JP7633300B2 - Liquid fertilizer manufacturing device and liquid fertilizer manufacturing method - Google Patents
Liquid fertilizer manufacturing device and liquid fertilizer manufacturing method Download PDFInfo
- Publication number
- JP7633300B2 JP7633300B2 JP2023054510A JP2023054510A JP7633300B2 JP 7633300 B2 JP7633300 B2 JP 7633300B2 JP 2023054510 A JP2023054510 A JP 2023054510A JP 2023054510 A JP2023054510 A JP 2023054510A JP 7633300 B2 JP7633300 B2 JP 7633300B2
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- composition ratio
- liquid fertilizer
- nitrogen
- operating conditions
- 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.)
- Active
Links
Images
Landscapes
- Fertilizers (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Description
本発明は、液体肥料製造装置及び液体肥料製造方法に関する。 The present invention relates to a liquid fertilizer manufacturing device and a liquid fertilizer manufacturing method.
液体肥料は穀物、野菜、果物、花卉等、様々な種類の植物の生育に有用である。液体肥料が含有する無機態窒素は、（１）アンモニア態窒素、（２）硝酸態窒素及び亜硝酸態窒素に大別される。
植物の生育条件は様々であり、栽培環境としては露地栽培、施設園芸が挙げられる。また、上述の通り、植物の種類も様々である。
Liquid fertilizers are useful for the growth of various types of plants, including grains, vegetables, fruits, flowers, etc. The inorganic nitrogen contained in liquid fertilizers is roughly divided into (1) ammonia nitrogen, (2) nitrate nitrogen, and nitrite nitrogen.
Plants have a wide variety of growing conditions, including outdoor cultivation and protected horticulture, and as mentioned above, there are also many different types of plants.
これらの、植物の生育条件や植物の種類によって、液体肥料が含有する無機態窒素に求められる組成比は様々であり、求められる組成比ではない液体肥料を散布すると、過剰害が発生してしまうことがあった。
有機物の消化液を濃縮して液体肥料を製造する方法として、特許文献１では、限外濾過膜を使用する方法が提案されている。
The composition ratio of inorganic nitrogen required in liquid fertilizer varies depending on the growing conditions and type of plant, and spraying liquid fertilizer that does not have the required composition ratio can cause excessive damage.
As a method for producing liquid fertilizer by concentrating digestive fluid of organic matter, Patent Document 1 proposes a method using an ultrafiltration membrane.
特許文献１で提案されている方法では、有機物の消化液を濃縮した濃縮液中の無機態窒素成分は、アンモニア態窒素が中心となる。このため、植物の生育条件や植物の種類によっては、無機態窒素成分の組成比を変える必要があった。
無機態窒素成分の組成比を変える方法としては、例えば、活性汚泥槽等の装置の設置や、作付け前に液体肥料を散布して数日経過させ、土壌中微生物の硝酸化成作用を用いる方法が挙げられるが、いずれも作業工程やコストが増加するという課題があった。
In the method proposed in Patent Document 1, the inorganic nitrogen components in the concentrate obtained by concentrating the digestive fluid of organic matter are mainly ammonia nitrogen, so it was necessary to change the composition ratio of the inorganic nitrogen components depending on the growing conditions and type of plants.
Methods for changing the composition ratio of inorganic nitrogen components include, for example, installing equipment such as an activated sludge tank, or spraying liquid fertilizer before planting and leaving it for several days to utilize the nitrification action of microorganisms in the soil. However, all of these methods have the problem of increasing the number of work steps and costs.
本発明の主たる目的は、無機態窒素成分の組成比が調整された液体肥料を簡便に製造できる液体肥料製造装置及び液体肥料製造方法を提供することにある。 The main object of the present invention is to provide a liquid fertilizer production apparatus and a liquid fertilizer production method that can easily produce liquid fertilizer with an adjusted composition ratio of inorganic nitrogen components.
本発明者らは、無機態窒素成分の組成比を簡便に調整できる液体肥料の製造装置及び製造方法について鋭意研究した結果、有機物の消化液を生物処理して膜分離する膜分離部の運転条件を制御することによって、上記課題を解決し得ることを見出し、本発明に至った。 The inventors conducted extensive research into a liquid fertilizer manufacturing apparatus and manufacturing method that allows easy adjustment of the composition ratio of inorganic nitrogen components. As a result, they discovered that the above-mentioned problems could be solved by controlling the operating conditions of the membrane separation section that biologically treats the digestive liquid of organic matter and separates it using membranes, and thus arrived at the present invention.
即ち、本発明は以下の特徴を有する。
［１］無機態窒素を含有する液体肥料を製造する液体肥料製造装置であって、
該無機態窒素の目標組成比に沿って運転条件を設定する制御部と、
該制御部の設定に従って、有機物の消化液を生物処理して膜分離する膜分離部と、
該膜分離部で濾過された分離液を濃縮する電気透析部と、を有する、液体肥料製造装置。
［２］前記分離液の組成比を測定する測定部を更に有する、［１］に記載の液体肥料製造装置。
［３］前記測定部の測定値に基づき、前記制御部が前記運転条件を再設定する、［２］に記載の液体肥料製造装置。
［４］前記膜分離部が、メンブレンバイオリアクターである、［１］～［３］のいずれかに記載の液体肥料製造装置。
［５］前記メンブレンバイオリアクターが流量調節装置を備え、前記制御部が前記流量調節装置の運転条件を設定する、［４］に記載の液体肥料製造装置。
［６］前記メンブレンバイオリアクターが液温調節装置を備え、前記制御部が前記液温調節装置の運転条件を設定する、［４］又は［５］に記載の液体肥料製造装置。
［７］前記メンブレンバイオリアクターがｐＨ調節装置を備え、前記制御部が前記ｐＨ調節装置の運転条件を設定する、［４］～［６］のいずれかに記載の液体肥料製造装置。
［８］無機態窒素を含有する液体肥料を製造する液体肥料製造方法であって、
下記工程（１）～（３）を有する、液体肥料製造方法；
工程（１）：該無機態窒素の目標組成比に沿って運転条件を設定する制御工程、
工程（２）：該制御工程の設定に従って、有機物の消化液を生物処理して膜分離する膜分離工程、
工程（３）：該膜分離工程で濾過された分離液を濃縮する電気透析工程。
［９］下記工程（４）を更に有する、［８］に記載の液体肥料製造方法；
工程（４）：前記分離液の組成比を測定する測定工程。
［１０］前記測定工程の測定値に基づき、前記制御工程で運転条件を再設定する、［９］に記載の液体肥料製造方法。
［１１］前記膜分離工程が、メンブレンバイオリアクターを用いる工程である、［８］～［１０］のいずれかに記載の液体肥料製造方法。
［１２］前記メンブレンバイオリアクターが流量調節機能を備え、前記制御工程で前記流量調節機能の運転条件を設定する、［１１］に記載の液体肥料製造方法。
［１３］前記メンブレンバイオリアクターが液温調節機能を備え、前記制御工程で前記液温調節機能の運転条件を設定する、［１１］又は［１２］に記載の液体肥料製造方法。
［１４］前記メンブレンバイオリアクターがｐＨ調節機能を備え、前記制御工程で前記ｐＨ調節機能の運転条件を設定する、［１１］～［１３］のいずれかに記載の液体肥料製造方法。
That is, the present invention has the following features.
