CN111153513A - Recycling method and recycling system of quenching water in methanol-to-olefin process - Google Patents
Recycling method and recycling system of quenching water in methanol-to-olefin process Download PDFInfo
- Publication number
- CN111153513A CN111153513A CN202010072239.5A CN202010072239A CN111153513A CN 111153513 A CN111153513 A CN 111153513A CN 202010072239 A CN202010072239 A CN 202010072239A CN 111153513 A CN111153513 A CN 111153513A
- Authority
- CN
- China
- Prior art keywords
- filter
- kmpr
- water
- concentrated solution
- backwashing
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 165
- 238000010791 quenching Methods 0.000 title claims abstract description 83
- 238000000034 method Methods 0.000 title claims abstract description 79
- 230000000171 quenching effect Effects 0.000 title claims abstract description 75
- 230000008569 process Effects 0.000 title claims abstract description 59
- 238000004064 recycling Methods 0.000 title claims abstract description 39
- 239000012528 membrane Substances 0.000 claims abstract description 182
- 239000010802 sludge Substances 0.000 claims abstract description 79
- 239000000706 filtrate Substances 0.000 claims abstract description 48
- 239000002184 metal Substances 0.000 claims abstract description 27
- 238000000926 separation method Methods 0.000 claims abstract description 8
- 238000011001 backwashing Methods 0.000 claims description 87
- 238000004062 sedimentation Methods 0.000 claims description 40
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 39
- 238000001914 filtration Methods 0.000 claims description 19
- 238000005273 aeration Methods 0.000 claims description 16
- 238000004140 cleaning Methods 0.000 claims description 16
- 150000001336 alkenes Chemical class 0.000 claims description 12
- 238000011010 flushing procedure Methods 0.000 claims description 12
- 238000004519 manufacturing process Methods 0.000 claims description 12
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 10
- 239000006228 supernatant Substances 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 7
- 238000005086 pumping Methods 0.000 claims description 6
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 5
- 238000009295 crossflow filtration Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000011084 recovery Methods 0.000 abstract description 30
- 239000003054 catalyst Substances 0.000 description 20
- 239000007787 solid Substances 0.000 description 11
- 239000000203 mixture Substances 0.000 description 8
- 238000005406 washing Methods 0.000 description 8
- 239000007788 liquid Substances 0.000 description 7
- 239000000843 powder Substances 0.000 description 6
- 239000006227 byproduct Substances 0.000 description 5
- 239000007789 gas Substances 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 3
- 239000012495 reaction gas Substances 0.000 description 3
- 238000013020 steam cleaning Methods 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 239000011248 coating agent Substances 0.000 description 2
- 238000000576 coating method Methods 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 229910000856 hastalloy Inorganic materials 0.000 description 2
- 239000012510 hollow fiber Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000005374 membrane filtration Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to a method for recycling quenching water in a methanol-to-olefin process, wherein the quenching water in the methanol-to-olefin process enters a first-stage membrane filter, the first-stage membrane filter separates the quenching water into filtrate and concentrated solution, the filtrate can be directly recycled to a quenching water tower, the water recycling rate after the treatment of the first-stage membrane filter is more than 90%, a membrane component of the first-stage membrane filter adopts a metal membrane, the concentrated solution enters a KMPR filter for separation, the concentrated solution is separated into produced water and sludge by the KMPR filter, the produced water can be directly recycled to the quenching water tower, and the sludge is directly discharged into a sludge treatment system. Compared with the prior art, the invention has high water recovery rate, can run at high temperature, backwashes on line and greatly improves the running stability of the system.
Description
Technical Field
The invention relates to a water treatment technology of a methanol-to-olefin process, in particular to a recycling method and a recycling system of quenching water in the 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 invention has the defects of low filtration precision, incomplete separation of the catalyst and the 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 invention completely separates oil, water and catalyst, but the recovery rates of the oil, the water and the catalyst are all not high, and simultaneously, due to the characteristics of the ceramic membrane, the defects of high investment and operation cost, poor stability and the like exist in the practical application.
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.
Disclosure of Invention
The invention aims to provide a method and a system for recycling quenching water in a methanol-to-olefin process, so as to solve the problem of recycling water in the prior quenching water treatment.
The invention adopts a metal membrane system, can process the quenching water at high temperature on line, intensively solve the recycling problem of the quenching water, realizes more than 95 percent of water recovery rate through a two-stage system, realizes high flux treatment under the high temperature condition, greatly reduces the investment cost, and simultaneously can ensure the stability of the system through on-line high-temperature backwashing and stable membrane surface flow velocity due to the special structure and material characteristics of the metal membrane.
