backwashing the membrane with filtrate, wherein the backwashing pressure is 0.4MPa, the backwashing period is 120min, and the backwashing time is 30 s. The primary membrane filter 3 is concentrated by 12 times, the concentrated solution enters the sedimentation tank 4, the concentrated solution is naturally cooled to 50 ℃, the sludge at the bottom is discharged into the sludge dewatering tower for treatment through a sludge discharge pump 8, the supernatant is sent into the KMPR filter 6 through a KMPR feeding pump 5, the air is introduced into the bottom of the KMPR filter 6 for aeration, the aeration rate is 60Nm3H is used as the reference value. And returning the clear liquid to the quenching water tower for recycling through a KMPR water producing pump 7 on the water producing side after passing through the KMPR filter 6, backwashing the KMPR filter every 30min, wherein the backwashing time is 5s, and the backwashing pressure is 0.1 MPa. The sludge is concentrated by 2 times, and the sludge at the bottom of the KMPR filter 6 is sent to a sludge dewatering tower for treatment through a sludge pump 8.
The quality of the filtrate, the recovery rate of each stage of water and the total recovery rate are as follows:
| ss content of filtrate | mg/L | 7 |
| Water recovery rate of first-stage membrane filter | ％ | 91.7 |
| KMPR water recovery | ％ | 50 |
| Total water recovery | ％ | 95.85 |
Example 3
Referring to the process scheme shown in FIG. 1, quench water was used at 90 ℃ and a solids content of 238 mg/L. Under the push of a feeding pump 1 of the primary membrane filter, the mixture enters a circulating pump 2 of the primary membrane filter and then is sent to the primary membrane filter 3, the aperture of a metal membrane in the primary membrane filter 3 is 100nm, and the mixture works under the conditions that transmembrane pressure difference is 0.4MPa, membrane surface flow rate is 0.5m/s and permeation side backpressure is 0.2 MPa; the filtrate is directly returned to the quenching water tower for reuse. And (3) periodically carrying out steam washing on the membrane, wherein the steam pressure is 0.6MPa, the washing period is 24 hours, and the washing time is 60 min. The operation is carried out for 20 hours, and chemical cleaning is carried out. The primary membrane filter 3 is concentrated by 10 times, the concentrated solution enters the sedimentation tank 4, the concentrated solution is naturally cooled to 40 ℃, the sludge at the bottom is discharged into the sludge dewatering tower for treatment through a sludge discharge pump 8, the supernatant is sent into the KMPR filter 6 through a KMPR feeding pump 5, air is introduced into the bottom of the KMPR filter 6 for aeration, the aeration rate is 30Nm3H is used as the reference value. And returning the clear liquid to the quenching water tower for recycling through a KMPR water producing pump 7 on the water producing side after passing through the KMPR filter 6, backwashing the KMPR filter every 60min, wherein the backwashing time is 10s, and the backwashing pressure is 0.03 MPa. 2.5 times concentrated, KMPR filterAnd 6, conveying the sludge at the bottom of the tower 6 into a sludge dewatering tower through a sludge discharge pump 8 for treatment.
The quality of the filtrate, the recovery rate of each stage of water and the total recovery rate are as follows:
| ss content of filtrate | mg/L | 13 |
| Water recovery rate of first-stage membrane filter | ％ | 90 |
| KMPR water recovery | ％ | 60 |
| Total water recovery | ％ | 96 |
Example 4
Referring to the process scheme shown in FIG. 1, quench water was used at 110 ℃ and a solids content of 195 mg/L. Under the push of a feeding pump 1 of the primary membrane filter, the mixture enters a circulating pump 2 of the primary membrane filter and then is sent to the primary membrane filter 3, the aperture of a metal membrane in the primary membrane filter 3 is 20nm, and the mixture works under the conditions of transmembrane pressure difference of 1MPa, membrane surface flow rate of 0.2m/s and osmotic side back pressure of 0.2 MPa; the filtrate is directly returned to the quenching water tower for reuse. Periodically backwashing the membrane with filtrate, wherein the backwashing pressure is 1MPa, the backwashing period is 30min, and the backwashing time is 10 s; steam backwashing pressure is 0.6Mpa, backwashing period is 20min, and backwashing time is 60 s; steam flushing pressure of 0.1MPa and flushing period of 6 hrAnd the washing time is 30 min. The primary membrane filter 3 is concentrated by 11 times, the concentrated solution enters the sedimentation tank 4, the concentrated solution is naturally cooled to 45 ℃, the sludge at the bottom is discharged into the sludge dewatering tower for treatment through the sludge discharge pump 8, the supernatant is sent into the KMPR filter 6 through the KMPR feeding pump 5, the air is introduced into the bottom of the KMPR filter 6 for aeration, the aeration amount is 50Nm3H is used as the reference value. And returning the clear liquid to the quenching water tower for recycling through a KMPR water producing pump 7 on the water producing side after passing through the KMPR filter 6, backwashing the KMPR filter every 150min, wherein the backwashing time is 20s, and the backwashing pressure is 0.08 MPa. The sludge is concentrated by 3 times, and the sludge at the bottom of the KMPR filter 6 is sent to a sludge dewatering tower for treatment through a sludge pump 8.