[1] A liquid fertilizer manufacturing apparatus for producing liquid fertilizer containing inorganic nitrogen,
A control unit that sets operating conditions according to the target composition ratio of inorganic nitrogen;
A membrane separation unit that biologically treats the organic digestive liquid and separates it into membranes according to the settings of the control unit;
and an electrodialysis section that concentrates the separated liquid filtered by the membrane separation section.
[2] The liquid fertilizer manufacturing apparatus described in [1], further comprising a measuring unit for measuring the composition ratio of the separated liquid.
[3] A liquid fertilizer manufacturing apparatus as described in [2], wherein the control unit resets the operating conditions based on the measurement values of the measurement unit.
[4] The liquid fertilizer manufacturing apparatus according to any one of [1] to [3], wherein the membrane separation section is a membrane bioreactor.
[5] The liquid fertilizer manufacturing apparatus according to [4], wherein the membrane bioreactor is equipped with a flow rate control device, and the control unit sets the operating conditions of the flow rate control device.
[6] A liquid fertilizer manufacturing apparatus according to [4] or [5], wherein the membrane bioreactor is equipped with a liquid temperature adjustment device, and the control unit sets the operating conditions of the liquid temperature adjustment device.
[7] A liquid fertilizer manufacturing apparatus according to any one of [4] to [6], wherein the membrane bioreactor is equipped with a pH adjusting device, and the control unit sets the operating conditions of the pH adjusting device.
[8] A liquid fertilizer production method for producing a liquid fertilizer containing inorganic nitrogen, comprising:
A method for producing a liquid fertilizer, comprising the following steps (1) to (3):
Step (1): A control step of setting operating conditions in accordance with the target composition ratio of inorganic nitrogen;
Step (2): A membrane separation step of biologically treating the organic digestive liquid and subjecting it to membrane separation according to the settings of the control step;
Step (3): An electrodialysis step for concentrating the separated liquid filtered in the membrane separation step.
[9] The liquid fertilizer production method according to [8], further comprising the following step (4):
Step (4): A measuring step of measuring the composition ratio of the separated liquid.
[10] A liquid fertilizer manufacturing method as described in [9], in which operating conditions are reset in the control process based on the measured values in the measurement process.
[11] The liquid fertilizer production method according to any one of [8] to [10], wherein the membrane separation process is a process using a membrane bioreactor.
[12] The liquid fertilizer production method according to [11], wherein the membrane bioreactor has a flow rate control function, and the control process sets operating conditions for the flow rate control function.
[13] The liquid fertilizer production method according to [11] or [12], wherein the membrane bioreactor has a liquid temperature adjustment function, and the control process sets operating conditions for the liquid temperature adjustment function.
[14] The liquid fertilizer production method according to any one of [11] to [13], wherein the membrane bioreactor has a pH adjustment function, and the control process sets operating conditions for the pH adjustment function.
本発明の液体肥料製造装置によれば、無機態窒素成分の組成比が調整された液体肥料を、簡便に製造することができる。
本発明の液体肥料製造方法によれば、簡便な操作で、無機態窒素成分の組成比が調整された液体肥料を製造することができる。
本発明によれば、更なる装置や作業工程は必要なく、植物の生育条件や植物の種類に応じて様々な組成比の液体肥料を迅速に提供することができる。
According to the liquid fertilizer production device of the present invention, liquid fertilizer having an adjusted composition ratio of inorganic nitrogen components can be easily produced.
According to the liquid fertilizer production method of the present invention, a liquid fertilizer having an adjusted composition ratio of inorganic nitrogen components can be produced by a simple operation.
According to the present invention, no additional equipment or work steps are required, and liquid fertilizers with various composition ratios can be quickly provided according to the growing conditions and types of plants.
以下、本発明の実施の形態について、図面を参照しつつ説明する。以下の実施の形態は本発明を説明するための単なる例示であって、本発明をこの実施の形態にのみ限定することは意図されない。
本発明は、その趣旨を逸脱しない限り、様々な態様で実施することが可能である。また、使用する図面は実施の形態の一例を説明するためのものであり、実際の大きさを表すものではない。
Hereinafter, embodiments of the present invention will be described with reference to the drawings. The following embodiments are merely examples for explaining the present invention, and are not intended to limit the present invention to these embodiments.
The present invention can be implemented in various forms without departing from the spirit of the present invention. The drawings are for the purpose of explaining an example of an embodiment, and are not intended to represent the actual size.
＜液体肥料製造装置＞
本発明の液体肥料製造装置は、無機態窒素を含有する液体肥料を製造する液体肥料製造装置であって、無機態窒素の目標組成比に沿って運転条件を設定する制御部と、制御部の設定に従って、有機物の消化液を生物処理して膜分離する膜分離部と、膜分離部で濾過された分離液を濃縮する電気透析部と、を有する。
<Liquid fertilizer production equipment>
The liquid fertilizer manufacturing apparatus of the present invention is a liquid fertilizer manufacturing apparatus that produces liquid fertilizer containing inorganic nitrogen, and has a control unit that sets operating conditions in accordance with a target composition ratio of inorganic nitrogen, a membrane separation unit that biologically treats the digestive liquid of organic matter and separates it through membranes in accordance with the settings of the control unit, and an electrodialysis unit that concentrates the separated liquid filtered by the membrane separation unit.
本発明の液体肥料製造装置は、制御部と、膜分離部と、電気透析部とを有し、後述する測定部を更に有することが好ましい。これらの他にも、一般的な液体肥料製造装置に付帯する設備を有することができる。 The liquid fertilizer production device of the present invention has a control unit, a membrane separation unit, and an electrodialysis unit, and preferably further has a measurement unit described below. In addition to these, it can also have equipment that is associated with a general liquid fertilizer production device.
図１では、本発明に関する設備として、制御部２４，２６，２８、膜分離部２０、電気透析部４０、測定部２９，４３を示している。また、膜分離部２０が備え得る設備として、液温調節装置２３、ｐＨ調節装置２５、流量調節装置２７を示している。
この他に、一般的な設備として、消化液タンク１０、処理水タンク３０、第１の流路１１、第２の流路２１、第３の流路３１等を示している。
1 shows, as the equipment related to the present invention,
In addition, as general equipment, a
無機態窒素は、前述した通り、（１）アンモニア態窒素、（２）硝酸態窒素及び亜硝酸態窒素に大別される。
本発明において製造される液体肥料は、前記無機態窒素を含有する液体肥料であり、（１）アンモニア態窒素と、（２）硝酸態窒素及び亜硝酸態窒素とを、任意の組成比で含有することができる。
ここで、硝酸態窒素とは、硝酸又は硝酸塩を指す。また、任意の組成比とは、植物の生育条件や植物の種類に応じて必要とされる様々な組成比の意味であり、これは即ち、無機態窒素の目標組成比である。
本発明の液体肥料は、前記無機態窒素を任意の濃度で含有することができる。
As mentioned above, inorganic nitrogen is broadly classified into (1) ammonium nitrogen, and (2) nitrate nitrogen and nitrite nitrogen.