The purpose of the invention can be realized by the following technical scheme:
the invention firstly discloses a method for recycling quenching water in a methanol-to-olefin process, which comprises the following steps:
quenching water in the methanol-to-olefin process enters a primary membrane filter, the primary membrane filter separates the quenching water into filtrate and concentrated solution, the filtrate can be directly reused in a quenching water tower, the water reuse rate after treatment by the primary membrane filter is more than 90%, and a membrane component of the primary membrane filter adopts a metal membrane; the concentrated solution enters a KMPR filter for separation, the KMPR filter separates the concentrated solution into produced water and sludge, the produced water can be directly recycled in a quenching water tower, the sludge is directly discharged into a sludge treatment system, and the KMPR filter further recovers more than 50% of the volume of the concentrated solution.
In one embodiment of the invention, the membrane component 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 one embodiment of the present invention, the operating conditions of the primary membrane filter are:
the filtration temperature is preferably from 80 to 130 c, more preferably from 85 to 110 c,
the filtration mode adopts cross-flow filtration, the cross-flow rate is preferably 0.2-6m/s, more preferably 0.5-1.5m/s,
the transmembrane pressure difference is preferably from 0.1 to 1MPa, more preferably from 0.2 to 0.4 MPa.
In one embodiment of the invention, the method for recycling the quenching water in the methanol-to-olefin process also comprises a cleaning mode of a first-stage membrane filter in the operation process,
the cleaning operation conditions of the primary membrane filter are as follows:
selecting conventional chemical cleaning, or filtrate backwashing, or steam flushing, or a combination of several cleaning modes;
the conventional chemical cleaning can be carried out under the conditions of heating or normal temperature;
the backwashing pressure of the filtrate 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: and (3) backwashing by adopting 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.
In the process, the water reuse rate after the treatment of the primary membrane filter is more than 90%, and the KMPR filter further recovers water with the volume of more than 50% of the concentrated solution.
In one embodiment of the invention, the water temperature of the quenching water in the methanol-to-olefin process is greater than 80 ℃, and the solid content is 150-700mg/L, and further 150-500 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.
In one embodiment of the present invention, the operating conditions of the KMPR filter are:
the filtration temperature is preferably from 5 to 50 c, more preferably from 30 to 45 c,
the aeration rate is preferably 10-100Nm3/h, more preferably 30-60Nm3/h。
In one embodiment of the invention, the operation process of the method for recycling the quenching water in the methanol-to-olefin process further comprises backwashing the KMPR filter, wherein the backwashing operation conditions of the KMPR filter are as follows: 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 one embodiment of the invention, the concentrated solution firstly enters a sedimentation tank, the sedimentation tank is used for receiving the concentrated solution and naturally cooling and settling the concentrated solution, and the concentrated solution treated by the sedimentation tank enters the KMPR filter for treatment
In one embodiment of the invention, the sedimentation tank naturally cools the concentrated solution to a temperature of less than 50 ℃, bottom sludge is discharged into a sludge dewatering tower through a sludge discharge pump for treatment, and supernatant is sent into a KMPR filter.
In one embodiment of the invention, under the process that the concentrated solution enters the KMPR filter for separation, the quenching water in the process of preparing olefin from methanol enters a primary membrane filter circulating pump under the driving of a primary membrane filter feeding pump, and then is sent to the primary membrane filter, wherein the primary membrane filter circulating pump is used for ensuring the membrane surface flow rate of the primary membrane filter; the supernatant in the sedimentation tank is sent to a KMPR filter through a KMPR feeding pump.
In one embodiment of the invention, the KMPR filter adopts an immersion type membrane filtration system, a membrane pool, membrane modules arranged in the membrane pool and used for separating concentrated liquid treated by a sedimentation pool, and a water production pipeline led out from the membrane pool, wherein a KMPR water production pump is arranged on the water production pipeline, one or more groups of membrane modules are arranged in the membrane pool, and an aeration device is arranged at the bottom of the membrane pool. The membrane component adopts hollow fiber type membrane filaments and adopts a curtain type or column type structure.
The invention also provides a recycling system of the quenching water in the methanol-to-olefin process, which comprises a primary membrane filter, a sedimentation tank and a KMPR filter, wherein the primary membrane filter 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 is used for receiving the concentrated solution and naturally cooling and settling the concentrated solution, the KMPR filter is used for receiving the concentrated solution treated by the sedimentation tank 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.