The quality of the filtrate, the recovery rate of each stage of water and the total recovery rate are as follows:
| ss content of filtrate | mg/L | 10 |
| Water recovery rate of first-stage membrane filter | ％ | 90.9 |
| KMPR water recovery | ％ | 66.7 |
| Total water recovery | ％ | 97. |
Example 5
Referring to the process flow shown in fig. 1, chilled water, water temperature 85 c,the solid content was 500 mg/L. Under the push of a feeding pump 1 of the primary membrane filter, the mixture enters a circulating pump 2 of the primary membrane filter and then is sent to a primary membrane filter 3, the aperture of a metal membrane in the primary membrane filter 3 is 100nm, and the mixture works under the conditions that transmembrane pressure difference is 0.3MPa, membrane surface flow rate is 1m/s and permeation side backpressure is 0.3 MPa; the filtrate is directly returned to the quenching water tower for reuse. Periodically backwashing the membrane with filtrate, wherein the backwashing pressure is 0.5MPa, the backwashing period is 50min, and the backwashing time is 20 s; steam backwashing pressure is 0.1Mpa, backwashing period is 60min, and backwashing time is 120 s. The primary membrane filter 3 is concentrated by 10 times, the concentrated solution enters the sedimentation tank 4, the concentrated solution is naturally cooled to the temperature of 25 ℃, the sludge at the bottom is discharged into the sludge dewatering tower for treatment through the sludge discharge pump 8, the supernatant is sent into the KMPR filter 6 through the KMPR feeding pump 5, the air is introduced into the bottom of the KMPR filter 6 for aeration, the aeration rate is 100Nm3H is used as the reference value. And returning the clear liquid to the quenching water tower for recycling through a KMPR water producing pump 7 on the water producing side after passing through the KMPR filter 6, backwashing the KMPR filter every 120min, wherein the backwashing time is 30s, and the backwashing pressure is 0.05 MPa. The sludge is concentrated by 2 times, and the sludge at the bottom of the KMPR filter 6 is sent to a sludge dewatering tower for treatment through a sludge pump 8.
The quality of the filtrate, the recovery rate of each stage of water and the total recovery rate are as follows:
the embodiments described above are intended to facilitate the understanding and use of the invention by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above embodiments, and those skilled in the art should make improvements and modifications within the scope of the present invention according to the disclosure of the present invention.
Claims (10)
1. A recycling system of quenching water in a methanol-to-olefin process is characterized by comprising a first-stage membrane filter (3), a sedimentation tank (4) and a KMPR filter (6),
the first-stage membrane filter (3) is used for receiving quenching water in the process of preparing olefin from methanol and separating the quenching water into filtrate and concentrated solution, the filtrate can be directly recycled,
the sedimentation tank (4) is used for receiving the concentrated solution and naturally cooling and settling the concentrated solution,
the KMPR filter (6) is used for receiving the concentrated solution treated by the sedimentation tank (4) and separating the concentrated solution into produced water and sludge, the produced water can be directly recycled, and the sludge is directly discharged into a sludge treatment system.
2. The recycling system of quench water in the methanol-to-olefin process according to claim 1, wherein a primary membrane filter feed pump (1) is further disposed in front of the primary membrane filter (3), and the primary membrane filter feed pump (1) is connected to the primary membrane filter (3) and is used for pumping the quench water in the methanol-to-olefin process into the primary membrane filter (3).
3. The recycling system of quenching water in the process of preparing olefin from methanol according to claim 1, wherein a primary membrane filter circulating pump (2) is further connected between the primary membrane filter feeding pump (1) and the primary membrane filter (3).
4. The recycling system of the quenching water in the methanol-to-olefin process as claimed in claim 1, wherein a KMPR feeding pump (5) is connected to the pipeline between the sedimentation tank (4) and the KMPR filter (6), and the KMPR feeding pump (5) is used for pumping the concentrated solution treated by the sedimentation tank (4) into the KMPR filter (6).
5. The recycling system of quench water in the methanol-to-olefin process as claimed in claim 1, wherein a sludge line is led out from the bottom of the KMPR filter (6) and the bottom of the sedimentation tank (4), and a sludge discharge pump (8) is arranged on the sludge line, and the sludge line is used for connecting with a sludge dewatering tower.
6. The recycling system of quenching water in the methanol to olefin process according to claim 1, wherein the primary membrane filter (3) is a metal membrane filter.
7. The recycling system of quenching water in methanol to olefin process according to claim 6, wherein the membrane module of the primary membrane filter (3) is coated with TiO2The metal film of the layer, the filtration precision of the metal film is 20-100nm, and the diameter of the filtration channel is 11-19 mm.
8. The recycling system of the quenching water in the methanol to olefin process as claimed in claim 1, wherein the KMPR filter (6) comprises a membrane tank, membrane modules arranged in the membrane tank for separating the concentrated solution treated by the sedimentation tank (4), and a water production line led out from the membrane tank, and one or more groups of membrane modules are arranged in the membrane tank.
9. The recycling system of quench water in methanol to olefin process according to claim 8, wherein the water production line is provided with a KMPR water production pump (7).
10. The recycling system of quench water in the methanol to olefin process of claim 8, wherein an aeration device is arranged at the bottom of the membrane tank.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111153513A (en) * | 2020-01-21 | 2020-05-15 | 上海凯鑫分离技术股份有限公司 | Recycling method and recycling system of quenching water in methanol-to-olefin process |
| CN111153513B (en) * | 2020-01-21 | 2024-07-02 | 上海凯鑫分离技术股份有限公司 | Recycling method and recycling system of quench water in methanol-to-olefin process |
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2020
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111153513A (en) * | 2020-01-21 | 2020-05-15 | 上海凯鑫分离技术股份有限公司 | Recycling method and recycling system of quenching water in methanol-to-olefin process |
| CN111153513B (en) * | 2020-01-21 | 2024-07-02 | 上海凯鑫分离技术股份有限公司 | Recycling method and recycling system of quench water in methanol-to-olefin process |
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