The liquid fertilizer produced in the present invention is a liquid fertilizer containing the inorganic nitrogen, and can contain (1) ammonia nitrogen, and (2) nitrate nitrogen and nitrite nitrogen in any composition ratio.
Here, nitrate nitrogen refers to nitric acid or nitrates. In addition, any composition ratio means various composition ratios required depending on the growing conditions and types of plants, that is, the target composition ratio of inorganic nitrogen.
The liquid fertilizer of the present invention can contain the inorganic nitrogen at any concentration.
＜消化液＞
本発明で用いる消化液は、有機物の消化液であり、し尿等の有機物を発酵処理した後の液である。
消化液としては、嫌気性発酵の消化液、好気性発酵の消化液が挙げられる。嫌気性発酵の消化液とは、空気を遮断した無酸素の状態下で発酵処理した液である。好気性発酵の消化液とは、空気で曝気した状態下での発酵処理液である。
<Digestive fluids>
The digestive fluid used in the present invention is a digestive fluid of organic matter, and is a liquid obtained after fermentation of organic matter such as human waste.
The digestive liquid includes digestive liquid from anaerobic fermentation and digestive liquid from aerobic fermentation. The digestive liquid from anaerobic fermentation is a liquid fermented under oxygen-free conditions with air blocked off. The digestive liquid from aerobic fermentation is a liquid fermented under air aeration conditions.
＜制御部＞
本発明の制御部は、無機態窒素の目標組成比に沿って運転条件を設定する。
本発明において、無機態窒素の組成比を調節するのは主に膜分離部であることから、制御部は、無機態窒素の目標組成比に沿って膜分離部の運転条件を設定する。
<Control Unit>
The control unit of the present invention sets the operating conditions in accordance with the target composition ratio of inorganic nitrogen.
In the present invention, since it is mainly the membrane separation section that adjusts the composition ratio of inorganic nitrogen, the control section sets the operating conditions of the membrane separation section in accordance with the target composition ratio of inorganic nitrogen.
後述するメンブレンバイオリアクターが流量調節装置を備える場合、制御部は、分離液の流量を測定し、流量調節装置の運転条件を設定する。
これ以降、この制御部を、「制御部（流量）」と称する場合もある。
When the membrane bioreactor described below is equipped with a flow rate regulator, the control unit measures the flow rate of the separated liquid and sets the operating conditions of the flow rate regulator.
Hereinafter, this control unit may be referred to as the "control unit (flow rate)."
後述するメンブレンバイオリアクターが液温調節装置を備える場合、制御部は、消化液の処理温度を測定し、液温調節装置の運転条件を設定する。
これ以降、この制御部を、「制御部（液温）」と称する場合もある。
When the membrane bioreactor described below is equipped with a liquid temperature regulator, the control unit measures the treatment temperature of the digestive liquid and sets the operating conditions of the liquid temperature regulator.
Hereinafter, this control unit may be referred to as the "control unit (liquid temperature)."
後述するメンブレンバイオリアクターがｐＨ調節装置を備える場合、制御部は、消化液の処理ｐＨを測定し、ｐＨ調節装置の運転条件を設定する。
これ以降、この制御部を、「制御部（ｐＨ）」と称する場合もある。
制御部は、１種を単独で用いてもよく、２種以上を併用してもよい。
When the membrane bioreactor described below is equipped with a pH adjusting device, the control unit measures the treated pH of the digestive liquid and sets the operating conditions of the pH adjusting device.
Hereinafter, this control unit may be referred to as the "control unit (pH)."
The control unit may be used alone or in combination of two or more types.
＜膜分離部＞
本発明の膜分離部は、前記制御部の設定に従って、前記消化液を生物処理して膜分離する。
膜分離部としては、消化液を生物処理して膜分離できる機能を有していればよく、具体的には、メンブレンバイオリアクターが挙げられる。
メンブレンバイオリアクターは、「膜分離活性汚泥法」とも称される。
<Membrane separation section>
The membrane separation unit of the present invention biologically treats the digestive liquid and performs membrane separation in accordance with the settings of the control unit.
The membrane separation section may have any function as long as it can biologically treat the digestive liquid and perform membrane separation, and a specific example thereof is a membrane bioreactor.
The membrane bioreactor is also called a "membrane separation activated sludge process."
本発明で用いるメンブレンバイオリアクターは、処理水と活性汚泥の入った処理槽と、精密濾過膜又は限外濾過膜等の膜を用いるものである。
メンブレンバイオリアクターで、消化液を活性汚泥で処理することにより、好気性細菌による硝化が進行し、アンモニア態窒素が、硝酸態窒素及び亜硝酸態窒素に変換される。処理後の消化液は前記膜で濾過され、前記膜を透過した分離液が電気透析部に送られる。
これ以降、「メンブレンバイオリアクター」を、「ＭＢＲ」と称する場合もある。
The membrane bioreactor used in the present invention uses a treatment tank containing treated water and activated sludge, and a membrane such as a microfiltration membrane or an ultrafiltration membrane.
In the membrane bioreactor, the digestive liquid is treated with activated sludge, whereby nitrification by aerobic bacteria progresses and ammonia nitrogen is converted into nitrate nitrogen and nitrite nitrogen. The treated digestive liquid is filtered through the membrane, and the separated liquid that permeates the membrane is sent to the electrodialysis section.
Hereinafter, "membrane bioreactor" may be referred to as "MBR."
＜電気透析部＞
本発明の電気透析部は、膜分離部で濾過された分離液を濃縮する。電気透析部としては、公知の電気透析装置を用いればよい。
電気透析装置としては、例えば、ＡＧＣエンジニアリング社製のＤＷ－１が挙げられる。
<Electrodialysis section>
The electrodialysis unit of the present invention concentrates the separated liquid filtered in the membrane separation unit. As the electrodialysis unit, a known electrodialysis device may be used.
An example of the electrodialysis device is DW-1 manufactured by AGC Engineering Co., Ltd.
電気透析装置とは、陽イオン交換膜と陰イオン交換膜を交互に、スペーサーを介して多数組積層し、その両端に１対の電極を配置し、陽極側の陰イオン交換膜と陰極側の陽イオン交換膜で仕切られたスペースである脱塩室（Ｄ室）と、それとは反対に陽極側の陽イオン交換膜と陰極側の陰イオン交換膜で仕切られたスペースである濃縮室（Ｃ室）が交互に配置されたものである。
Ｄ室に原液を供給すると陽イオンは陰極に向かって陽イオン交換膜を透過して陰極寄りのＣ室に移動する。その際、Ｃ室の陰極側は陰イオン交換膜で仕切られているため、さらに隣のＤ室に移動することはできない。
同様に、陰イオンはＤ室から陽極側のＣ室に移動する。結果としてＤ室で脱塩され、Ｃ室で濃縮される。
An electrodialysis device is a device in which multiple sets of cation exchange membranes and anion exchange membranes are alternately stacked with spacers between them, with a pair of electrodes disposed at both ends, and deionization chambers (chambers D), which are spaces partitioned by the anion exchange membrane on the anode side and the cation exchange membrane on the cathode side, and concentration chambers (chambers C), which are spaces partitioned by the cation exchange membrane on the anode side and the anion exchange membrane on the cathode side, are arranged alternately.