Further, a primary membrane filter feeding pump is arranged in front of the primary membrane filter, and the primary membrane filter feeding pump is connected with the primary membrane filter and is used for pumping quenching water in the methanol-to-olefin process into the primary membrane filter; and a primary membrane filter circulating pump is also connected between the primary membrane filter feeding pump and the primary membrane filter.
Furthermore, a KMPR feeding pump is connected to a pipeline between the sedimentation tank and the KMPR filter, and is used for pumping the concentrated solution treated by the sedimentation tank into the KMPR filter.
Furthermore, sludge pipelines are led out from the KMPR filter and the bottom of the sedimentation tank, a sludge discharge pump is arranged on the sludge pipelines, and the sludge pipelines are used for being connected with a sludge dewatering tower.
In one embodiment of the invention, the primary membrane filter is a metal membrane filter. 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 filtering precision of the metal film is 20-100nm, and the diameter of the filtering channel is 11-19 mm.
In the metal membrane filter, membrane tubes are arranged in a cavity in a manner similar to a tube type heat exchanger, and each metal tube is independently welded to the flower plates at two ends to form a sealing manner different from other membrane components. The membrane tube wall thickness is <2 mm. 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 membrane component made of all metal materials has a better temperature tolerance range and stronger temperature impact and mechanical impact resistance. Steam cleaning can be achieved. The material and the structure are the key for realizing steam cleaning and backwashing.
Compared with the prior art, the invention has the following advantages and beneficial effects:
(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 embodiment 1;
FIG. 2 is a schematic cross-sectional view of a primary membrane filter;
FIG. 3 is a schematic view of a primary membrane filter configuration.
Detailed Description
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 cleaning of the primary membrane filter 3 and the KMPR filter 6,
the cleaning operation conditions for the primary membrane filter 3 are as follows: selecting one or a combination of a plurality of cleaning modes of conventional chemical cleaning, filtrate backwashing, steam backwashing or steam flushing; conventional chemical cleaning can be carried out under the conditions of heating or normal temperature; the backwashing pressure of the filtrate 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 with low pressure steam at 1-6bar for 1-10min for 20-120 min; the steam flushing conditions were: low pressure steam, washing pressure of 1-10abr, washing time of 1-60min, preferably 30-60min, and washing period of 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 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 invention is described in detail below with reference to the figures and specific embodiments.
Example 1
Referring to the process scheme shown in FIG. 1, quench water, water temperature 80 ℃ and a solid content of 700 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 0.1MPa, 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. The concentration is 2.5 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 | 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; the steam flushing pressure is 0.1Mpa, the flushing period is 6 hours, and the flushing time is 30 min. Concentrating by 11 times with a first-stage membrane filter 3, allowing the concentrated solution to enter a sedimentation tank 4, naturally cooling the concentrated solution to 45 deg.C, and cooling to the bottomThe sludge is discharged into a sludge dewatering tower for treatment through a sludge discharge pump 8, the supernatant is sent into a KMPR filter 6 through a KMPR feeding pump 5, air is introduced into the bottom of the KMPR filter 6 for aeration, and the aeration rate 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 scheme shown in FIG. 1, the quenching water is cooled to 85 ℃ and has a solid content of 500 mg/L. Driven by a feeding pump 1 of the first-stage membrane filter, enters a circulating pump 2 of the first-stage membrane filter and then is sent to the first-stage membrane filter3, the aperture of the metal membrane in the primary membrane filter 3 is 100nm, and the primary membrane filter works under the conditions that the transmembrane pressure difference is 0.3MPa, the membrane surface flow rate is 1m/s, and the back pressure of a permeation side 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:
| ss content of filtrate | mg/L | 10 |
| Water recovery rate of first-stage membrane filter | ％ | 90 |
| KMPR water recovery | ％ | 50 |
| Total water recovery | ％ | 95 |
The embodiments described above are described to facilitate an 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 based on the disclosure of the present invention.
Claims (10)
1. A method for recycling quenching water in a process for preparing olefin from methanol, which is characterized in that,
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 water reuse rate after the treatment of the first-stage membrane filter (3) is more than 90%,
the membrane component of the first-stage membrane filter (3) adopts a metal membrane,
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 to a quenching water tower, the sludge is directly discharged into a sludge treatment system, and the KMPR filter (6) further recovers water with the volume of the concentrated solution being more than 50%.
2. The recycling method of quenching water in methanol to olefin process according to claim 1, 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.
3. The method for recycling quenching water in the methanol-to-olefin process according to claim 1, wherein the operating conditions of the primary membrane filter (3) are as follows:
the filtration temperature is preferably from 80 to 130 c, more preferably from 85 to 110 c,
the filtration mode adopts cross-flow filtration, the cross-flow rate is preferably 0.2-6m/s, more preferably 0.5-1.5m/s,
the transmembrane pressure difference is preferably from 0.1 to 1MPa, more preferably from 0.2 to 0.4 MPa.