When the stock solution is supplied to compartment D, the cations pass through the cation exchange membrane toward the cathode and move to compartment C, which is closer to the cathode. However, because the cathode side of compartment C is separated by an anion exchange membrane, the cations cannot move further to the adjacent compartment D.
Similarly, anions move from compartment D to compartment C on the anode side. As a result, they are desalted in compartment D and concentrated in compartment C.
電気透析部では、処理対象である分離液を、電気透析濃縮液と、電気透析脱塩液に分ける。電気透析濃縮液は、処理前の分離液よりも塩濃度が高く、電気透析脱塩液は、処理前の分離液よりも塩濃度が低い。
電気透析部の機能は上述の通りであり、無機態窒素を濃縮することはできるが、無機態窒素の組成比を積極的に調節するものではない。
In the electrodialysis section, the separated liquid to be treated is separated into an electrodialysis concentrate and an electrodialysis desalted liquid. The electrodialysis concentrate has a higher salt concentration than the separated liquid before treatment, and the electrodialysis desalted liquid has a lower salt concentration than the separated liquid before treatment.
The function of the electrodialysis section is as described above, and although it can concentrate inorganic nitrogen, it does not actively adjust the composition ratio of inorganic nitrogen.
＜測定部＞
本発明の液体肥料製造装置は、前記分離液の組成比を測定する測定部を更に有してもよい。
ここで分離液とは、前記活性汚泥で処理され、精密濾過膜又は限外濾過膜等の膜で濾過されたものであり、組成比とは、分離液が含有する無機態窒素の組成比である。
測定部は、分離液の組成比を測定できれば、どの位置に設置されていてもよい。図１を用いて説明すると、測定部２９のように、膜分離部２０から次工程に向かう第２の流路２１に設置されていてもよいし、測定部４３のように、電気透析濃縮液流路４２に設置されていてもよい。
<Measurement section>
The liquid fertilizer manufacturing apparatus of the present invention may further include a measurement unit that measures a composition ratio of the separated liquid.
The separated liquid herein refers to a liquid that has been treated with the activated sludge and filtered through a membrane such as a microfiltration membrane or an ultrafiltration membrane, and the composition ratio refers to the composition ratio of inorganic nitrogen contained in the separated liquid.
The measuring section may be located anywhere as long as it can measure the composition ratio of the separated liquid. For example, as shown in FIG. 1, the measuring section may be located in the
測定部は、分離液中の無機態窒素の組成比を測定できるものであればよく、自動の計測装置でも、手動の計測装置でもよい。 The measuring unit may be any device capable of measuring the composition ratio of inorganic nitrogen in the separated liquid, and may be either an automatic measuring device or a manual measuring device.
＜運転条件の設定／制御＞
制御部が設定する運転条件としては、例えば、ＭＢＲでの消化液の滞留時間、ＭＢＲでの消化液の処理温度、ＭＢＲでの消化液の処理ｐＨが挙げられる。ここで、ＭＢＲでの消化液の滞留時間は、ＭＢＲでの分離液の流量によって調節可能である。
これら、ＭＢＲの運転条件によって、アンモニア態窒素が、硝酸態窒素及び亜硝酸態窒素に変換される程度を調節することができる。即ち、無機態窒素の組成比を調節することができる。
但し、ＭＢＲでの処理は、硝酸態窒素及び亜硝酸態窒素が、アンモニア態窒素に変換されるものではないため、被処理水である消化液以上にアンモニア態窒素の組成比を高くすることはできない。
<Setting/controlling operating conditions>
Examples of the operating conditions set by the control unit include the residence time of the digested liquid in the MBR, the treatment temperature of the digested liquid in the MBR, and the treatment pH of the digested liquid in the MBR. Here, the residence time of the digested liquid in the MBR can be adjusted by the flow rate of the separated liquid in the MBR.
By adjusting these operating conditions of the MBR, it is possible to adjust the degree to which ammonia nitrogen is converted into nitrate nitrogen and nitrite nitrogen, i.e., the composition ratio of inorganic nitrogen can be adjusted.
However, since the treatment in an MBR does not convert nitrate nitrogen and nitrite nitrogen into ammonia nitrogen, the composition ratio of ammonia nitrogen cannot be made higher than that of the digestive liquid, which is the water to be treated.
ＭＢＲでの消化液の滞留時間を長くすれば、硝化が進行するため、アンモニア態窒素の比率が減少し、硝酸態窒素及び亜硝酸態窒素の比率が増加する傾向にある。
ＭＢＲでの消化液の処理温度が適切であれば、硝化が進行するため、アンモニア態窒素の比率が減少し、硝酸態窒素及び亜硝酸態窒素の比率が増加する傾向にある。
ＭＢＲでの消化液の処理ｐＨが適切であれば、硝化が進行するため、アンモニア態窒素の比率が減少し、硝酸態窒素及び亜硝酸態窒素の比率が増加する傾向にある。
If the residence time of the digested liquid in the MBR is extended, nitrification will progress, and the ratio of ammonia nitrogen will tend to decrease and the ratios of nitrate nitrogen and nitrite nitrogen will tend to increase.
If the treatment temperature of the digested liquid in the MBR is appropriate, nitrification will proceed, and the ratio of ammonia nitrogen will tend to decrease and the ratios of nitrate nitrogen and nitrite nitrogen will tend to increase.
If the treatment pH of the digested liquid in the MBR is appropriate, nitrification will proceed, and the ratio of ammonia nitrogen will tend to decrease and the ratios of nitrate nitrogen and nitrite nitrogen will tend to increase.
上述したＭＢＲの運転条件は、ＭＢＲで用いる活性汚泥の種類と状態、用いる消化液の特性によって適切な範囲は異なる。このため、ラボレベルで運転条件の適切な範囲を事前に確認する、または、実機での運転を通じて運転条件の適切な範囲を確認する等が必要である。
上記の方法で確認した適切な範囲に従って、運転条件を適宜設定すればよい。
The appropriate range of the operating conditions for the MBR described above varies depending on the type and state of the activated sludge used in the MBR and the characteristics of the digestive fluid used. Therefore, it is necessary to confirm the appropriate range of operating conditions in advance at the laboratory level, or to confirm the appropriate range of operating conditions through operation of the actual equipment.
The operating conditions may be appropriately set according to the appropriate range confirmed by the above method.
設定した運転条件によって得られた無機態窒素の組成比が、目標とした無機態窒素の組成比と異なることが測定部の測定値によって確認された場合、各制御部は運転条件を再設定する。
この場合、予めプログラムを組んでおき、測定部の測定値を断続的または連続的に監視し、その情報を各制御部にフィードバックし、各制御部が運転条件を再設定するようにしておけばよい。
When it is confirmed by the measurement value of the measurement unit that the composition ratio of inorganic nitrogen obtained under the set operating conditions is different from the target composition ratio of inorganic nitrogen, each control unit resets the operating conditions.
In this case, a program may be prepared in advance to monitor the values measured by the measuring units intermittently or continuously, and feed that information back to each control unit so that each control unit can reset the operating conditions.
制御部が設定した運転条件を実現するため、ＭＢＲは流量調節装置、液温調節装置、ｐＨ調節装置を備えることが好ましい。
これらは、１種を単独で用いてもよく、２種以上を併用してもよい。
複数の調節装置を備えれば、無機態窒素の組成比を調節することが容易となる。
In order to realize the operating conditions set by the control unit, the MBR is preferably equipped with a flow rate regulator, a liquid temperature regulator, and a pH regulator.
These may be used alone or in combination of two or more.
Providing multiple adjustment devices makes it easier to adjust the composition ratio of inorganic nitrogen.
ＭＢＲでの消化液の滞留時間で運転条件を設定する場合、ＭＢＲは流量調節装置を備え、制御部（流量）は分離液の流量を測定し、流量調節装置の運転条件を設定する。流量調節装置は、制御部（流量）の設定に従って、ＭＢＲでの消化液の滞留時間を調節する。
得られた無機態窒素の組成比が目標値と異なることが確認された場合、制御部（流量）は、流量調節装置の運転条件を再設定する。
流量調節装置は、流量の調節が可能な公知の装置を用いればよく、制御部（流量）は、流量の制御が可能な公知のシステムを用いればよい。
When the operating conditions are set based on the residence time of the digestion liquid in the MBR, the MBR is equipped with a flow rate regulator, and the control unit (flow rate) measures the flow rate of the separated liquid and sets the operating conditions of the flow rate regulator. The flow rate regulator adjusts the residence time of the digestion liquid in the MBR according to the setting of the control unit (flow rate).
If it is confirmed that the obtained composition ratio of inorganic nitrogen is different from the target value, the control unit (flow rate) resets the operating conditions of the flow rate regulator.
The flow rate adjusting device may be a known device capable of adjusting the flow rate, and the control unit (flow rate) may be a known system capable of controlling the flow rate.
ＭＢＲでの消化液の処理温度で運転条件を設定する場合、ＭＢＲは液温調節装置を備え、制御部（液温）は消化液の処理温度を測定し、液温調節装置の運転条件を設定する。液温調節装置は、制御部（液温）の設定に従って、ＭＢＲでの消化液の処理温度を調節する。
得られた無機態窒素の組成比が目標値と異なることが確認された場合、制御部（液温）は、液温調節装置の運転条件を再設定する。
液温調節装置は、液温の調節が可能な公知の装置を用いればよく、制御部（液温）は、液温の制御が可能な公知のシステムを用いればよい。
When the operating conditions are set based on the treatment temperature of the digestive liquid in the MBR, the MBR is equipped with a liquid temperature regulator, and the control unit (liquid temperature) measures the treatment temperature of the digestive liquid and sets the operating conditions of the liquid temperature regulator. The liquid temperature regulator regulates the treatment temperature of the digestive liquid in the MBR according to the setting of the control unit (liquid temperature).
If it is confirmed that the obtained composition ratio of inorganic nitrogen is different from the target value, the control unit (liquid temperature) resets the operating conditions of the liquid temperature adjustment device.
The liquid temperature adjusting device may be a known device capable of adjusting the liquid temperature, and the control unit (liquid temperature) may be a known system capable of controlling the liquid temperature.
ＭＢＲでの消化液の処理ｐＨで運転条件を設定する場合、ＭＢＲはｐＨ調節装置を備え、制御部（ｐＨ）は消化液の処理ｐＨを測定し、ｐＨ調節装置の運転条件を設定する。ｐＨ調節装置は、制御部（ｐＨ）の設定に従って、ＭＢＲでの消化液の処理ｐＨを調節する。
得られた無機態窒素の組成比が目標値と異なることが確認された場合、制御部（ｐＨ）は、ｐＨ調節装置の運転条件を再設定する。
ｐＨ調節装置は、ｐＨの調節が可能な公知の装置を用いればよく、制御部（ｐＨ）は、ｐＨの制御が可能な公知のシステムを用いればよい。
ＭＢＲでの消化液の処理ｐＨを調節する際に硝酸を用いると、硝酸自体が無機態窒素であり、液体肥料の成分として有効利用できることから、好ましい。
When the operating conditions are set based on the treatment pH of the digested liquid in the MBR, the MBR is equipped with a pH adjusting device, and the control unit (pH) measures the treatment pH of the digested liquid and sets the operating conditions of the pH adjusting device. The pH adjusting device adjusts the treatment pH of the digested liquid in the MBR according to the setting of the control unit (pH).
If it is confirmed that the obtained composition ratio of inorganic nitrogen is different from the target value, the control unit (pH) resets the operating conditions of the pH adjustment device.
The pH adjusting device may be a known device capable of adjusting pH, and the control unit (pH) may be a known system capable of controlling pH.
It is preferable to use nitric acid when adjusting the pH of the digested liquid being treated in the MBR, since nitric acid itself is inorganic nitrogen and can be effectively used as a component of liquid fertilizer.
＜液体肥料製造方法＞
本発明の液体肥料製造方法は、無機態窒素を含有する液体肥料を製造する液体肥料製造方法であって、下記工程（１）～（３）を有する；
工程（１）：該無機態窒素の目標組成比に沿って運転条件を設定する制御工程、
工程（２）：該制御工程の設定に従って、有機物の消化液を生物処理する膜分離工程、
工程（３）：該膜分離工程で濾過された分離液を濃縮する電気透析工程。
<Liquid fertilizer manufacturing method>
The liquid fertilizer production method of the present invention is a liquid fertilizer production method for producing a liquid fertilizer containing inorganic nitrogen, and includes the following steps (1) to (3):
Step (1): A control step of setting operating conditions in accordance with the target composition ratio of inorganic nitrogen;
Step (2): A membrane separation step of biologically treating the organic digestive liquid according to the settings of the control step;
Step (3): An electrodialysis step for concentrating the separated liquid filtered in the membrane separation step.
＜工程（１）＞
工程（１）は、無機態窒素の目標組成比に沿って運転条件を設定する制御工程であり、その主旨は、液体肥料製造装置の項目で説明した「制御部」と同様である。
一方、工程（１）においては、制御部ではなく、制御工程としていることからも明らかなように、制御部という特定の設備を指すものではなく、制御する操作、制御する行為も含めて、制御工程とする。
<Step (1)>
Step (1) is a control step for setting operating conditions in accordance with a target composition ratio of inorganic nitrogen, and its gist is the same as that of the "control unit" described in the section on the liquid fertilizer manufacturing apparatus.
On the other hand, as is clear from the fact that it is referred to as a control process rather than a control unit in process (1), the control process does not refer to a specific piece of equipment called a control unit, but includes the controlling operation and the act of controlling.
＜工程（２）＞
工程（２）は、制御工程の設定に従って、有機物の消化液を生物処理する膜分離工程であり、その主旨は、液体肥料製造装置の項目で説明した「膜分離部」と同様である。
一方、工程（２）においては、膜分離部ではなく、膜分離工程としていることからも明らかなように、膜分離部という特定の設備を指すものではなく、膜分離する操作、膜分離する行為も含めて、膜分離工程とする。
<Step (2)>
Step (2) is a membrane separation step in which the digestive liquid of organic matter is biologically treated according to the settings of the control step, and its gist is similar to that of the "membrane separation section" explained in the section on the liquid fertilizer production apparatus.