4. The recycling method of quenching water in the methanol to olefin process according to claim 1, wherein the recycling method of quenching water in the methanol to olefin process further comprises cleaning the first-stage membrane filter (3),
the cleaning operation conditions of the primary membrane filter (3) are as follows:
selecting conventional chemical cleaning, or filtrate backwashing, or steam flushing, or a combination of several cleaning modes;
the conventional chemical cleaning can be carried out under the conditions of heating or normal temperature;
the backwashing pressure of the filtrate 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: and (3) backwashing by adopting 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 operating conditions of the steam flush were: flushing with low pressure steam at 1-10bar for 1-60min for 1-24 hr.
5. The method for recycling quenching water in the methanol-to-olefin process as claimed in claim 1, wherein the KMPR filter (6) is operated under the following conditions:
the filtration temperature is preferably from 5 to 50 c, more preferably from 30 to 45 c,
the aeration rate is preferably 10-100Nm3H, more preferably 30-60Nm3/h。
6. The method for recycling quenching water in the methanol-to-olefin process as claimed in claim 1, wherein the method for recycling quenching water in the methanol-to-olefin process further comprises backwashing the KMPR filter (6), and the backwashing operation conditions of the KMPR filter (6) are as follows:
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.
7. The method for recycling quenching water in the methanol-to-olefin process according to claim 1, wherein the concentrated solution is firstly fed into a sedimentation tank (4), the sedimentation tank (4) is used for receiving the concentrated solution, naturally cooling and settling the concentrated solution, and the concentrated solution treated by the sedimentation tank (4) is fed into the KMPR filter (6) for treatment; the sedimentation tank (4) naturally cools the concentrated solution to the temperature of less than 50 ℃, the sludge at the bottom is discharged into a sludge dewatering tower for treatment, and the supernatant is sent into a KMPR filter (6).
8. The method for recycling 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, wherein a KMPR water production pump (7) is arranged on the water production line, one or more groups of membrane modules are arranged in the membrane tank, and an aeration device is arranged at the bottom of the membrane tank.
9. 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.
10. The recycling system of the quenching water in the methanol to olefin process according to claim 9, wherein a primary membrane filter feed pump (1) is further arranged in front of the primary membrane filter (3), and the primary membrane filter feed pump (1) is connected with the primary membrane filter (3) and is used for pumping the quenching water in the methanol to olefin process into the primary membrane filter (3); a primary membrane filter circulating pump (2) is connected between the primary membrane filter feeding pump (1) and the primary membrane filter (3);
a KMPR feeding pump (5) is connected on a 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);
sludge pipelines are led out from the bottoms of the KMPR filter (6) and the sedimentation tank (4), a sludge discharge pump (8) is arranged on the sludge pipelines, and the sludge pipelines are used for being connected with a sludge dewatering tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010072239.5A CN111153513B (en) | 2020-01-21 | 2020-01-21 | Recycling method and recycling system of quench water in methanol-to-olefin process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010072239.5A CN111153513B (en) | 2020-01-21 | 2020-01-21 | Recycling method and recycling system of quench water in methanol-to-olefin process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111153513A true CN111153513A (en) | 2020-05-15 |
| CN111153513B CN111153513B (en) | 2024-07-02 |
Family
ID=70565453
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010072239.5A Active CN111153513B (en) | 2020-01-21 | 2020-01-21 | Recycling method and recycling system of quench water in methanol-to-olefin process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111153513B (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001225057A (en) * | 2000-02-18 | 2001-08-21 | Japan Organo Co Ltd | Water purifying device |
| JP2001269554A (en) * | 2000-03-27 | 2001-10-02 | Japan Organo Co Ltd | Metallic membrane filter and water treatment method |
| US20030196905A1 (en) * | 2001-12-31 | 2003-10-23 | Dobri Dobrev | Metal membrane filter, and method and apparatus for the production thereof |
| CN104030466A (en) * | 2014-04-30 | 2014-09-10 | 河海大学 | Novel immersion ultrafilter apparatus |