On the other hand, as is clear from the fact that it is referred to as a membrane separation process rather than a membrane separation section in step (2), the membrane separation process does not refer to a specific piece of equipment called a membrane separation section, but includes the operation and act of membrane separation.
＜工程（３）＞
工程（３）は、膜分離工程で濾過された分離液を濃縮する電気透析工程であり、その主旨は、液体肥料製造装置の項目で説明した「電気透析部」と同様である。
一方、工程（３）においては、電気透析部ではなく、電気透析工程としていることからも明らかなように、電気透析部という特定の設備を指すものではなく、電気透析する操作、電気透析する行為も含めて、電気透析工程とする。
<Step (3)>
The step (3) is an electrodialysis step for concentrating the separated liquid filtered in the membrane separation step, and its gist is the same as that of the "electrodialysis section" explained in the section on the liquid fertilizer production apparatus.
On the other hand, as is clear from the fact that the step (3) is referred to as an electrodialysis step rather than an electrodialysis unit, the electrodialysis step does not refer to a specific facility called an electrodialysis unit, but includes the operation and act of electrodialysis.
＜工程（４）＞
本発明の液体肥料製造方法は、下記工程（４）を更に有してもよい；
工程（４）：前記分離液の組成比を測定する測定工程。
工程（４）の主旨は、液体肥料製造装置の項目で説明した「測定部」と同様である。
一方、工程（４）においては、測定部ではなく、測定工程としていることからも明らかなように、測定部という特定の設備を指すものではなく、測定する操作、測定する行為も含めて、測定工程とする。
<Step (4)>
The liquid fertilizer production method of the present invention may further include the following step (4):
Step (4): A measuring step of measuring the composition ratio of the separated liquid.
The gist of step (4) is the same as that of the "measuring unit" explained in the section on the liquid fertilizer manufacturing apparatus.
On the other hand, as is clear from the fact that it is referred to as the measurement process rather than the measurement unit in step (4), the measurement process does not refer to a specific piece of equipment called a measurement unit, but includes the operation and act of measuring.
下記の好ましい理由は、液体肥料製造装置の項目で説明した主旨と同様であり、詳細は割愛する。
・本発明の液体肥料製造方法では、測定工程の測定値に基づき、制御工程で運転条件を再設定することが好ましい。
・工程（２）の膜分離工程は、ＭＢＲを用いる工程であることが好ましい。
・ＭＢＲは流量調節機能を備え、前記制御工程で流量調節機能の運転条件を設定することが好ましい。
・ＭＢＲは液温調節機能を備え、前記制御工程で液温調節機能の運転条件を設定することが好ましい。
・ＭＢＲはｐＨ調節機能を備え、前記制御工程でｐＨ調節機能の運転条件を設定することが好ましい。また、ＭＢＲのｐＨを調節する際には硝酸を用いることが好ましい。
The reasons why the following is preferable are the same as those explained in the section on the liquid fertilizer manufacturing apparatus, and details will be omitted.
In the liquid fertilizer producing method of the present invention, it is preferable to reset the operating conditions in the control step based on the measured values in the measurement step.
The membrane separation step (2) is preferably a step using an MBR.
It is preferable that the MBR has a flow rate adjusting function, and the operating conditions of the flow rate adjusting function are set in the control step.
It is preferable that the MBR has a liquid temperature adjustment function, and the operating conditions of the liquid temperature adjustment function are set in the control step.
It is preferable that the MBR has a pH adjustment function, and the operating conditions of the pH adjustment function are set in the control step. It is also preferable to use nitric acid when adjusting the pH of the MBR.
＜液体肥料＞
本発明における液体肥料は、本発明の液体肥料製造装置、又は、液体肥料製造方法で得られるものであり、無機態窒素を含有する。
液体肥料は、前記無機態窒素以外に、肥料として一般的な添加剤を後から配合してもよい。また、無機態窒素を後から配合して、個別の使用場面に応じて、無機態窒素の組成比を調節することも可能である。
<Liquid fertilizer>
The liquid fertilizer of the present invention is obtained by the liquid fertilizer production apparatus or the liquid fertilizer production method of the present invention, and contains inorganic nitrogen.
In addition to the inorganic nitrogen, the liquid fertilizer may contain other additives that are common in fertilizers. It is also possible to add inorganic nitrogen later to adjust the composition ratio of inorganic nitrogen depending on the individual use situation.
＜用途＞
本発明における液体肥料は、一般的な肥料として使用可能であるが、特に、植物の生育条件や植物の種類に応じた、土耕及び水耕栽培における元肥、追肥として好適に用いられる。
<Applications>
The liquid fertilizer of the present invention can be used as a general fertilizer, but is particularly suitable for use as a base fertilizer or top dressing in soil culture or hydroponic culture depending on the growing conditions and type of plant.
以下に実施例を示し、本発明を更に詳細に説明するが、本発明は、その要旨を超えない限り、以下の実施例により限定されるものではない。
以下の実施例及び比較例においては、下記の方法により各種物性を測定した。
The present invention will be described in more detail below with reference to examples. However, the present invention is not limited to the following examples as long as the gist of the present invention is not exceeded.
In the following examples and comparative examples, various physical properties were measured by the following methods.
［評価方法］
（１）アンモニア態窒素の濃度
ＨＣＡＨ社製「ＤＲ２７００吸光光度計」を使用し、ネスラー法により分析した。
[Evaluation method]
(1) Concentration of Ammonia Nitrogen The concentration of ammonia nitrogen was analyzed by the Nessler method using a DR2700 spectrophotometer manufactured by HCAH.
（２）硝酸態窒素及び亜硝酸態窒素の濃度
東ソー社製「ＩＣ－２１００」を用い、イオンクロマトグラフ法により測定した。
東ソー社製「ＴＳＫｇｅｌ ＳｕｐｅｒＩＣ－Ａ ＨＳ」をカラムとし、ＮａＨＣＯ３、ＮａＣＯ３混合液を移動相として、電気伝導度により検出した。
(2) Concentration of nitrate nitrogen and nitrite nitrogen The concentration was measured by ion chromatography using Tosoh Corporation's "IC-2100".
A Tosoh Corporation "TSKgel SuperIC-A HS" column was used, and a mixture of NaHCO 3 and NaCO 3 was used as the mobile phase, and detection was performed by electrical conductivity.
［実施例１］
原水として、築上町消化液を用いた。築上町消化液は、有機物の消化液であり、し尿由来の好気発酵消化液である。
膜分離部として、三菱ケミカル社製の限外濾過膜（膜素材：ポリフッ化ビニリデン、公称孔径０．０５μｍ、膜形状：中空糸）を備えた、容積２ｍ３の水槽を用いた。
消化液を水槽に投入し、限外濾過膜を消化液に浸漬させた。このとき、消化液の液温（処理温度）は２５℃とした。
この状態で、連続で吸引濾過をして、限外濾過膜で濾過された分離液と、濾過されなかった汚泥を含む分散液に分けた。分離液の流量は６０Ｌ／ｈとした。このときの消化液の滞留時間は３３時間であった。
得られた分離液を処理水タンクに貯槽した。
[Example 1]
The raw water used was Chikujo Town digestive fluid, which is a digestive fluid of organic matter and is an aerobic fermentation digestive fluid derived from human waste.
As the membrane separation section, a water tank having a volume of 2 m3 and equipped with an ultrafiltration membrane manufactured by Mitsubishi Chemical Corporation (membrane material: polyvinylidene fluoride, nominal pore size: 0.05 μm, membrane shape: hollow fiber) was used.
The digestive fluid was poured into a water tank, and the ultrafiltration membrane was immersed in the digestive fluid. At this time, the temperature of the digestive fluid (treatment temperature) was 25°C.
In this state, continuous suction filtration was performed to separate the separated liquid filtered through the ultrafiltration membrane from the dispersion liquid containing the unfiltered sludge. The flow rate of the separated liquid was 60 L/h. The residence time of the digested liquid was 33 hours.
The separated liquid obtained was stored in a treated water tank.
分離液を、ＡＧＣエンジニアリング社製の電気透析装置「ＤＷ－１型」（カチオンイオン交換膜：ＣＭＶＮ、アニオンイオン交換膜：ＡＭＶＮ）で処理した。電気透析電圧は１５Ｖとし、電気透析濃縮液と電気透析脱塩液に分けた。
電気透析脱塩液は、１．１ｍ３／ｈの流量で処理水タンクに戻し、循環運転とした。
得られた電気透析濃縮液について、アンモニア態窒素の濃度と、硝酸態窒素及び亜硝酸態窒素の濃度を測定した。
結果を表１に示す。
The separated liquid was treated with an electrodialysis device "DW-1 type" (cation ion exchange membrane: CMVN, anion ion exchange membrane: AMVN) manufactured by AGC Engineering Co., Ltd. The electrodialysis voltage was set to 15 V, and the separated liquid was separated into an electrodialysis concentrated liquid and an electrodialysis desalted liquid.
The electrodialysis desalted liquid was returned to the treated water tank at a flow rate of 1.1 m 3 /h for circulating operation.
The electrodialysis concentrate thus obtained was subjected to measurement of the concentrations of ammonia nitrogen, nitrate nitrogen and nitrite nitrogen.
The results are shown in Table 1.
［実施例２］
分離液の流量を３０Ｌ／ｈとし、このときの消化液の滞留時間が６７時間であったこと以外は、実施例１と同様にして、電気透析濃縮液を得た。
結果を表１に示す。
[Example 2]
An electrodialysis concentrate was obtained in the same manner as in Example 1, except that the flow rate of the separated liquid was 30 L/h and the residence time of the digested liquid was 67 hours.
The results are shown in Table 1.
［実施例３］
消化液の液温（処理温度）を１０℃としたこと以外は、実施例１と同様にして、電気透析濃縮液を得た。
結果を表１に示す。
[Example 3]
An electrodialysis concentrate was obtained in the same manner as in Example 1, except that the liquid temperature (treatment temperature) of the digested liquid was set to 10°C.
The results are shown in Table 1.
表１から明らかなように、本発明の製造方法（実施例１～３）は、運転条件の設定により、電気透析濃縮液の、アンモニア態窒素／硝酸態窒素及び亜硝酸態窒素の組成比を調整することができた。これにより、本発明によって、無機態窒素成分の組成比が調整された液体肥料を簡便に製造することができる。 As is clear from Table 1, the manufacturing method of the present invention (Examples 1 to 3) was able to adjust the composition ratio of ammonia nitrogen/nitrate nitrogen and nitrite nitrogen in the electrodialysis concentrate by setting the operating conditions. This makes it possible to easily manufacture liquid fertilizer with an adjusted composition ratio of inorganic nitrogen components by the present invention.
１０ 消化液タンク、１１ 第１の流路
２０ 膜分離部（ＭＢＲ）、２１ 第２の流路、２２ 汚泥引抜流路
２３ 液温調節装置、２４ 制御部（液温）、２５ ｐＨ調節装置、２６ 制御部（ｐＨ）、２７ 流量調節装置、２８ 制御部（流量）、２９ 測定部
３０ 処理水タンク、３１ 第３の流路
４０ 電気透析部、４１ 電気透析脱塩液流路、４２ 電気透析濃縮液流路、４３ 測定部
REFERENCE SIGNS
Claims (18)
該無機態窒素の目標組成比に沿って運転条件を設定する制御部と、
該制御部の設定に従って、有機物の消化液を生物処理して膜分離する膜分離部と、
該膜分離部で濾過された分離液を濃縮する電気透析部と、
該分離液の組成比を測定する測定部と、を有し、
該測定部による該無機態窒素の組成比の測定値に基づき、該制御部が、該消化液の処理温度、該消化液の処理ｐＨ、及び該分離液の流量のうち、１つ以上の運転条件を再設定する、液体肥料製造装置。 A liquid fertilizer manufacturing apparatus for producing liquid fertilizer containing inorganic nitrogen,
A control unit that sets operating conditions according to the target composition ratio of inorganic nitrogen;
A membrane separation unit that biologically treats the organic digestive liquid and separates it into membranes according to the settings of the control unit;
an electrodialysis section for concentrating the separated liquid filtered by the membrane separation section;
A measurement unit that measures the composition ratio of the separated liquid ,
A liquid fertilizer manufacturing apparatus, wherein the control unit resets one or more operating conditions among the treatment temperature of the digested liquid, the treatment pH of the digested liquid, and the flow rate of the separated liquid based on the measured value of the composition ratio of the inorganic nitrogen by the measurement unit.
工程（１）：該無機態窒素の目標組成比に沿って運転条件を設定する制御工程と、
工程（２）：該制御工程の設定に従って、有機物の消化液を生物処理して膜分離する膜分離工程と、
工程（３）：該膜分離工程で濾過された分離液を濃縮する電気透析工程と、
工程（４）：前記分離液の組成比を測定する測定工程と、を含み、
該制御工程において、該測定工程での該無機態窒素の組成比の測定値に基づき、該消化液の処理温度、該消化液の処理ｐＨ、及び該分離液の流量のうち、１つ以上の運転条件を調整する、液体肥料製造方法。 A liquid fertilizer production method for producing a liquid fertilizer containing inorganic nitrogen, comprising :
Step (1): A control step of setting operating conditions according to a target composition ratio of the inorganic nitrogen;
Step (2): A membrane separation step of biologically treating and membrane-separating the organic digestive liquid according to the setting of the control step;
Step (3): An electrodialysis step of concentrating the separated liquid filtered in the membrane separation step ;
Step (4): A measuring step of measuring the composition ratio of the separated liquid,
A liquid fertilizer production method, in which in the control step, one or more operating conditions among the treatment temperature of the digested liquid, the treatment pH of the digested liquid, and the flow rate of the separated liquid are adjusted based on the measured value of the composition ratio of the inorganic nitrogen in the measurement step.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2023054510A JP7633300B2 (en) | 2023-03-30 | 2023-03-30 | Liquid fertilizer manufacturing device and liquid fertilizer manufacturing method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2023054510A JP7633300B2 (en) | 2023-03-30 | 2023-03-30 | Liquid fertilizer manufacturing device and liquid fertilizer manufacturing method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2024142387A JP2024142387A (en) | 2024-10-11 |
| JP7633300B2 true JP7633300B2 (en) | 2025-02-19 |
Family
ID=92978161
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2023054510A Active JP7633300B2 (en) | 2023-03-30 | 2023-03-30 | Liquid fertilizer manufacturing device and liquid fertilizer manufacturing method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP7633300B2 (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090282882A1 (en) | 2006-02-24 | 2009-11-19 | Beesterzwaag Behkeer B.V. | Process for the conversion of liquid waste biomass into a fertilizer product |
| JP2011143363A (en) | 2010-01-15 | 2011-07-28 | Swing Corp | Method and apparatus for treating nitrogen in waste water |
| JP2014008431A (en) | 2012-06-28 | 2014-01-20 | Swing Corp | Method and apparatus for anaerobic digestion treatment of organic wastewater |
| JP2017221915A (en) | 2016-06-16 | 2017-12-21 | 三菱ケミカル株式会社 | Apparatus for treating waste water and method for treating waste water |
| JP2018114438A (en) | 2017-01-17 | 2018-07-26 | 三菱ケミカルアクア・ソリューションズ株式会社 | Wastewater treatment method and wastewater treatment equipment |
| JP2019131432A (en) | 2018-01-31 | 2019-08-08 | 光保 矢部 | Method of producing liquid fertilizer for nutritious liquid cultivation and system for recovering fertilizer component by condensation separation |
| JP2019181377A (en) | 2018-04-11 | 2019-10-24 | 株式会社日立製作所 | Nitrogen treatment method |
| JP2021186744A (en) | 2020-05-29 | 2021-12-13 | 極東開発工業株式会社 | Fermentation apparatus, liquid fertilizer manufacturing apparatus, and liquid fertilizer manufacturing method |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4951826B2 (en) * | 2001-08-10 | 2012-06-13 | 栗田工業株式会社 | Biological nitrogen removal method |
| JP2014097478A (en) * | 2012-11-15 | 2014-05-29 | Hitachi Ltd | Effluent treatment method and effluent treatment apparatus |
| JP6829585B2 (en) * | 2016-11-14 | 2021-02-10 | 株式会社日水コン | Sewage treatment system and sewage treatment method |
| JP7713773B2 (en) * | 2020-09-09 | 2025-07-28 | 水ｉｎｇ株式会社 | Water treatment method and water treatment device |
-
2023
- 2023-03-30 JP JP2023054510A patent/JP7633300B2/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090282882A1 (en) | 2006-02-24 | 2009-11-19 | Beesterzwaag Behkeer B.V. | Process for the conversion of liquid waste biomass into a fertilizer product |
| JP2011143363A (en) | 2010-01-15 | 2011-07-28 | Swing Corp | Method and apparatus for treating nitrogen in waste water |
| JP2014008431A (en) | 2012-06-28 | 2014-01-20 | Swing Corp | Method and apparatus for anaerobic digestion treatment of organic wastewater |
| JP2017221915A (en) | 2016-06-16 | 2017-12-21 | 三菱ケミカル株式会社 | Apparatus for treating waste water and method for treating waste water |
| JP2018114438A (en) | 2017-01-17 | 2018-07-26 | 三菱ケミカルアクア・ソリューションズ株式会社 | Wastewater treatment method and wastewater treatment equipment |
| JP2019131432A (en) | 2018-01-31 | 2019-08-08 | 光保 矢部 | Method of producing liquid fertilizer for nutritious liquid cultivation and system for recovering fertilizer component by condensation separation |
| JP2019181377A (en) | 2018-04-11 | 2019-10-24 | 株式会社日立製作所 | Nitrogen treatment method |
| JP2021186744A (en) | 2020-05-29 | 2021-12-13 | 極東開発工業株式会社 | Fermentation apparatus, liquid fertilizer manufacturing apparatus, and liquid fertilizer manufacturing method |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2024142387A (en) | 2024-10-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Wang et al. | The performance of coupling membrane filtration in recirculating aquaponic system for tilapia culture | |
| da ROCHA et al. | Lettuce production in aquaponic and biofloc systems with silver catfish Rhamdia quelen | |
| Banti et al. | An innovative bioreactor set-up that reduces membrane fouling by adjusting the filamentous bacterial population | |
| CA3211058A1 (en) | Systems and methods for hydroponic plant cultivation | |
| JP3587102B2 (en) | Method for producing water using deep ocean water, method for treating deep ocean water, and apparatus therefor | |
| KR102185297B1 (en) | Liquid fertilizer production method and high-quality liquid fertilizer based on lfqc and chlorella microbiological fertilizer manufacture method | |
| JP2019131432A (en) | Method of producing liquid fertilizer for nutritious liquid cultivation and system for recovering fertilizer component by condensation separation | |
| JP7633300B2 (en) | Liquid fertilizer manufacturing device and liquid fertilizer manufacturing method | |
| US7875181B2 (en) | Water treatment process | |
| US12577523B2 (en) | Systems and methods for producing ammonium nitrate | |
| Lim et al. | Performance of thin film composite membranes for ammonium removal and reuse of ammonium-enriched solution for plant growth | |
| US20210179507A1 (en) | Process for biological ammonia production by nitrogen fixing cyanobacteria | |
| EP3183218B1 (en) | Diffused aeration systems and methods for cleaning fouled diffusers in aeration systems | |
| JP2010240635A (en) | Method of desalting mixed water of wastewater and seawater by compound fermentation method | |
| JP2002172392A (en) | Method and apparatus for producing mineral-containing liquid from seawater | |
| KR20210031243A (en) | Complex Microorganism for removing Nitrate and Phosphate and Method of Purifying water for Hydroponics using the Complex Microorganism | |
| KR101963646B1 (en) | Complex Microorganism for removing Nitrate and Phosphate, Method of Manufacturing thereof and Method of Purifying water for Hydroponics using the Complex Microorganism | |
| JP7797370B2 (en) | Liquid fertilizer manufacturing method and manufacturing device | |
| KR20150022188A (en) | Method for fabricating of aerobic granule sludge and sequencing batch reactor apparatus | |
| JP7633301B2 (en) | Liquid fertilizer manufacturing device and liquid fertilizer manufacturing method | |
| Kamshybaev et al. | Water treatment by membrane filtration for the needs of an agricultural enterprise from an underground water source | |
| US20250049004A1 (en) | Aquaponic system set pplying filtration with reverse osmosis membrane | |
| JP2021036781A (en) | Culture method, culture equipment, wastewater treatment method and wastewater treatment equipment | |
| US20250186948A1 (en) | Sustainable nutrient water recovery by hybrid electrodialysis - forward osmosis process | |
| JP2001087770A (en) | Water utilizing sea deep water and its production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20230707 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20240917 |
|
| A521 | Request for written amendment filed |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20241118 |
|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20250107 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20250206 |
|
| R150 | Certificate of patent or registration of utility model |
Ref document number: 7633300 Country of ref document: JP Free format text: JAPANESE INTERMEDIATE CODE: R150 |