| CN205590371U (en) * | 2016-04-25 | 2016-09-21 | 浙江兴兴新能源科技有限公司 | MTOMTP chilled water (chw) of low energy consumption and membrane treatment equipment of washing water |
| CN106362598A (en) * | 2015-07-22 | 2017-02-01 | 成均馆大学校产学协力团 | Apparatus and method for continuously measuring membrane fouling index |
| CN206184114U (en) * | 2016-11-22 | 2017-05-24 | 联泓新材料有限公司 | Methyl alcohol system for alkene chilled water (chw) make up filtration system |
| CN211734024U (en) * | 2020-01-21 | 2020-10-23 | 上海凯鑫分离技术股份有限公司 | Recycling system of quenching water in methanol-to-olefin process |
-
2020
- 2020-01-21 CN CN202010072239.5A patent/CN111153513B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001225057A (en) * | 2000-02-18 | 2001-08-21 | Japan Organo Co Ltd | Water purifying device |
| JP2001269554A (en) * | 2000-03-27 | 2001-10-02 | Japan Organo Co Ltd | Metallic membrane filter and water treatment method |
| US20030196905A1 (en) * | 2001-12-31 | 2003-10-23 | Dobri Dobrev | Metal membrane filter, and method and apparatus for the production thereof |
| CN104030466A (en) * | 2014-04-30 | 2014-09-10 | 河海大学 | Novel immersion ultrafilter apparatus |
| CN106362598A (en) * | 2015-07-22 | 2017-02-01 | 成均馆大学校产学协力团 | Apparatus and method for continuously measuring membrane fouling index |
| CN205590371U (en) * | 2016-04-25 | 2016-09-21 | 浙江兴兴新能源科技有限公司 | MTOMTP chilled water (chw) of low energy consumption and membrane treatment equipment of washing water |
| CN206184114U (en) * | 2016-11-22 | 2017-05-24 | 联泓新材料有限公司 | Methyl alcohol system for alkene chilled water (chw) make up filtration system |
| CN211734024U (en) * | 2020-01-21 | 2020-10-23 | 上海凯鑫分离技术股份有限公司 | Recycling system of quenching water in methanol-to-olefin process |
Non-Patent Citations (1)
| Title |
|---|
| 陈芬、胡莉娟主编: "《水体污染处理新技术及应用》", 中国科学技术大学出版社, pages: 174 - 175 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN111153513B (en) | 2024-07-02 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP2636439B1 (en) | Method for cleaning and separating mto reaction gas containing catalyst micropowders | |
| CN103951098B (en) | In MTO technology, quenched water and washing water take off method and the device of solid oil removing | |
| CN102030433B (en) | Method for treating pure terephthalic acid refined wastewater | |
| CN102515377B (en) | Integrated membrane electroplated nickel-contained rinsing water zero-discharging process and special equipment thereof | |
| CN110818149A (en) | PTA refining mother liquor recovery method and recovery system | |
| CN113461199A (en) | Method and system for separating sodium carbonate and sodium bromide from PTA (pure terephthalic acid) oxidation tail gas washing tower discharge liquid | |
| JP2014005226A (en) | Process for producing terephthalic acid | |
| CN106672911A (en) | Oxidation-extraction technology for production of hydrogen peroxide by anthraquinone process | |
| CN111499069A (en) | Comprehensive treatment system and treatment method for waste cutting fluid | |
| CN112723633A (en) | Treatment method and system for liquid discharged from PTA (pure terephthalic acid) oxidation tail gas washing tower | |
| CN111732083A (en) | Fluidized bed hydrogen peroxide process | |
| CN211734024U (en) | Recycling system of quenching water in methanol-to-olefin process | |
| CN211920978U (en) | Recycling system of quenching water in methanol-to-olefin process | |
| CN203820559U (en) | Device for solid removal and oil removal of quenching water and washing water in process of producing olefins from methanol | |
| RU2471767C1 (en) | Simple method and system for efficient recycling of mother solution from apparatus for producing purified terephthalic acid | |
| CN111153469A (en) | Recycling method and recycling system of quenching water in methanol-to-olefin process | |
| CN111056903B (en) | Process and device for recovering benzene partial hydrogenation catalyst | |
| CN113105056A (en) | Method for resource utilization of purified terephthalic acid wastewater | |
| CN111153513A (en) | Recycling method and recycling system of quenching water in methanol-to-olefin process | |
| CN111392818A (en) | Dynamic membrane for treating oily sewage and preparation method and application thereof | |
| CN112742177A (en) | Method and device for purifying and removing heat stable salt in amine liquid | |
| EP2634168B1 (en) | Crossflow type filtering operation method using ceramic filter | |
| CN112827323A (en) | Purification system, purification method and application of methanol-to-olefin product gas | |
| CN212999353U (en) | Recycling system of purified water of methanol-to-olefin process | |
| CN112624471A (en) | Short-process coal gasification black water purification method and device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant |